CN1376088A - 供给催化剂湿润剂的稀释剂滑流 - Google Patents

供给催化剂湿润剂的稀释剂滑流 Download PDF

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CN1376088A
CN1376088A CN00804721A CN00804721A CN1376088A CN 1376088 A CN1376088 A CN 1376088A CN 00804721 A CN00804721 A CN 00804721A CN 00804721 A CN00804721 A CN 00804721A CN 1376088 A CN1376088 A CN 1376088A
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J·D·霍托维
D·H·伯恩斯
S·E·库菲尔德
T·罗特曼
R·维德亚纳坦
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Abstract

一种用于将包括固态聚合物、未反应的单体、稀释剂和微量污染物的聚合反应流出物送到高压闪蒸区的方法和装置,在高压闪蒸室大部分流体成分被闪蒸,其中包含稀释剂和微量单体的滑流从闪蒸的流体成分中被分离出来。该滑流经过烯烃的去除得到一种基本上不含烯烃的物流而再循环至催化剂浆料制备区。虽然去除其它污染物的处理步骤是可以非必要进行的,但是大部分闪蒸后的流体成分直接再循环至聚合反应区而不需要昂贵的去除烯烃步骤。聚合物和夹带的流体被送到一个低压闪蒸区,在这里流体被闪蒸、压缩并与来自高压闪蒸罐的闪蒸物相混合。因为大部分流体在高压闪蒸区被除去,因而产物流体在再循环之前的压缩和冷却被保持在最低限度。

Description

供给催化剂湿润剂的稀释剂滑流
发明背景
本发明涉及单体在液态稀释剂中的聚合。
加聚反应一般在液体中进行，该液体是所得到的聚合物的溶剂。在二十世纪五十年代，当高浓度(线性的)乙烯聚合物第一次应用于商业上时就是采用上述方法。人们很快发现制造这种聚合物的更有效的方法是在浆液条件下进行聚合。更具体地说，所选择的聚合技术是在管道回路反应器中进行的连续浆液聚合。在聚合之后，该聚合物须从稀释剂中被分离出来且回收的稀释剂再循环使用。
用于该反应的固体催化剂优选首先与稀释剂混合，所得到的催化剂浆料被导入反应器内。
不管是严格的环保标准还是经济成本都要求在这种方法中产生尽可能少的废物。因此，现代化的浆液厂在分离和稀释剂回收过程中应尽可能少“排放”稀释剂，以使只需要补充少量稀释剂。事实上，所需补充的稀释剂的量是如此之少，以致于补充的稀释剂的量不足以产生催化剂浆料，因此一定要使用再循环稀释剂。然而，再循环稀释剂不可避免地含有一些溶解于其中的未反应的单体。虽然含有一些单体是可以接受的，但是在这一步骤中优选是不含单体的稀释剂。此外，使聚合物分离和稀释剂回收复杂化的原因是在再循环稀释剂中存在少量其它的不想要的化合物，如除了稀释剂之外的烷烃，除了单体之外的烯烃，在反应器中产生的极低分子量的低聚物如二聚物和三聚物，惰性材料如氮气，最后是氧，由于氧会使催化剂中毒因而必须将其除去或至少基本上除去。
发明概述
本发明的目的是提供一种用于聚合物回收和稀释剂再循环的方法和设备，其中不含单体的稀释剂可用于制备催化剂浆料。
本发明的另一个目的是简化了在浆液烯烃聚合方法中聚合物回收和稀释剂再循环所需要的设备和方法步骤；及
本发明的再一个目的是省去了从直接再循环回至反应器的稀释剂中分离出单体的步聚。
此外，本发明的目的是减少了所需要的蒸汽压缩量。
根据本发明，聚合反应区的流出物被分离为聚合物物流和稀释剂物流；然后滑流从稀释剂物流中分离开来，经过除去单体之后到达催化剂混合区，剩余的稀释剂物流被再循环至聚合反应区。
附图的简要说明
在构成本说明书一部分的附图中，
该附图是浆液聚合方法的示意图，其中滑流从稀释剂再循环物流中分离出来以提供用于湿润催化剂的不含单体的稀释剂。
发明详述
令人惊奇的是，通过从高压闪蒸塔塔顶取出被单体和共聚单体污染的稀释剂滑流，将该滑流与新鲜的共聚单体进料混合后送入共聚单体净化塔，然后把这样得到的部分净化的稀释剂滑流送到轻烯烃去除塔，净化塔的数量可以被分成两个，且过程操作上只需要较少量的总能量。更让人意想不到的是取出被少量共聚单体污染的物流并将其与相对大量的新鲜共聚单体混合会带来好处而不是坏处。
本发明适用于至少一种单体在至少基本上没有反应性的液体中发生的任何聚合反应。
本发明尤其适用于在稀释剂中的烯烃聚合反应，其中所得到的聚合物在聚合反应条件下是不溶的。本发明更特别适用于在使用稀释剂的回路反应器中进行的任何烯烃聚合反应，从而得到聚合物和稀释剂的产物浆液体。适合的烯烃单体是每分子有多至8个碳原子且没有距离双键比距离4-位更近的支链的1-烯烃。本发明尤其适用于乙烯和高级1-烯烃的共聚合反应，所述高级1-烯烃如丁烯、1-戊烯、1-己烯、1-辛烯和1-癸烯。特别优选的是乙烯和相对于乙烯和共聚单体的总重为0.01-10wt.％，优选为0.01-5wt.％，最优选为0.1-4wt.％的高级烯烃。另一方面足够量的共聚单体被用来提供上面所描述的结合在聚合物中的共聚单体量。
适合的稀释剂(与溶剂或单体不同)在本领域中是已知的，包括在反应条件下是惰性和液态的烃。适合的烃包括异丁烷、正丁烷、丙烷、正戊烷、异戊烷、新戊烷和正己烷，特别优选异丁烷。
用于浆液烯烃聚合反应的适合的催化剂在本领域中是已知的。特别适合的是广泛公开的负载在载体(如二氧化硅)上的氧化铬，例如，在Hogan and Banks，US2,285,721(1958年3月)中所述的，其中公开的内容在这里引作参考。这里所说的二氧化硅载体还包括任何已知的含二氧化硅的载体，如二氧化硅-氧化铝、二氧化硅-氧化钛和二氧化硅-氧化铝-氧化钛。也可使用任何其它已知的载体(如磷酸铝)。本发明还适用于使用有机金属催化剂的聚合反应，所述催化剂包括那些在本领域中常被称为“Ziegler”的催化剂。
在这种使用回路反应区域的聚合反应中，使用定位支路(settling legs)可以间歇地取出聚合物(混合有稀释剂)，这在本领域是已知的。然而，反应器流出物优选连续地被取出，这是可行的，例如通过在尽可能高的固体浓度下操作反应器。对于典型的0.936-0.970密度聚合物(更一般的是0.950-0.960)来说，这意味着相对于反应区域的聚合物微粒和稀释剂的重量可能至少有40wt.％的固体。对于其它树脂，所述固体可能高达70wt.％或更高。对于较低密度树脂(0.920-0.935)来说，所述固体含量相对于反应区域的聚合物微粒和稀释剂的重量一般为20-30wt.％。虽然连续卸料与从定位支路间歇卸料相比具有一些优点，然而它也存在如下缺点，即较多的稀释剂随着聚合物一起被卸出。根据本发明一个优选的实施方案，将高压闪蒸(例如加热反应器的流出物)与低压闪蒸和最多只需经过最小的净化(即比如除去氧、和/或水)的大部分稀释剂的再循环相结合，且取出经过进一步处理除去了单体的再循环稀释剂滑流提供用于催化剂制备的不含单体的稀释剂，从而提供了一种特别有效的方法。这种方法的好处还在于通过仅仅使用两个蒸馏塔代替四个蒸馏塔，既降低了建造费用又降低了操作费用。
现在参照附图对本发明的一个实施方案进行说明，附图显示了一个具有垂直段12、上部水平段14和下部水平段16的回路反应器10。所述上部和下部水平段确定了上部和下部水平流动区域。另一方面，该上部和/或下部段可以是连续的曲线形结构，即两个肘管连接在一起。所述反应器可以通过传统装置冷却，如两管式热交换器。每一段通过光滑的弯管或肘管18和下一段相连，因而提供了一种基本上没有内部障碍物的连续流动通道。聚合反应混合物在电机20驱动的叶轮(图中未示出)的作用下循环流动。大致地设计了一个用于连续地卸出中间产物浆液的细长中空附件22。图中显示连续的卸料机构22紧邻其中一个下部水平反应器回路段16的下游末端并紧邻连接肘管18设置。
图中显示了连续的卸料附件位于回路反应器的下部水平段的下游末端，这是一个优选的位置。另一个优选的位置是在下降的(基于流向)垂直段的肘管的底部。该位置可以在靠近回路中最末端的区域。在这里流体在催化剂导入位置之前向上流动，从而使得新鲜的催化剂在第一次通过卸料点之前可以在反应器中得到最大可能的停留时间。然而，连续卸料附件可以位于任何段或任何肘管处。
被连续回收的中间产物浆液(反应器流出物)通过聚合反应流出物回收管道24流到高压闪蒸室28。会使催化剂失效的水或其它适宜的试剂一般通过水注入管道26注入。由于这些物质本身会使催化剂中毒，一定要将它们从流向反应器的再循环中除去或至少基本上除去。管道24包括一个装有加热流体的套管30，该加热流体可以直接加热聚合反应流出物回收管道24中的浆液物质，因而提供了一个闪蒸管式加热器在反应器流出物导入主蒸汽分离闪蒸区—高压闪蒸室28之前对其进行加热。
在实施方案中显示的包括大部分非固态聚合反应流出物成分的蒸汽通过高压闪蒸汽体管道32被回收。该蒸汽主要是异丁烷稀释剂，还含有大多数未反应的乙烯和1-己烯单体。固体(聚合物)及夹带的少量溶剂和单体通过高压闪蒸室固体回收管道34回收，所述管道34包含上部阀36和下部阀38。阀36定期被打开以使聚合物通过管道34向下流动。然后阀36关闭而阀38打开以使得聚合物流出而进行回收，同时不可避免地使一些回流的蒸汽进入两阀之间的管道34的区域。如果有任何的聚合物微粒随着蒸汽向上流动，那么可以通过传统的过滤器和/或旋风分离器将它们除去。
管道34中回收的固体被放空后进入第二闪蒸区——低压闪蒸室40，在这里该固体从夹带的液体和/或蒸汽中分离出来。该固体通过具有上部阀44和第二下部阀46的管道42流动，阀44和46的操作方式与阀36和38一样。然后，所得到的聚合物可以通过传统的最后工序(如螺杆挤出机)进行加工。
来自低压闪蒸室40的塔顶馏出物(该馏出物含有大量的夹带的液体和/或蒸汽)通过低压闪蒸气体管道48到达压力装置，如第一段闪蒸气体压缩器50、闪蒸气体冷却器52和第二段闪蒸气体压缩器54。所得到的含有微量其它物质(低聚物、氢气、甲烷、乙烷、丙烷和水)的经压缩和冷却的气体(主要是稀释剂、单体、氮气、丁烷和己烷)与管道32中运送的高压闪蒸气体混合后供至混合后的闪蒸气体管道58。混合后的闪蒸气体物流然后流过脱氧床60。
由于氧通常会使催化剂中毒，所以优选使管道58中运送的全部物流经过脱氧步骤。当新鲜的乙烯进料物流离开供应器之后，由于新鲜的乙烯进料流通常几乎不含氧从而不会使催化剂中毒。如果新鲜的乙烯含有氧，那么在将其用作单体前一般要经过净化步骤。不管怎样，新鲜的主单体(如乙烯)一般要通过主单体处理器(如图中的标号83所示)以除去水和任何其它存在于新鲜乙烯中的会使催化剂中毒的物质，如CO、CO2、含硫化合物或本领域已知的被氧化的化合物。
来自脱氧床60的流出物通过脱氧的闪蒸气体(总稀释剂再循环)管道62到达稀释剂再循环冷却器68。在这个位置滑移管道被引出以用于除去特殊的单体，这可以通过下述方式完成，即借助于稀释剂再循环蒸汽滑流管道64或稀释剂再循环液体滑流管道66或者上述两种管道来引出蒸汽物流，如果需要的话，可以通过阀(图中未示出)来控制这些管道。
大部分含有单体的再循环稀释剂通过稀释剂再循环平衡容器进料管70流到稀释剂再循环平衡(贮藏)容器72。容器72用作闪蒸罐，因为它是一个蒸汽-液体分离鼓。轻组分(主要是乙烯单体和稀释剂)通过轻组分除去管道76闪蒸出来并成为再循环管道78内混合的稀释剂滑流的一部分。包括稀释剂、1-己烯单体及乙烯单体的大部分再循环物流借助于主稀释剂再循环管道74直接流回到反应器而不需要经过任何单体去除步骤。如果需要的话，其它的净化步骤(如除去水)可以在该物流回路上进行，例如通过共聚单体和再循环稀释剂处理器75。
因而发现在物流62中的全部稀释剂再循环被分开进入混合的稀释剂滑流再循环管道78和主稀释剂再循环管道74。
在本发明一个更具体的实施方案中，如果过量的轻组分(例如，即氮气、乙烷、丙烷)在主稀释剂再循环管道74积聚，更多量的稀释剂蒸汽滑流可借助管道64和/或76回收，优选借助管道76回收。
类似地，为了控制主稀释剂再循环管道中的重组分(如正己烷或低聚物)，增加的液体再循环可借助稀释剂再循环液体滑流管道66而被回收。
新鲜的1-己烯共聚单体通过己烯共聚单体进料管道86输入并被送到己烯脱气和重组分去除塔92。
己烯脱气和重组分去除塔92的塔顶馏出物通过己烯脱气塔顶管道94被排出并导入到脱气和轻组分去除塔98中。如图中所示新鲜的稀释剂(这里用的是异丁烷)通过新鲜的稀释剂补充管道84被输入。因为全部过程的高效率因而只需少量的补充稀释剂，例如每小时的补充量小于1wt.％，相对于反应器中生成的每磅聚合物一般只有约0.001-0.5磅，优选0.005-0.01磅。因为管道94中运送的物流主要含带有一些乙烯的异丁烷，其中乙烯可以很容易地在塔98中被分离并通过蒸汽去除管道100排出，因而为方便起见，新鲜的稀释剂补充管道84和己烯脱气塔顶馏出管道94可以合并成异丁烷脱气和轻组分去除塔入口管道96。在塔98中除了可以从新鲜的和再循环的异丁烷中除去乙烯，还可以从新鲜的和再循环的异丁烷中除去氧气和氮气。这些被除去的物质可以送去燃烧，或者氧气和氮气可以从乙烯中分离出来，回收的乙烯可通过传统的设备(图中未示出)再循环至反应区域。
混合后的滑移通过管道78被送到己烯脱气和重组分去除塔92，所述塔92是一个用于净化新鲜的1-己烯单体的标准部件。通过管道94除去塔92中的轻组分(异丁烷和乙烯)，及通过管道112除去塔92中的己烷从而在塔92中产生净化的1-己烯(通过管道110回流至反应区域)。
根据本发明，通过将含有不想要的单体的滑流稀释剂物流导入塔92中而使其得到净化，和它一起导入的还有全部新鲜的1-己烯单体。例如通过下述方式完成，将混合滑流管道78和新鲜的1-己烯单体导入管道86连接在一起以形成通往塔92的己烯脱气和重组分去除塔入口管道90。当然如果需要精确调节两种不同的进料物流的导入点，则可使用管道78和86分别导入。
如果需要的话，其它少量含稀释剂的物流也可以被输送到脱气塔92，所述物流如fluff drying purge(典型地除含稀释剂之外，还含有少量的轻组分如氮气、乙烯和1-己烯共聚单体)。
再循环稀释剂然后通过不含烯烃的稀释剂再循环管道102从脱气和轻组分去除塔98中回收。泵103用于使液体滑流再循环稀释剂回流到催化剂混合区域并提高反应器内的压力。在管道102上还可以存在冷却器(图中未示出)。该物流已经在塔92中除去了1-己烯共聚单体及在塔98中除去了乙烯单体(通过管道100排出)。经过这样净化的滑流再循环稀释剂被导入催化剂浆料罐106中，并在这里与通过催化剂管道104导入的干燥的催化剂相混合。所得到的催化剂/净化浆料然后通过催化剂浆料导入管道108用来自管道109的异丁烷冲入反应区域。
此外关于新鲜进料的管道，还提供了一个非必要成分的进料管道80用于任何其它可能需要的成分，如用于控制分子量的氢。
主单体进料(在实施方案中描述的是乙烯)通过新鲜的主单体进料管道82被输入。管道74、80和82可以分别导入反应区域或连在一起形成混合的新鲜乙烯和主稀释剂再循环管道88(如图中所示)。
高压闪蒸室区域的操作压力为100-1500磅/平方英寸(7-105kg/cm2)，优选125-275磅/平方英寸(8.8-19kg/cm2)，更优选150-250磅/每平方英寸(10.5-17.6kg/cm2)。该高压闪蒸室区域的操作温度为100-250°F(37.8-121℃)，优选130-230°F(54.4-110℃)，更优选150-210°F(65.6-98.9℃)。一般地，较窄的范围尤其适于使用1-已烯共聚单体和异丁烷稀释剂的聚合反应，较宽的范围适于高级1-烯烃共聚单体和烃稀释剂。
低压闪蒸室区域的操作压力为1-50磅/平方英寸(0.07-3.5kg/cm2)，优选5-40磅/平方英寸(0.35-2.8kg/cm2)，更优选10-40磅/每平方英寸(0.7-2.8kg/cm2)。该低压闪蒸罐区域的操作温度为100-250°F(37.8-121℃)，优选130-230°F(54.4-110℃)，更优选150-210°F(65.6-98.9℃)。虽然低压闪蒸室区域在较高的温度下操作是可能的，但是一般地低压闪蒸室区域的温度等于或低于高压闪蒸室区域的温度1-20°F(0.6-11℃)。一般地，较窄的范围尤其适于使用1-己烯共聚单体和异丁烷稀释剂的聚合反应，较宽的范围适于高级1-烯烃共聚单体和烃稀释剂。
使用高压闪蒸室可以容易地将至少80wt.％的流体成分(液体和蒸汽)闪蒸到塔顶(即，经过管道32)。所选择的温度和压力优选使至少90wt.％的流体成分闪蒸到塔顶，更优选的是至少95wt.％。对于用异丁烷稀释剂、乙烯单体和足够的1-己烯共聚单体产生0.945-0.956密度的聚合物(按照ASTM D 1505-68测定)的情况，一般使用的压力为150-200磅/每平方英寸(10.5-14kg/cm2)，如前所述，当使用闪蒸管式加热器或其它设备提供一个合适的温度时，从高压闪蒸区域闪蒸出的塔顶馏出物为90-95wt.％。
虽然在本发明的附图中描述了将使用闪蒸管式加热器的系统和高压闪蒸罐/低压闪蒸罐相结合，但是仅仅带有低压闪蒸并带有或不带有闪蒸管式加热器的系统同样适用，即管道26可以直接连至低压闪蒸罐40，这与把高压闪蒸罐的闪蒸限制为零是一样的。
关于将再循环稀释剂用于制备催化剂浆料及将其导入反应区域有两个因素需要考虑。
第一个需要考虑的是干燥的催化剂与稀释剂的实际接触以湿润催化剂并制得催化剂浆料。所述湿润所需要的稀释剂量仅为全部再循环稀释剂量的约0.01-5％(重量)，优选0.02-2wt.％，更优选0.03-1wt.％。在这一步骤中，于这种接触的再循环稀释剂中应不含单体或至少基本上不含单体。
第二个需要考虑的因素是所述浆料冲入反应区域。虽然稀释剂中不含单体或至少基本上不含单体是优选的，但是在这里含有少量的共聚单体和甚至很少量的乙烯还是可以容许的。
根据本发明，因为用来湿润和冲洗该催化剂的再循环稀释剂仅需要再循环稀释剂量的约0.5-20％(重量)，更优选1-10wt.％，最优选2-5wt.％，所以只是再循环而不需要去除烯烃的剩余的稀释剂为80-99.5wt.％，更优选90-99wt.％，最优选95-98wt.％。正如前面所说的在想要控制重组分或轻组分积聚的情况下，在回收任何滑流再循环稀释剂之前，主稀释剂再循环量趋向于这些范围的下限，即约为总稀释剂的80-90wt.％或至少85-95wt.％。当所述百分比定为基于全部再循环稀释剂时，由于很少量的异丁烷被夹带在流向低压闪蒸室的聚合物中，所以这些同样的百分比数字可用来定义为基于从高压闪蒸室的塔顶馏出物排出的稀释剂的再循环物流(代替全部再循环稀释剂)。
对于管道102中的再循环稀释剂所用的术语“基本上不含烯烃”是指再循环稀释剂中所含的烯烃量足够少，以致于当它们用于湿润催化剂以产生催化剂浆料时或用于冲洗该浆料进入反应区域时，对于烯烃聚合反应中催化剂的作用没有影响。
在使用乙烯的情况下，对于管道102中的再循环稀释剂所用的术语“基本上不含烯烃”是指其烯烃含量基于单体和稀释剂的重量优选为0-1ppm，或1-10ppm，或多达5-200ppm。根据本发明，在管道102中的再循环稀释剂的高级烯烃含量可以达到与在再循环稀释剂管道中同样低的水平，虽然在使用高级烯烃的情况下(如1-己烯)，这种含量基于单体和稀释剂的重量为0-2wt.％或1-10wt.％是可以容许的。
实施方案的计算说明
下面是根据本发明的一个实施方案介绍模拟的聚合作用和聚合物后加工过程。所有被描述的物质以kg/hr计。
不含氧的新鲜乙烯单体以约12000kg/hr的速度通过一个处理设备以除去任何水分或其它会使催化剂中毒的成分，如图所示。没有氢被输入。新鲜的1-己烯共聚单体以约60kg/hr的速度输入。补充的异丁烷稀释剂以约18kg/hr的速度导入。负载在二氧化硅载体上的氧化铬被导入浆料罐。
聚合反应流出物从反应区域被回收后不断地被排出，并通过一个闪蒸管道加热器以蒸发出至少大部分的液态稀释剂，然后被导入高压闪蒸室。该高压闪蒸室操作的压力为约165磅/平方英寸(11.6kg/cm2)，温度为180°F(82.2℃)。大部分(94wt.％)液体被闪蒸到塔顶并分为主物流和滑流。该主物流(主要是带有少量乙烯和1-己烯的异丁烷稀释剂)再循环至反应区域。该滑流如图1所示需要先除去1-己烯和然后除去乙烯(分别通过己烯脱气和异丁烷脱气塔)。约144kg/hr的乙烯和少量的氮气、乙烷、异丁烷和微量氧、丙烷、丁烷和水从异丁烷脱气塔的顶部排出。很少量1-己烯、正己烯、低聚物及可能含有的很少量异丁烷从己烯脱气塔的底部排出。聚合物和少量夹带的液体从高压闪蒸罐的下部流到低压闪蒸罐，在低压闪蒸罐中大部分剩余的液体被闪蒸出来从塔顶排出，因而该聚合物被回收，全部过程如图所示。所得的聚合物的密度约为0.95g/cc，通过ASTM D1238，Condition E测量的熔体流动指数约为0.2。
虽然为说明本发明的目的已对本发明作了详细的描述，但是本发明并不局限于此，对本发明所做的所有改变和改进同样落在本发明的主题和保护范围之内。

Claims (20)

1、一种方法，其包括：
将来自聚合反应区的流出物导入闪蒸区，所述流出物包括固态聚合物及含有稀释剂的流体，所述闪蒸区的温度和压力条件能使所述流体的主要部分闪蒸到塔顶形成闪蒸气流；
分别回收所述固态聚合物和剩余流体作为所述方法的中间产物；
将所述闪蒸气流分成两种物流，一种是由所述闪蒸气流的主要部分组成的主稀释剂再循环物流，另一种是由所述闪蒸气流的小部分组成的稀释剂再循环滑流；
将所述主稀释剂再循环物流再循环至所述聚合反应区；
将所述稀释剂再循环滑流通过一个烯烃去除区以得到至少基本上没有烯烃的再循环稀释剂滑流；及
将所述基本上没有烯烃的再循环稀释剂滑流送到催化剂混合区。
2、如权利要求1的方法，其中所述固态聚合物是由乙烯和高级1-烯烃制得的共聚物，其中所述闪蒸区是一个高压闪蒸区，且其中所述固态聚合物的回收是通过将所述方法的所述中间产物送到比高压闪蒸区的压力低的第二闪蒸区里进行的，在这里从所述中间产物中闪蒸出所述剩余流体的至少主要部分，其中所述烯烃去除区包括第一烯烃去除区，在这里未反应的高级1-烯烃被除去，和第二烯烃去除区，在这里未反应的乙烯被除去。
3、如权利要求2的方法，其中所述流出物在导入所述高压闪蒸区之前被加热。
4、如权利要求2的方法，其中所述高压闪蒸区的操作温度为54.4-110℃(130-230°F)，压力为875-1894kPa(127-275磅/平方英寸)。
5、如权利要求2的方法，其中所述第二闪蒸区的操作温度为54.4-110℃(130-230°F)，压力为34.4-276kPa(5-40磅/平方英寸)。
6、如权利要求2的方法，其中导入所述高压闪蒸区的所述流体包括占绝对量的含有较少量未反应的乙烯单体和未反应的高级1-烯烃的稀释剂。
7、如权利要求2的方法，其中所述高级1-烯烃是1-己烯，所述稀释剂是异丁烷。
8、如权利要求7的方法，其中在所述第二烯烃去除区中包含氢气、氮气、甲烷和乙烷的轻组分也被除去。
9、如权利要求2的方法，其中所述至少基本上不含烯烃的再循环稀释剂滑流在所述催化剂混合区与负载在二氧化硅载体上的氧化铬相混合。
10、如权利要求2的方法，其中所述主稀释剂再循环物流通过一个处理器区以除去会使催化剂中毒的物质，从而得到一种基本上不会使催化剂中毒的含有烯烃的主稀释剂再循环物流。
11、如权利要求10的方法，其中所述基本上不会使催化剂中毒并含有烯烃的主稀释剂再循环物流被送到所述聚合反应区而不需要任何烯烃去除步骤。
12、如权利要求2的方法，其中对所述主稀释剂再循环物流监控其轻组分，并根据在所述主稀释剂再循环物流中的过量轻组分产生蒸汽稀释剂再循环滑流的增加体积。
13、如权利要求2的方法，其中对所述主稀释剂再循环物流监控其重组分，并根据在所述主稀释剂再循环物流中的过量重组分产生液体稀释剂再循环滑流成分的增加体积。
14、如权利要求2的方法，其中所述基本上没有烯烃的再循环稀释剂滑流被分成第一部分和第二部分，所述第一部分被用于在所述催化剂混合区中与固体催化剂相接触以产生催化剂浆料，所述第二部分被用于将所述催化剂浆料冲洗到所述聚合反应区。
15、如权利要求14的方法，其中所述第一部分基于所述闪蒸气流中总稀释剂为0.02-2wt.％。
16、一种方法，包括：
连续地回收来自闭合回路聚合反应区的流出物，所述流出物包括固态乙烯/1-己烯共聚物和一种包含异丁烷及少量乙烯单体和1-己烯共聚单体的流体；
将所述流出物通过一个加热区，然后通入一个操作温度为65.6-98.9℃(150-210°F)、操作压力为1.03MPa-1.72MPa(150-250磅/平方英寸)的高压闪蒸区，其中90-95wt.％的所述流体闪蒸到塔顶形成以异丁烷为主的高压闪蒸气流；
分别回收所述共聚物和夹带的液体作为所述方法的中间产物并将所述方法的所述中间产物送到一个操作温度为65.6-98.9℃(150-210°F)、操作压力为68.9-276kPa(10-40磅/平方英寸)的低压闪蒸区；
蒸发并闪蒸来自所述低压闪蒸区的所述夹带的液体以产生以异丁烷为主的低压闪蒸区闪蒸气流；
压缩和冷却所述低压闪蒸区闪蒸物流以产生一种压缩的低压闪蒸区闪蒸物流，将所述压缩的低压闪蒸区闪蒸物流与所述高压闪蒸气流相混合形成总再循环异丁烷物流；
将所述总再循环异丁烷物流分为两种物流，一种是含有所述总再循环异丁烷物流中88-92％的异丁烷的主异丁烷再循环物流，另一种是含有所述总再循环异丁烷物流中剩余的异丁烷的异丁烷再循环滑流；
将所述主异丁烷再循环物流通过一个处理区以除去水分，然后将其送到所述聚合反应区；
将所述异丁烷再循环滑流和新鲜1-己烯进料一起通过第一分馏区从而基本上把所述异丁烷再循环滑流中含有的1-己烯全部分离出来并回收基本上不含1-己烯的异丁烷再循环滑流；
将所述基本上不含1-己烯的异丁烷再循环滑流送到第二分馏区，在这里包括乙烯的轻组分被除去，从而得到一种基本上不含烯烃的异丁烷再循环滑流；
将所述基本上不含烯烃的异丁烷再循环滑流冷却以产生冷却的基本上不含烯烃的异丁烷再循环滑流；
将所述冷却的基本上不含烯烃的异丁烷再循环滑流送到催化剂混合区，在这里它被用于制备包含有负载在二氧化硅上的氧化铬的催化剂浆料；及
将所述催化剂浆料送到所述聚合反应区。
17、一种方法，其包括：
在液体稀释剂存在的条件下使乙烯和高级1-烯烃在聚合反应区发生共聚反应以得到共聚物；
从所述聚合反应区回收流出物，所述流出物包括分离出的固态共聚物、分离出的稀释剂、分离出的未反应的乙烯及分离出的未反应的高级1-烯烃；
将所述流出物送到处于一定温度和压力条件下的闪蒸区，从而使大部分流体成分在此闪蒸到塔顶以形成闪蒸气流；
回收所述分离出的固态共聚物并保存来自所述闪蒸区的流体成分作为所述方法的产物；
将所述闪蒸气流分成两种气流，一种是由所述闪蒸气流的主要部分组成的主回收稀释剂再循环物流，另一种是由所述闪蒸气流的小部分组成的回收稀释剂再循环滑流；
将所述主要的回收稀释剂再循环物流循环到所述聚合反应区；
将所述回收稀释剂再循环滑流和新鲜的高级1-烯烃进料送到高级1-烯烃脱气区；
从所述高级1-烯烃脱气区排出一种脱气的1-烯烃共聚单体进料物流和一种包含稀释剂和乙烯的塔顶物流；
将所述包含稀释剂和乙烯的塔项物流送到轻组分去除区；
从所述轻组分去除区中除去作为塔顶馏出物的乙烯和回收一种至少基本上不含烯烃的稀释剂再循环物流作为所述轻组分去除区的产物；及
将所述至少基本上不含烯烃的稀释剂再循环滑流送到一个催化剂混合区。
18、如权利要求17的方法，其中所述1-烯烃是1-己烯，所述稀释剂是异丁烷其中所述流出物被不断地排出。
19、一种装置，其包括：
一个具有用于回收反应器流出物的连续卸料设备的闭合回路反应器；
一个高压闪蒸罐，在其上部具有一个高压蒸汽闪蒸卸料设备，在其下部具有一个聚合物卸料设备；
一个将所述连续卸料设备与所述高压闪蒸罐连接起来的加热的闪蒸管道，所述流出物通过该管道流到所述高压闪蒸罐；
一个具有入口的液-汽分离容器，在其上部具有一个蒸汽闪蒸卸料设备，在其下部具有一个液体卸料设备；
一个将所述高压闪蒸罐的蒸汽闪蒸卸料设备与所述液-汽分离容器的入口连接起来的第一管道，通过该管道所述高压闪蒸罐的塔顶馏出物被送到所述液-汽分离容器；
一个具有入口设备、塔顶蒸汽回收设备、中间产物回收设备和次重组分去除设备的重组分去除塔；
至少一个用于将所述第一管道与所述重组分去除塔入口设备连接起来的第二管道，所述第二管道用于从所述第一管道中取出滑流；
一个将所述汽-液分离容器的蒸汽闪蒸卸料没备与所述至少一个第二管道设备相连的第三管道设备；
一个将所述液-汽分离容器的液体卸料设备与所述闭合回路反应器相连的第四管道设备；
一个具有入口、除去蒸汽的塔顶设备和底部产品回收设备的稀释剂脱气塔；
一个将所述重组分去除塔的塔顶蒸汽回收设备与所述稀释剂脱气塔所述入口相连的第五管道设备；
一个用于混合催化剂与稀释剂的浆料鼓；
一个将所述稀释剂脱气塔的下部产品回收设备与所述浆料鼓相连的第六管道，用于使脱气后的产物通过该管道从所述稀释剂脱气塔流向所述浆料鼓；
一个将所述浆料鼓与所述闭合回路反应器设备相连的第七管道，用于使催化剂浆料通过该管道流到所述闭合回路反应器设备；
一个用于向所述重组分去除塔中导入共聚单体的第八管道设备；
一个用于导入稀释剂并和所述第五管道开放式相连的(opencommunication)第九管道；
一个用于导入单体的第十管道，所述第十管道与所述第四管道开放式相连；及
与所述浆料鼓相连的管道设备，该管道用来将催化剂导入所述浆料鼓。
20、根据权利要求19的装置，其还包括：
一个具有入口、塔顶蒸汽出口和底部聚合物回收出口的低压闪蒸罐；
将所述高压闪蒸室罐聚合物卸料设备与所述低压闪蒸罐的入口相连的管道设备；
具有入口设备和出口设备的蒸汽压缩设备；
将所述低压闪蒸罐的塔顶蒸汽出口与所述压缩装置的入口设备相连的管道设备，通过该管道将流体从所述低压闪蒸罐流到所述压缩设备；及
将所述压缩设备的出口设备与所述第一管道相连的管道设备，通过该管道将压缩的流体送到所述第一管道。
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