CN116547308A - 丙烯聚合设备及丙烯聚合方法 - Google Patents
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Abstract
用于生产聚丙烯和聚丙烯共聚物的环流气相反应器聚丙烯设备及方法。
Description
技术领域
本发明涉及一种适用于超大规模丙烯聚合的聚合设备。本发明还涉及一种使用该设备进行丙烯聚合的方法。
背景技术
环流与气相反应器的结合在20多年前就以商标的形式为人们所知，并且几乎已经进入聚烯烃领域的任何教科书。其基本工艺布局记载在例如涉及制备丙烯均聚物和共聚物的WO9858975A1中，该基本工艺包括在高温高压以及催化剂的存在下，在至少一个浆态反应器和气相反应器中将丙烯任选地与共聚单体聚合，至少一个浆态反应器中的含未反应单体的聚合产物被直接输送到第一气相反应器中，基本上无需将未反应单体送入浆态体反应器中再循环。
环流-气相反应器配置的一个重要方面是单程转化。例如，早先的WO9925741描述了一种将从浆态反应器获得的聚合物浆液引入具有流化床(C，D)的气相反应器中的方法，第一流化区(C)位于第二流化区(D)之上，所述流化区具有不同的流动模式，由此来优化该工艺的单程转化。
遗憾的是，与特大型聚丙烯设备相比，中等规模的聚丙烯生产设备的运营成本以及生产每吨产品的固定成本明显更高。然而，随着生产规模的扩大，质量问题和操作问题也会随之增加。可以通过在反应器中增加更多的支路来增加环流反应器的容量。在工业领域，环流反应器的支路已经从2个增加到6个，甚至支路为8个的环流反应器也不少见。然而，与支路为4个的环流反应器相比，使用支路为8个的环流反应器的单次循环时间将大约增加一倍。不幸的是，这种改造可能会导致一些缺陷，例如，会出现明显的浓度梯度。如在聚丙烯均聚反应中，氢气与丙烯的比例会在环流反应器的整个长度上发生变化，特别是在丙烯与乙烯的无规共聚反应中，乙烯与丙烯的比例会在环流反应器中形成明显的梯度。不言而喻，当C2/C3比率在环流反应器的整个长度上下降时，随机性将受到影响。因此，当生产例如无规丙烯-乙烯共聚物时，诸如局部添加乙烯或向反应器提供多个进料点等方法成为必须。总而言之，升级环流反应器是非常繁琐的。
对于生产量非常高的聚合工艺，特别是对于规模非常大的气相反应器来说，另一个挑战是如何在宽的操作区间内控制温度，例如还在50％的可调节率(turn down ratios)下，以建立宽的操作窗口(例如宽的温度范围)。可调节率是指在减少生产量的情况下运行设备的能力。可调节率通常定义为[1-(最小产能/设计产能)]。
在可调节的情况下，冷却水返流(CWR)的流动温度会升高到冷却水系统正常操作窗口以外的高温。使用不锈钢设备则会存在效率降低和腐蚀开裂的问题。在将氯添加到冷却水回路和/或塔中以防止生物滋长的时候，避免冷却水返流流动的不必要高温是特别重要的。
因此，仍然需要一种能够扩大到超大规模的工艺及设备，并至少部分避免这些及其他相关问题。
发明内容
本发明提供一种制备丙烯均聚物或丙烯共聚物的设备，其包括：
1)用于供给催化剂(1)、可选的助催化剂(2)、可选的活化剂和/或可选的外给电子体(3)的进料罐；
2)可选的用于催化剂混合的预接触单元(4)，通过进料管路(5，5'，5”)与进料罐连接；
3)与进料罐(1，2，3)或预接触单元(4)连接的预聚合反应器(6)；
4)丙烯进料罐(7)；
5)与预聚合反应器连接的第一环流反应器(8)；
6)通过环流反应器连接管线(10)与第一环流反应器连接的第二环流反应器(9)；
7)向第一环流反应器(8)、第二环流反应器(9)和/或所述环流反应器之间的连接管线(10)中的一个或多个输送单体和可选的共聚用单体(11)以及氢气(12)
的装置；
8)气相反应器(13)，配备有气体循环管线(14)、循环气体压缩机(15)和循环气体冷却器(16)，该气相反应器通过直接进料管线(17)至少与第二个环流反应器相连接；
9)用于将单体(44)和/或共聚单体(18)和/或氢气(19)送入气相反应器(13)的装置；优选地，所述送入单体和/或共聚单体的装置适合将单体和/或共聚单体以冷凝(condensed)形式送入；
10)可选的与气相反应器相连的产物排出容器(20)；
11)可选的产物出口加热器(21)；
12)与可选的产物排出容器(20)或与气相反应器(13)相连的产物收集罐(22)；
13)至少一个净化仓(purge bin)(23)；
14)至少一个丙烯氮气回收单元(24)；
15)用于将烃汽流(hydrocarobon steam)(送入柱(28)的柱供应管线(241)；
16)氮气再进料管线(243)，用于将富含氮气的汽流(steam)重新送入净化仓(23)；
17)可选的热氧化器单元(43)；
18)排气管线(242)，用于将排气流排放到可选的热氧化器(43)；
19)用于丙烯均聚物或丙烯共聚物回收的装置(25)，可选地包括用于均化、添加(additivation)和造粒的装置；
20)回收气体处理装置(26)，包括至少一个压缩机(27)、所述柱(28)和回流进料容器(28a)，回流进料容器(28a)通过回收管线(29)与气相反应器(13)的气体循环管线(14)相连；
21)用于循环气体冷却器(16)的冷却回路(30)；
22)(蒸汽)喷出(blow down)单元(31)，包括高压喷出仓(32)、低压喷出仓(33)，该喷出单元(31)可选地通过连接管线(34)与产物收集罐(22)连接；
23)连接回收气体处理单元(26)和丙烯进料罐(7)的回收进料管线(35)，其中，循环气体冷却器(16)是闭环冷却水系统(300)内的热交换器，闭环冷却水系统包括冷却水泵(301)、二次热交换器(302)、膨胀箱(303)和在二次热交换器上方的旁路(304)。
本发明进一步提供一种制备丙烯均聚物和共聚物的方法，包括：
a)在进料罐(1、2、3)中提供催化剂、可选的助催化剂、可选的活化剂和/或可选的外给电子体；
b)将所述催化剂、所述可选的助催化剂、所述可选的活化剂和/或所述可选的外给电子体送入预接触单元(4)，提供混合催化剂体系；将所述混合催化剂体系送入预聚合反应器(6)中或将直接所述催化剂、所述可选的助催化剂、所述可选的活化剂和/或所述可选的外给电子体送入预聚合反应器(6)；
c)通过导入丙烯单体和可选地导入共聚单体引发预聚合，从而获得预聚物；
d)将所述预聚物送入第一环流反应器(8)，并使丙烯可选地与单体一起聚合，产生第一中间体；
e)通过环流反应器连接管线(10)将第一中间体送入第二环流反应器(9)，并进一步将丙烯可选地与单体一起聚合，产生第二中间体，由此，丙烯从丙烯进料罐(7)通过丙烯返料管线(41)送入第一环流反应器(8)和第二环流反应器(9)；
f)在其他进料点(11，12)向环流反应器引入可选的共聚单体和/或氢气；
g)通过直接进料管线(17)将含有未反应单体的第二中间体直接送入气相反应器(13)；
h)在所述气相反应器(13)中进一步聚合丙烯和可选的共聚单体，方法是经由气体循环管线(14)在向上方向上通过所述气相反应器(13)进行气体循环，从而使循环气体在循环气体冷却器(16)中得到冷却；
i)将气相反应器的产物排出至可选的产物排出容器(20)，然后经由可选的产物出口加热器(21)进入产物收集罐(22)，形成原料混合物，或者，将气相反应器产物直接排出至产物收集罐(22)中；，形成原料混合物；
j)将所述原料混合物送入净化仓(23)；
k)用氮气和催化剂失活剂吹扫所述原料混合物，催化剂失活剂优选为水蒸汽(steam)；
l)在丙烯氮气回收单元(24)中将来自净化仓(23)的氮气、失活剂和烃类分离，从而
-提供基本纯净的氮气汽流(steam)，通过氮气再进料管线(243)将所述基本纯净的氮气汽流送入净化仓(23)；
-提供贫烃废料汽流(steam)，通过排气管线(242)将所述贫烃废料汽流送入可选的热氧化器单元(43)；
-提供富烃的干燥汽流(steam)，通过柱供应管线(241)将所述富烃的干燥汽流送入柱(28)中，由此，所述柱(28)在高于气相反应器(13)的压力下运行，以去除低聚物、蜡和油；
m)通过第一回收管线(29)将部分未冷凝(non-condensed)丙烯重新导回至气相反应器，和/或通过第二回收进料管线(35)将冷凝丙烯送入丙烯进料罐(7)，和/或将部分冷凝丙烯送入丙烯丙烷分流器(splitter)。由此，优选地，能从所述未冷凝丙烯中清除惰性轻物质(lights)，并将其导向锅炉亦即蒸汽(steam)生产单元。
其中，循环气体冷却器(16)是在闭环冷却水系统(300)内的热交换器，该系统(300)包括冷却水泵(301)、二次热交换器(302)、膨胀箱(303)和在二次热交换器上方的旁路(304)。
与以往的Borstar设备不同，本发明的设备包含回收管线(29)，其可使未冷凝的丙烯重新引回气相反应器(13)。令人惊异的是，该设置在总转换率方面甚至在单体因子方面都是有益的。例如，在生产无规聚丙烯共聚物时，可以产生巨大的节约效益。
在本发明的方法中，柱(28)在高于气相反应器(13)的压力下运行。这使得部分烃类可以通过回收管线(29，29')再循环回气相反应器中。令人惊讶的是，在有乙烯的情况下，高氢气浓度是可能的，该方法的特点是高单程转化率。另一个令人惊讶的方面是，大量氢气被回收。这对高熔体流动速率等级非常有利：气相反应器所需的新鲜氢气可以减少。
另一方面，所得到的氮气、水蒸汽和丙烯被分离为
-富含烃类的干燥汽流(贫氮<0.5mol％)，该气流被送回柱(28)中；
-纯氮(>99mol％)汽流，通过氮气再进料管线(243)送回净化仓(23)；
-废水流和贫烃氮气流被送入热氧化器单元(43)。
本发明的设备的配置是，循环气体冷却器(16)是在闭环冷却水系统(300)内的热交换器，该系统包括冷却水泵(301)、二次热交换器(302)、膨胀箱(303)和在二次热交换器上方的旁路(304)。在本发明的设备和方法中，气体循环流由热交换器冷却，以在气相反应器中有非常有效的温度控制，所述气相反应器通常且优选为流化床反应器。聚合热优选转移到闭环冷却水系统(300)，该系统包括冷却水泵(301)、二次热交换器(302)、膨胀箱(303)和在二次热交换器上方的旁路(304)。聚合热通过闭环冷却水系统的热交换器被进一步转移到共同区域(common site)冷却水系统(例如可以是冷却水塔)。主要优点为，通过主热交换器的冷却水流可以在高于循环气体的露点之上的温度保持不变，为气相反应器的生产速率提供宽的操作窗口。使得50％或更高的可调节率成为可能。可调节率是指在减少生产量的情况下运行设备的能力。可调节率被定义为[1-(最小产能/设计产能)]。
在使用直接冷却水系统的情况下，冷却水返流温度会上升到高于共同区域冷却水系统的一般设计操作温度，即操作窗口会被限制。
本发明的设备优选具有以下一项或多项：
1)(通过击落气体中的液体粒子来分离气液的)气液分离鼓(knock down drum)(38)
2)气相反应器区域减压旋流器(39)
3)气相反应器(用)喇叭形气液分离鼓(40)。
这些单元提高本发明设备的安全性。
在本发明的方法中，循环气体冷却器(16)为热交换器，热量被转移到闭环冷却水系统，所述系统包括冷却水泵、二次热交换器、膨胀箱和在二次热交换器上方的旁路。更优选的是，聚合热通过闭环冷却水系统转移到共同区域冷却水系统(例如冷却水塔)，使恒定的冷却水能在高于循环气体露点的温度下流过气体循环内的热交换器。
在另一个方面，本发明的方法的特征在于，可调节率可超过50％。高可调节率使该方法在不同的产物和需求方面具有较高的灵活性。
分流比例(split)即在环流反应器和气相反应器中产生的物质的量之比分别为40-60比60-40。
在又一个方面，在第一和/或第二环流反应器(优选在两个环流反应器)中的聚合温度低于72℃，更优选低于70℃。
附图说明
下面结合附图对本发明进行说明。
图1中的附图标记
1 催化剂进料罐
2 可选的助催化剂进料罐
3 可选的用于活化剂和/或可选的外给电子体的进料罐
4 用于催化剂混合的可选的预接触单元
5，5'，5” 连接进料罐和催化剂进料罐(vessel)或预聚合反应器的进料管线
6 预聚合反应器
7 丙烯进料罐
8 第一环流反应器
9 第二环流反应器
10 环流反应器连接管线
11 用于添加单体和可选的共聚单体的装置
12 用于通入氢气的装置
13 气相反应器
14 气体循环管线
15 循环气体压缩机
16 循环气体冷却器
17 直接进料管线
18 用于添加共聚单体的装置
19 用于供给氢气的装置
20 可选的产物排出容器
21 产物出口加热器
22 产物收集罐
23 净化仓
24 丙烯氮气回收单元
25 出口管线(用于聚合物粉末)，配置有用于丙烯均聚物或丙烯共聚物的回收装置(可选地包括用于均质化、添加和造粒的装置)；
26 回收气体处理单元
27 气体回收压缩机
28 柱
28a 回流回收进料容器
29、29' 回收进料管线
30 用于循环气体冷却器的冷却回路
31 喷出单元
32 高压喷出仓
33 低压喷出仓
34 连接管线
35 回收进料管线
36 另一进料管线，可选地具有干燥器
38 气液分离鼓
39 气相反应器区域减压旋流器
40 气相反应器(用)喇叭形气液分离鼓轮
41,41',41” 丙烯进料管线
42 用于催化剂失活的装置(例如，用于引入低压蒸汽的装置)
43 热氧化器单元
44 用于输送液体丙烯单体的装置
48 净化仓进料管线
49 连接产物收集罐(22)和气体回收压缩机(27)的管线
51 从净化仓(23)到丙烯氮气回收单元(24)之间的进料管线
241 柱供应管线
242 排出管线
243 氮气再进料管线
244 外部氮气进料管线
245 用于催化剂失活剂(通常是低压蒸汽)的进料管线
246 另一氮气进料管线
247 用于输送氮气的管线
249 用于低聚物的出口管线
图1示出用于实施本发明方法的设备。
图2示出本发明的冷却装置。
图2中的附图标记
300 气相反应循环气体冷却器
301 闭环冷却水系统的冷却水泵
302 二次热交换器
303 闭环冷却水系统的膨胀箱
304 在二次热交换器之上的旁路
305 区域冷却水泵
306 区域冷却水塔
310 流向气相反应器的气体循环流
311 来自气相反应器的、压缩阶段后的气体循环流
312 闭环冷却水流
313 进入气相反应器循环冷却器的总闭式循环冷却水流
314 从气相反应器循环冷却器流出的闭环冷却水流
315 区域冷却水供应流
316 区域冷却水返回流
图3示出比较例的冷却水装置。
图3中的附图标记
400 气相反应器(用)循环气体冷却器
401 气相反应器冷却系统的冷却水泵
402 冷却水返流控制管线
403 冷却水旁路
404 冷却水供应控制管线
405 区域冷却水泵
406 区域冷却水塔
410 进入气相反应器的气体循环流
411 来自气相反应器的在压缩阶段后的气体循环流
412 新鲜冷却水供应流
413 进入气相反应器(用)循环气体冷却器的总冷却水流
具体实施方式
就本发明的设备结合图1作进一步描述。
本发明的用于制备丙烯均聚物和共聚物的设备包括用于催化剂(1)、可选的助催化剂(2)、可选的活化剂和/或可选的外给电子体(3)的进料罐。可选地，还具有用于催化剂混合的预接触单元(4)，其通过进料管线(5，5'，5”)与进料罐相连。在各种实施方案中，对于各种催化剂系统，预接触单元(tank)并不是必需的。
本发明装置还包括与进料罐(1、2、3)或预接触单元(4)连接的预聚合反应器(6)。预聚合在本领域是已知的。该设备还包括丙烯进料罐(7)、与预聚合反应器相连的第一环流反应器(8)和通过环流反应器连接管线(10)与第一环流反应器相连的第二环流反应器(9)，以及将共聚单体(11)和氢气(12)送入第一环流反应器(8)、第二环流反应器(9)和/或环流反应器之间的环流反应器连接管(10)中的一个或多个的装置。这样的配置常见于现有设备。
除了环流反应器之外，本发明的设备还包括气相反应器(13)，其配备有气体循环管线(14)、循环气体压缩机(15)和循环气体冷却器(16)，该气相反应器通过直接进料管线(17)至少与第二环流反应器相连接。本发明的设备还包括用于向气相反应器(13)输送单体(44)和/或共聚单体(18)和/或氢气(19)。此外，本发明的设备还可选地包括与气相反应器相连的产物排出容器(20)，该产物排出容器有助于操作的稳定性。可选地，本发明的设备还具有产物出口加热器(21)。通常情况下，产物出口加热器为若干单元。本发明的设备还包括与可选的产物排出容器(20)或与气相反应器(13)相连的产物收集罐(22)，以及至少一个净化仓(23)。
除此之外，该装置还包括至少一个丙烯氮气回收单元(24)，该单元有将烃类汽流送入柱(28)的柱供应管线(241)、将富氮汽流重新送入净化仓(23)的氮气再进料管线(243)、可选的热氧化装置(43)和用于将排出汽流可选地排出至可选的热氧化器(43)的排出管线(242)。可选地，还可以有进料管线，如氮气再进料管线(243)、外部氮气进料管线(245)、用于催化剂失活剂(即，通常为低压蒸汽)的进料管线。优选地，还包含用于低聚物的出口(249)。
本发明设备还包括用于丙烯均聚物或丙烯共聚物回收的装置(25)，所述装置(25)可选地包括用于均化、添加和造粒的装置、回收气体处理单元(26)，所述回收气体处理单元(26)包括至少一个压缩机(27)、所述柱(28)和回流进料容器(28a)，该回流进料容器(28a)通过回收管线(29)与气相反应器(13)的气体循环管线(14)相连。
除此之外，还有用于循环气体冷却器(16)的冷却回路(30)。该循环气体冷却器有助于实现较宽的操作窗口。
此外，还有喷出单元(31)，其包括高压喷出仓(32)、低压喷出仓(33)，该喷出单元(31)可选地通过连接管线(34)与产物收集罐(22)相连。
本发明设备还包括连接回收气体处理单元(26)和丙烯进料罐(7)的回收进料管线(35)。这条重要的回收进料管线(35)使丙烯还得以返送到环流反应器中，即，形成综合回收系统。
对本发明的冷却装置结合图2进行描述。冷却介质(通常是水)通过冷却水泵(301)在闭环冷却水系统中进行循环。水进入二次热交换器(302)，在该二次热交换器(302)中热量被转移到区域冷却水回路。区域冷却水回路包括区域冷却水塔(306)、区域冷却水泵(305)，但也可以包括热用户，即重新使用热量用于住宅供暖或类似用途。二次热交换器可以是任何类型，如板式、壳式和管式。
为了适当调节温度并保持通过主换热器(300)的流量恒定，在闭环冷却水系统中的二次换热器之上还有旁路(304)。在该闭环冷却水系统中，热量在气相反应器(用)循环气体冷却器(300)中从气体传递到水。如本领域所知，还有闭环冷却水系统的膨胀箱(303)。
图3示出带有循环泵的区域冷却水系统中的直接热交换器。该配置用于比较目的，并不可取。可以看出，区域冷却水回路直接与气相反应器(用)循环气体冷却器(400)连接。
实验部分
在下面的实施例中对本发明的设备和方法进行具例说明，但这些实施例是用于说明目的，而不是限制本发明的范围。
实施例1和2
在REF1和REF2中，没有使用气体循环冷却器，只有一个环流反应器。在实例IE1中，使用了气相反应器和气体循环冷却器。在实例IE2中，降低了再循环。
表1
可以看出，本发明设备及方法同时使得气相反应器具有高产量和高单程转化率。
实施例3
在第二个实验评估中，评估了催化剂效果(IE1对REF2)。
表2
本发明的方法获得了意想不到的催化效果：
实施例4
在使用本发明设备及方法的又一实验评估中，监测生产无规乙烯-丙烯共聚物时的冷却水温度。本发明使用了图2所示的闭环冷却水系统，而比较例中使用了图3所示的装置。
结果如表3所示。
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Claims (91)
1.用于制备丙烯均聚物或丙烯共聚物的设备，包括：
1)催化剂(1)、可选的助催化剂(2)、可选的活化剂和/或可选的外给电子体(3)的进料罐；
2)可选的用于催化剂混合的预接触单元(4)，通过进料管线(5，5'，5”)与进料罐连接；
3)与进料罐(1，2，3)或预接触单元(4)连接的预聚合反应器(6)；
4)丙烯进料罐(7)；
5)与预聚合反应器连接的第一环流反应器(8)；
6)通过环流反应器连接管线(10)与第一环流反应器连接的第二环流反应器(9)；
7)向第一环流反应器(8)、第二环流反应器(9)和/或环流反应器之间的环流反应器连接管线(10)中的一个或多个送入单体和可选的共聚单体(11)以及氢气(12)的装置；
8)气相反应器(13)，配备有气体循环管线(14)、循环气体压缩机(15)和循环气体冷却器(16)，所述气相反应器通过直接进料管线(17)至少与第二环流反应器相连接；
9)用于将单体(44)和/或共聚单体(18)和/或氢气(19)送入气相反应器(13)的装置；由此，优选地，所述用于送入单体和/或共聚单体的装置适合将单体和/或共聚单体以冷凝形式送入；
10)可选的与气相反应器相连的产物排出容器(20)；
11)可选的产物出口加热器(21)；
12)与可选的产物排出容器(20)或与气相反应器(13)相连的产物收集罐(22)；
13)至少一个净化仓(23)；
14)至少一个丙烯氮气回收单元(24)；
15)将烃类汽流送入柱(28)的柱供应管线(241)；
16)氮气再进料管线(243)，用于将富含氮气的汽流重新送入净化仓(23)；
17)可选的热氧化器单元(43)；
18)排出管线(242)，用于将排出汽流可选地排放到可选的热氧化器(43)；
19)用于丙烯均聚物或丙烯共聚物回收的装置(25)，可选地包括用于均化、添加和造粒的装置；
20)回收气体处理单元(26)，包括至少一个压缩机(27)、柱(28)和回流进料容器(28a)，回流进料容器(28a)通过回流管线(29)与气相反应器(13)的气体循环管线(14)相连；
21)用于循环气体冷却器(16)的冷却回路(30)；
22)喷出单元(31)，包括高压喷出仓(32)、低压喷出仓(33)，所述喷出单元(31)可选地通过连接管线(34)与产物收集罐(22)连接；
23)连接回收气体处理单元(26)和丙烯进料罐(7)的回收进料管线(35)，其中，循环气体冷却器(16)是在闭环冷却水系统(300)内的热交换器，所述系统包括冷却水泵(301)、二次热交换器(302)、膨胀箱(303)和在二次热交换器上方的旁路(304)。
2.根据权利要求1所述的设备，其中，所述设备进一步包括以下一项或多项：
24)气液分离鼓(38)
25)气相反应器区域减压旋流器(39)
26)气相反应器喇叭形气液分离鼓(40)。
3.制备丙烯均聚物或丙烯共聚物的方法，包括：
a)在进料罐(1、2、3)中提供催化剂、可选的助催化剂、可选的活化剂和/或可选的外给电子体；
b)将所述催化剂、所述可选的助催化剂、所述可选的活化剂和/或所述可选的外给电子体送入预接触单元(4)，提供混合催化剂体系；将所述混合催化剂体系送入预聚合反应器(6)，或将所述催化剂、所述可选的助催化剂、所述可选的活化剂和/或所述可选的外给电子体送入预聚合反应器(6)；
c)通过引入丙烯单体和可选地引入共聚单体，引发预聚合，从而获得预聚物；
d)将所述预聚物送入第一环流反应器(8)，将丙烯可选地与共聚单体一起进行聚合，产生第一中间体；
e)通过环流反应器连接管线(10)将第一中间体送入第二环流反应器(9)，将丙烯可选地与共聚单体一起进行进一步聚合，产生第二中间体物，由此，丙烯通过丙烯再进料管线(41)从丙烯进料罐(7)送入第二环流反应器；
f)在其他进料点向环流反应器引入共聚单体和/或氢气；
g)通过直接进料管线(17)将含有未反应单体的第二中间体直接送入气相反应器(13)；
h)通过送入丙烯和/或共聚单体和/或氢气并经由气体循环管线(14)在向上方向上进行气体循环，在所述气相反应器(13)中进一步聚合丙烯和可选的共聚单体，从而使循环气体在循环气体冷却器(16)中得到冷却；
i)可选地，将气相反应器的产物排出至可选的产物排出容器(20)中，然后通过连接管线(34)进入产物收集罐(22)，形成原料混合物，
或将气相反应器产物直接排出至产物收集罐(22)，形成原料混合物；
j)将所述原料混合物送入净化仓(23)；
k)用氮气和催化剂失活剂吹扫所述原料混合物，催化剂失活剂优选为水蒸汽；
l)在丙烯氮气回收单元(24)中将来自净化仓(23)的氮气、失活剂和烃分离，从而
-提供基本纯净的氮气汽流，通过氮气再进料管线(243)将所述基本纯净的氮气汽流送入净化仓(23)；
-提供贫烃废料汽流，通过排出管线(242)将所述贫烃废料汽流送入热氧化器单元(43)；
-提供富烃的干燥汽流，通过柱供应管线(241)将所述富烃的干燥汽流送入柱(28)中，由此，所述柱(28)在比气相反应器(13)的压力高的压力下运行，以去除低聚物、蜡和油；
m)将冷凝的丙烯和丙烷再送入以下一个或多个中
-通过回收进料管线(35)送入到所述丙烯进料罐(7)；
-送入可选的丙烷/丙烯分流器
并通过管线29将至少一部分非冷凝物送入气相反应器；
其中，循环气体冷却器(16)是热交换器，热量通过闭环冷却水系统(300)转移，所述系统(300)包括冷却水泵(301)、二次热交换器(302)、膨胀箱(303)和在二次热交换器上方的旁路(304)。
4.根据权利要求3所述的方法，其中，聚合热通过闭环冷却水系统转移到共同区域的冷却水系统，例如冷却水塔，使恒定的冷却水能在高于循环气体露点的温度下流过气体循环内的热交换器。
5.根据权利要求3或4所述的方法，其中，使气相反应器的生产率有50％的可调节率。
6.根据权利要求3至5中任一项所述的方法，其中，第一和/或第二环流反应器中的聚合温度，优选在两个环流反应器中的聚合温度都低于72℃，更优选低于70℃。
7.根据权利要求3至6中任一项所述的方法，其中，在气相反应器中以40％至60％的分流比例制备均聚物。
8.根据权利要求4至7中任一项所述的方法，其中，在气相反应器中以40％至60％的分流比例制备无规乙烯-丙烯共聚物。
9.根据权利要求3至8中任一项所述的方法，其中，气相反应器中的聚合温度为80℃至90℃，压力为19至25barg，更优选为20至24barg。
10.根据权利要求3至9中任一项所述的方法，其中，柱的操作压力为26barg，更优选为25barg，最优选为24barg。
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| EP20209881.0A EP4006060A1 (en) | 2020-11-25 | 2020-11-25 | Propylene polymerization plant and propylene polymerization process |
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| PCT/EP2021/082469 WO2022112159A1 (en) | 2020-11-25 | 2021-11-22 | Propylene polymerization plant and propylene polymerization process |
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| FI111848B (fi) | 1997-06-24 | 2003-09-30 | Borealis Tech Oy | Menetelmä ja laitteisto propeenin homo- ja kopolymeerien valmistamiseksi |
| FI111952B (fi) | 1997-11-17 | 2003-10-15 | Borealis Tech Oy | Menetelmä ja laitteisto polymeerien valmistamiseksi |
| EP3438133A1 (en) * | 2017-08-04 | 2019-02-06 | Basell Polyolefine GmbH | Polymerization process including discharging polyolefin particles from a gas-phase polymerization reactor |
| CN111295399B (zh) * | 2017-11-06 | 2022-09-06 | 埃克森美孚化学专利公司 | 基于丙烯的抗冲共聚物及生产方法和设备 |
| CN109776702A (zh) * | 2017-11-10 | 2019-05-21 | 北京华福工程有限公司 | 聚丙烯或丙烯乙烯共聚物的制备方法 |
| CN207685181U (zh) * | 2017-11-10 | 2018-08-03 | 北京华福工程有限公司 | 抗冲聚丙烯的聚合系统 |
| CN110394125A (zh) * | 2019-08-30 | 2019-11-01 | 徐州聚西廷新型材料科技有限公司 | 一种聚丙烯的制备方法 |
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- 2021-11-22 US US18/252,464 patent/US20240010765A1/en active Pending
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- 2021-11-22 KR KR1020237019510A patent/KR20230104942A/ko unknown
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| TWI792703B (zh) | 2023-02-11 |
| MX2023005497A (es) | 2023-05-26 |
| EP4006060A1 (en) | 2022-06-01 |
| JP2023550314A (ja) | 2023-12-01 |
| TW202221046A (zh) | 2022-06-01 |
| US20240010765A1 (en) | 2024-01-11 |
| WO2022112159A1 (en) | 2022-06-02 |
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