Title of Invention	A PROCESS FOR THE CONTINUOUS PRODUCTION OF A COMPOSITION COMPRISING RUBBER, HYDROCARBON RESIN AND SOLVENT
Abstract	The present invention relates to a process for the continuous production of a composition which is an adhesive formulation comprising rubber (20), a hydrocarbon resin (22) and a solvent (26) employing at least two two-screw extruders (10a, 10b) placed in series and the temperature of the composition which leaves the extruders is lower than the boiling point of the solvent at the process pressure.

Full Text

Improved process for the continuous production of a composition comprising rubber, hydrocarbon resin and solvent This invention relates to a process for the continuous production of a composition comprising rubber, hydrocarbon resin and solvent, in particular an adhesive formulation. The object of this invention is that of providing an improved process of the abovementioned type, in particular having marked versatility and which can be implemented through machinery of limited size. This object is achieved through a production process of the type indicated above, which is implemented through the use of two or more two-screw extruders placed in series. The use of several extruders placed in series allows very much greater flexibility in installation than in the case where a single extruder is used. The latter must in fact necessarily be of a very great length and is therefore not easily fitted into small spaces, apart from being intrinsically complex to make from the construction point of view. In addition to this, the use of separate extruders makes it possible to select the corresponding process parameters, such as temperature and rate of rotation of the screws and the like, independently and freely, so that the extrusion process can be adapted to specific operating requirements with great versatility- Advantageously the temperature at the outlet of each extruder is less than the boiling point of the solvent in which the other ingredients are dissolved. The two- screw extruders which can be used are of a conventional type, advantageously of the co-rotating type. Two-screw extruders of the contrarotating type may however be used. The extruders used have a ratio between the outside and inside diameters of the screws which preferably lies between 1.4 and 2.0 and even more preferably between 1.55 and 1.8, in order that their outer dimensions can be substantially reduced. If two extruders are used in series, the process according to the invention preferably provides for the addition of solvent in a fractionated way at a plurality of points downstream from the initial, section of the first extruder and at a plurality of points located along the second extruder. Again preferably, a fraction of solvent is added to the composition leaving the first extruder before it enters the second extruder. In preferred embodiments of the process according to the invention the rubber and the resin are all added to the initial section of the first extruder. As an alternative it is possible to add a fraction of the resin in the initial section of the first extruder and the remaining fraction at a point downstream from the initial section . of the first extruder. The rubber used may be selected from the group comprising natural rubbers, synthetic rubbers and their mixtures, for example styrene- isoprene-styrene (SIS) , styrene-butadiene-styrene (SBS) and "natural rubber" (NR) . As is known, a hydrocarbon resin is a resin prepared through the polymerisation of unsaturated constituents of coal tar, rosin or petroleum. Preferably hydrocarbon resins having adhesion-imparting properties, for example of the type marketed by the name of Escorez or Wing-tack and their mixtures, are used. The solvent is for example selected from the group comprising pentane, hexane, heptane, dichloropropane and their mixtures. Further features and advantages of this invention will be apparent from the . following detailed description with reference to the appended drawings, in which: Figure 1 diagrammatically illustrates two two-screw extruders placed in series, in which a process according to the invention is carried out, and Figures 2, 3 and. 4 diagrammatically illustrate corresponding pairs of two- screw extruders placed in series, in which corresponding further embodiments of the process according to the invention are carried out. A process for the continuous production of a composition comprising rubber, hydrocarbon resin and solvent provides for the use (Figure 1) of a first two-screw extruder 10a and a second one 10b, for example of the co-rotating type placed in series. In first extruder 10a there is a first length 12, a second length 14, a third length 16, a fourth length 18 and a fifth length 19 in succession. First length 12 is approximately 16-D long (whereby D is meant the diameter of one of the two screws of extruder 10a), second length. 14 is approximately 12 D long, third length 16 is approximately 12 D long, fourth length 18 is approximately 8 D long and fifth length 19 is approximately 20 D long. Rubber 20, a fraction of hydrocarbon resin 22, and conventional additives 24, for example antioxidising agents, are added at the start of first length 12. The ingredients added are homogenized in first length 12. The remaining fraction of resin 22 is added at the end of first length 12, "while a first fraction of solvent 26 is added in second length 14. The remaining ingredients are dissolved in solvent 26 in second length 14. Further fractions of solvent 26 are added respectively in third and fifth lengths 16, 19. Further dissolution of the remaining ingredients in solvent 26 takes place in lengths 16, 18 and 19. The temperature when the composition obtained, leaves first extruder 10a must necessarily be lower than the boiling point of solvent 26 at the process pressure. A further fraction of solvent 26 is then added to the composition leaving first extruder 10a, before it is placed in second extruder 10b. Advantageously the overall fraction of solvent placed in first extruder 10a or added to the composition leaving it comprises between 50 and 80% of the total. The remaining fraction is added in second extruder 10b. Within the latter there is a first length 287 a second length 30 and a third length 32 in succession. The first length 28 is approximately 15 D long (whereby D is meant the diameter of one of the two screws of extruder 10) , second length 30 is approximately 12 D long and third length 32 is approximately 12 D long. Further fractions of solvent 26 are added to first and second lengths 28, 3 0 respectively. Further dissolution of the remaining ingredients in solvent 26 takes place in lengths 28, 30, 32. Also the temperature of the composition obtained at the outlet from second extruder 10b must necessarily be less than the boiling point of solvent 26 at the process pressure. Advantageously the temperature of the composition within second extruder 10b is less than the temperature of the composition within first extruder 10a. The rotation speed of the screws of first extruder 10a lies for example between 20 and 300 rpm, while the rotation speed of the screws of second extruder 10b lies for example between 60 and 6 00 rpm. These rotation speeds may be adjusted independently of each other, so that the viscosity of the final composition can be controlled in the desired way. Preferably the rotation speed of the screws of second extruder 10b is greater than that of the screws of first extruder 10a. Another embodiment of the production process according to the invention is illustrated with reference to Figure 2. A first change in comparison with the preceding instance lies in the fact that solvent 25 is not added in second length 3 0 of second extruder 10b. A second change in comparison with the preceding instance lies in the fact that master batch 34 (comprising a concentrated mixture of dye in the resin) is added at the points where resin 22 is added. Yet another embodiment of the production process according to the invention is illustrated with reference to Figure 3. The only change in comparison with the situation in Figure 1 lies in the fact that no solvent 26 is added to the composition leaving first extruder 10a before it is placed in second extruder 10b. Another embodiment of the production process according to the invention is illustrated with reference to Figure 4. In this case first length 12 of first extruder 10a is 28 D long, equivalent to ttie sum of the lengths of the first and second lengths of the first extruder in Figure 3. In addition to this the whole quantity of resin 22 is added to the initial section of first length 12, after which the first addition of solvent 26 is instead made. The structure of the remaining parts of first extruder 10a and all of second extruder 10b, and the ways of adding the remaining fractions of solvent 26 remain unchanged in comparison with what has been described with reference to Figure 3. Of course, while the principle of the invention remains unchanged, details of embodiments and embodiments may vary widely from what has been described purely by way of example without thereby going beyond its scope. CLAIMS 1. Process for the continuous production of a composition 2. comprising rubber (20) , a hydrocarbon resin (22) and a 3. solvent (26) through the use of at least two- screw 4. extruders (10a, 10b) placed in series. 5. Production process according to claim 1, providing for 6. addition of the said solvent (26) at least. one point 7. downstream from the initial section of the first extruder 8. (10a). 9. Production process according to either of the preceding 10. claims, through the use of a first and a second extruder 11. (10a, 10b) placed in series. 4. Production process according to claim 3, in.which the said solvent (26) is added in a fractionated way at a plurality of points downstream from the initial section of the first extruder (10a) and at a plurality of points located along the second extruder (10b) . 5. Production process according to claim 4, in which a 6. fraction of solvent (26) is added to the composition leaving 7. the first extruder (10a) before it is placed in the second 8. extruder (10b) . 9. Production process according to any of the preceding 10. claims, in which, the said rubber (20) is added in the initial 11. section of the first extruder (10a) . 7. Production process according to any of the preceding claims, in which the said resin (22) is added in the initial section of the first extruder (10a). 8. Production process according to any of preceding claims 1 to 6, in which a fraction of the said resin (22} is added to the initial section of the first extruder (10a) and the remaining fraction is added at a point downstream from the initial section of the first extruder (10a) . 9. Production process according to any of the preceding claims 3 to 8, in which the rotation speed of the screws of the first extruder (10a) lies between 20 and 300 rpm, while the rotation speed of the. screws of the second extruder (10b) Lies between 60 and 600 rpm. Production process according to any of the preceding claims, in which the said rubber (20) is selected from the group comprising natural rubbers, synthetic rubbers and their mixtures • 11. Production process according to any of the preceding claims, in which the said hydrocarbon resin (22) has adhesion-imparting properties. 12; Production process according to any of the preceding claims, in which the said solvent (26) is selected from the group comprising pentane, hexane, heptane, dichlorppropane and their mixtures. 13. Production process according to any of the preceding claims, in which the said at least two two-screw extruders (10a., 10b) are of the co-rotating type. 14. Production process according to any of the preceding claims, in which at least one of the said at least two- screw extruders (10a, 10b) has a ratio between the outer diameter and the inner diameter of the screws lying between 1,4 and 2.0 and preferably between 1.55 and 1.8. 15. Production process according to any of preceding claims from 3 to 14, in which the temperature of the composition within the second extruder (10b) is less than the temperature of the composition in the first extruder (10a) . Dated this 1 day of May 2006

Documents:

1489-chenp-2006 complete specification as granted.pdf

1489-CHENP-2006 CORRESPONDENCE OTHERS.pdf

1489-CHENP-2006 CORRESPONDENCE PO.pdf

1489-CHENP-2006 FORM-18.pdf

1489-CHENP-2006 FORM-3.pdf

1489-CHENP-2006 PETITION.pdf

1489-CHENP-2006 POWER OF ATTORNEY.pdf

1489-chenp-2006-abstract.jpg

1489-chenp-2006-abstract.pdf

1489-chenp-2006-claims.pdf

1489-chenp-2006-correspondnece-others.pdf

1489-chenp-2006-description(complete).pdf

1489-chenp-2006-drawings.pdf

1489-chenp-2006-form 1.pdf

1489-chenp-2006-form 3.pdf

1489-chenp-2006-form 5.pdf

1489-chenp-2006-pct.pdf

1489-chenp-2006.tif