CN1802200A - 伪等温径向反应器 - Google Patents
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Abstract
一种用于催化反应的伪等温径向化学反应器,包括:大体为柱形的壳体,其相对端由相应的底板封闭;反应区,其中放在所述反应区中的相应催化床和多个热交换器得到支撑。
Description
技术领域
本发明总体上涉及用于催化反应的伪等温径向反应器,所述伪等温径向反应器包括:大体为柱形的壳体,其相对端由相应的底板封闭;反应区,其中支撑放在所述反应区中的至少一个相应的催化床和多个热交换器。
在以下描述和所附权利要求书中,术语“伪等温反应器”用于表示用于化学反应的反应器,其中将反应温度控制在预定最优值附近的值的有限范围内。
此外,参看反应器的主轴,反应物和反应产物横越反应区发生在径向上。
背景技术
如所知的,在所有伪等温反应器中,必不可少的是,随着反应的继续,反应物和产物在预定停留时间内保留在反应器内部,这既允许反应物起反应,又允许反应物和产物的混合物与反应器外部交换热量(例如,通过设置在反应区内的热交换器),以便维持反应器自身内的伪等温条件。
在现有技术中,广泛使用具有由反应物轴向横越的催化床的伪等温反应器。
这些反应器允许获得很高的生产能力,但是气体横越催化床引起大的压降。
为了避免上述压降,已经提出降低催化床的高度,同时增加其半径来保持生产率不变。然而,从构造的观点看,以此方式制成的反应器,即具有大直径壳体,不是节省成本的。
为了解决压降的问题和同时使得伪等温径向反应器更节省成本,已经研制出径向横越催化床的反应器,其大体上在高度方向上延伸,在高度和直径之间的比率(例如,在合成氨中)约等于10。
尽管这些反应器既解决了上述压降问题,又解决了与大直径壳体的结构相关的经济问题,但是它们引入认识到的新缺陷。
事实上,在所述径向反应器中,由于催化床的相当大的长度,已经注意到,曾经沿所述床的入口壁分布的气体反应物具有对床自身不充分的横越速度(crossing speed)。
所述横越速度对反应物和热交换板之间的热交换系数产生负面影响。
由于这些原因,不再可能对反应的伪等温性进行最优控制。
发明内容
构成本发明基础的技术问题是,实现了上述类型的化学反应器,所述化学反应器具有结构和功能特征,例如以允许对反应的伪等温性进行有效控制,以便克服上述现有技术的缺陷。
上述技术问题通过一种用于催化反应的伪等温径向化学反应器解决,所述伪等温径向化学反应器包括:大体为柱形的壳体,其相对端由相应的底板封闭;反应区,其中放在所述反应区中的相应催化床和多个热交换器得到支撑,其特征在于,它包括至少一个第二另外的反应区,所述反应区包括放在所述第二反应区中的相应催化床和多个热交换器,所述第一和所述第二反应区彼此流体连通。
根据以下为了表征和非限定的意义,参看附图给出的根据本发明的化学反应器的实施例的详细描述,本发明的进一步的特征和优点将变得更清楚。
附图说明
图1示意性地示出实现本发明的化学反应器的截面图。
图2和图3分别示意性地示出图1的细节的截面图。
具体实施方式
参看图1,具有垂直轴A-A的等温径向化学反应器整体示意性地用1表示,所述等温径向化学反应器一般用于执行通过催化剂的存在而激活的化学反应,在此具体(但非限定)实例中用于合成氨。
所述反应器1包括柱形壳体2和相对底板即下底板3和上底板4。上底板4装配有用于输入反应物的开口5,而下底板3装配有用于排放反应产物的开口6。
所述壳体2包括与所述壳体2共轴的柱形筒(cartridge)7,在所述壳体2中限定第一反应区8,所述第一反应区8代表性地位于上线9和下线10之间,以保持预定催化床11(以本质上已知的方式被支撑,因此没有表示出),用于由反应气体轴向横越。
所述催化床11沿平行于轴A-A的方向由大体为环形的柱形篮(basket)14的壁12和13(分别为内壁和外壁)束缚,其中穿孔于篮14上,以便允许反应物的径向通道通过催化床11。
所述篮14的底部由设置在线10处的底板16封闭。
与所述壳体共轴的柱形中央导管17从第一室18延伸,直到第二室19,其中所述第一室18用于收集反应气体,且底部由线9束缚,所述第二室19用于收集从第一反应区8出来的气体,且底部由线10束缚。
在所述篮14和筒7之间存在用于在催化床11内分布反应物的间隙20。同样,在所述篮14和中央导管17之间存在用于收集从催化床11出来的反应物/产物混合物的间隙21。
将多个热交换器22浸入并支撑在催化床11中。所述热交换器22为板状、矩形和盒状,优选长侧23平行于壳体2自身的轴A-A径向排列。
根据非限定性实施例,所述热交换器22可排列在多个与所述壳体2共轴的同心行上。
所述热交换器22包括用于工作的热交换流体的入口连接器24和出口连接器25,所述连接器位于所述交换器22的相对短侧上。
与本发明的一个特征一致并根据一个优选实施例,在所述壳体2中限定第二反应区26,所述第二反应区26代表性地束缚在上线27和下线27之间,以接收预定催化床29,打算由反应气体和由反应产物轴向横越。
第二反应区26通过上述底部由线27束缚的室19与第一反应区8相连和流体连通。
所述催化床29沿平行于轴A-A的方向由环形的柱形篮32的壁30和31(分别为内壁和外壁)束缚,其中穿孔于篮32上,以便允许反应物的径向通道通过催化床29。
所述篮32的底部也由设置在线28处的环形底板34封闭。
在所述篮32和筒7之间存在用于在催化床29内分布反应物的间隙48。所述间隙48通过连接器21和连接室19与催化床11连通。
在所述篮32和壳体2的轴A-A之间存在收集室35,所述收集室35用于收集从催化床29出来的反应物/产物混合物,并且通过排放管与开口6流体连通。
将多个热交换器29埋入并支撑在催化床29中。所述热交换器36为板状、矩形和盒状,长侧37平行于壳体2自身的轴A-A。
根据非限定性实施例,所述热交换器36可排列在多个与所述壳体2共轴的同心行上。
所述热交换器36包括用于工作的热交换流体的入口连接器38和出口连接器39,所述连接器位于所述交换器36的相对短侧上。
热交换器36通过输送管41和相应的环形收集管42与中央导管17流体连通。
热交换器36也通过导管43与热交换器22流体连通。
参看上述设备,将反应物流通过开口5连续供给反应器1。
所述流通过输送管44、环形分布管45和连接器46供给所述热交换器22内部,在这里它与第一反应区8交换热量。
在所述热交换器22内部以及交换器36内部,反应物流具有工作的热交换流体的作用。
在热交换器36的出口处,反应物流由环形收集管42收集,且通过导管41送入中央导管17中。
中央导管17携带反应物流到室18,从这里它沿间隙20留下,经过篮14的壁12,通过第一反应区8径向散布,其中在第一反应区8,反应物流部分反应。
从反应区9出来的反应物/产物混合物收集在间隙21中,且从这里传到收集室19,从这里,通过间隙48,分布在第二反应区26内。
在第二反应区26内,径向横越催化床29,反应完成。
在第二反应区26的出口处,产物流入收集室35,它们从这里通过排放管47传送到出口开口。
由于上述配置,反应气体沿比现有技术的单个催化床短的相应的催化床的入口壁分布,从而通过反应气体获得所述催化床11和29的更大的横越速度。
同样,为了避免损坏催化剂,和为了防止反应器的内部部分变差,改善了为了提高反应器的反应产量所需要的等温性控制。
根据本发明的一个有利实施例,可能根据所需要交换的热量的量,在每个催化床中设置不同数量的热交换器。
换言之,根据分别表示根据平面B-B和C-C的反应器的截面的图2和图3,可能将更大数量的交换器22***第一催化床11中,在这里,反应物浓度最高,反应发生更快,从而需要更大的热交换。
另一方面,在第二催化床29内需要较少数量的交换器36,在这里,反应物浓度比先前的情况小,反应的进行更慢,从而需要更少的热交换。
同样,也节省了要使用的交换器的数量,从而获得经济效果。
为了同样的目的,为了通过反应气体控制催化床的横越速度,从而控制反应的等温性,可能改变催化床的长度(参看图1的实例)。
由于根据本发明的反应器,可能执行用于优化伪等温催化反应的方法,所述方法包括将反应物供给反应区8的步骤,其中所述反应区8包括催化床11和放在所述催化床11中的多个热交换器22,所述方法还包括另外的步骤:收集来自所述反应区8的反应物和产物;将所述反应物和产物传送到第二反应区26,其中所述第二反应区26包括相应的催化床29和放在所述催化床29中的相应的多个热交换器36;将所述反应物和产物供给所述第二反应区26;以及在所述催化床29中完成所述反应。
对这样想出的本发明容易作出进一步的改变和修改,而这些改变和修改全都由所附权利要求书限定的本发明的保护范围所覆盖。
Claims (7)
1.一种用于催化反应的伪等温径向化学反应器,包括:大体为柱形的壳体(2),其相对端分别由相应的底板(3)和(4)封闭;反应区(8),其中放在所述反应区(8)中的相应催化床(11)和多个热交换器(22)得到支撑,其特征在于,它包括另外的至少一个第二反应区(26),所述反应区(26)包括放在所述第二反应区(26)中的相应催化床(29)和多个热交换器(36),所述第一和所述第二反应区(8和26)彼此流体连通。
2.根据权利要求1所述的化学反应器,其特征在于,所述第一和所述第二反应区(8和26)串联连接。
3.根据权利要求2所述的化学反应器,其特征在于,所述反应区(8,26)的至少一个的多个热交换器(22)与外部流体连通。
4.根据权利要求3所述的化学反应器,其特征在于,这两个反应区(8,26)的多个热交换器(22,36)彼此流体连通。
5.根据权利要求4所述的化学反应器,其特征在于,所述多个热交换器(22,36)的至少一个热交换器为板状、矩形和盒状。
6.根据权利要求5所述的化学反应器,其特征在于,所述多个热交换器(22)关于所述反应器的轴(A-A)共轴径向排列。
7.一种用于优化伪等温催化反应的方法,包括将反应物供给反应区(8)的步骤,其中所述反应区(8)包括催化床(11)和放在所述催化床(11)中的多个热交换器(22),其特征在于,所述方法包括另外的步骤:收集来自所述反应区(8)的反应物和产物;将所述反应物和产物传送到第二反应区(26),其中所述第二反应区(26)包括相应的催化床(29)和放在所述催化床(29)中的相应的多个热交换器(36);将所述反应物和产物供给所述第二反应区(26);以及在所述催化床(29)中完成所述反应。
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EP03001868A EP1442786A1 (en) | 2003-01-29 | 2003-01-29 | Pseudo isothermal radial reactor |
EP03001868.3 | 2003-01-29 |
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CN1802200A true CN1802200A (zh) | 2006-07-12 |
CN100540130C CN100540130C (zh) | 2009-09-16 |
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CNB2004800031610A Expired - Fee Related CN100540130C (zh) | 2003-01-29 | 2004-01-15 | 伪等温径向反应器 |
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US (1) | US7981271B2 (zh) |
EP (2) | EP1442786A1 (zh) |
CN (1) | CN100540130C (zh) |
AR (1) | AR042959A1 (zh) |
AU (1) | AU2004208476B2 (zh) |
BR (1) | BRPI0407147B1 (zh) |
CA (1) | CA2512889C (zh) |
MX (1) | MXPA05008125A (zh) |
RU (1) | RU2340391C2 (zh) |
UA (1) | UA81798C2 (zh) |
WO (1) | WO2004067163A1 (zh) |
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MX2007001173A (es) | 2004-01-15 | 2007-09-25 | Methanol Casale Sa | Reactor catalitico de lecho fijo. |
US8759600B2 (en) | 2010-06-28 | 2014-06-24 | Uop Llc | Reduced fluidization of solid particles in radial flow fluid/solid contacting |
RU172558U1 (ru) * | 2016-11-11 | 2017-07-12 | Общество с ограниченной ответственностью "Новые газовые технологии - синтез" (ООО "НГТ - синтез") | Реактор для проведения химических реакций |
FR3083129B1 (fr) * | 2018-06-28 | 2021-06-11 | Ifp Energies Now | Procede d'oligomerisation d'ethylene avec enchainement reacteur agite gaz/liquide et reacteur piston |
FR3088925B1 (fr) | 2018-11-27 | 2021-06-11 | Air Liquide | Procédé de production d’hydrogène par reformage à la vapeur et conversion de CO |
CN113230982A (zh) * | 2021-06-10 | 2021-08-10 | 中国石油化工股份有限公司 | 一种反应设备以及石脑油耦合甲醇制高辛烷值汽油的反应再生***与方法 |
BE1030481B1 (de) * | 2022-04-27 | 2023-11-27 | Thyssenkrupp Ind Solutions Ag | Ammoniakkonverter für schwankenden Teillastbetrieb |
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2003
- 2003-01-29 EP EP03001868A patent/EP1442786A1/en not_active Withdrawn
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2004
- 2004-01-15 EP EP04702314A patent/EP1587611A1/en not_active Ceased
- 2004-01-15 UA UAA200508343A patent/UA81798C2/uk unknown
- 2004-01-15 CA CA2512889A patent/CA2512889C/en not_active Expired - Fee Related
- 2004-01-15 WO PCT/EP2004/000232 patent/WO2004067163A1/en active Application Filing
- 2004-01-15 AU AU2004208476A patent/AU2004208476B2/en not_active Ceased
- 2004-01-15 RU RU2005127095/12A patent/RU2340391C2/ru not_active IP Right Cessation
- 2004-01-15 MX MXPA05008125A patent/MXPA05008125A/es active IP Right Grant
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TWI507245B (zh) * | 2009-10-19 | 2015-11-11 | Davy Process Techn Ltd | 觸媒載體、反應器管、反應器及用於實行反應之方法 |
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Publication number | Publication date |
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BRPI0407147B1 (pt) | 2014-12-16 |
AR042959A1 (es) | 2005-07-13 |
CA2512889A1 (en) | 2004-08-12 |
BRPI0407147A (pt) | 2006-02-07 |
CA2512889C (en) | 2012-07-31 |
MXPA05008125A (es) | 2005-12-05 |
AU2004208476B2 (en) | 2009-06-11 |
AU2004208476A8 (en) | 2004-08-12 |
RU2005127095A (ru) | 2006-02-27 |
WO2004067163A1 (en) | 2004-08-12 |
EP1587611A1 (en) | 2005-10-26 |
CN100540130C (zh) | 2009-09-16 |
AU2004208476A1 (en) | 2004-08-12 |
RU2340391C2 (ru) | 2008-12-10 |
EP1442786A1 (en) | 2004-08-04 |
US7981271B2 (en) | 2011-07-19 |
UA81798C2 (uk) | 2008-02-11 |
US20060171868A1 (en) | 2006-08-03 |
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