Reduction of fouling in high pressure reactors

Patent metadata

Field	Value
Publication number	US-9499645-B2
Application number	US-201514924952-A
Country	US
Kind code	B2
Filing date	Oct 28, 2015
Priority date	Dec 5, 2012
Publication date	Nov 22, 2016
Grant date	Nov 22, 2016

Abstract

The Application of equations of state to experimental and literature data permits the formation of a model and phase diagram(s) that show under what conditions polyethylene is likely to precipitate out of a high pressure solution of polyethylene in supercritical ethylene. This then permits a better definition to run a high pressure reactor to reduce the likelihood of phase separation, loss of cooling and potentially decomposition of the reactor contents.

First claim

What is claimed is:

1. A method to determine the curve of the liquid liquid equilibrium boundary as a function of molecular weight distribution (MWD) for a multitude of different products comprising from about 80 to about 100 wt. % of ethylene and about 0 up to about 20 weight % of one or more C 3-8 alpha olefins having a molecular weight from about 8,000 to about 500,000 produced in super critical ethylene in a high pressure reactor at temperatures from about 80° C. to about 350° C. and pressures from about 100 MPa to about 350 MPa comprising:
a) modeling experimental or literature data for the liquid liquid equilibrium using an equation of state model to describe the effects of the molecular weight and the polydispersity of the polyethylene on the liquid liquid equilibrium curve
b) determining the composition-specific parameters of the model from a); and,
c) applying an equation of state selected from PC-SAFT, SAFT-VR, SAFT-LJ, soft SAFT, SW-PC-SAFT, CK-PC-SAFT, and GC-SAFT-VR to the temperature, pressure and composition conditions of the reaction to generate the liquid liquid equilibrium boundary and optionally the critical polymer concentration.

2. The process according to claim 1 wherein the reactor is a tubular reactor.

3. A process to prepare a liquid polymer lean/liquid polymer rich and liquid liquid phase diagram for a reactor for polymerizing a system comprising a polymer having a weight average molecular weight from about 8,000 to about 500,000 comprising from about 80 to about 100 wt % of ethylene and about 0 to about 20 wt % of one or more C 3-8 alpha olefins in super critical liquid ethylene at temperatures from about 80° C. to about 350° C. and pressures from about 100 MPa to about 350 MPa to define operating conditions at which the polymer is substantially dissolved in the liquid phase comprising: preparing a phase diagram for liquid polymer lean/liquid polymer rich for said reactor and process at temperatures from about 150° C. to about 350° C. and pressures from about 100 to about 350 MPa;
b) inserting into said phase diagram a liquid liquid phase boundary determined according to claim 1 .

4. A method for conducting the polymerization of a polymer having a weight average molecular weight from about 8,000 to about 500,000 comprising about 80 to about 100 wt % of ethylene and about 0 to about 20 wt. % of one or more C 3-8 alpha olefins in super critical liquid ethylene at temperatures from about 80° C. to about 350° C. and pressures from about 100 MPa to about 350 MPa to define operating conditions at which the polymer is substantially dissolved in the liquid phase Comprising monitoring the heat balance of said reaction and determining when there is an apparent loss of cooling and comparing the operating conditions to the phase diagram according to claim 3 , and adjusting one or more of the temperature and pressure conditions to bring the operating conditions more than about 5% more within the liquid area of the phase diagram.

5. The method according to claim 4 , wherein the operating conditions are adjusted to bring them within the liquid area of the phase diagram by more than about 10%.

6. The method according to claim 5 , wherein the phase diagram is digitized and stored on a microprocessor and heat balance for the reaction is monitored using a microprocessor and the operating conditions are adjusted using a microprocessor.

7. A method to extend the run time between cleanings of a high pressures reactor for the polymerization of a polymer having a weight average molecular weight from about 8,000 to about 500,000 comprising about 80 to about 100 wt % of ethylene and about 0 to about 20 wt % of one or more C 3-8 alpha olefins in super critical ethylene at temperatures from about 80° C. to about 350° C. and pressures from about 100 MPa to about 350 MPa comprising operating according to claim 5 , so that not more than about 30 minutes elapse between the apparent loss of cooling and achieving the new operating conditions within the liquid area within the phase diagram.

8. The method according to claim 7 , wherein the time to achieve the adjusted operating conditions is less than about 15 minutes.

9. A method to dissolve precipitated polymer in a high pressures reactor for the polymerization of a polymer having a weight average molecular weight from about 8,000 to about 500,000 comprising about 80 to about 100 wt % of ethylene and about 0 to about 20 wt % of one or more C 3-8 alpha olefins in super critical liquid ethylene at temperatures from about 80° C. to about 350° C. and pressures from about 100 MPa to about 350 MPa comprising operating according to claim 7 , so that not more than about 30 minutes elapse between the apparent loss of cooling and achieving the new operating conditions within the liquid area within the phase diagram.

10. The method according to claim 9 , wherein the phase diagram is digitized and stored on a microprocessor and heat balance for the reaction is monitored using a microprocessor and the operating conditions are adjusted using a microprocessor.

11. The method according to claim 10 wherein the time to achieve the adjusted operating conditions is less than about 15 minutes.

Assignees

• Nova Chemicals International Sa

Inventors

• Tchir William Joseph
• Cheluget Eric

Classifications

• C08F10/02 Primary

  Ethene · CPC title

• C08F2/002

  Scale prevention in a polymerisation reactor or its auxiliary parts · CPC title

• C08F2/01 Primary

  characterised by special features of the polymerisation apparatus used · CPC title

• G16C20/10

  Analysis or design of chemical reactions, syntheses or processes · CPC title

• C08F110/02 Primary

  Ethene · CPC title