CN1320478A - 一种低温差放热气－固相催化反应器 - Google Patents

一种低温差放热气－固相催化反应器 Download PDF

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CN1320478A
CN1320478A CN00105264.0A CN00105264A CN1320478A CN 1320478 A CN1320478 A CN 1320478A CN 00105264 A CN00105264 A CN 00105264A CN 1320478 A CN1320478 A CN 1320478A
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楼寿林
楼韧
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Hangzhou Linda Chemical Technology Engineering Co ltd
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Priority to CN00105264.0A priority Critical patent/CN1320478A/zh
Priority to DE60142287T priority patent/DE60142287D1/de
Priority to AU62020/01A priority patent/AU6202001A/en
Priority to PCT/CN2001/000611 priority patent/WO2001091894A1/zh
Priority to EP01935930A priority patent/EP1291072B1/en
Priority to AT01935930T priority patent/ATE469695T1/de
Priority to RU2002131458/12A priority patent/RU2262380C2/ru
Priority to CNB018085709A priority patent/CN1168530C/zh
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Abstract

一种低温差放热气－固相催化反应器,用冷管向并流换热,具有触媒层温差小、触媒活性高、结构简单可靠、操作性能好、投资省的优点。

Description

一种低温差放热气一固相催化反应器
本发明是一种气固相催化反应装置，用于流体催化反应和传热过程，属化学工程领域，特别适用于甲醇合成反应过程，也可用于氨、甲烷、甲醚合成过程。
对于由加压下甲醇合成、氨合成这类气固相放热催化反应，随着反应过程的进行，不断放出的反应热使催化剂层温度提高。为了提高反应器的效率，需要把反应热移出以降低反应气温度。在工业反应器中曾广为使用的一种是多段原料气冷激来降低反应气温度，这种反应器因原料气冷激时在降低反应气温度的同时也降低了反应物浓度，影响了合成率。另一种如西德Lurgi公司的用于甲醇合成的列管式反应器，见附图1，在受压外壳P中有上下管板H1、H2间的多根圆管b，管中装有催化剂K，原料气从上部进气口1进入分布到各管中，在管内装触媒层中合成甲醇，管间侧面进水。反应热被管外沸腾水连续移热，产生蒸汽由侧面管出，反应气由底部出气管出塔，该塔温差小，但触媒装填系数小，投资大。
本发明的任务是依据气一固相催化放热可逆反应的特点，克服现有技术的特点，提供一个触媒层温差小、触媒活性高、结构简单可靠、操作性能好的反应器。
下面结合附图，作进一步说明。
一种低温差放热气一固相催化反应器，主要由外壳P、隔板H、冷管胆Cb、支架S、多孔板R组成，外壳P是一受压容器，顶部封头有进气口1，底部封头有出气口2，隔板H把受压容器分隔为上部分气室和下部反应室，反应室底部支架S支撑冷管胆Cb，底部多孔板R支承反应室中冷管胆外的触媒层K，主要是冷管胆Cb包含有进气管a、环管c、冷管b，环管c连结进气管a和冷管b，冷管b是U形管，环管c连结进气管a和U形冷管b的一端，冷管这一端成为下行冷管，U形冷管的另一端上端开口成为上行冷管，进气管a穿过隔板并用填料函活动密封，冷管胆Cb中的U形冷管与环管c成为同轴心的不同圈径多排冷管，每排中全部U形冷管右端上口与环管c相连成为下行冷管，或者全部U形冷管左端上口与环管c相连成为下行冷管。合成原料气由外壳P顶部进气口进入上部分气室，经进气管a到环管c分布到各下行冷管b，原料气在下行冷管b中先由上到下流动与冷管b管外的反应气并流换热，然后经U形弯头在上行冷管中由下到上与管外反应气逆流换热到顶部出上行冷管，到管外进入触媒层由上到下一边反应一边与U形冷管中的原料气向并流换热，反应气到底部经多孔板由底部出气管出反应器。
图2是低压甲醇合成塔示意图，图3是冷管和环管c连结图，图2中外壳P为受内压壳体，内压为4～9MPa，外壳P为一个带有上下封头的圆筒形容器，上封头有原料气进口1，下封头有反应气出口2，容器上部有圆形隔板H，隔板支承在筒壁上并用焊接或活动密封，把容器分为上下二部分，隔板H上装有多个填料函，用作隔板和冷管胆Cb进气管a间密封。原料气主要为H2、CO、CO2、N2混合气由进气口1进塔，经上部分气室分流到各冷管胆的进气管a，再经各环管c分流到每一冷管胆的各个U型冷管b1、b2……中，原料气在U形管下行管段由上到下流动到底部U形弯头后改变方向，在上行管段为由下到上流动出冷管，气体在冷管内被管外反应气加热到250℃左右，热气进入管外触媒层中由上到下流动一边反应一边与管内原料气换热直到底部，再经多孔板R由出气口2出塔。因气体在触媒层反应被U形冷管移热，因此触媒层温差很小。图3为冷管和环管c连结图，表示冷管胆c中每排U形冷管按二根U形管一组，二根U形管分大小二个不同弯头，小弯头U形管套在大弯头U形管里面，由大弯头U形管左侧为下行冷管与环管c相连，小弯头U形管右侧管为下行冷管与环管c相连，冷管管径可为16～38mm。
本发明中外壳P的上封头和简体也可分开为二件用法兰连结，以便拆下隔板装触媒和检修设备。本发明因触媒装在冷管间，故增加了触媒装填系数，达到75％，而西德Lurgi管壳式的甲醇反应器催化剂装在管内，装填系数只达30％，且因气体流通截面减少增加了反应器压差。Lurgi塔上下管板与数千条管子固定焊结易泄漏。本发明因上行冷管和下行冷管用一支长管弯成U形弯头不用下环管连结，避免用下环管时环管与冷管接头漏气，增加了结构可靠性。
实施例：图2的低压甲醇合成塔直径2米，高8.5米，装NC306或C302铜基甲醇，触媒装填量20M3，冷管面积300M2，合成压力5.0MPa，进塔气成份：H276.4％,CO10.53％,CO23.16％,H2O0.02％,N24.99％,CH44.35％，进塔气量150000NM3/h，触媒层热点温差250，温差＜10℃，甲醇产量330吨/日。而用图1的西德Lurgi管壳式塔在同样产量下合成塔需直径3米，高10米，投资增加一倍以上。

Claims (3)

1．一种低温差放热气一固相催化反应器，主要由外壳P、隔板H、冷管胆Cb、支架S、多孔板R组成，外壳P是一受压容器，顶部封头有进气口1，底部封头有出气口2，隔板H把受压容器分隔为上部分气室和下部反应室，反应室中装有触媒层K，反应室底部支架S支撑冷管胆Cb，底部多孔板R支承反应室中冷管胆外的触媒层K，其特征是冷管胆Cb包含有进气管a、环管c、冷管b，冷管b是U形管，环管c连结进气管a和U形冷管b的一端，冷管这一端成为下行冷管，U形冷管的另一端上端开口成为上行冷管，进气管a穿过隔板H并用填料函活动密封，合成原料气由外壳P顶部进气口进入上部分气室，经进气管a到环管c分布到各冷管b，原料气在下行冷管中先由上到下流动与冷管b管外的反应气并流换热，然后经U形弯头在上行冷管中由下到上与管外反应气逆流换热到顶部出上行冷管，到管外进入触媒层由上到下一边反应一边与U形冷管中的原料气向并流换热，反应气到底部经多孔板由底部出气管2出反应器。
2．根据权利要求1所述的反应器，其特征是冷管胆Cb中的U形冷管b成同轴心的不同圈径多排冷管，每排中全部U形冷管右端上口与环管c相连成为下行冷管，或者全部U形冷管左端上口与环管c相连成为下行冷管。
3．根据权利要求1所述的反应器，其特征是冷管胆Cb中的U形冷管b成同轴心的不同圈径多排冷管，每排U形冷管按二根U形管一组，二根U形管分大小二个不同弯头，小弯头U形管套在大弯头U形管里面，由大弯头U形管左侧上端与环管c相连，小弯头U形管右侧上端与环管c相连，或大弯头U形管右侧为下行冷管与环管c相连，小弯头U形管左侧管为下行冷管与环管c相连，构成相邻二根管子中气体上下流动方向均不相同。
CN00105264.0A 2000-04-24 2000-04-24 一种低温差放热气－固相催化反应器 Pending CN1320478A (zh)

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CN00105264.0A CN1320478A (zh) 2000-04-24 2000-04-24 一种低温差放热气－固相催化反应器
DE60142287T DE60142287D1 (de) 2000-04-24 2001-04-23 Geringer temperaturdifferenz und zugehöriges verfahren
AU62020/01A AU6202001A (en) 2000-04-24 2001-04-23 A gas-solid phase exothermic catalytic reactor with low temperature difference and its process
PCT/CN2001/000611 WO2001091894A1 (fr) 2000-04-24 2001-04-23 Procede de catalyse en phase solide-gazeuse thermique dans des conditions d'ecart de basses temperatures et recipient de reaction connexe
EP01935930A EP1291072B1 (en) 2000-04-24 2001-04-23 A gas-solid phase exothermic catalytic reactor with low temperature difference and its process
AT01935930T ATE469695T1 (de) 2000-04-24 2001-04-23 Exothermer katalytischer gas-festphasenreaktor mit geringer temperaturdifferenz und zugehöriges verfahren
RU2002131458/12A RU2262380C2 (ru) 2000-04-24 2001-04-23 Каталитический реактор для экзотермических процессов, протекающих в газ-твердой фазе с невысокой разностью температур
CNB018085709A CN1168530C (zh) 2000-04-24 2001-04-23 一种低温差放热气-固相催化方法及反应器

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CN100386138C (zh) * 2003-12-06 2008-05-07 杭州林达化工科技有限公司 内部换热催化反应方法及设备
CN101301597B (zh) * 2007-05-11 2012-10-31 曼德韦有限公司 冷却管反应器

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CN100435925C (zh) * 2005-08-05 2008-11-26 杭州快凯高效节能新技术有限公司 低阻力甲醇合成反应器
RU2481887C2 (ru) * 2008-01-25 2013-05-20 Басф Се Реактор для осуществления реакций под высоким давлением, способ пуска реактора и способ осуществления реакции
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GB201308429D0 (en) * 2013-05-10 2013-06-19 Johnson Matthey Plc Reactor
CN105642197A (zh) * 2014-09-24 2016-06-08 楼韧 一种大型反应器及其装置和工艺
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CN108057399A (zh) * 2018-01-19 2018-05-22 湖南安淳高新技术有限公司 一种氨合成反应器及氨合成工艺

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CN100386138C (zh) * 2003-12-06 2008-05-07 杭州林达化工科技有限公司 内部换热催化反应方法及设备
CN101301597B (zh) * 2007-05-11 2012-10-31 曼德韦有限公司 冷却管反应器

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ATE469695T1 (de) 2010-06-15
EP1291072B1 (en) 2010-06-02
EP1291072A4 (en) 2003-07-09
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