Patent ID: 10273318

Abstract:
The invention provides a process to prepare an ethylene-based polymer, said process comprising polymerizing ethylene in the presence of at least one initiator system selected from the following: a) class 1 initiator system, b) class 2 initiator system, c) class 3 initiator system, or d) a combination thereof; and at a inlet pressure (P2) greater than, or equal to, 1000 Bar (100 MPa); and in a reactor system comprising at least one hyper compressor and a reactor configuration comprising at least one reactor, which comprises at least one reaction zone; and wherein the inlet pressure (P2) is reduced by at least 200 Bar, as compared to a similar polymerization, in the same reactor system, except it is operated at a higher inlet pressure (P1), and at a different hyper compressor throughput, and at a different maximum temperature for at least one reaction zone, and optionally, at a different amount of CTA system fed to the reactor configuration; and wherein, for the process, the “Ratio of total reactor consumption of the highest temperature class initiator system(s) (Y)” meets the following Equation D: 0.95*x^((P1−P2)/10 MPa)<Y<1.04*z^((P1−P2)/10 MPa) (Eqn. D), wherein x is greater than, or equal to, 0.97; and wherein z is less than, or equal to, 1.03. The invention also provides a process to prepare an ethylene-based polymer, said process comprising polymerizing ethylene in the presence of at least one initiator system selected from the following: a) a class 1 initiator system, b) a class 2 initiator system, c) a class 3 initiator system, or d) a combination thereof; and at an inlet pressure (P2) greater than, or equal to, 1000 Bar (100 MPa); and in a reactor system comprising a reactor configuration comprising at least one reactor, which comprises at least one reaction zone; and wherein the inlet pressure (P2) is reduced by at least 200 Bar, as compared to a similar polymerization, in the same reactor configuration, except it is operated at a higher inlet pressure (P1), and at a different maximum temperature for at least one reaction zone, and optionally, at a different amount of CTA system fed to the reactor configuration; and wherein, for the process, the “Ratio of total reactor consumption of the highest temperature class initiator system(s) (Y)” meets the following Equation D: 0.95*x^((P1−P2)/10 MPa)<Y<1.04*z^((P1−P2)/10 MPa) (Eqn. D), wherein x is greater than, or equal to, 0.97; and wherein z is less than, or equal to, 1.03.