the present invention is directed to making tips materials from an elastomer and a monovinylaromatic polymer . the process eliminates many of the intermediate steps between the elastomer manufacture and the monovinylaromatic polymerization reactor system . this is done by polymerizing the elastomer from an elastomer monomer feedstock in a solvent that is compatible with the polymerization reaction for the monovinylaromatic monomer feedstock . in one preferred embodiment of the invention , the polymers utilized in making tips materials consisted of a polybutadiene elastomer and a polystyrene class of monovinylaromatic compound . in this embodiment of the invention , the butadiene monomer is polymerized in a solvent comprising a styrene monomer , using an elastomer reactor system that is unique to tips manufacture . upon satisfactory polymerization of the butadiene and styrene into random styrene - butadiene rubber , this elastomer reaction solution receives additional styrene monomer and is then reacted in a tips reactor system to form a transparent impact polystyrene material . in a similar manner , tips can be manufactured in the same equipment described in the above - mentioned klussman , et al , patent by selecting appropriate sb or sbs structures that will form lamellar or rod morphologies . thus , in the first reactor , a random sb rubber with a block of polystyrene ( ps ) is made with a structure represented by the following symbolic representation : wherein b represents a rubber molecule and s is a styrene molecule . this structure is the most likely to occur in such a reaction , since it is well known that a butadiene - rich random sb rubber results from the butadiene reacting faster than the styrene , causing the butadiene to be depleted before the styrene . the klussman system is utilized to form the random sb - block ps structure shown above in a diluent of cyclohexane or cyclopentane . this solution is then sent to the sol vent exchange section where the diluent is replaced by or “ exchanged ” with styrene monomer . after the “ exchange ” of styrene monomer for the cyclohexane or cyclopentane diluent , the resulting solution is then sent to a tips reactor system where additional structure changes occur to the molecule . these changes are the result of the grafting which occurs when the sb portion is polymerized in the presence of peroxide initiators . the resulting molecular structure can be symbolized by the following representation that is thought to occur as the random sb - ps material is polymerized into a graft - random sb - ps structure : referring now to the drawings , and more particularly to fig1 a photomicrograph is shown which represents the morphology of a standard tips material . fig2 offers a photomicrograph of the morphology of a standard tips material . a comparison of the two photos shows why tips materials are transparent . the structure of the rubber particles in the tips material is smaller than the wavelength of visible light , thereby allowing light to pass through the material unhindered , rendering the final product transparent ; whereas the rubber particles in the hips material are not smaller than the wavelength of visible light and the resultant hips material is hazy to solid white in appearance . fig3 is a schematic representation of the reactor system utilized to manufacture tips materials according to the present invention . for a more detailed description of this system refer to the klussman patent , which was incorporated by reference herein . generally , the reactor system of fig3 comprises a first reactor r 1 , a solvent exchange reactor ser , and a tips formation reactor r 2 . random sb - ps material is formed in r 1 similar to the method of manufacturing hips material as described by klussman . butadiene and styrene monomers are added to a compatible diluent such as hexane , cyclohexane or cyclopentane , and introduced into reactor r 1 . simultaneously , a polymerizing catalyst such as butyl lithium , is added to the feed solution . since the rate of polymerization of butadiene into rubber at 50 degrees c . is about 60 times greater than the rate of polymerization of styrene into polystyrene , cooling is necessary to allow removal of the exothermic heat of reaction and thereby slow the butadiene reaction down to a controllable level . once all of the butadiene is polymerized in the butadiene / styrene solution , the styrene will start to rapidly polymerize , so that it is necessary to “ kill ” or neutralize the reaction as the solution exits reactor r 1 and enters the solvent exchange reactor ser . this can be done by the addition of a neutralizer such as methyl alcohol or other alcohol or a phenol to neutralize the polyanions on the ends of the butadiene and polystyrene chains . it is possible to vary and control the elastomer concentrations in the final tips product by adjusting more than one operating parameter of the process illustrated in fig3 . for example , the elastomer concentration of the solution as it goes from r 1 to the ser can be as high as 30 weight percent , depending on the amount of elastomer initially added to the reaction , and depending upon the molecular weight of the constituents involved . the molecular weight of the elastomer can be controlled by varying the amounts of organo - lithium initiator used in the reactor . once the reaction solution goes to the ser , the elastomer concentration can also be varied by adjusting the ratio of styrene / diluent that is used ; and finally , the level of the sb - block ps in the final tips product can be varied depending on the conversion rate in the final reactor , r 2 . in one example , if a reaction solution is created in the first reactor by varying the above - mentioned parameters so that the solution has an elastomer concentration consisting of 12 weight percent random sb - ps coming out of r 1 , and the ser is run at conditions to achieve a one - to - one hexane / styrene exchange , the solution would enter r 2 with a 12 % sb - ps concentration . by then polymerizing styrene monomer in r 2 to a level of just 60 % ( decimally 0 . 60 ), the final elastomer concentration coming out of r will be increased by a factor of 1 /. 60 , or to 20 % in the final tips product . by setting original reaction concentrations to end up with an elastomer concentration ( random sb - block ps ) of 30 wt . % in the reaction solution coming from r 1 , the operator can end up with an elastomer concentration as high as 50 wt . %; i . e ., 30 %/. 60 = 50 %. it is believed that the maximum practical level of elastomer achievable in r 1 is in the range of about 30 wt . %, so that the maximum practical elastomer concentration obtainable in the final tips product would be about 50 %. a lower practical level of elastomer content for tips material would be about 6 wt . %, although lower levels are certainly possible with this process . the advantages of the process in making tips materials are obvious from this description given for fig3 : a . a wide range of random sb - ps elastomer tips materials can be made by changing the molecular weight and the ratio of butadiene to styrene in reactor r 1 ; b . the random sb - ps solution can be concentrated by adjusting the styrene / diluent ratio used in the ser ; and , c . the concentration of sb - ps in the final product can be changed by the amount of styrene converted in reactor r 2 . fig4 is a graphic representation of the times of conversion of a 75 / 25 bd / sm solution in different solvents at 122 degrees f . it can be seen from the graph that the fastest reaction of butadiene occurs in a toluene solvent and addition of the styrene occurs at about 120 hours . in toluene , addition of the styrene achieves the fastest bd / sm reaction as indicated by the steepness of the curve after 120 hours . the slowest solvent appears to be hexane which requires almost 480 hours for the butadiene to react to 80 % conversion and which then allows a very slow or gradual bd / sm conversion slope after the addition of the styrene . because of these slow rates of conversion , the conventional polybutadiene manufacturing process using one of these solvents as the butadiene diluent is very slow and must be so to provide control of the rapid exothermic reaction . however , as a result , the rates of conversion are also slow for conventional polybutadiene manufacture . fig5 is a table showing the properties of polybutadiene / styrene reactions in hexane wherein the ratios of bd to sm range from about 50 / 50 up to about 35 / 65 , using a butyl lithium initiator . fig6 is a graphic representation of the time - rate of conversion of butadiene into polybutadiene in the reactions utilizing hexane as a solvent , i . e ., runs # 22 - 25 . each line represents the amount of unreacted butadiene in the solution at any particular time . it can be seen that the concentration of bd is higher over time for run # 22 and the lowest for run # 24 . this graph shows that temperature and reaction time can be obtained that are suitable for a commercial process . the benefit from this is clearly that the reaction of bd into pb is much faster in sm but is still under control , thus allowing a controlled increase in conversion rates in the bd reactor and a consequent increase in commercial production rates with no adverse economic costs . fig7 is a table that shows the reaction conditions for runs carried out at high smibd ratios . the characterization of the materials is also shown . fig8 shows the morphology of a commercial finaclear 530 ( atofina petrochemicals , houston , tex .). fig9 and 11 show the morphologies that are obtained in runs 65 , 70 and 71 . it can be seen that the morphologies of the products show lamella and rod structures ; thus , the materials from the r 1 reactor system are clearly illustrated as being very useful for manufacturing tips . fig1 is a table of the reaction conditions for laboratory runs 65 , 70 , and 71 and a run using the commercial rubber , finaclear 530 . fig1 is a graphical representation that shows the polymerization conditions of solutions obtained from dissolving finaclear 530 , and from runs 65 , 70 and 71 in styrene . these solutions would have similar compositions as those exiting the solvent exchange system of fig3 . this figure shows % solids vs reaction time using the initiator lupesol 233 ( atofina chemicals , king of prussia , pa .). the conditions selected are those utilized in the r 2 reactor system employed to make hips or tips . fig1 shows the morphology of tips manufactured using finaclear 530 . fig1 , 16 and 17 show the morphology of tips obtained using materials from runs 65 , 70 and 71 . it is can be seen that the morphology of all of the samples are rod morphologies , similar to those obtained by blending finaclear 530 with gpps . fig1 shows the storage modulus ( g ′) from − 120 ° c . to + 30 ° c . it can be seen that the material made with commercial finaclear 530 has a modulus that is between those produced with laboratory samples . the glass transition temperature of the elastomer is identified by the abrupt change in g ′ that occurs around around − 50 ° c . the magnitude of g ′ indicates that the laboratory samples can be made stiffer ( higher g ′) or more flexible ( lower g ′). the importance of this observation is that the resulting tips materials can be made stiffer or more flexible by changing the ratio of sm / bd in r 1 . the results obtained by the present inventive process and apparatus clearly indicate that at 50 - 60 degrees c ., polymerization of 1 , 3 - budadiene in the presence of a styrene monomer solvent yields random copolymers of butadiene and styrene . the final products consist of styrene polymerized in the presence of sbr &# 39 ; s having 50 - 60 % styrene , and yield highly crosslinked materials that are clear and homogenous . the process is capable of manufacturing commercial tips materials at much less cost and much higher productivity levels .