CN1120041C - 具有接触管束的反应器 - Google Patents

具有接触管束的反应器 Download PDF

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CN1120041C
CN1120041C CN99809598A CN99809598A CN1120041C CN 1120041 C CN1120041 C CN 1120041C CN 99809598 A CN99809598 A CN 99809598A CN 99809598 A CN99809598 A CN 99809598A CN 1120041 C CN1120041 C CN 1120041C
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reactor
circulating line
exchange medium
heat exchange
contact tube
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CN1312733A (zh
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F·科尔
G·奥尔贝特
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Abstract

本发明提出了一种具有一个接触管束(2)的反应器(1)，通过它的包围接触管的空间进行热交换介质循环。该反应器在反应器两端具有带外套孔(5，6)的环形管道(3，4)，用一台泵通过一个外部的热交换器进行热交换介质的输入和输出，其中热交换介质输入下环形管道(4)并通过上环形管道(3)向热交换器输出。该反应器还具有导向板(7)，这些导向板交替地在反应器中部和反应器边缘留出一个通道截面。其中，上环形管道(3)和下环形管道(4)分别用一个圆筒外套形中间壁(8，9)分成一个内环形管道(11，13)和一个外环形管道(12，14)，而热交换介质输入外部下环形管道(14)则是这样进行的：通过反应器外部的一个区域进入内部上环形管道(11)、通过外套孔(5)进入包围接触管(2)的空间、通过外套孔(6)进入内部下环形管道(13)并紧接着通过反应器外部的一个区域进入外部上环形管道(12)。

Description

具有接触管束的反应器
本发明涉及一种具有一接触管束的反应器，通过它的包围接触管的空间进行热交换介质循环，以及涉及该反应器进行氧化反应的应用。
这类反应器的一般结构由一个通常为圆筒形的容器组成，在该容器内通常垂直布置一束即许多接触管。这些可能含有接触剂的接触管用其端部密封固定在管板内并分别与一个在上端或在下端与该容器连接的端盖连通。流经这些接触管的反应混合物经端盖输入或输出。通过包围这些接触管的空间进行热交换介质循环，以便尤其是在以强大的热效应进行反应时达到热平衡。
出于经济上的原因，反应器应使用尽可能多的接触管，所用的接触管数量通常为15000至30000的范围(参见DE-A-4431949)。
众所周知，就热交换介质循环而言，反应器的任一水平断面内都应达到热交换介质的尽量均匀的温度分布，以便尽可能全部接触管均匀参与反应(例如DE-B-1601162)。通过分别在反应器端部安装的带有许多外套孔的外部环形管道进行供热或散热来实现温度分布的均匀性，这种环形管道例如在DE-B-3409159中进行了描述。
热传导的进一步改善通过安装导向板来实现，这种导向板交替地在反应器中部和反应器边缘打开一个通流横断面。这种装置特别适用于具有一个中心自由空间的环形布置的管束，例如参见GB-B-310175。
多数反应器具有的接触管的数量都在上述大约15000至30000的范围内并配有导向板，热交换介质的压力损失很大。所以，为了克服压力损失，必须把导走氧化反应时放出的热通常所用的硝酸钾和亚硝酸钠的低共熔融盐用扬程大约4至5米的泵打入上述规格的反应器中，这种熔融盐在使用温度约为350至400℃的情况下，具有与水相似的粘度。
对这类大型反应器来说，泵系统最好布置在上下环形管道之间，其中热交换介质例如经一根环形管道输入反应器的下部范围。
对这类大型反应器来说，如果熔融盐直接泵入反应器上部或上环形管道，则要求4至5米的扬程，势必尤其是由于昂贵的泵轴密封、较长的泵轴以及通过泵轴较大的热输入下部电动机轴承而导致一个技术上不利的和易于发生故障的泵系统。此外，上述的扬程势必需要一个放在高处的熔融盐容器，出于安全原因，这是不受欢迎的。
众所周知，热交换介质在反应器上端即顺流输入和反应混合物同样在反应器上端输入接触管是对反应有利的(见DE-A-4431449)。
与逆流运行方式比较，顺流运行具有诸多优点，例如：较高的通过能力、较低的接触剂热点温度、热交换介质温度在接触管的最终反应方向内的符合理想的升高、在整个反应器横断面内热交换介质的良好的温度均匀性即良好的水平温度层、由于不存在热交换介质的反馈而在接触管空间的整个高度内呈现明确的工况。
但如果热交换介质例如直接经一根上环形管道输入反应器上部区域并以反应器下部区域例如直接经一根下环形管道输出，则正如DE-A-4431449所述，或DE-A-2201528所示(图1)，反应混合物和热交换介质的顺流运行在泵系统方面就会遇到上述的困难。
所以本发明旨在提出一种在泵系统方面不存在上述缺点的反应器。这种泵系统将反应器下部区域内的热交换介质输入下环形管道并从上环形管道输出热交换介质，而不改变具有许多接触管例如高达40000，特别是15000至30000根接触管的大型反应器的良好结构；但热交换介质和输入接触管的反应混合物却可按顺流方式环流这些接触管。
本发明以具有一个接触管束的反应器为出发点，热交换介质循环通过它所包围的接触管的空间进行，该反应器具有在反应器两端的、设有外套孔的环形管道，必要时在热交换介质或热交换介质的分流通过一个或多个外部热交换器转移的情况下，用一台或多台泵进行热交换介质的输入或输出，其中热交换介质输入下环形管道并经上环形管道回到泵中，该反应器具有导向板，这些导向板交替地在反应器中部和反应器边缘留有一个通道截面。
本发明的特征为：上下环形管道分别用一个圆筒形外套中间壁分成一个内环形管道和一个外环形管道；外部下环形管道的热交换介质经内部上环形管道的反应器外面的一个区域、经该管道外套孔输入包围接触管的空间，再经这些圆周上的孔进入内部下环形管道并最后经反应器外部的一个区域通过外部上环形管道输出。
业已发现，上下环形管道之间的空间可用来进行热交换介质的导向，其中热交换介质和反应混合物的顺流运行方式的优点是与热交换介质输入下环形管道的有效的泵系统分不开的。
为此，本发明分别在上环形管道和下环形管道中设置了一个圆筒形外套中间壁来分别把它们隔成一个内环形管道和一个外环形管道。热交换介质输入外部下环形管道，后者通过上下环形管道之间的区域与内部上环形管道连接，热交换介质从这里按已知的方式经管道外套孔进入包围接触管的空间，并通过导向板按已知的方式形成弯曲形状的流体。热交换介质经管道外套孔按已知的方式离开反应器包围接触管的空间并进入下部内环形管道，后者又通过上下环形管道之间的区域与上部外环形管道连接。
有利的是，上下环形管道之间的区域通过一个圆筒形外套封闭，形成一个空心圆筒，该圆筒通过垂直位于反应器基面上的径向中间壁分成若干小室，这些小室到环形管道的隔墙交替地留有内外环形段，其中从俯视图看出，在封闭的环形段上方总是有一个敞开的环形段，或者正好相反。所以来自一台泵或多台泵的热交换介质和来自反应器室的热交换介质交替地、总是从下到上地流经这些小室。
原则上，这些小室的数量没有限制，但出于合理性的原因，其数量可为12至96个，最好24至48个，这样，各12至24个小室(相当于每四分之一圆周有3至6个小室)交替地用于把热交换介质输入(转向)包围住接触管的反应器室的上部区域或从下部区域输出热交换介质。
原则上，把上环形管道以及下环形管道分别隔成一个内环形管道和一个外环形管道的圆筒形外套中间壁可具有任意的直径，该直径位于环形管道的外直径和内直径之间，但圆筒形外套中间壁的该直径最好小于或等于环形管道的外直径和内直径的算术平均值。
根据一个优选的结构型式，在流向一个泵或多个泵的热交换介质的所流经的小室的至少一部分中分别设置了一个旁通室，该旁通室具有到反应器室的孔以及在外部上环形管道的范围内具有一块调节板，其中该调节板的位置可通过一个伺服传动装置和一根传动轴在反应器纵轴内进行调节。在这个结构型式中，来自反应器室的热交换介质的可调节的分流已经减少到反应器的平均高度，所以热交换介质的剩余部分只流经包围住接触管的反应器室的下部。这种结构型式对于接触管下部留下的热散发最佳化。此外，达到了减小压力损失的目的，这样就可减小泵功率，从而提高经济性。
该反应器不受热交换介质种类的限制；这种热交换介质同样可用来散热，亦即用来进行散热反应，也可用来向流经接触管的反应混合物供热，亦即用来进行吸热反应。
该反应器特别适用于进行氧化反应，尤其是特别适用于制造邻苯二甲酸酐、马来酸酐、乙二醛、异丁烯醛和甲基丙烯酸。
下面结合实施例和附图来详细说明本发明，附图表示：
图1，右侧：按本发明具有热交换介质循环的反应器的一个纵断面；
图1，左侧：按先有技术具有热交换介质循环的反应器的一个纵断面；
图2，右侧：在上环形管道和中间空心圆筒之间的分界面范围内通过本发明反应器剖开的一个横断面(断面A-A)；
图2，左侧：在平面A-A内通过先有技术的反应器剖开的一个横断面；
图3，右侧：在中间空心圆筒的范围内通过本发明反应器剖开的一个横断面(断面B-B)；
图3，左侧：在平面B-B内通过先有技术的反应器剖开的一个横断面；
图4，右侧：在中间空心圆筒和下环形管道之间的分界面范围内通过本发明反应器剖开的一个横断面(断面C-C)；
图4，左侧：在平面C-C内通过先有技术的反应器剖开的一个横断面；
图5：为了说明热交换介质导向到包围接触管的空间而从本发明反应器截取的一段；
图6：为了说明热交换介质从包围接触管的空间输出到一台或多台泵而从本发明反应器截取的一段；
图7：本发明反应器一个优选结构型式的一段；
图8：具有两个热交换介质循环的本发明反应器的一个横断面。
图1表示具有一个垂直接触管束2的圆筒形反应器1，该管束在圆筒中心留有一个内腔，该反应器具有一根下环形管道4以及一根上环形管道3，热交换介质输入该下环形管道并通过该上环形管道输出。其中热交换介质的输入或输出是通过外套孔5和6来实现的，该反应器还具有导向板7，用来产生一种曲折形的热交换介质循环。
先有技术的反应器结构(图1左侧)与本发明的反应器结构(图1右侧)是相同的。
从图1右侧可清楚看出，与先有技术比较，本发明反应器进行了如下的修改：
上环形管道3通过一个圆筒外套形的中间壁8分成一个内部的上环形管道11和一个外部的上环形管道12；相似地，下环形管道4用一个圆筒外套形中间壁9分成一个内部的下环形管道13和一个外部的下环形管道14。
环形管道3和4之间的部位最好用一个圆筒形外套15封闭成一个空心圆筒.在这个部位内，热交换介质进行转向，即从外部下环形管道14转到内部上环形管道11或从内部下环形管道13转到外部上环形管道12。在中间空心圆筒范围内的热交换介质的这种转向最好借助垂直位于反应器基面上的径向中间壁17构成的小室来实现(图3)。
中间空心圆筒分界面范围内的热交换介质转向到上或下环形管道可从图2右侧或图4右侧所示的横断面一目了然：通过圆筒外套形中间壁8或9和径向中间壁17形成了若干内外圆形段。根据本发明，如图2右侧或图4右侧所示，这些环形段交替地作为敞开的环形段18或封闭的环形段19构成。这里交替的意思是：在每个内部或外部环形管道上，一个敞开的环形段总是紧跟着一个封闭的环形段；此外，从俯视图看去，横断面A-A中的一个敞开的环形段18与横断面C-C内的一个封闭的环形段19对应，或者相反。通过这种结构可使来自一台泵或多台泵的热交换介质和来自反应器室的热交换介质交替地总是从下到上地流经这些小室，如图3所示。
为了说明热交换介质的导向，图5和图6示出了本发明反应器的一段：
图5示出了一个小室16，来自泵的热交换介质经外部下环形管道14通过敞开的环形段18流入小室16中、从下向上流经该小室、在上部范围经另一个敞开的环形管段18、流入内部上环形管道11并经孔5流入包围接触管的反应器室中。
而来自包围接触管的反应器室的热交换介质则通过孔6经内部下环形管道13和敞开的环形段18进行导向而流经与图5所示的小室16直接相邻的图6所示的小室16。热交换介质从该小室16经另一个敞开的环形段18流入上部外环形管道12并从该处向泵流去。
图7表示本发明反应器的一个优选结构型式。根据这个结构型式，在流向泵的热交换介质所流的小室16的至少一部分中，分别设置了一个带有一个通向反应器室的孔21的附加旁通小室20，以及在通向上部外环形管道12的小室16的隔壁范围内设置了一块调节板22。调节板22的位置可通过一个适当的伺服传动装置和一根传动轴23在反应器纵轴的方向内进行改变。
图8表示具有两个热交换介质循环的本发明反应器的一个优选结构型式。这个反应器在结构上与图1右侧所示只有一个热交换介质循环的反应器相似。在第二个热交换介质循环中，用相应的参考号表示与第一热交换介质循环相应的特征。
类似地，可对本发明反应器补充别的热交换介质循环。从而可使反应器最佳匹配要进行的反应的相应具体的热分布特性。

Claims (8)

1.具有一个接触管束(2)的反应器(1)，在其包围接触管的空间内进行热交换介质循环，该反应器具有在反应器两端的带有外套孔(5、6)的环形管道(3，4)，必要时在热交换介质或热交换介质的分流通过一个或多个外部热交换器转移的情况下，用一台或多台泵进行热交换介质的输入或输出，其中热交换介质输入下环形管道(4)并经上环形管道(3)回到泵中，该反应器具有导向板(7)，这些导向板交替地在反应器中部和反应器边缘留出一个通道截面，其特征为：上环形管道(3)和下环形管道(4)分别用一个圆筒外套形的中间壁(8，9)分成一个内环形管道(11，13)和一个外环形管道(12，14)；热交换介质经外部下环形管道(14)输入、通过反应器外部的一个区域输入内部上环形管道(11)、通过外套孔(5)输入包围接触管(2)的空间、再经外套孔(6)进入内部下环形管道(13)并紧接着经反应器外部的一个区域通过外部上环形管道(12)输出。
2.按权利要求1的反应器(1)，其特征为，下环形管道(4)和上环形管道(3)之间的区域通过一个圆筒形外套(15)封闭，其中形成一个空心圆筒，该空心圆筒通过垂直位于反应器基面上的径向中间壁(17)分成小室(16)，该小室朝环形通道(3，4)的隔壁交替地留有内外环形段，其中从俯视图看去，在封闭环形段(19)的上方总是有一个敞开的环形段(18)，或者正好相反。
3.按权利要求1或2的反应器(1)，其特征为，小室(16)的数量为12至46个，最好为24至48个。
4.按权利要求1至3任一项的反应器(1)，其特征为，圆筒外套形的中间壁(8，9)的直径小于或等于环形管道(3，4)的外直径和内直径的算术平均值。
5.按权利要求1至4任一项的反应器(1)，其特征为，在流向泵的热交换介质所流经的小室(16)的至少一部分中，分别设置了一个旁通小室(20)，该旁通小室具有一个通向反应器室的外套孔(21)以及在外部上环形管道(12)的范围内具有一块调节板(22)，其中调节板(22)可通过一个伺服传动装置(24)和一根传动轴(23)在反应器纵轴的方向内进行调节。
6.按权利要求1至5任一项的反应器(1)，其特征为，通过包围接触管的空间可进行的两个或多个热交换介质循环。
7.按前述权利要求任一项的反应器在氧化反应中的应用。
8.按权利要求7所述的反应器在氧化反应中的应用，其特征在于，所述氧化反应是制造邻苯二甲酸酐、马来酸酐、乙二醛、异丁烯醛或甲基丙烯酸的氧化反应。
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