Method of ethylene polymerization for producing products having various properties with high productivity and a tubular reactor used therefor
A method for continuous ethylene polymerization under high pressure using a polymerization reaction zone comprises a primary reaction zone and a secondary reaction zone wherein the secondary reaction zone has a length of 1.5-6.5 times the length of the primary reaction zone and a cross-sectional area of 1.2-4 times the cross-sectional area of the primary reaction zone. Ethylene is fed continuously into the primary reaction zone at the starting point of the primary reaction zone. Low temperature initiator alone, or an initiator mixture containing mainly low temperature initiator is introduced into the primary reaction zone at the starting point of the primary reaction zone. Initiator alone or an initiator mixture is introduced into the secondary reaction zone at two or more different points of the secondary reaction zone. Ethylene polymer products of various physical properties are produced with high productivity, while the pressure drop is minimized.
1. A method for continuous ethylene polymerization using a polymerization reaction zone comprising a primary reaction zone and a secondary reaction zone according to the process sequence of the polymerization reaction, wherein the secondary reaction zone has the length of 1.5-6.5 times as long as the length of the primary reaction zone and the cross-sectional area of 1.2-4 times as large as the cross-sectional area of the primary reaction zone, and wherein ethylene is fed continuously into the primary reaction zone at the starting point of the primary reaction zone, low temperature initiator alone or initiator mixture containing mainly low temperature initiator is introduced into the primary reaction zone at the starting point of the primary reaction zone, and initiator alone or initiator mixture is introduced into the secondary reaction zone at two or more different points of the secondary reaction zone.
2. The method according to claim 1 , wherein the low temperature initiator is a compound which can initiate ethylene polymerization reaction at 140-160° C.
3. The method according to claim 1 , wherein the initiator mixture containing mainly low temperature initiator comprises 50 mol % or more of the low temperature initiator and does not comprise oxygen.
4. The method according to claim 1 , wherein the secondary reaction zone is divided into a front part and a latter part, and the latter part of the secondary reaction zone is cross-sectionally larger in area than the primary reaction zone and cross-sectionally smaller in area than the front part of the secondary reaction zone.
5. The method according to claim 1 , wherein at least one of the initiator introduced into the secondary reaction zone is a high temperature initiator alone or an initiator mixture containing mainly high temperature initiator.
6. The method according to claim 5 , wherein the high temperature initiator is a compound, which can initiate an ethylene polymerization reaction at 190-250° C.
7. The method according to claim 5 , wherein the initiator mixture containing mainly high temperature initiator comprises 50 mol % or more of the high temperature initiator, and does not comprise oxygen.
8. The method according to claim 1 , wherein ethylene is additionally fed into the polymerization reaction zone at one or more different points of the polymerization reaction zone excepting the starting point of the primary reaction zone.
9. The method according to claim 8 , wherein ethylene is additionally fed into the polymerization reaction zone at one or more points of the secondary reaction zone.
10. The method according to claim 1 , wherein ethylene is preheated before being fed into the polymerization reaction zone.
11. The method according to claim 8 , wherein ethylene is preheated before being fed into the polymerization reaction zone.
12. A tubular reactor for continuous ethylene polymerization having a polymerization reaction zone comprising:
a primary reaction zone having ethylene feeding part and initiator introduction part at the starting point thereof; and
a secondary reaction zone having two or more initiator introduction parts at different points thereof,
wherein the secondary reaction zone has the length of 1.5-6.5 times as long as the length of the primary reaction zone and the cross-sectional area of 1.2-4 times as large as the cross-sectional area of the primary reaction zone.
13. The tubular reactor according to claim 12 , wherein the secondary reaction zone is divided into a front part and a latter part, and the latter part of the secondary reaction zone is cross-sectionally larger in area than the primary reaction zone and cross-sectionally smaller in area than the front part of the secondary reaction zone.
14. The tubular reactor according to claim 12 , further comprising one or more additional ethylene feeding parts at one or more different points in the polymerization reaction zone excepting the starting point of the primary reaction zone.
15. The tubular reactor according to claim 14 , wherein the secondary reaction zone comprises the additional ethylene feeding part(s).
16. The tubular reactor according to claim 12 , further comprising ethylene preheating part(s) which is connected to the ethylene feeding part(s).
17. The tubular reactor according to claim 14 , further comprising ethylene preheating part(s) which is connected to the ethylene feeding part(s).