CN101249393A - 用于混合两种或多种气流或液流的方法和装置 - Google Patents

用于混合两种或多种气流或液流的方法和装置 Download PDF

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CN101249393A
CN101249393A CNA2007101995089A CN200710199508A CN101249393A CN 101249393 A CN101249393 A CN 101249393A CN A2007101995089 A CNA2007101995089 A CN A2007101995089A CN 200710199508 A CN200710199508 A CN 200710199508A CN 101249393 A CN101249393 A CN 101249393A
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T·汉森
M·S·斯克乔思-拉斯穆森
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Abstract

本发明提供用于混合两种或多种气流或液流的一种方法，其中在入口室中组合各气流然后在一个或多个阶段中重复加速和减速该气流，在每个步骤中将加速的组合气流的最大线性速度值保持在气流的质量流速的范围内。本发明还提供用于混合两种或多种气流或液流的装置，一个实施例包括有座的机体；带塞的心轴，该塞安装在该座中而该座和塞有许多锥形的表面构成相同的多个锥形环形空间。在混合时心轴能使该塞在该座中在轴向上移动。另一个实施例包括机体，带管塞的心轴。笼和环形的混合元件围绕该管塞。

Description

用于混合两种或多种气流或液流的方法和装置
技术领域
本发明涉及充分混合两种或多种流体流。
本发明特别涉及用于混合两种或多种流体流的方法和装置，在流体中产生流速的变化。
在催化部分氧化反应器中本发明是特别有用的，那里烃类进料和氧化剂进料必须非常充分地混合。要得到在接着的催化床中优化的反应这是很重要的。
背景技术
在现有技术中已知各种流体混合器，还有在催化部分氧化之前用于烃类与氧化剂混合的那些混合器。
为了这个目的，Schulzer Chemtech公司已经开发了一种静态混合器，它们表示在因特网上可找到的小册子中。该混合器包括一根管子，在管子内表面上或在安装在管子中的轴上有叶片，而叶片产生混合、湍流的流况。
在美国专利5,026,946号中表示一种混合器，其中将烃类与氧化剂混合。该混合器包括两个同心的管子，内管在一端封闭并装设多个小孔。烃在管之间的环形空间内流动，氧化剂通过孔从内管流出并与烃混合。
美国专利5,112,527号公开一种用于低烷烃如天然气的自热转化的工艺。为了均匀混合气态的烷烃、蒸汽和含有气体的氧气在入口通道中安装静态混合器。但是，在静态混合器中的混合效率和产生的压力降将随着流过混合器的气量而变化。
日本专利JP 32 13 132号描述了另一个混合器，在壳体中通过转轴混合各种气体。轴的表面和壳体的内表面两者都呈现螺纹凹槽的形状。这把气体推入到流动面积有一些最大和最小尺寸的流动通道。
在美国专利6,092,921号中公开的混合器/扩散器包括入口室、膨胀器和出口室，其中将一个物体插入到膨胀器中产生锥形的环形流动通道。
充分混合两种或多种气体或液体不可避免地要损失压力降。现有技术混合装置的普遍现象是，当在操作中流速增加时，产生的压力降也显著增加。而当流量减小时混合的质量也随之降低。
因此本发明的目的是提供一种简单的混合方法和装置，它充分混合两种或多种流体，在流速改变时同样混合充分，但不会改变通过混合器产生的压力降和混合效率。
发明内容
按照上述目的本发明涉及一种用于混合两种或多种流体流的方法，其中在入口室将各种流体组合随后在一个或多个阶段中重复加速和减速。通过调节最小流动通道的面积，在每个步骤中将加速的组合流的最大线性速度值保持在进料流的质量流速的范围内。
本发明还提供用于混合两种或多种气流或液流的装置。装置的一个实施例包括有座的主体；带塞的心轴，将心轴安装在该座中和该座和该塞有许多锥形的表面构成相同的多个锥形的环形空间。在混合操作时使心轴能在轴向在该座中移动该塞。该心轴和该塞可以包括流动通道。
本发明的另一个实施例提供用于混合两种或多种气态或液态进料流的一种装置，和它包括主体和与同轴安装在主体中的管塞连接的可移动的心轴。靠近心轴的管塞是穿孔的，而在另一端它是开口的。通过穿孔进料流进入管塞。带喷嘴的笼围绕管塞，许多环形混合元件围绕笼，这些混合元件是互相分隔的。笼和混合元件在一端闭合，而那里的管塞端是开口的。
本发明在流速的一定范围内在恒定的压力降下保证各流体的充分混合。
附图说明
图1是本发明混合装置一个实施例的剖面图。
图2是安装在反应器入口本发明混合装置的剖面图。
图3是按照本发明混合和控制进料气体的反应器图。
图4是本发明混合装置另一个实施例的剖面图。
图5是本发明混合装置又一个实施例的剖面图。
具体实施方式
在所有的工艺过程中都有各种气体和/或各种液体的混合，而安装在这样的混合下游的设备的性能取决于混合的效率。
一个例子是用烃(hydrocarbon)、蒸汽和氧化剂生产包含H2/CO的合成气，氧化剂可以是空气、氧气或混合物，即富氧的空气。将原材料混合随后进行催化氧化。还有，很重要的是在气体混合物进入催化床之前避免在氧气和烃之间的反应。
为了得到催化床中优化的反应，非常重要的是在进入催化床之前将各气流充分混合。
混合两种或多种气体或液体的一种有效方法是让刚刚放在一起的各流体多次加速和减速并有足够高的最大速度，这有助于防止在催化床的上游产生反应。当加速的流体在下一个室中减速时，在室中产生涡流道混合各流体。
与石油化工厂中其他的管道部件和反应器内部产生的压力降比较，这种压力降是有点高。
重要的是在装置的所有生产能力下得到充分的混合，而不会在高生产能力时造成过度大的压力降，而在装置低生产能力时损失混合的效率。
本发明提供一种方法和装置，用于在很宽的生产能力范围内通过多次加速和减速并在恒定的压力降下混合两种或多种流体。通过改变在混合器加速部分中窄的流动通道的流通面积达到这个目的。通过这种方式，在很宽的流速范围内维持流体的快速线性速度、增加的压力降和混合效率都不变。
现在已经发现通过包括座和带塞的心轴的混合器达到了这个目的，其中座和塞的表面形成各环形空间和各室，流体通过它们流动。环形空间是锥形的，能使心轴上下移动(当垂直安装时)从而调节流通面积。
该座包括各室之间的很多孔，它们是各室之间流通连接的孔。这迫使各室中的气体多次改变流动方向90°，一般3-5次，取决于特定的设计。
心轴和塞可以是穿孔的，从而使液体可以流入到这个通道中并从安装在塞上的喷淋喷嘴流出。
另一种是，可移动的塞可以是管子，在心轴的一端有多个孔而其另一端是开口的。代替座，由笼围绕管塞，而笼由水平的气体混合元件围绕。各部件互相分隔，从而使进料气体仅能流过没有被管塞堵塞的各室和笼的一部分。
这就保持最大的线性速度因而所需的压力降和生成的涡流也是恒定的，这对用变化的流速充分混合各流体是很重要的。
将设计一种混合器以便在一定的压力降下获得最好的混合，因而必须将压力降保持恒定。
在设计座和塞之间有环形流动通道的气-气混合器时，将流速与环形空间流通面积之间的关系表示如下：
R 1 = F D seat 2 - D plug 2 * P ref P * T T ref
式中：F是总的气流流速，以Nm3/sec(标准立方米/秒)表示
Dseat和Dplug是座的内直径和塞在相同位置环形空间中的直径，以m(米)表示
P是混合器中压力，以MPa(兆帕)表示和Pref是3.0MPa
T是混合器中温度以K(绝对温度)表示和Tref是473.15K。
R1必须在1*106和1*108Nm3/sec/m2之间的范围内优选地是在5*106和2*107Nm3/sec/m2之间。
组合的进料流速和在座中各室之间孔的横截面积之间的关系用比R2表示，R2可用下式表示
R 2 = F n * D hole 2 * P ref P * T T ref
式中：F是总的气流流速，用Nm3/sec表示
n是孔数
Dhole是在室之间一个孔的直径，以m表示
P是混合器中压力，以MPa表示和Pref是3.0MPa
T是混合器中温度，以K表示和Tref是473.15K
R2必须在5*105和1*107Nm3/sec/m2之间的范围内优选地是在1*106和2*106 Nm3/sec/m2之间。
可将该混合器安装在需要充分混合两种或多种流体的任何地方。在CPO反应器中将混合器安装在反应器的入口法兰中是方便的。由各附图进一步描述该混合器。
本发明的一个实施例表示在图1中。混合器1包括座2和塞3；要混合的流体如箭头所指进入流过两个环形通道，从那里它们流到入口室，该室可选地由多孔介质4充填，从那里它们流过孔8到室9。混合后的流体流过出口5。在已经进入到室9后，流体流过第1个环形空间6，在那里在塞3和座2之间流体加速。流体从环形空间以高速流出进入到一个室7中，在那里它们被减速和被迫改变方向，第1个90°从垂直到水平进入到室中，然后从水平到垂直通过孔8到室9。在室9中生成涡流造成附加的充分混合。然后方向从垂直变到水平接着又变到垂直流入到下一个环形空间6。从而在室7和9内产生湍流和合适的混合。
在图2中表示混合器一个实施例的安装。将混合器安装在催化部分氧化(CPO)反应器的上入口10，机体11与入口连接。将导管12插入到机体11中和将塞3的心轴17穿过机体11和导管12并通过起动器13使其可上下移动，从而它改变座2和塞3之间的流通面积。在心轴17和导管12之间安装内管14。
氧化剂/蒸汽进料通过氧化剂入口15进入混合器并在心轴17和内管14之间流动，而烃/蒸汽进料通过烃入口16进入并在内管14和导管12之间流动。这些气体在混合器的加速/减速部分流到一起，在混合器的下游混合的气体通过出口5离开混合器并进入CPO反应器。
在操作时混合器的性能表示在图3中。在CPO反应器20中安装催化剂床21。混合气体流过灭火器22到达CPO反应器中催化床21入口的空间。
将压力表23安装在氧化剂入口管并将另一个压力表24安装在混合器出口。压力测量仪表25接受从23和24来的信号，它计算出跨过混合器的压力降并将这个信号送到控制器26。控制器26通过送信号到起动器13使起动器上下移动心轴调节环形空间的流通面积来保持压力降恒定。这就保证在很宽的可操作的生产能力范围内有恒定的压力差和最优的混合。
在图4中表示混合器的另一个实施例。在这个图中，混合器1包括机体11和心轴17，将心轴连接到管塞33。在接近心轴17处管塞33有孔39，管塞33的另一端是开口的。可选地，在孔39的上游和管塞33的内部安装多孔材料4。管塞33同轴地被笼34，即带喷嘴的管子围绕。在管塞和笼之间的空间刚好这样宽，使管塞可在笼内滑动。可用预先决定的方式，如螺旋形方式设置喷嘴。围绕笼34，放置水平的环形丝网混合元件35，在水平方向这些部件是互相隔离的，部件35被穿孔管36包围。
笼和混合元件在下端封闭而管塞下端是开口的。当垂直安装时，笼34的高度与管塞33无穿孔部分的高度基本上是相同的。从而当管塞33分别定位在上部、中部或下部位置时可以堵塞零个、某些或全部的喷嘴。
还有，笼喷嘴的总面积是显著地小于混合器任何其他流动通道的流通面积。
氧化剂/蒸汽入口流从入口环形32进入混合器，而烃/蒸汽入口流从包围的入口环形引进入。两个流流入多孔材料4中，从那里它们通过入口孔39进入管塞33。在气体流混合之后，混合后的气体从穿孔管36流入到出口沟道37和通过出口孔38流出混合器1。
在图5中表示有环形气体流动通道的混合器的别的用途和实施例。在这个实施例中在心轴和塞3内钻孔形成流动通道41，因而液体可在这个内部液体流动通道中流动。在液体流动通道的出口将喷淋喷嘴42连接到塞3，从而将液体喷淋高速引入到混合的气体中。在通道中液体的一个例子是液总烃。
本发明对混合两种或多种流体是有用的，特别是对流速产生显著的变化和适当的混合是很重要的各种流体。
需要充分混合的一个例子是上述的CPO工艺。这个工艺是在全世界都很重要的工艺因为H2/CO合成气体是很多工艺过程的进料气体，例如是生产氢气、生产甲醇、生产甲醛的进料气体。
实例
下面描述本发明的一个实施例。下面假设，安装按照本发明的混合器常将心轴设置在垂直位置。
下面描述的实施例是尺寸适合实验工厂的一种混合器，用于验证商用CPO反应器的设计。本发明不会以任何方式局限于小尺寸的反应器和混合器。
混合器是40-80优选地是55-65mm高和外直径是40-80优选地是55-65mm。
心轴是100-400优选地是200-300mm长，塞是40-80优选地是55-65mm高和与该座一起构成1-5个优选地2-4个环形空间。
环形空间的间隙是0.25-1优选地是0.6-0.7mm。在有3个环形空间的混合器中该座的3个锥形部分分别有最小/最大直径为9.3-12.3mm、12.3-14.0 mm、和14.0-18.3mm。
锥形表面与心轴的轴线形成10°-30°优选是地17.4°-17.6°的角。
在环形空间之间的各室有外直径30-55优选地是35-45mm，和高度3-7优选地是4-6mm，组成钻孔连接的各孔是2-6优选地是3-5mm高和有直径为3-8优选地是5-7mm。
在操作时心轴可以上下移动5-10优选地6-8mm。
要混合气体的入口包括2-9优选地3-5个孔，每个有直径3-8优选地5-7mm；和混合后气体出口包括2-9优选地5-7个孔，每个有直径3-8优选地5-7mm。
这个实施例适合烃与氧化剂的混合，其中组合的气流形成流量170-190优选地175-185 Nm3/h有分子量2-50优选地21-23gram/mole(克/摩尔)，在20-650优选地190-210°下，在0.5-4.5优选地2.9-3.1MPa下进行混合。
本发明的另一个实施例是工业化尺寸的混合器。
这个混合器是400-800优选地550-650mm高和外直径是400-800优选地是550-650mm。
心轴是100-700优选地是200-500mm长，塞是400-800优选地是550-650mm高和与座一起构成1-6优选地2-4个环形空间。
环形空间的间隙是2.5-10优选地是5.5-7.5mm。该座的锥形部分有中间直径50-200优选地95-180mm。
锥形表面与心轴的轴线构成10°-45°优选地17.4°-17.6°的角。
在环形空间之间的各室有外直径300-550优选地350-450mm，和高是30-70优选地40-60mm，各孔是20-60优选地是30-50mm高和有直径为30-80优选地50-70mm。
在操作时心轴可以上下移动10-100优选地60-80mm。
要混合气体的入口包括2-9优选地3-5个孔，每个有直径30-90优选地50-70mm；和混合后气体出口包括2-9优选地5-7个孔，每个有直径30-90优选地50-70mm。
这个实施例适合混合烃和氧化剂，其中组合的气流形成流量17000-19000优选地17500-18500Nm3/h，有分子量2-50优选地21-23gram/mole，在20-650优选地190-210℃下，在0.5-4.5优选地2.9-3.1MPa下进行混合。
笼式混合器的一个实施例是一个混合器，其中机体有外直径60-65优选地61-63mm，和安装3-8优选地4-6个混合元件，每个有高度5-15优选地8-12mm，外直径30-40优选地35-37mm和内直径18-22优选地19-21mm。因此各部件内侧的笼有直径18-22优选地19-21mm和每个部件装设3-10个优选地4-8个喷嘴其尺寸为1-5优选地1-3 mm。将喷嘴布置成螺旋形。靠近心轴的管塞有许多行的孔，每种有4-10优选地6-8个孔，有6-14优选地8-12mm的方形间矩和有孔直径3-7优选地4-6mm。
管塞的无穿孔部分有长度/高度35-75优选地38-60mm。
这个实施例用于总气流170-190优选地175-185Nm3/h有分子量2-50优选地21-23gram/mole在0.5-4.5优选地2.9-3.1MPa和20-650优选地190-210℃下。

Claims (11)

1.用于混合两种或多种流体流的方法，其特征在于
在入口室组合各流体然后在一个或多个阶段重复地加速和减速该流体，和
在每个步骤中将加速的组合气流的最大线性速度值维持在各流体流的质量流速范围内。
2.按照权利要求1所述的方法，其特征在于在混合操作时通过调节最小流通通道的面积保持最大的线性速度。
3.按照权利要求1所述的方法，其特征在于通过一次或多次使减速的组合流改变其流动方向90°获得附加的混合，优选地每阶段改变方向3-5次。
4.按照权利要求1、2或3用于混合两种或多种气流或液流的装置，其特征在于它包括：
机体；
座；
有塞的心轴；
入口室；
安装在该座内的塞；
该座和塞有多个锥形表面形成相同多的锥形环形空间；
该座的形状适合在两个环形空间之间形成两个室和在所述的两室之间有孔流通连接；和
在混合操作时心轴能使该塞在该座中轴向移动。
5.按照权利要求4所述的装置，其特征在于在入口室中安装多孔介质。
6.按照权利要求3、4和5的装置，其特征在于气流流速和环形空间的横截流通面积之间的关系表示如下：
R 1 = F D seal 2 - D plug 2 * P ref P * T T ref
式中：
F是总的气流流速以Nm3/sec表示，
Dseat和Dplug是座的内直径和在环形空间中相同位置塞的直径，以
m表示
P是混合器中压力以MPa表示和Pref是3.0Mpa
T是混合器中温度，以K表示和Tref是473.15K
R1是在1*106和1*108Nm3/sec/m2之间优选地在5*106和2*107Nm3/sec/m2之间的范围内；和
其中气流流速和在室之间形成孔连接的各孔横截流通面积之间的关系表示如下：
R 2 = F n * D hole 2 * P ref P * T T ref
式中F是总的气流流速，用Nm3/sec表示
n是孔数
Dhole是各室之间孔的直径，以m表示
P是混合器中压力以Mpa表示和Pref是3.0Mpa
T是混合器中温度，以K表示和Tref是473.15K；和
R2是在5*105和1*107Nm3/sec/m2之间和优选地在1*106和2*106Nm3/sec/m2之间的范围内。
7.按照权利要求4、5和6所述的装置，其特征在于心轴和塞还包括内部的液流通道和与内部的液流通道出口端连接的喷淋喷嘴。
8.按照权利要求1、2或3所述的用于混合两种或多种气体或液体进料流的装置，其特征在于它包括：
机体；
与同轴安装在机体内的管塞连接的可移动的心轴；其中
管塞靠近心轴的一端是穿孔的而另一端是开口的；和
进料流通过穿孔进入管塞；
有喷嘴围绕管塞的笼和它与管塞基本上没有间隙；其中
在垂直安装时笼的高度和管塞无穿孔部分的高度基本相等；和
管塞的无穿孔部分当定位在上、中或下位置时能堵塞零个、一些或全部喷嘴；和
多个环形混合元件围绕笼；其中
混合元件是互相隔离的；
笼和混合元件在一端是封闭的而那里的管塞端是开口的；和
笼喷嘴总的流通面积显著地小于混合器任何其他流通通道的流通面积。
9.按照权利要求8所述的装置，其特征在于在穿孔的上游安装多孔介质和将多孔介质安装在管塞中。
10.按照权利要求4、5、6、7和9所述的装置，其特征在于进料流是烃流、水蒸汽流和氧化剂流。
11.按照权利要求10所述的装置，其特征在于混合流形成催化部分氧化工艺的进料流。
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EP1930069A1 (en) 2008-06-11
US20080140261A1 (en) 2008-06-12
JP2008142710A (ja) 2008-06-26
RU2468857C2 (ru) 2012-12-10
DE602007009175D1 (de) 2010-10-28
ATE481159T1 (de) 2010-10-15
JP5132289B2 (ja) 2013-01-30
RU2007145268A (ru) 2009-06-20
CN101249393B (zh) 2011-12-07
ZA200710587B (en) 2008-11-26

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