[특허]Gas phase polymerization and method of controlling same

Union Carbide Chemicals & Plastics Technology Corporation

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특허 상세정보

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Gas phase polymerization and method of controlling same

특허상세정보
국가/구분	United States(US) Patent 등록
국제특허분류(IPC7판)	C08F-002/34 C08F-010/16 C08F-010/00
미국특허분류(USC)	526/060; 526/059; 526/901
출원번호	UP-0558941 (2004-05-26)
등록번호	US-7625987 (2009-12-16)
국제출원번호	PCT/US04/016549 (2004-05-26)
§371/§102 date	20060927 (20060927)
국제공개번호	WO04/111097 (2004-12-23)
발명자 / 주소	Parrish, John R. Lambert, Glenn A. Thomas, Daniel N.
출원인 / 주소	Union Carbide Chemicals & Plastics Technology Corporation
인용정보	피인용 횟수 : 1 인용 특허 : 38

초록
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A process for controlling a continuous gas phase exothermic process in a reactor comprising: (i) effecting a gas phase exothermic reaction under a set of operating conditions in the presence of a cooling agent, the cooling agent having a pre-selected concentration and feed rate of an induced cooling agent; (ii) determining a maximum production rate (I) without regard to limitations due to the cooling agent under the operating conditions; (iii) determining a maximum production rate (II) with regard to limitations due to the cooling agent under the operating conditions; (iv) calculating an optimal concentration of the induced cooling agent such that the difference between (I) and (II) is minimized; and (v) adjusting the feed rate of the induced cooling agent to achieve the concentration value calculated in (iv).

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What is claimed is: 1. A process for controlling a continuous gas phase exothermic process in a reactor comprising: (i) effecting a gas phase exothermic reaction under a set of operating conditions in the presence of a cooling agent, the cooling agent having a concentration and a feed rate of an induced cooling agent; (ii) determining a maximum production rate (I) without regard to limitations due to the cooling agent under the operating conditions; (iii) determining a maximum production rate (II) with regard to limitations due to the cooling agent under the operating conditions; (iv) calculating an optimal concentration of the induced cooling agent such that the difference between (I) and (II) is minimized; and (v) adjusting the feed rate of the induced cooling agent to achieve the concentration value calculated in (iv) wherein the cooling agent comprises reactants, inerts and the induced cooling agent. 2. The process of claim 1, wherein the continuous gas phase exothermic process is an ethylene polymerization process or a propylene polymerization process. 3. The process of claim 1, wherein the reactor is a fluidized bed reactor and comprises a reactor bed, a reactor outlet and a reactor inlet and the calculation of the optimal concentration of the induced cooling agent comprises: (i) calculating a cycle gas mass enthalpy at the reactor outlet conditions; (ii) calculating a total cycle gas inlet mass enthalpy at the reactor inlet conditions; (iii) calculating a change in the cycle gas mass enthalpy across the reactor bed; (iv) calculating a target cycle gas mass enthalpy change across the bed; and (v) iteratively calculating the concentration of the induced cooling agent that produces a cycle gas mass enthalpy change across the bed substantially equal to the target cycle gas mass enthalpy change across the bed. 4. The process of claim 1, wherein the operating conditions comprise an inlet temperature, a bed temperature, a reactor pressure, a cycle gas composition, and a weight percentage condensing of the reactor inlet stream. 5. The process of claim 1, wherein the production rate is calculated from the following equation: wherein Fresin is resin production, QL is heat loss to atmosphere, FRxin is reactor inlet flow, HRxino is reference enthalpy of reactor inlet flow, Fvap is vapor flow to reactor, Hvap is enthalpy of vapor feed to reactor, Fliq is liquid flow to reactor, Hliq is enthalpy of liquid feed to reactor, and ΔHrxn is heat of reaction. 6. The process of claim 3, wherein the cycle gas mass enthalpy of the reactor at outlet conditions is calculated by the following equation: Hbed=Hovap/wtmolg wherein, Hbed is the cycle gas mass enthalpy at reactor outlet conditions, Hovap is the vapor molar enthalpy of the cycle gas at the reactor outlet conditions, and wtmolg is the average molecular weight of the gas. 7. The process of claim 3, wherein the total cycle gas mass enthalpy at the reactor inlet is calculated by the following equations: HCvap=Hivap/wtmol g a. HCliq=Hliq/wtmol1 b. Hv1=Wtcnd*HCliq+(1-Wtcnd )*HCvap c. wherein HCvap is the vapor cycle gas mass enthalpy at reactor inlet conditions, Hivap is the vapor molar enthalpy of the cycle gas at reactor inlet conditions, wtmolg is the average molecular weight of the cycle gas, HCliq is the liquid mass enthalpy of the cycle gas at reactor inlet conditions, Hliq is the liquid molar enthalpy of the cycle gas at reactor inlet conditions, wtmol1 is the average molecular weight of the liquid, Hv1 is the total inlet mass enthalpy, and Wtcnd is the weight fraction of the condensed cycle gas at the reactor inlet. 8. The process of claim 3, wherein the change in the cycle gas mass enthalpy across the reactor bed is calculated by the following equation: H=Hbed-Hv1 wherein, H is the change in the cycle gas mass enthalpy across the bed, Hbed is the cycle gas mass enthalpy at reactor outlet conditions, and Hv1 is the total cycle gas mass enthalpy at reactor inlet conditions. 9. The process of claim 3, wherein the target cycle gas mass enthalpy change across the bed is calculated by the following equation: Htarget=H*PRnlc/PRlc wherein Htarget is the target cycle gas mass enthalpy change across the bed, H is the change in cycle gas mass enthalpy change across the bed, PRnlc is the production rate not limited by the cooling agent concentration, and PRlc is the production rate that is limited by the cooling agent concentration. 10. The process of claim 1, wherein the induced cooling agent is a liquid saturated hydrocarbon containing 3 to 7 carbon atoms or polymerizable condensable comonomers. 11. The process of claim 1, wherein the induced cooling agent is isopentane. 12. The process of claim 1, wherein the induced cooling agent is hexane. 13. The process of claim 3, wherein the iterative calculation of the concentration is achieved by a bisection method, a Newton method, a secant method, or a regula falsi method. 14. The process of claim 1, wherein the induced cooling agent is a gas inert to the process. 15. The process of claim 1, wherein the induced cooling agent is an induced condensing agent. 16. The process of claim 15, wherein the induced condensing agent is a saturated hydrocarbon containing 3 to 7 carbon atoms. 17. The process of claim 16, wherein the induced condensing agent is isopentane. 18. The process of claim 16, wherein the induced condensing agent is hexane. 19. The process of claim 2, wherein ethylene and at least one alpha-olefin are polymerized. 20. The process of claim 2, wherein ethylene is polymerized. 21. The process of claim 19, wherein the alpha-olefin comprises one or more C3-C12 alpha-olefins. 22. The process of claim 1, wherein the induced cooling agent is non-condensable. 23. The process of claim 1, wherein the reactants, the inerts, and the induced cooling agent are all condensing. 24. The process of claim 1, wherein the reactants, the inerts, and the induced cooling agent all are not condensing. 25. The process of claim 1, wherein the reactants are condensing but the inerts and the induced cooling agent are not condensing. 26. The process of claim 1, wherein the reactants and the inerts are condensing and the induced cooling agents are not condensing. 27. The process of claim 1, wherein the reactants and the induced cooling agent are not condensing and the inerts are condensing. 28. The process of claim 1, wherein the reactants and the induced cooling agent are condensing and the inerts are not condensing. 29. The process of claim 1, wherein the inerts and the induced cooling agent are condensing and the reactants are not condensing. 30. The process of claim 1, wherein the induced cooling agent is condensing but the reactants and the inerts are not condensing.

이 특허에 인용된 특허 (38)

이 특허를 인용한 특허 피인용횟수: 1

Meier, Gerhardus; Schueller, Ulf; Fibla, Claudio; Mihan, Shahram. Olefin polymerization process. USP20190210202472.

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Gas phase polymerization and method of controlling same

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Gas phase polymerization and method of controlling same

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