Process to produce improved poly alpha olefin compositions
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IPC분류정보
국가/구분
United States(US) Patent
등록
국제특허분류(IPC7판)
C07C-002/04
C07C-002/02
C07C-002/00
C07C-002/06
C10M-105/04
C10M-169/04
C10M-103/00
C10M-105/32
C10M-169/02
C10M-171/02
C10M-107/10
C10M-111/04
출원번호
US-0612391
(2012-09-12)
등록번호
US-9365788
(2016-06-14)
발명자
/ 주소
Emett, Craig J.
Hagemeister, Mark P.
Harrington, Bruce A.
Lin, Chon Y.
Matsunaga, Phillip T.
Ruff, Charles J.
Stavens, Kevin B.
출원인 / 주소
ExxonMobil Chemical Patents Inc.
대리인 / 주소
Parsons, Luke A.
인용정보
피인용 횟수 :
0인용 특허 :
66
초록▼
This invention is directed to a two-step process for the preparation of improved poly alpha olefins wherein the first step involves oligomerizing low molecular weight linear alpha olefins in the presence of a single site catalyst and the second step involves oligomerization of at least a portion of
This invention is directed to a two-step process for the preparation of improved poly alpha olefins wherein the first step involves oligomerizing low molecular weight linear alpha olefins in the presence of a single site catalyst and the second step involves oligomerization of at least a portion of the product from the first step in the presence of an oligomerization catalyst. The dimer product from the first oligomerization is characterized by a tri-substituted vinylene olefin content of at least 25 wt %.
대표청구항▼
1. A process to produce a poly alpha olefin, the process comprising: a) contacting a first catalyst, an activator system, and a first monomer in a first reactor to obtain a first reactor effluent, the first reactor effluent comprises a dimer product, a trimer product, and optionally a higher oligome
1. A process to produce a poly alpha olefin, the process comprising: a) contacting a first catalyst, an activator system, and a first monomer in a first reactor to obtain a first reactor effluent, the first reactor effluent comprises a dimer product, a trimer product, and optionally a higher oligomer product,b) feeding at least a portion of the dimer product to a second reactor,c) contacting said dimer product with a second catalyst, and optionally a second monomer in the second reactor, wherein the second catalyst comprises a Lewis acid and is free of a metallocene compound, andd) obtaining a second reactor effluent comprising the poly alpha olefin,wherein the first monomer fed into the first reactor comprises one or more C6 to C24 olefins,wherein the first catalyst is represented by the formula of X1X2M1(CpCp*)M2X3X4 wherein M1 is a bridging element of silicon, M2 is a metal center of the first catalyst, Cp and Cp* are the same or different substituted or unsubstituted indenyl or tetrahydroindenyl rings that are each bonded to both M1 and M2, and X1, X2, X3, and X4 are independently selected from hydrogen, branched or unbranched C1 to C20 hydrocarbyl radicals, or branched or unbranched substituted C1 to C20 hydrocarbyl radicals; and the activator system is a combination of an activator and a co-activator, wherein the activator is a non-coordinating anion, and the co-activator is a tri-alkylaluminum compound wherein the alkyl groups contained in the tri-alkylaluminum compound are independently selected from C1 to C20 alkyl groups, wherein a molar ratio of the activator to the first catalyst is in a range of 0.1 to 10 and a molar ratio of the co-activator to the first catalyst is 1 to 1000, and the first catalyst, the activator, the co-activator, and the first monomer are contacted in the absence of hydrogen, at a temperature of 80° C. to 150° C., and with a reactor residence time of 2 minutes to 6 hours; andwherein the dimer product of the first reactor effluent contains greater than or equal to 50 wt % of tri-substituted vinylene represented by the following structure: wherein the dashed line represents two possible locations where unsaturated double bond may be located and Rx and Ry are independently selected from a C3 to C21 alkyl group. 2. The process of claim 1, further comprising separating at least a portion of the dimer product from the trimer and optional higher oligomer products prior to feeding said dimer product to the second reactor. 3. The process of claim 2, wherein said separating step comprises distillation. 4. The process of claim 1, wherein said portion of the dimer product from the first reactor is fed directly into the second reactor. 5. The process of claim 1, wherein the first reactor effluent further comprises unreacted monomer, and the unreacted monomer is fed to the second reactor. 6. The process of claim 1, wherein the first reactor effluent contains less than 50 wt % of di-substituted vinylidene represented by the following formula: RqRzC═CH2 wherein Rq and Rz are independently selected from alkyl groups. 7. The process of claim 1, wherein Rx and Ry are independently selected from a C3 to C11 alkyl group. 8. The process of claim 1, wherein the dimer product of the first reactor effluent contains greater than 60 wt % of tri-substituted vinylene dimer. 9. The process of claim 1, wherein the second reactor effluent has a product having a carbon count of C28-C32, wherein said product comprises at least 70 wt % of said second reactor effluent. 10. The process of claim 1, wherein the second reactor effluent has a kinematic viscosity at 100° C. in a range of from 1 to 3.6 sSt. 11. The process of claim 1, wherein the second monomer is selected from the group including 1-hexene, 1-octene, 1-nonene, 1-decene, 1-dodecene, and 1-tetradecene. 12. The process of claim 1, wherein the contacting in the first reactor occurs at a temperature range of 80° C. to 150° C. 13. The process of claim 1, wherein the contacting in the second reactor occurs at a temperature range of 15° C. to 60° C. 14. The process of claim 1, wherein the contacting in the first reactor occurs without addition of hydrogen to the reactor. 15. The process of claim 1, wherein the productivity rate in the step a) is greater than 4,000 gPAO/gcatalyst*hour, wherein gPAO/gcatalyst represents grams of poly alpha olefin formed per grams of the first catalyst used. 16. The process of claim 1, wherein a residence time in the first reactor is in a range of 1 to 6 hours and a residence time in the second reactor is in a range of 1 to 6 hours. 17. The process of claim 1, wherein the second catalyst further comprises a co-catalyst. 18. The process of claim 1, wherein the second catalyst comprises a Friedel-Crafts catalyst. 19. The process of claim 18, wherein the second catalyst is used with a protic promoter or activator. 20. The process of claim 1, wherein the second catalyst comprises BF3. 21. The process of claim 20, wherein the second catalyst is used with at least two different activators selected from alcohols and alkyl acetates.
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