Method and apparatus for reducing volatiles in polymerized styrene

Abstract: Methods and apparatus are disclosed for purifying polymerized monovinyl aromatic compounds such as polystyrene by reducing the residual monomer content of the finished polymer. Said methods and apparatus utilizes a combination of sequentially ordered multiple heat exchangers and multiple devolatilizers to not only remove substantial portions of volatiles from the polymer but also to allow strict control of other parameters such as melt flow index and molecular weight distribution.

Description: BACKGROUND OF THE INVENTION The present invention is generally related to the removal of undesirable components from polymerized monovinyl aromatic compounds and more particularly is directed to the removal of volatile materials at the end of the polymerization process for monovinyl aromatic compounds such as polystyrene, while incorporating options to improve and optimize critical polymer properties. It is well known in the polymer industry that volatiles such as unreacted monomer, dimers, and trimers may be removed from newly polymerized monovinyl aromatic compounds by means such as vacuum distillation and flash devolatilization. The vacuum process subjects the polymer to sub-atmospheric conditions to draw out the volatile components and the flash process may involve vacuum as well as heat to further drive out the volatiles. In addition to vacuum and heat devolatilization techniques, another method known in the art is that of "stripping" of volatiles by the use of stripping agents such as steam. U.S. Patent 3,311,676 to Toekes teaches the devolatilization of a rubber modified polystyrene by the use of a preheater, a heat exchanger, and a vacuum vessel which Toekes classifies as a phase separator. The preheater heats the volatile-containing polystyrene material into the range of 200 to 240°C and the heat exchanger maintains the temperature of the material while subjecting it to a reduced pressure in the range of 0.02 to 0.06 bars (15 to 50 mm Hg). The vacuum on the heat exchanger is a result of its connection to the phase separator which operates at a pressure of 6.10 -3 to 1.32 bars (5 to 100 mm Hg). Toekes describes the process wherein a foam is generated in the heat exchanger and flows into the phase separator thereby accelerating the removal of volatiles by a many-fold increase in surface area of the material. The Toekes apparatus and procedure claims a reduction in volatiles to approximately 0.5 to 1.5 percent by weight which corresponds to a volatile level of 5000 to 15,000 PPM. According to Toekes , the monomer and EB (ethylbenzene) level was reduced to "below 0.1%" which corresponds to 1000 PPM. U.S. 3,668,161 to Newman et al. discloses a method for separating volatiles from a polymer by passing the polymer through a first flash devolatilization zone maintained at a vacuum and heating the partially devolatilized composition, adding a foaming agent and then passing through a second devolatilization zone at reduced pressure to vaporize and remove remaining volatile constituents. Polystyrene materials devolatilized by this process according to examples contained in the patent ended up with residual styrene in the amount of 2000 PPM. U.S. 3,865,672 to Metzinger dated February 11, 1975 discloses a process to remove volatiles from a polymer solution by using a single stage vacuum evaporation system in which the temperature of the polymer solution increases in the direction of the flow. Metzinger is concerned primarily with polymers containing acrylonitrile or methacrylonitrile. The process is achieved in Metzinger by the use of a counter-flow heat exchanger combined with a vacuum devolatilization zone. The counter-flow heat exchanger thus allows the heat to increase in the polymer as it proceeds through the devolatilization zone. More particularly, Metzinger discloses a vertical tube bundle heat exchanger operating in a downflow configuration wherein the polymer solution is fed at the top, devolatilized during the downflow, and then removed at the bottom. Likewise, the temperature gradient maintained in the heat exchanger increases from top to bottom such that the devolatilized polymer is subjected to increasing temperatures as it flows through the devolatilizing system. According to Metzinger , the volatile content was reduced to 3000 PPM. U.S. 3,928,300 to Hagberg dated December 23, 1975 discloses a process for devolatilizing polystyrene by subjecting it to a downflow "falling strand" devolatilizer. A falling strand devolatilizer consists of a shell-and-tube heat exchanger in a vertical configuration stationed in the upper portion of a "flash tank". The flash tank has a vapor pump communicating therewith to remove volatiles which are flashed out of the polymer. The vertical shell-and-tube heat exchanger comprises a series of parallel tubes held rigidly within the heat exchanger shell in a vertical orientation. Heated polymer flows through the tubes in response to gravity and the pressure differential established by the vapor pump which creates a vacuum in the flash tank. The heated polymer exits the tubes of the heat exchanger in strands or strings which then release the volatiles due to the combination of heat from the heat exchanger and the low pressure in the flash tank. The strands drop to the lower end of the conical flash tank and then are regulated by a plug valve and flowed downward into a hold tank which may also be used as a second flash tank. The Hagberg patent claims a method of controlling the volatiles in the polymer by varying both the length and the diameter of the tubes in the shell-and-tube heat exchanger. The residual monomer and ligamer remaining in the polymer after the Hagberg process is shown as ranging from 1000 to 110,000 PPM. U.S. 3,966,538 also to Hagberg issued June 29, 1976 is a divisional case of the Hagberg patent above with claims directed to the apparatus rather than the process. U.S. 4,294,652 to Newman issued October 13, 1981 discloses apparatus and process almost identical to the aforedescribed Hagberg devices. The only difference between the Newman device and the Hagberg devices is that the lower holding tank of Hagberg has been modified slightly by adding a pump-around pump and two baffles plus a vapor line out of the hold tank to achieve some slight additional devolatilizing in the lower holding tank. Although the Newman disclosure contains no specific examples of actual trial runs, Newman claims devolatilization of monomer content to less than about 100 to 500 PPM. No figures are stated for other volatiles contained in the finished polymer. U.S. 4,439,601 to McCurdy et al issued March 27, 1984 discloses a process for devolatilization of mass processible polymers through the use of two or more flash devolatilizers in series having an oil heated jacket and by utilizing a nonrefrigerated cooling process to condense the volatiles which are separated from the flash zones. The nonrefrigerated cooling process described uses a coolant such as water circulated through a heat exchanger to condense the volatiles in the multi-stage flash devolatilization. Each flash devolatilizer is operated at a lower pressure than the preceding one. No figures are given in the McCurdy disclosure for the levels of volatiles remaining in the finished polymer product. U.S. 4,777,210 to Sosa et al issued October 11, 1988, discloses methods and apparatus for producing high-impact polystyrene having discrete particles of rubber in a styrene matrix. The process utilizes a preinversion reactor to closely control viscosity of the solutions and to produce desirable high-impact polystyrene products. U.S. 4,857,587 to Sosa et al issued August 15, 1989, discloses methods and apparatus for producing high-impact polystyrene by removing inhibiting impurities from the recycle stream of the styrene polymerization zone, through the use of a flash devolatiliser heated by external heater coils. U.S. 5,200,476 to Sosa et al, issued April 6, 1993, discloses a system for reducing volatiles in a polymerization line, said system utilizing partial condensers, total condensers, devolatilizers, and filter beds arranged in series. The disclosures and specifications of the three aforementioned Sosa et al patents are herein incorporated by reference in their entirety into the present application. FR-A-2,220,545 discloses an apparatus for the continuous recovery of alkenylaromatic monomers, said apparatus comprising a falling strand devolatilizing means for alkenylaromatic polymer-monomer melt, a heating means for the melt, a first and second flash vaporization chambers positioned in contiguous descending vertical relationship and communicating with one another, means for reducing the pressure in each chamber and means for maintaining an elevated temperature in each chamber. The pressure in the second flash vaporization chamber is less than that in the first flash vaporization chamber. SUMMARY OF THE INVENTION The present invention discloses a process according to the claims for devolatilizing monovinyl aromatic compounds after polymerization which process utilizes a combination of sequentially ordered multiple heat exchangers and multiple devolatilizers to not only remove substantial portions of volatiles from the polymer but also to allow strict control of other parameters such as melt flow index and molecular weight distribution. BRIEF DESCRIPTION OF THE DRAWINGS Figure 1 is a schematic diagram fo the heat exchanger / devolatilizer system of the present invention. BRIEF DESCRIPTION OF THE PREFERRED EMBODIMENTS In the present invention, devolatilization processes and apparatus are disclosed for use with polymerization systems such as those disclosed in the aforementioned Sosa et al patents. The present invention as disclosed in Figure 1 is particularly suitable for use with the HIPS manufacturing process of Sosa (US 4,477,210). In Figure 1 of the present application, the reactor R-1 is identified at 10 in the present system. Normally, reactor R-1 would comprise the last reactor in the series of reactors for manufacturing high-impact polystyrene. With the present invention, however, R-1 can be utilized as the penultimate reactor by adjusting the heat input of heat exchanger 11 high enough to serve as an additional polymer reactor. Heat exchanger 11 is connected to reactor R-1 by flowline 110. It should be noted that preferably heat exchanger 11 is of the "upflow" type where heated polymer enters at the bottom end of the vessel and flows upward through a shell-and-tube heat exchanger to exit through the top of the vessel via exit line 111. Polymer flows from heat exchanger 11 into a downflow heat exchanger 12 at the opposite end of flowline 111. Downflow exchanger 12 is situated in a flash devolatilization tank 13 (DV-1) maintained at a vacuum of from 2.66 to 26.6 KPa (20 Torr up to 200 Torr). In one preferred embodiment, the heat exchanger 12, also known as a devolatilizer preheater, was maintained at an operating temperature of about 287.8°C (550°F) and consisted of a shell-and-tube heat exchanger having tubes about 2.54cm (one inch) in diameter and 1.524m (5 feet) long. In this embodiment, heat exchanger 11 was maintained at around 148.9°C (300°F). The polymer exiting the devolatilizer preheater 12 accumulated in the lower section of devolatilizer vessel 13 at a temperature of about 226.7°C (440°F). A polymer flowline 112 connected to the lower end of devolatilizer tank 13 communicates partially devolatilized polymer to the second devolatilizer 14 (DV-2) having a "hoop" falling strand devolatilizer nozzle system 15 located concentrically therein. Devolatilized vapors are removed from devolatilizers 13 and 14 through vapor removal lines 19 and 17 respectively. These lines are maintained at a vacuum by connection to a vacuum source such as a vacuum pump (not shown). The volatiles removed through vapor lines 19 and 17 are then passed to a normal condenser and reduced to their liquid stage whereupon they may be recycled back into the polystyrene polymerization process at any desirable point. The structure of the second devolatilizer 14 comprises an outer vessel 16 containing the hoop nozzle manifold 15 located in the upper portion thereof. Hoop nozzle manifold 15 comprises a circular flow tube having a plurality of small orifice nozzles directed downwardly in vessel 16 to allow molten polymer entering from line 112 to fall downward in relatively small diameter continuous vertical strands, thereby exposing a large surface area of the polymer to the vacuum level contained in devolatilizer 14. The vacuum level in devolatilizer 14 is maintained at a level of from less than 0.13 (1) up to about 2.66 KPa (20 Torr). The diameter of the nozzles located in manifold 15 is less than about 0.397cm (5/32 inch), preferably less than about 0.198cm (5/64 inch), and most preferably in the range of about 0.119cm (3/64 inches) or smaller in flow diameter. The diameter of the flow tubes in the devolatilizer preheater 12-is of from 2.286 to 2.54cm (0.9 to 1.0 inches). A flowline 113 exits the lower end of the second devolatilizer 14 and transmits the completely devolatilized polymer material to a finishing operation such as a pelletizer 18. Thus, in typical operation, polymer from a polystyrene manufacturing process, such as that disclosed in the incorporated Sosa '210 patent, enters the devolatilization system from the final reactor R-1, indicated at 10, through flowline 110 into the first heat exchanger 11. From there the polymer flows upward through the shell-and-tube heat exchanger and out through flowline 111 into a second heat exchanger denoted as the devolatilizer preheater and indicated at 12, which is also a shell-and-tube heat exchanger arranged in a downflow configuration. Heated polymer then passes through the downflow heat exchanger into a vacuum flash tank 13 allowing volatiles to flash off as they exit the heat exchanger 12. The vaporized volatiles are removed through vapor line 19 from devolatilizer 13. Partially devolatilized polymer is then drawn off through flowline 112 and injected through a circular manifold nozzle system 15 in a second devolatilizer 16 also maintained at a vacuum. This allows additional devolatilization of the polymer as the volatiles are removed from vapor line 17 by vacuum means known to those skilled in the art. Volatiles removed by means of lines 17 and 19 are recycled back into the polymer reaction system as indicated in the aforementioned incorporated Sosa patent '587. The heated polymer exiting the nozzles of manifold 15 into the second devolatilizer chamber 16 maintained at a vacuum then flows down and is collected at the bottom end of chamber 16 and removed by flowline 113. The completely devolatilized polymer is then cooled, pelletized at pelletizer 18 and readied for shipment to the consumer. Table I below indicates the parameters of operating the system of Figure I such that different characteristics of the polymer may be adjusted or manipulated to obtain different properties of crystal polystyrene, high-impact polystyrene, general purpose polystyrene or of other polymerized monovinyl aromatic compounds. The parameters in Table 1 indicate the widest desirable ranges of parameters. PARAMETER HEAT EXCHANGER PREHEATER DV-1 DV-2 Temperature 148.9 - 287.8°C (300 - 550°F) 226.7 - 287.8°C (440 - 550°C) 226.7°C (440°F) - Pressure 68.9 - 137.8 KPa (10 - 20 PSI) 34.45 - 68.9 KPa (5 - 10 PSI) - - Vacuum - - 1.33 - 26.6 KPa (10 - 200 Torr) 0 - 2.66 KPa (0 - 20 Torr) Nozzle Diameter - - - < 3/64" - ½" (0.119 - .27cm) A B C D E POLYMER PROPERTY HEAT EXCHANGER PREHEATER DV-1 DV-2 NOZZLE DIAM. 1. Melt Flow Index 204.4-260°C T= (400-500°F) 260-287.8°C T= (500-550°F) 2. Mol. Wt. Dist. 148.9-204.4°C T= (300-400°F) 226.7-287.8°C T= (440-550°F) 3. Volatiles Level 148.9-204.4°C T= (300-400°F) 226.7-287.8°C T= (440-550°F) 0.397 to < 0.119cm (5/32" to < 3/64") 4. Swell Index 148.9-204.4°C T= (300-400°F) 226.7-287.8°C T= (440-550°F) 26.6 KPa (P= 200 Torr) P < 2.66 KPa (P < 20 Torr) 5. High Production Rates 204.4-260°C T= (400-500°F) 260-287.8°C T= (500-550°F) 13.3 KPa (p= 100 Torr) P > 2.66 KPa (p > 20 Torr) Table II indicates preferred ranges of parameters for obtaining the desired polymer properties as indicated in column 1 of Table II. In Table I the temperature ranges for the heat exchanger and the preheater are shown as 160 to 287.8°C (320 to 550°F) and 226.7 to 287.8°C (440 to 550°F) respectively. The pressure/vacuum of the vessels is indicated in the second line of Table I as being 68.9 - 137.8 KPa (10 to 20 psi) for the heat exchanger,34.45 to 68.9 KPa (5 to 10 psi) for the preheater, 1.33 to 26.6 KPa (10 to 200 Torr) for the first devolatilizer and 0.13 to 2.66 KPa (1 to 20 Torr) for the second devolatilizer. Line 3 of Table I indicates a preferred nozzle diameter in the second devolatilizer of from 0.397cm (5/32 inch) down to as small as 0.119cm (3/64 inch) and less. Table II indicates desirable ranges to obtain certain particular product properties in a monovinyl aromatic polymer containing rubber. For example, in line 1, to manipulate the final product and obtain the most desirable melt flow index, the system would be operated in such a manner that the first heat exchanger 11 is operated at a relatively high temperature, i.e., 204.4 to 260°C (400 to 500°F), in order to act as an additional reactor. The preheater would then be operated at an elevated temperature of 260 to 287.8°C (500 to 550°F). This would result in an additional 10 to 15 percent conversion occurring in the heat exchanger and a very low molecular weight product, thereby achieving a desirable melt flow index. Line 2 of Table II indicates a method of obtaining a high molecular weight product and a low molecular weight distribution. This prevents the formation of short polymer chains by operating the heat exchanger at a relatively low 148.9 to 204.4°C (300 to 400°F) thereby preventing rapid polymerization of any unreacted monomer into short polymer chains in the heat exchanger. The preheater then is operated at temperatures in the range of 226.7 to 287.8°C (440 to 550°F). Reduced volatiles levels in the finished polymer can be achieved by manipulating the temperature, pressure and mass flow rate in vessels 11, 12, 13, and 14; or alternatively, by changing the nozzle diameter in the second devolatilizer to sizes as low as 0.119cm (3/64") or less. Optimization of these three parameters is critical to yield materials with good properties and low levels of volatile materials. In the fourth line of Table II is a parameter indicated as "swell index" which relates to the amount of cross-linking of the rubber particles in the finished product. The swell index is manipulated by adjusting the vacuum levels in the two devolatilizers. The percent solids leaving the reactor R-1 in the polymer/monomer flow is approximately 70%. The final solids level at the exit line of devolatilizer 13 (DV-1) would normally be in the range of 99.5% when the vacuum in DV-1 is maintained at around 20 Torr. This results in a reduction in volatiles, but on the other hand, results in an undesirable swell index. The 99.5% solids level exiting DV-1 is a result of cross-linking of rubber particles in the high-impact polystyrene matrix which makes the rubber particles less flexible and therefore less desirable. By maintaining a solids content of 98.5% exiting the first devolatilizer, a greater flexibility in the rubber particles is achieved. By utilizing either an optimum nozzle diameter or the correct pressure and temperature through the second devolatilizer, one is able to manipulate the swell index by leaving some volatiles in DV-1, thus having a percent solids of only 98.5% rather than 99.5%. These remaining volatiles can then be removed in devolatilizer 14 as a result of a proper balance of strand diameter and pressure drop in the devolatilizer. If the operator of the present system wishes to maintain high production rates rather than concentrating on the aforementioned parameters, the manipulation involved would be to raise the temperature of the heat exchanger and utilize it as an additional reactor. This is indicated in line 5 of Table II wherein the temperature in the heat exchanger is maintained at a level of 204.4 to 260°C (400 to 500°F) and the temperature in the preheater at a level of 260 to 287.8°C (500 to 550°F). The vacuum level in DV-1 is maintained at around 100 Torr and in DV-2 at around 2.66 KPa (20 Torr). This results in high production rates but with a sacrifice in molecular weight distribution characteristics. Thus, the present invention discloses methods and apparatus for devolatilizing polymer from systems such as high-impact polystyrene manufacturing processes, which devolatilizing processes and apparatus allow the manufacturer to control several different parameters of the finished product, including melt flow index, molecular weight distribution, volatile levels, swell index and production rates. These are achieved by the use of a combination upflow heat exchanger, downflow heat exchanger and dual devolatilization tanks as well as temperature control, vacuum level control and nozzle diameter control to manipulate the various parameters and property characteristics of the finished product. During actual manufacturing runs of general purpose polystyrene and high-impact polystyrene using conventional processes, applicants were obtaining finished polymers with volatile contents no lower than 700 PPM. In order to reduce the volatile contents below this level it was necessary using conventional technology to utilize stripping agents such as steam stripping to further remove volatiles from the polymer without degrading the quality of the polymer. By utilizing the present invention however, it was found that by manipulating the operating conditions as described hereinabove, it was possible to obtain finished polymers with volatile contents of 200 PPM and less, without the need for extensive additional stripping methods such as steam stripping. CONDITIONS POLYMER PROPERTIES Exp. # # Heat Exchanger [T(°F)] T°C Preheat [T(°F)] T°C DV-1 [T(°F)] [P(Torr)] P (KPa) DV-2 [T(°F)] [P(Torr)] P (KPa) MFI MWD Residual SM (ppm) S.I. Rate Lbs/hr Kg/hr 1 260 (500) - 260 (500) 3.07 (23) 260 (500) 0.5 (4.0) 5.1 2.5 390 11.7 54.48 (120) 2 160 (320) 243.3 (470) 243.3 (470) 2.66 (20) 243.3 (470) 0.93 (7.0) 3.3 2.5 300 9.9 36.77 (81) 3 190.56 (375) 237.78 (460) 254.44 (490) 2.66 (20) 246.11 (475) 0.4 (3.0) 3.0 2.9 190 9.5 38.59 (85) 4 190.56 (375) 237.78 (460) 254.44 (490) 12.4 (93) 246.11 (475) 0.4 (3.0) 3.0 2.9 470 13.0 38.59 (85) 5 287.8 (550) - 271.11 (520) 2.4 (18) 271.11 (520) 0.4 (3.0) 2.2 3.9 500 - 27.24 (60) 6 137.78 (280) 265.56 (510) 271.11 (520) 2.53 (19) 271.11 (520) 0.44 (3.3) 3.3 2.6 240 - 34.05 (75) 7 129.44 (265) 281.67 (539) 271.11 (520) 2.4 (18) 271.11 (520) 0.33 (2.5) 1.8 2.2 210 - 34.96 (77) 8 148.89 (300) 260 (500) 260 (500) 2.4 (18) 260 (500) 0.4 (3.0) 1.8 2.7 210 - 29.51 (65) 9 260 (500) 260 (500) 271.11 (520) 2.66 (20) 271.11 (520) 0.48 (3.6) 6.9 2.9 280 - 36.77 (81) Table III above illustrates specific examples taken from pilot plant operations utilizing the process of the present invention. For example, the MFI can be varied from as low as 1.8 to as high as 6.9 by varying the temperature in the heat exchanger from 129.44 to 260°C (265°F to 500°F). The MWD can be adjusted from 2.2 to 3.9 by varying the temperatures in the heat exchanger from 129.44 to 287.8°C (265°F to 550°F). Production rates can be increased from a low of 27.24 Kg/hr (60 lbs/min). to a high of 54.48 (120), and swell index from 9.5 to 13. Additionally, various parameters can be varied to achieve optimum levels of different polymer properties. In some cases, one particular property of the polymer can be varied by more than one method. Certain properties, for instance, can be optimized by either adjusting the thermodynamic parameters of the process, including temperatures and pressures; or the properties can be optimized by adjusting a particular parameter such as strand diameter in DV-2. Strand diameter in this devolatilizer is normally varied by adjusting the nozzle flow diameter. As mentioned hereinabove, nozzle diameter is preferably in the range of 0.397cm (5/32") or less, and more preferably 0.119cm (3/64") or less. The minimum diameter of the nozzle in DV-2 is limited by the physical practicalities of forming many small holes in the hoop manifold 15, by the maximum practical workable pressure drop across the nozzles, by the maximum pressure rating of the manifold, and to a certain extent by the maximum desirable shear rate in the material being flowed through the nozzles. Although a specific preferred embodiment of the present invention has been described in the detailed description above, the description is not intended to limit the invention to the particular forms of embodiments disclosed therein, since they are to be recognized as illustrative rather than restrictive. For example, whereas particular heat exchanger configurations, such as upflow and downflow are disclosed in particular locations, it is clear that one skilled in the art could obtain similarly improved products by utilizing downflow or horizontal flow heat exchangers in place of upflow; and likewise could utilize upflow or horizontal flow heat exchangers in place of the disclosed downflow unit. Thus, the invention is declared to cover all changes and modifications of the specific examples of the invention herein disclosed for purposes of illustration within the scope of the claims.

Claims: A method of removing volatiles from newly polymerized monovinyl aromatic compounds, said method comprising the steps of: taking a product stream from a monovinyl aromatic polymerization stream; flowing said product stream through a heat exchanger into a first vacuum devolatilizer; flowing a partially devolatilized product stream from said first devolatilizer into a second vacuum devolatilizer operated at a greater vacuum than said first devolatilizer; flowing a devotatilized product stream from said second devolatilizer; and simultaneously drawing volatilized components from said vacuum devolatilizers, characterized in that , between the heat exchanger and the first vacuum devolatilizer, a devolatilizer preheater has been inserted for adding heat to said product stream so that the preheater is operated at a higher temperature than the heat exchanger, wherein said first vacuum devolatilizer is connected to said preheater. The devolatilization method of claim 1 wherein the heat exchanger is of the "upflow" type and the preheater is of the "downflow" type. The devolatilization method of claim 1 wherein said heat exchanger is operated at a temperature between 148.9 °C (300 °F) and 204.4 °C (400 °F) The devolatilization method of any one of the preceding claims wherein said preheater is operated at temperatures of from 226.7°C (440°F) up to 287.8°C (550°F). The devolatilization method of any one of the preceding claims wherein said second devolatilizer is a vertical falling strand devolatilizer having a plurality of polymer ejection nozzles mounted on a manifold, and said product stream is flowed through said nozzles in strands of less than 0.397cm (5/32 inch) diameter. The devolatilization method of claim 5 wherein said polymer strands are flowed through said nozzles in diameters of less than 0.198cm (5/64 inches). The devolatilization method of claim 6 wherein said strand diameters are no greater than 0.119cm (3/64 inches). The devolatilization method of any one of the preceding claims wherein said first devolatilizer is operated at a vacuum of 1.3 up to 26.6 KPa (10 up to 200 Torr). The devolatilization method of any one of the preceding claims wherein said second devolatilizer is operated at a vacuum of less than 2.66 KPa (20 Torr). The devolatilization method of claim 1 wherein the second vacuum devolatilizer has a plurality of strand-forming nozzles located therein. The devolatilization method of claim 10 wherein the melt flow index and molecular weight distribution of said product stream are varied by varying the amount of heat added to said product stream in said heat exchanger. The devolatilization method of claim 1 or claim 10 wherein said heat exchanger is operated at a temperature of between 148.9°C (300°F) and 204.4°C (400°F), and said preheater is operated at a temperature of between 226.7°C (440°F) and 287.8°C (550°F). The devolatilization method of claim 10 wherein the swell index of said product stream is varied by varying the level of vacuum in said vacuum devolatilizers and varying the size of said strand-forming nozzles. The devoiatilization method of claim 4 wherein the vacuum level in said first devolatilizer is maintained at around 26.6 KPa (200 Torr) and the vacuum level in said second devolatilizer is maintained at less than 2.66 KPa (20 Torr). The devolatilization method of claim 14 wherein said strand-forming nozzles have openings of less than 0.198 cm (5/64 inches) diameter. The devolatilization method of claim 10 wherein the volatile level of said product stream is reduced by maintaining said heat exchanger at a temperature of 148.9°C (300°F) to 204.4°C (400°F), said preheater at a temperature of 226.7°C (440°F) to 287.8°C (550°F), said first devolatilizer at a vacuum level of 1.33 ― 26.6 KPa (10-200 Torr), said second devolatilizer at a vacuum level of less than about 2.66 KPa (20 Torr), and said strand-forming nozzles at a diameter no greater than 0.119 cm (3/64 inches).

Inventors: BLACKMAR BRUCE P, DAVIS SCOTT W, SCATES ROBERT M, SOSA JOSE M, WAGUESPACK JAMES N, BLACKMAR, BRUCE P., DAVIS, SCOTT W., SCATES, ROBERT M., SOSA, JOSE' M., WAGUESPACK, JAMES N.
Applicants: FINA TECHNOLOGY, FINA TECHNOLOGY, INC.
Application year: 1995
Main classification: C08F6
IPC codes: C08F6