CN1118341A - α-烯烃低聚为聚α-烯烃的方法 - Google Patents
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- 238000000034 method Methods 0.000 title claims description 27
- 229920013639 polyalphaolefin Polymers 0.000 title abstract description 5
- 239000003054 catalyst Substances 0.000 claims abstract description 16
- 239000013638 trimer Substances 0.000 claims abstract description 3
- 238000006384 oligomerization reaction Methods 0.000 claims description 16
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- 239000004215 Carbon black (E152) Substances 0.000 claims description 11
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- 125000004432 carbon atom Chemical group C* 0.000 claims description 5
- VSCWAEJMTAWNJL-UHFFFAOYSA-K aluminium trichloride Chemical compound Cl[Al](Cl)Cl VSCWAEJMTAWNJL-UHFFFAOYSA-K 0.000 claims description 4
- 238000005194 fractionation Methods 0.000 claims description 4
- 239000002904 solvent Substances 0.000 claims description 4
- KCXMKQUNVWSEMD-UHFFFAOYSA-N benzyl chloride Chemical compound ClCC1=CC=CC=C1 KCXMKQUNVWSEMD-UHFFFAOYSA-N 0.000 claims description 3
- 229940073608 benzyl chloride Drugs 0.000 claims description 3
- 238000004821 distillation Methods 0.000 claims description 3
- YNLAOSYQHBDIKW-UHFFFAOYSA-M diethylaluminium chloride Chemical compound CC[Al](Cl)CC YNLAOSYQHBDIKW-UHFFFAOYSA-M 0.000 claims description 2
- UAIZDWNSWGTKFZ-UHFFFAOYSA-L ethylaluminum(2+);dichloride Chemical group CC[Al](Cl)Cl UAIZDWNSWGTKFZ-UHFFFAOYSA-L 0.000 claims description 2
- NBRKLOOSMBRFMH-UHFFFAOYSA-N tert-butyl chloride Chemical compound CC(C)(C)Cl NBRKLOOSMBRFMH-UHFFFAOYSA-N 0.000 claims description 2
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- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 description 2
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- 125000000383 tetramethylene group Chemical group [H]C([H])([*:1])C([H])([H])C([H])([H])C([H])([H])[*:2] 0.000 description 2
- -1 Aluminum alkyl halide Chemical class 0.000 description 1
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- C07C2/00—Preparation of hydrocarbons from hydrocarbons containing a smaller number of carbon atoms
- C07C2/02—Preparation of hydrocarbons from hydrocarbons containing a smaller number of carbon atoms by addition between unsaturated hydrocarbons
- C07C2/04—Preparation of hydrocarbons from hydrocarbons containing a smaller number of carbon atoms by addition between unsaturated hydrocarbons by oligomerisation of well-defined unsaturated hydrocarbons without ring formation
- C07C2/06—Preparation of hydrocarbons from hydrocarbons containing a smaller number of carbon atoms by addition between unsaturated hydrocarbons by oligomerisation of well-defined unsaturated hydrocarbons without ring formation of alkenes, i.e. acyclic hydrocarbons having only one carbon-to-carbon double bond
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- C07C2/04—Preparation of hydrocarbons from hydrocarbons containing a smaller number of carbon atoms by addition between unsaturated hydrocarbons by oligomerisation of well-defined unsaturated hydrocarbons without ring formation
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Abstract
一种在均相液体催化剂存在下将α-烯烃低聚为聚α-烯烃的方法,α-烯烃可用作液体催化剂的溶剂,低聚反应在加压下进行,将α-烯烃和液体催化剂以溶液形式通过反应器,在其出口端排放出不同低聚度的α-烯烃和未转化的α-烯烃的混合物。用蒸馏法分离该混合物,将未转化的单体与一部分二聚物和三聚物以及碳原子数小于20的较轻α-烯烃一起循环到反应器的进口端并与α-烯烃混合,高级低聚物作为产品回收。
Description
本发明涉及在均相的液体催化剂存在下将α—烯烃低聚为聚α—烯烃的方法,α—烯烃也可以用作液体催化剂的溶剂,低聚反应在加压下进行,其步骤是将α—烯烃和液体催化剂以溶液形式通过反应器,在该反应器的出口端排放出由不同低聚度的α—烯烃和未转化的α—烯烃组成的混合物,将该混合物用蒸馏法分馏。
聚α—烯烃是合成油例如机油、传动油、电缆油和绝缘油生产中的主要成分。因此,它们具有显著的经济价值。
已知,在GB—PS 1,535,325中有一种低聚α—烯烃的方法。在该已知的方法中,采用具有至少3个碳原子的α—烯烃作为原料。它们被聚合为具有20—60个碳原子的低聚物。为此,在该已知的方法中,制备了含有两种催化剂组分的溶液,其溶剂或是待转化的单体或是另一种烃,将该两种溶液与液体单体一起加入反应器中。烷基铝卤化物和有机卤化物已被推荐作为催化剂组分。然后,将该反应混合物搅拌,所生成的反应产物,一部分用气—液相色谱测定,一部分用蒸馏法分离。
在该已知的方法中,对于未转化的单体以及沸点和粘度都很低的低聚物究竟如何处理均未分别加以说明。因此,该已知的方法需要加以改进。
就高级低聚物的产率而言,该已知的方法也需要改进。
在本说明的开始章节就提出了一种根据本发明的方法,其中将未转化的单体与一部分二聚物和三聚物以及碳原子数小于20的较轻α—烯烃一起循环到反应器的进口端并与α—烯烃混合,而高级低聚物则作为产品回收。
根据本发明的方法,将参与反应的物质即α—烯烃或α—烯烃的混合物(优选1—丁烯和1—己烯)首先与溶液中的催化剂混合,然后送入低聚反应器。
已经证实,适用于本发明的一种催化剂组分是乙基三氯化二铝,另一种组分是苄基氯。该两种化合物均为液体。优选未经稀释的状态使用,但是,也可以用溶剂例如1—己烯稀释。
已发现,乙基二氯化铝、二乙基氯化铝、三氯化铝以及叔丁基氯化物即使不属于最优选者,但是也适于作催化剂。
在放热的低聚反应过程中,为防止温度过度升高,在进入反应器之前,先将催化剂和α—烯烃原料冷却是有利的。在这种情况下,反应器同样需要稍加冷却。在某些情况下,在第一台低聚反应器的下游还安装了第二台反应器,以利于反应进行完全。
为了从反应混合物中将催化剂组分除去,可在低聚产物通过该反应器后将其通过例如装有硅胶或氧化铝凝胶的吸附塔。通过吸附塔后,将该低聚物的混合物送入降膜蒸发器。在该降膜蒸发器中进行C4/C6烃与该低聚物的分离。根据本发明,将C4/C6烃循环到第一台反应器并掺入到烃进料中。
可以使用装有内部构件的薄层蒸发器或精馏塔代替降膜蒸发器。然而,就所希望达到的目的即粗分离烃的混合物而言,结构较简单和较便宜的降膜蒸发器仍然是优选的。
从降膜蒸发器中排出的液态低聚物,实际上已成为沸点较高的物质,在减压下(任选在真空下),将其分馏为至多约C20和C(20+)的聚α—烯烃馏分,以便降低其沸点。相应地包括具有8—20个碳原子的烃的C(20-)馏分呈气态从分离塔的顶部排出,然后被冷却以便将其液化。它可以作为产品处理,但是,根据其组成并随烃混合物原料的组成而定,也可以再将该馏分添加到起始混合物中,按照与上述C4/C6烃馏分的相同方式重新进行低聚反应。
然后将分离塔底部排出的聚α—烯烃在另一台分离塔中再次分馏为重馏分和轻馏分,这些馏分分别地供给不同的用途。
在本发明的方法中,使低聚反应在温度为5—150℃和压力为10—50巴的条件下进行是有利的。
超过或低于上述温度和压力范围会产生以下缺点:
较低的压力和/或较高的温度导致在低聚过程中产生不符合要求的气相,而在较低的温度下反应进行得太慢。
根据本发明,将未转化的单体与低级低聚产物一起循环有利于显著提高产率从而节省原料。按GB—PS 1,535,325已知方法,中试(实施例VI)的产率仅达到56%(C24—C56),然而,本发明的方法却可以在工业规模将高级低聚物的产率提高到80%以上,参照以下具体的操作实施例将进一步证明上述结果。
此外,根据本发明将一定量的单体和/或低聚物进行循环,也可以使产品性能适合于特殊的要求。
下面,将通过以示意图表示的操作实施例对本发明作详细说明。
将1—丁烯(250kg/h)和1—己烯(250kg/h)作为原料通过管道1送入所述装置中。该混合物的温度为5℃。在将其送入反应器2之前,先与来自附图所示的贮槽3中的苄基氯(10kg/h)混合。此外,将来自附图所示的贮槽4中的乙基三氯化二铝(10kg/h)送入反应器的顶部。
反应器2是列管式反应器,低聚反应在管中进行。在该管的外壁空间用冷却剂包围,以消散反应放出的热量,冷却剂的进料和出料在图中仅示意地加以表示。该低聚物的混合物经过反应器2后,再通过管道5继续进入第二台无填充物的列管式低聚反应器6,低聚反应在其中进行直到反应完全。离开该反应器的闪蒸气体在冷却器7中冷却,然后再返回到反应器6。
将反应产物在冷却器8中冷却到80℃,然后从底部送入吸附塔9。吸附塔9装有氧化铝凝胶或硅胶的填料,其作用是通过吸附将催化剂组分从反应混合物中除去。为清楚起见,吸附塔9在示意图中仅示出一套。事实上安装了两套,以便在任一时间两台吸附塔之一可以按照现有技术以任选方式再生。
将已除去催化剂组分的聚α—烯烃混合物通过管道10送入降膜蒸发器11。降膜蒸发器11装配了加热介质在其中连续流动的加热套,其进料和出料在图中仅示意地加以表示。降膜蒸发器11中的温度保持为200℃,未转化的C4—C6烃与聚α—烯烃分离。将未转化的烃从降膜蒸发器11的顶部通过管道12排出,在冷却器13中冷却到8℃而液化,然后收集在分离器14中。从该处用泵15通过管道16和17将其再次循环到管道1,并在那里与烃的起始混合物混合。从分离器14循环的产物总量为400kg/h。
离开降膜蒸发器11的聚α—烯烃馏分,用泵37以600kg/h的流量通过管道18送入分离塔19的上部。分离塔19装有内部构件并有油槽式的加热装置(仅以示意图表示)。在分离塔19中,呈气态的C8—C20烯烃经过分离塔顶与高级低聚产物分离。由于该产品经过在塔中的处理已成为较高沸点的物质,因此,该塔在减压下操作从而使其沸点降低。在这种情况下,压力为0.1巴是适合的。塔顶馏分在冷却器20中冷凝,并收集在分离器21中。通过真空泵22使分离塔19保持在减压下操作。离开21的液体用泵23向前输送。一部分液体作为回流通过管道24返回到分离塔19。其余部分以180kg/h的流量作为产品通过管道25排放,如果不拟作为产品使用,则将其大部分(100kg/h)通过管道26返回到管道17,再次与原料混合。
分离塔19的底部产品用泵27并通过管道28输送到聚α—烯烃分离塔29的上部。该分离塔同样装有内部构件和油槽式的加热装置(仅以示意图表示)。它也可以在减压下操作,优选的压力为0.02巴。
在聚α—烯烃分离塔29中可使聚α—烯烃分离为较轻和较重的聚α—烯烃。约在C30—C36之间切取馏分。重聚α—烯烃作为产品通过管道30以240kg/h的流量排放。轻聚α—烯烃经过分离塔29,以气态形式的塔顶馏分在冷却器31中冷凝并收集在分离器32中。通过真空泵33使分离塔29保持在减压下操作。在32排放的液体压力在泵34中升高到4巴。一部分排放的液体,以180kg/h流量作为产品通过管道36排放。其余部分作为回流通过管道35返回到分离塔29。
Claims (9)
1.一种在均相的液体催化剂存在下低聚α—烯烃为聚α—烯烃的方法,α—烯烃也可以用作液体催化剂的溶剂,低聚反应在加压下进行,其步骤是将α—烯烃和液体催化剂以溶液形式通过反应器,在该反应器的出口端排放出由不同低聚度的α—烯烃和未转化的α—烯烃组成的混合物,将该混合物用蒸馏法分馏,其中将未转化的单体与一部分二聚物和三聚物以及碳原子数小于20的较轻α—烯烃一起循环到反应器的进口端并与α—烯烃混合,而高级低聚物则作为产品回收。
2.根据权利要求1的方法,其中α—烯烃单体包括C3—C18烃。
3.根据权利要求1的方法,其中该液体催化剂由乙基三氯化二铝和苄基氯组成。
4.根据权利要求1的方法,其中该液体催化剂选自乙基二氯化铝、二乙基氯化铝、三氯化铝以及叔丁基氯化物。
5.根据上述权利要求中任一项或多项的方法,在5—150℃的温度下进行。
6.根据上述权利要求中任一项或多项的方法,在10—50巴的压力下进行。
7.根据上述权利要求中任一项或多项的方法,基本上与上述的或列举的实例相同。
8.一种适用于上述权利要求中任一项或多项的方法的低聚装置。
9.根据权利要求8的装置,基本上与有关的或在附图中说明的相同。
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Application Number | Priority Date | Filing Date | Title |
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DEP4415912.9 | 1994-05-05 | ||
DE19944415912 DE4415912A1 (de) | 1994-05-05 | 1994-05-05 | Verfahren zur Oligomerisierung von alpha-Olefinen zu Poly-alpha-Olefinen |
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CN1118341A true CN1118341A (zh) | 1996-03-13 |
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Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
CN 95104800 Pending CN1118341A (zh) | 1994-05-05 | 1995-05-04 | α-烯烃低聚为聚α-烯烃的方法 |
Country Status (3)
Country | Link |
---|---|
EP (1) | EP0680942A1 (zh) |
CN (1) | CN1118341A (zh) |
DE (1) | DE4415912A1 (zh) |
Cited By (1)
Publication number | Priority date | Publication date | Assignee | Title |
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CN115040883A (zh) * | 2022-08-01 | 2022-09-13 | 中化泉州石化有限公司 | 一种用于乙烯齐聚生产a-烯烃的反应装置及反应方法 |
Families Citing this family (27)
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US6147271A (en) * | 1998-11-30 | 2000-11-14 | Bp Amoco Corporation | Oligomerization process |
US6239321B1 (en) * | 2000-02-28 | 2001-05-29 | Bp Amoco Corporation | Upgrading light oligomers |
WO2002088205A2 (en) * | 2001-04-27 | 2002-11-07 | Honam Petrochemical Corporation | Method for preparing polyalphaolefin from 1-octene |
US7989670B2 (en) | 2005-07-19 | 2011-08-02 | Exxonmobil Chemical Patents Inc. | Process to produce high viscosity fluids |
EP1910431B1 (en) | 2005-07-19 | 2013-11-27 | ExxonMobil Chemical Patents Inc. | Polyalpha-olefin compositions and processes to produce the same |
WO2007011462A1 (en) | 2005-07-19 | 2007-01-25 | Exxonmobil Chemical Patents Inc. | Lubricants from mixed alpha-olefin feeds |
US8535514B2 (en) | 2006-06-06 | 2013-09-17 | Exxonmobil Research And Engineering Company | High viscosity metallocene catalyst PAO novel base stock lubricant blends |
US8834705B2 (en) | 2006-06-06 | 2014-09-16 | Exxonmobil Research And Engineering Company | Gear oil compositions |
US8921290B2 (en) | 2006-06-06 | 2014-12-30 | Exxonmobil Research And Engineering Company | Gear oil compositions |
US8501675B2 (en) | 2006-06-06 | 2013-08-06 | Exxonmobil Research And Engineering Company | High viscosity novel base stock lubricant viscosity blends |
US8299007B2 (en) | 2006-06-06 | 2012-10-30 | Exxonmobil Research And Engineering Company | Base stock lubricant blends |
JP5555490B2 (ja) | 2006-07-19 | 2014-07-23 | エクソンモービル・ケミカル・パテンツ・インク | メタロセン触媒を用いたポリオレフィンの製造方法 |
US8513478B2 (en) | 2007-08-01 | 2013-08-20 | Exxonmobil Chemical Patents Inc. | Process to produce polyalphaolefins |
CN101925617B (zh) * | 2008-01-31 | 2012-11-14 | 埃克森美孚化学专利公司 | 在生产茂金属催化的聚α烯烃中线性α烯烃的改进利用 |
US8865959B2 (en) | 2008-03-18 | 2014-10-21 | Exxonmobil Chemical Patents Inc. | Process for synthetic lubricant production |
CN105175597A (zh) | 2008-03-31 | 2015-12-23 | 埃克森美孚化学专利公司 | 剪切稳定的高粘度pao 的制备 |
US8394746B2 (en) | 2008-08-22 | 2013-03-12 | Exxonmobil Research And Engineering Company | Low sulfur and low metal additive formulations for high performance industrial oils |
US8476205B2 (en) | 2008-10-03 | 2013-07-02 | Exxonmobil Research And Engineering Company | Chromium HVI-PAO bi-modal lubricant compositions |
US8716201B2 (en) | 2009-10-02 | 2014-05-06 | Exxonmobil Research And Engineering Company | Alkylated naphtylene base stock lubricant formulations |
US8530712B2 (en) | 2009-12-24 | 2013-09-10 | Exxonmobil Chemical Patents Inc. | Process for producing novel synthetic basestocks |
US8642523B2 (en) | 2010-02-01 | 2014-02-04 | Exxonmobil Research And Engineering Company | Method for improving the fuel efficiency of engine oil compositions for large low and medium speed engines by reducing the traction coefficient |
US8748362B2 (en) | 2010-02-01 | 2014-06-10 | Exxonmobile Research And Engineering Company | Method for improving the fuel efficiency of engine oil compositions for large low and medium speed gas engines by reducing the traction coefficient |
US8759267B2 (en) | 2010-02-01 | 2014-06-24 | Exxonmobil Research And Engineering Company | Method for improving the fuel efficiency of engine oil compositions for large low and medium speed engines by reducing the traction coefficient |
US8598103B2 (en) | 2010-02-01 | 2013-12-03 | Exxonmobil Research And Engineering Company | Method for improving the fuel efficiency of engine oil compositions for large low, medium and high speed engines by reducing the traction coefficient |
US8728999B2 (en) | 2010-02-01 | 2014-05-20 | Exxonmobil Research And Engineering Company | Method for improving the fuel efficiency of engine oil compositions for large low and medium speed engines by reducing the traction coefficient |
US9815915B2 (en) | 2010-09-03 | 2017-11-14 | Exxonmobil Chemical Patents Inc. | Production of liquid polyolefins |
JP5975408B2 (ja) | 2011-10-10 | 2016-08-23 | エクソンモービル ケミカル パテンツ インコーポレイテッド | ポリアルファオレフィン組成物及びポリアルファオレフィン組成物の製造方法 |
Family Cites Families (2)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US2389240A (en) * | 1940-11-07 | 1945-11-20 | Phillips Petroleum Co | Process for the conversion of hydrocarbons |
GB1535325A (en) * | 1975-11-27 | 1978-12-13 | Uniroyal Inc | Oligomerization of alpha-olefins |
-
1994
- 1994-05-05 DE DE19944415912 patent/DE4415912A1/de not_active Withdrawn
-
1995
- 1995-05-04 CN CN 95104800 patent/CN1118341A/zh active Pending
- 1995-05-04 EP EP95106749A patent/EP0680942A1/de not_active Withdrawn
Cited By (1)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
CN115040883A (zh) * | 2022-08-01 | 2022-09-13 | 中化泉州石化有限公司 | 一种用于乙烯齐聚生产a-烯烃的反应装置及反应方法 |
Also Published As
Publication number | Publication date |
---|---|
DE4415912A1 (de) | 1995-11-09 |
EP0680942A1 (de) | 1995-11-08 |
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