EXTRUSION PROCESS FOR GRAFTING RUBBERS
The invention relates to a process for producing a grafted rubber comprising: a) providing an ethylene propylene rubber having a weight average molecular weight (Mw) of at least 80 kg/mol in a continuous extrusion reactor by feeding the rubber in a slab/melt dosing unit and transporting the rubber to the continuous extrusion reactor by a melt pump; b) drying the rubber in the continuous extrusion reactor to a moisture content of between about 0.2 and about 0.5 wt %; c) providing the dried rubber to a first injection zone of the continuous extrusion reactor at a temperature of between 190 and 250° C., d) in the first injection zone, providing successively a first amount of maleic anhydride and a first free-radical initiator to the dried rubber; e) reacting maleic anhydride with the rubber in a first reaction zone of the continuous extrusion reactor to produce a grafted rubber; f) in a second injection zone, providing successively a second amount of maleic anhydride and a second free-radical initiator, the first and the second free radical initiator is an organic peroxide with a half-life (ty2) of more than 1 second if measured in mono-chlorobenzene at 220° C. g) applying shear to the grafted rubber in a second reaction zone of the continuous extrusion reactor, the shear sufficient to reduce the weight average molecular weight (Mw) of the grafted rubber by a factor of at least 2.
1 . A process for producing a grafted rubber comprising:
a) providing an ethylene propylene rubber having a weight average molecular weight (Mw) of at least 80 kg/mol in a continuous extrusion reactor by feeding the rubber in a slab/melt dosing unit and transporting the rubber to the continuous extrusion reactor by a melt pump;
b) drying the rubber in the continuous extrusion reactor to a moisture content of between about 0.2 and about 0.5 wt %;
c) providing the dried rubber to a first injection zone of the continuous extrusion reactor at a temperature of between 190 and 250° C.,
d) in the first injection zone, providing successively a first amount of maleic anhydride and a first free-radical initiator to the dried rubber;
e) reacting maleic anhydride with the rubber in a first reaction zone of the continuous extrusion reactor to produce a grafted rubber;
f) in a second injection zone, providing successively a second amount of maleic anhydride and a second free-radical initiator, the first and the second free radical initiator is an organic peroxide with a half-life (t 1/2 ) of more than 1 second if measured in mono-chlorobenzene at 220° C.
g) applying shear to the grafted rubber in a second reaction zone of the continuous extrusion reactor, the shear sufficient to reduce the weight average molecular weight (Mw) of the grafted rubber by a factor of at least 2.
2 . .A process according to claim 1 , wherein the rubber is dried to an amount of between about 0.2 and about 0.3 wt %.
3 . A process according to claim 1 , wherein the dried rubber is provided to the first reaction zone at a temperature of between about 195 and 220° C.
4 . A process according to claim 1 , wherein the wherein the organic peroxide is chosen from di-t-butyl peroxide, 2,5-dimethyl-2,5-di-(t-butylperoxy) hexane, 2,5-dimethyl-2,5-di-(t-butylperoxy) hexyne-3.
5 . A process according to claim 1 , wherein between 1.0 and 5.0 phr maleic anhydride and between 0.05 and 0.8 phr of the organic peroxide is introduced via the injection zones.
6 . A process according to claim 1 , wherein the total amount of maleic anhydride and peroxide is unevenly split between the first and the second injection zone.
7 . A process according to claim 1 wherein the continuous extrusion reactor has a length to diameter ratio of 56:1 or less.