CN1208046A - 高固含量淤浆聚合 - Google Patents

高固含量淤浆聚合 Download PDF

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CN1208046A
CN1208046A CN98116048A CN98116048A CN1208046A CN 1208046 A CN1208046 A CN 1208046A CN 98116048 A CN98116048 A CN 98116048A CN 98116048 A CN98116048 A CN 98116048A CN 1208046 A CN1208046 A CN 1208046A
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J·D·浩托维
H·D·汉斯雷
D·J·普莱泽罗姆司基
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Abstract

一种烯烃聚合方法,其中单体、稀释剂和催化剂是在一个连续的环管反应器中循环的,并且淤浆产物是以连续排放产物的方式回收的。产物的连续提取使得反应可在固含量很高的循环淤浆中进行。在一个优选的实施方案中,淤浆在闪蒸管道加热器中经加热并通入高压闪蒸室中,在此,大部分稀释剂被分离出来,接着,不需加压,经简单的热交换器冷凝后供重复利用。同时,该烯烃聚合也可借助更激烈的循环在高固含量反应器中进行。

Description

高固含量淤浆聚合
本发明涉及烯烃单体在一种液态稀释剂中的聚合作用。
加成聚合通常是在能溶解所得聚合物的一种液体溶剂中进行的。当高密度(线形)乙烯聚合物在本世纪五十年代开始成为市售商品时，就是采用这种方法的。不过，不久就发现了在呈淤浆的情况下进行聚合是制备这类聚合物的更有效的方法。更具体地说，这种聚合技术选择在环管反应器中进行连续的淤浆聚合，而产物是借助一种以间歇操作方式回收产物的沉降管排出的。就世界范围来说，该技术已经取得每年生产数十亿磅乙烯聚合物的成功。随着这种技术的成功，对于一定生产能力的工厂来说，建造数量少的大反应器相对于建造数量多的小反应器的优点已经显露出来。
然而，沉降管的采用会引起两个问题，首先，表现在“间歇”技术对基本连续方法的影响。每当沉降管内积聚的聚合物淤浆达到需“排放”或“起动”时，就会干扰上游环管反应器中淤浆的流动和下游回收系统。还需经常维护基本上呈周期地开闭连接上游反应器与下游回收系统的沉降管的阀门机构，这是因为要使密封沉降管的大口径阀门保持严密的封闭状态是很困难的。
其次，因为反应器已经扩大，因此，会因沉降管的采用而出现逻辑上的问题。如果环管管径加倍，则反应器容积就为原来的四倍。然而，由于涉及阀门机构，沉降管的体积不容易进一步增大，因此，所需沉降管的数目就会超过实际可利用的空间、
虽然有这些限制因素，但在液态稀释剂中进行淤浆聚合制备烯烃聚合物时，仍是一直采用沉降管的。这是因为，不象本体淤浆聚合(即单体是稀释剂)那样，通常可得到高于60％固体含量，而烯烃聚合物淤浆在稀释剂中的固含量通常限制在不超过37-40(重量)％。因此，已经认为，为了在沉降管出口处的最终淤浆产物的固含量高于37-40％，沉降管是必须采用的。从名词的含义就可看出，因为沉降发生在沉降管内，从而可提高最后回收的淤浆产物中的固含量。
另一个影响反应器中实际最高固含量的因素是循环速度，在反应器直径一定的情况下，较高的循环速度可允许有较高的固体含量。因为，如循环速度较低，聚合物会在反应器中积累而结垢，因此，这种结垢现象就成为操作上的一种限制因素。
本发明的一个目的是利用淤浆产物连续排放法在液态稀释剂中以淤浆聚合制备烯烃聚合物。
本发明另一个目的是在稀释剂中实施烯烃淤浆聚合过程，其中反应器中的固体含量高至足以使直接连续排放的产品具有工业适用性。
本发明的另一个目的是在稀释剂中以较高的循环速度实施烯烃淤浆聚合过程。
本发明还有一个目的是在稀释剂中，在大于30000加仑(136.4米3)反应区内实施烯烃淤浆聚合过程。
本发明再有一个目的是提供容量大于30000加仑(136.4米3)，并具有连续排放装置的环管反应器设备。
根据本发明的一个方面，烯烃聚合过程是在高固含量反应器中通过连续提取淤浆产物而实施的。
根据本发明的另一个方面，在环管反应器中的烯烃聚合过程是在较高的循环速度(对一定的反应器管径来说)下进行的。
根据本发明的还有一个方面，提供一种环管聚合设备，这种环管反应器中的一个垂直段的下游端置有一个细长的中空附件，而该中空附件是使流体直接与加热的闪蒸管道相连通的，因此适合于淤浆产物的连续排放。
附图包括下列各图：图1是环管反应器和聚合物回收系统的透视示意图；图2是沿图1中2-2线所示的连续排料附件的剖面图；图3是沿图2中3-3线所示的连续排料组件的柱塞阀之剖面图；图4是切线位置连续排料组件的剖面图；图5是环管反应器中弯管接头的侧视图，展示了沉降管和连续排料组件；图6是沿图5中6-6线所示的两个连续排料组件的排列方位剖面图；图7是另一方位的连续排料组件的侧视图；图8是叶轮机构的剖面图；图9展示另一种环管结构的示意图，其中环管上段14a呈180度半圆形，而垂直段的长度至少是水平段长度的两倍；图10是长轴以水平配置的环管结构示意图。
已经出乎意料地发现，在惰性稀释剂存在下于环管反应器中进行烯烃聚合时，连续地排出淤浆产物可使反应器在固含量高得多的情况下进行作业。通常，在以异丁烷为稀释剂、以乙烯为主体聚合物的工业生产中，反应器中的最高固含量限制在37-40(重量)％。然而，已经发现，采用连续排料可使固含量有明显的提高。此外，由于布置了这种能选择性地从固含量较高的淤浆层中提出淤浆的连续排料附件，所以连续排料本身会使从反应器中排出的产物的固含量与反应器中固含量相比，有一定的额外增加。因此，根据本发明，固含量可达到高于40(重量)％。
在本申请中，由于聚合产率，尤其用以二氧化硅为载体的氧化铬时是极高的，因此没有涉及催化剂的重量。
还出乎意料地发现，可采用更激烈的循环(伴随而来有较高的固含量)。实际上更加激烈的循环与连续排料相结合，通过连续排料方式，可从反应器提取到高于50(重量)％固含量的产物。例如，连续排料方式可使反应器在固含量高5-6个百分点的情况下运作，即反应器中固体量可提高10％；更加激烈的循环能另外增加7-9个百分点，由此可使反应器中固含量达到50％以上。但是，由于连续排料是安排用来从高于平均固含量的淤浆液流层中提取淤浆的，所以实际上回收产物的固含量高出反应器中淤浆平均固含量约3个百分点(或更高)。因此这样的运行能使淤浆产物的有效固含量达到55(重量)％或更高，即反应器中平均固含量为52％，而提取产物之固含量实际为高于55％(高出3个百分点)。
必须强调指出的是，对工业规模运作来说，即使固含量增加少至一个百分点也是具有重要意义的。因此，反应器中平均固体含量从37-40％提高到41％也是有意义的，那么，将固含量提高到高于50％确实是惊人的。
本发明适用于在稀释剂存在下，任何烯烃在环管反应器中聚合，来制造聚合物与稀释剂的淤浆产物。适用的烯烃单体为每分子含至多8个碳原子并在双键的第4位碳原子以内无支链的1-烯烃。本发明尤其适用于乙烯的均聚合和乙烯与高级1-烯烃，(如丁烯、1-戊烯、1-己烯、1-辛烯或1-癸烯)的共聚合。特别优选的是乙烯与0.01-10(重量)％，优选为0.01-5(重量)％、最优选为0.1-4(重量)％(以乙烯与共聚单体的总重量计)的高级烯烃的共聚合。换句话说，可使用足够的共聚单体以制得含上述共聚单体量的聚合物。
适用的稀释剂(相对于溶剂或单体)在技术上是众所周知的，包括惰性的、在反应条件下呈液态的烃类。适用的烃包括异丁烷。丙烷、正戊烷、异戊烷、新戊烷及正己烷，而异丁烷是特别优选的。
适用的催化剂在技术上是众所周知的。尤其适用的是已公开的经诸如二氧化硅载体的铬氧化物，例如在Hogan和Banks的美国专利2285721(1958年3月)所公开的，其公开内容已列入本文以供参考。
现参见附图：图1展示了有垂直段12、上水平段14和下水平段16的环管反应器10。这些上、下水平段限定了上部和下部水平流动的区域。反应器是通过由管12和夹套18构成的双管热交换器来冷却的。反应器的每段借助一个平滑的弯头或弯管20与相邻段连接，这就提供了一个基本没有内部阻塞的连续物流通道。聚合混合物借助由马达24驱动的叶轮22(图8所示)进行循环。单体、共聚单体(如果有的话)及补充的稀释剂分别经管道26和28导入，它们可从一个或从多个位置上直接进入反应器或与回收管道30的冷凝稀释剂一起进入反应器(如图所示)。催化剂经由催化剂导入装置32提供的催化剂导入区域导入。连续排放中间淤浆产物的细长中空附件概括地由字符34表示。连续排料机构34位于或邻近于反应器环管之下水平段16的一个下游端并邻近或位于连接弯管20处。
如图所示，环管反应器下水平段的一个下游端点是连续排料附件的优选位置。该位置可处于催化剂导入点之前、环道中流体转为向上流动的最后点的邻近区域，以便允许新鲜的催化剂于第一次通过排放点之前，能在反应器中滞留尽可能长的时间。然而，连续排料附件可置于任何一段或任何一个弯管上。
为了降低流体的流动速度，也可将装有连续排料附件的反应器环管段的直径加大，这样还可使流动的液流分层从而使流出的产物中含更高的固含量。
连续提取的中间淤浆产物经导管36通入高压闪蒸室38。导管36周围有一外管40。该管内有为闪蒸管道36中淤浆料间接加热的热流体。留在闪蒸室38的已蒸发的稀释剂经管道42供包括用循环冷凝器50作简单热交换的冷凝处理的进一步加工，然后通过回收稀释剂管30，无需加压而返回到系统中。回收冷凝器50可利用在本技术领域任何已知条件下适用的任何已知的热交换流体。然而，优先采用能经济地提供一定温度的流体。该流体适宜的温度范围为40°F-130°F(4℃-54℃)。从高压闪蒸室38提取聚合物微粒，经管道44供利用本技术领域已知技术作进一步加工。优选的是，让该聚合物微粒进入低压闪蒸室46，然后经管道48作为聚合物产物而回收。分离的释释剂通过压缩机47进入管道42。高压闪蒸装置已概略地公开在Hanson和Sherk的美国专利4424341(1984年1月3日)中，该专利的公开内容已列入本文以供参考。已出人意料地发现，连续排料不仅允许在反应器上游有较高的固含量，而且也可使高压闪蒸室更好地运行，因此可使大部分回收的稀释剂被闪蒸出来并且不需压缩而被回收。实际上，按本方法，一般可回收70-90％稀释剂。这是由几个因素引起的，首先，由于流体连续流动代替了间歇流动，闪蒸管线加热器运行更好。还有，因为存在压力降，在用来调整反应器物料流量的比例调节阀后的压力降低了，这就是说，流体闪蒸时的温度可以降低。因此，能更有效地利用闪蒸管道加热器。
参看图2，图中较详细地展示了弯管20与连续排料机构34。连续排料机构包括排料筒52、淤浆提取管道54、紧急切断阀55、调整流量的电动比例调节阀58以及闪蒸管道60。反应器是在充满“液体”情况下运行的。由于溶有单体，该液体稍具有可压缩性，因此可用阀门调节该充满液体的系统的压力。稀释剂输入通常保持稳定，电动比例调节阀58用来调整连续提取的速率，以保持整个反应器的压力处于规定的设定范围内。
参看图3，该图取自沿图2剖面线3-3，它详细展示了与连续排料机构34相组合的光滑曲线或弯管20，因此弯管20是一带附件的弯管。如图所示，该排料机构包括连在弯管上的排料筒52，在本示例中该排料筒与弯管外表面的切线成直角。离开排料筒52进入淤浆提取管道54。在排料筒52中配置柱塞阀62有两个目的，第一，它作为一种简单而可靠的清扫机构，如果排料筒发生聚合物阻塞，可用来清扫排料筒。第二，它可作为一个整个连续排料组件的简单而可靠的切断阀。
图4展示排料筒52最佳的连接方位，其中该筒呈切方位固定在弯管20的弯曲处。并且正好处于淤浆物流转为向上流动前的那一点上。向弯管内表面的开口呈椭圆的。为了改善固体的排放，开口还可扩大。
图5展示了四个部件的配置，第一，该图展示了排料筒52的角度方位，如图所示，该排料筒(1)与垂直于水平段16中心线的平面成α角，及(2)配制在水平段16的下游端。与平面的夹角取自该平面的下游方向。如图5所示，夹角的顶点是弯管半径的圆心。该平面可称作为水平段的横截面，这里所述的夹角约为24度。第二，该图也展示了多个连续排料附件34和34a。第三，该图展示了一个配置在通过下水平段16中心线的垂平面上的附件34和另一个附件34a，如图6详细所示，附件34a是与该平面成一夹角配置的。最后，该图展示了连续排料附件34与供间歇排料(根据需要)用的常规沉降管64的组合。
如图所见的相对大小，连续排料筒比常规沉降管小得多。三个2英寸(5.1厘米)内径的连续排料附件能排放的淤浆产物与14.8英寸(37.6厘米)内径的沉降管一样多。这一点是很有意义的，由于工业上通用的容积为15000-18000加仑(68-82米3)的环管反应器需要6个8英寸(20厘米)沉降管。因为制造可靠的大口径阀门很困难，所以不希望增加沉降管的尺寸。如前已指出的，管径加倍，则反应器容积就为原来的四倍，因而没有足够的空间可供配置这么多四倍大容积的沉降管。因此本发明可使大容积的反应器更有效地运作，这样，根据本发明就可制造30000加仑(136米3)或更大的反应器。通常，连续排料筒的额定内径为1英寸(2.5厘米)至小于8英寸(20厘米)。优选的是，排料筒的内径为约2-3英寸(5.0-7.5厘米)。
图6是沿图5的6-6剖面线的剖面图，并展示了配置在与通过反应器中心线的垂平面成β角位置的排料筒34a。该垂平面可称为反应器的中心垂平面。这一β角如果不是零的话，则可取在垂心平面的任一侧或双侧。角的顶点位于反应器中心线上。该角处在垂直于反应器中心线的平面上，如图6所示。
应该指出，这里有三个方位概念。第一是连接方位，即如图4的切线方位和如图2或图7的垂直方位或在0与90度之间的任何角度。第二是关于附件连接在沿弯管曲线向上多远的方位，以α角表示(图5)。该α角可以是0-60度的任何角度，但优选为0-40度，更优选为0-20度。第三是β角，指与垂直段的中心平面(图6)的夹角。该角可为0-60度，优选为0-45度，更优选为0-20度。
图7展示一种垂直方向连接的连续排料筒52的实施方案，α角方位为0度(虽处于末端，但仍在直线部分上)、β角方位为0度，即排料筒正好位于通过下水平段16中心线的垂平面上。
图8详细地展示了驱动淤浆沿物流通道连续流动的叶轮装置22。如在本实施方案中看到的，叶轮是按装在作为循环的反应物料推动区的一段稍扩大的环管中。优选的是，该系统的运行能使采用异丁烷为介质制造主体为乙烯的聚合物体系，在标称直径为2英尺(0.61米)、总的液流通道长950英尺(289米)的反应器中，物料推动区上游端与下游端之间产生至少为18磅/英寸2表压(0.138兆帕表压)，更优选至少为22磅/英寸2表压(0.152兆帕表压)的压差。压差达50磅/英寸2表压(0.345兆帕2表压)或更高也是可能的。这可以通过调整叶轮的转速、降低叶轮与泵壳体内壁之间的间隙或采用在技术上已知的效率更高的叶轮设计来达到。也可通过采用至少一个辅助泵来产生更高的压差。
通常，该系统运行产生的压差(以反应器单位长度的压力损失来表示)，对于标称直径为24英寸(0.61米)的反应器来说，至少是每英尺(0.3米)反应器长度的压力降为0.07，一般为0.07.0.15英尺(0.021-0.045米)。优选的是，对于24英寸(0.61米)直径的反应器，每单位长度的压力降为0.09-0.11。对较大直径的反应器来说，高速  度浆料，要求反应器的单位长度压力降较大。压力降的单位经消去后是英尺/英尺，假定淤浆密度一般为约0.5-0.6。
现参阅图9，图中展示的是上段为180度半圆形的优选构型。垂直段长度至少是水平段长度的两倍，一般约7-8倍。例如，垂直的物流通道长度为190-225英尺(58米-69米)而水平段物流通道长度为25-30英尺(7.6米-9.2米)。除这里所述的4个环管和图1中所示的8个环管外，还可采用任何个数的环管，但是通常采用4或6个环管。标称直径为2英尺(0.61米)的环管意味着其内径为约21.9英寸(0.56米)。流道通常在500英尺(152米)以上，一般超过900英尺(275米)，而十分满意的是约900-1350英尺(275米-412米)。
工业用泵，如用于密闭环管反应器中循环反应物料的泵是经制造商按例行程序检验过的，并且避免气蚀所需的压力是容易按常规测定的。
                       实施例
采用配置有4个垂直排料管的聚合反应器对乙烯和己烯-1进行聚合，反应器中输送物料的是由Lawrence Pumps公司制造的安装在M51879/FAB壳体中的26英寸(66厘米)D51795/81-281泵叶轮。这种泵与循环强度较低的24英寸(61厘米)循环泵相比较(压降为0.66英尺对0.98)，然后与类型相同但循环强度更大的循环泵相比，连续排料组件的类型如图5中34所示。结果列于下表，
                                      数据表
聚合条件说明   24英寸(61厘米)泵   26英寸(66厘米)泵   26英寸(66厘米)泵+CTO
运行日期   1994.10，4-9   1995.5.24-28   1996.11.15-18
反应器平均固含量，重量％     39     45        53
聚合物产出速率，毫磅/小时     40.1     40.7        39.9
反应器循环泵功率，千瓦     430     691        753
循环泵压差磅/英寸2     14.3     22.4        23.7
循环泵压头，英尺     61.8     92.5        92.4
反应器淤浆流率mGPM     39     46        45
反应器淤浆密度克/厘米3     0.534     0.558        0.592
反应器温度，°F     215.6     218.3        217.0
乙烯浓度，重量％     4.43     3.67        4.9
己烯-1浓度，重量％     0.22     0.17        0.14
反应器传热系数     270     262        241
反应器内径，英寸     22.0625     22.0625        22.0625
反应器容积，加仑     18700     18700        18700
反应器长度，英尺     941     941        941
反应器每英尺长度的压差，英尺/英尺     0.066     0.098        0.098
虽然已对本发明作了详细的说明，但不能认为这是对本发明的限制，而本发明应包括属于本发明精神和范围的所有变化。

Claims (34)

1.一种聚合方法包括：
在环管反应区使至少一种烯烃单体在液态稀释剂中进行聚合，以制备一种包含液态稀释剂和固态烯烃聚合物微粒的液态淤浆；
在所述反应区中，所述固态烯烃聚合物微粒在所述淤浆中固含量保持在高于40(重量)％，以所述聚合物微粒和所述液体稀释剂重量计；
连续地提取包含被提取的液态稀释剂和固态聚合物微粒的所述淤浆，该淤浆是所述方法的中间产物。
2.根据权利要求1的方法，其中所述烯烃单体包括乙烯。
3.根据权利要求1的方法，其中所述烯烃单体包括乙烯和0.01-5(重量)％的己烯，以所述乙烯和所述己烯的总重量计以及其中所述液态稀释剂是环己烷。
4.根据权利要求3的方法，其中在所述反应区中，所述固态烯烃聚合物微粒在所述淤浆中的固含量高于50(重量)％，以所述聚合物微粒重量和所述液态稀释剂重量计。
5.根据权利要求1的方法，其中为了循环所述淤浆通过所述反应区，在推动区至少保持18磅/英寸2(1.26千克/厘米2)表压的压差。
6.根据权利要求1的方法，其中在推动区保持每英尺长的反应器物流通道大于0.07的压差。
7.根据权利要求6的方法，其中所述压差为每英尺长的所述反应器物流通道为0.07-0.15英尺/英尺。
8.根据权利要求1的方法，其中所述反应区是完全充满液体的。
9.根据权利要求1的方法，其中所述反应区的容积大于20000加仑(91米3)。
10.根据权利要求1的方法，其中所述反应区的容积大于30000加仑(136.4米3)。
11.根据权利要求1的方法，其中所述方法的所述中间产物是连续地通过加热区的，在加热区，所述中间产物经加热成为热的中间产物，然后在高压闪蒸区经减压，所述的中间产物经加热至大部分所述已提取的液态稀释剂蒸发，从而使稀释剂从提取的固体聚合物微粒中分离出来，分离的液态稀释剂无需加压，通过与温度约40°F-约130°F(4℃-54℃)的流体进行热交换，冷凝后供循环使用。
12.根据权利要求1的方法，其中所述淤浆是连续地从所述环管反应区中，在催化剂导入区前、物流向上转向最后点的附近区域提取的。
13.根据权利要求1的方法，其中所述淤浆是连续地从至少一个邻近水平物流下方的端点区域提取的。
14.根据权利要求13的方法，其中所述淤浆是在下水平段的中心垂平面上，沿所述水平物流的下方并在所述物流朝上转向前的位置上提取的。
15.根据权利要求13的方法，其中所述至少一个区域是在下水平段的中心垂平面上，沿所述水平物流的下方并在所述物流已朝上转向后的区域。
16.根据权利要求13的方法，其中所述的一个区域是在所述水平物流的下方与下水平段中心垂平面成一夹角取向的，该夹角为0-45度。
17.根据权利要求16的方法，其中所述至少一个区域是与所述水平段中心垂平面成0-20度夹角取向的。
18.根据权利要求16的方法，其中所述至少一个区域是指所述物流朝上转向之前的区域。
19.根据权利要求16的方法，其中所述至少一个区域是指所述物流已朝上转向之后的区域，偏离朝上物流中心线至少1度，但小于45度。
20.根据权利要求13的方法，其中所述的至少一个区域就是一个区域。
21.根据权利要求13的方法，其中所述至少一个区域是多个区域。
22.一种聚合方法包括：
在环管反应区，使至少一种烯烃单体在液态稀释剂中进行聚合以制备一种包含液态稀释剂和固态烯烃聚合物微粒的液态淤浆；
也可按下列步骤提取包含被提取的液态稀释剂和固态聚合物微粒的所述淤浆：
(A)使所述淤浆排入至少一个沉降区，然后从所述沉降区提取一批沉降的淤浆并作为所述方法的中间产物，随后关闭所述沉降区；及
(B)然后连续地提取包含被提取的液态稀释剂和固态聚合物微粒的所述淤浆，该淤浆是所述方法的中间产物。
23.根据权利要求22的方法，该方法还包括在起动步骤(B)期间，调整反应器条件使反应器中固体含量提高至少10％。
24.一种环管反应器设备包括：
多个垂直段；
多个上水平段；
多个下水平段；
其中每一所述垂直段的上端通过一光滑上弯管与一个所述上水平段相连接，垂直段的下端通过一光滑下弯管与一个所述下水平段相连接，由此规定了适用于输送流体淤浆的连续的流通道，所述反应器基本上是没有内部障碍的，
供单体反应剂、聚合催化剂和稀释剂导入所述反应器的装置；
使所述淤浆沿所述物流通道连续地运行的装置；
邻近所述下水平段之一的一下游端，至少有一个细长中空附件，所述细长中空附件与物流通道保持连通以供连续提取淤浆产物；以及
以流体与所述附件保持连通的，用于从所述附件向闪蒸装置输送淤浆产物的长闪蒸管道，所述闪蒸管道周围设置有用于加热所述淤浆产物的加热器。
25.根据权利要求24的设备，其中所述的至少一个附件与一个所述的下水平段相连，因此形成一个带附件的下水平段，所述附件是沿带附件的下水平段的中心垂平面取向的，并在邻近光滑下弯管处与带附件的下水平段的下游端相连接。
26.根据权利要求24的设备，其中所述附件是以0-90度角相连的。
27.根据权利要求24的设备，其中所述至少一个附件是与连在带附件的下水平段的下游端的所述光滑弯管相连接的，由此形成一个带附件的光滑弯管。
28.根据权利要求27的设备，其中所述附件与邻近垂直段中心线成至少1度但小于45度夹角的位置与所述带附件的光滑弯管相连接。
29.根据权利要求28的设备，其中所述附件是以0-90度角相连接的。
30.根据权利要求28的设备，其中所述至少一个附件是以垂直位至切线位方向与带附件的弯管相连的。
31.根据权利要求28的设备，其中所述至少一个附件是与带附件的弯管成切线方位相连的。
32.根据权利要求31的设备，其中所述至少一个附件连接在与所述的中心垂平面成20-45度夹角的位置上。
33.根据权利要求31的设备，其中所述的至少一个附件就是一个附件。
34.根据权利要求31的附件，其中所述的至少一个附件是多个附件。
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JP3084014U (ja) 2001-08-09 2002-02-28 日東製網株式会社 無菌精製冷海水製造装置

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CN100431682C (zh) * 1999-03-09 2008-11-12 菲利浦石油公司 供给催化剂湿润剂的稀释剂滑流
CN100531892C (zh) * 2002-02-19 2009-08-26 埃克森美孚化学专利公司 使用环管反应器的连续淤浆聚合方法
CN101503483B (zh) * 2002-09-17 2012-09-05 切夫里昂菲利普化学有限责任公司 改进的用于环管反应器内淤浆聚合的泵送装置和方法
CN100338099C (zh) * 2002-09-25 2007-09-19 切夫里昂菲利普化学有限责任公司 从高固体含量聚合淤浆中连续取料
CN1856357B (zh) * 2003-09-24 2010-11-10 巴塞尔聚烯烃有限公司 在具有变直径的回路反应器内进行烯烃聚合反应的方法
CN1922219B (zh) * 2004-02-13 2011-06-01 托塔尔石油化学产品研究弗吕公司 改进聚合环流反应器中乙烯和烯烃共聚单体共聚的方法
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CN101796080B (zh) * 2007-09-03 2013-03-27 英尼奥斯制造业比利时有限公司 淤浆相聚合方法
CN102666606A (zh) * 2009-10-30 2012-09-12 英尼奥斯制造业比利时有限公司 淤浆相聚合方法
CN102666606B (zh) * 2009-10-30 2014-01-29 英尼奥斯制造业比利时有限公司 淤浆相聚合方法
CN103857709A (zh) * 2011-12-19 2014-06-11 博里利斯股份公司 提供先进的产量分配控制的环式反应器
CN103857709B (zh) * 2011-12-19 2015-11-25 博里利斯股份公司 提供先进的产量分配控制的环式反应器
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CN103804556A (zh) * 2012-11-07 2014-05-21 中国石油化工股份有限公司 烯烃聚合方法和乙烯聚合物及其制备方法
CN103804556B (zh) * 2012-11-07 2016-09-14 中国石油化工股份有限公司 烯烃聚合方法和乙烯聚合物及其制备方法
CN110385099A (zh) * 2018-04-20 2019-10-29 中国科学院过程工程研究所 一种环管反应器及环管反应器的控制方法

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RU2221812C2 (ru) 2004-01-20
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