CN1168530C - 一种低温差放热气-固相催化方法及反应器 - Google Patents
一种低温差放热气-固相催化方法及反应器 Download PDFInfo
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Abstract
一种低温差放热气-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。隔板(H)把容器分为上、下部分气室，反应室装有触媒层(K)，底部支架(S)支撑冷管胆(Cb)，底部多孔板(R)支撑冷管胆外的触媒层。冷管胆中的进气管(a)穿过隔板(H)并用填料函活动密封，冷管内冷气与管外触媒层中反应气向并流换热，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
技术领域
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、烃类等合成反应过程，也可用于甲胺、氨、甲烷、甲醚等合成过程。
背景技术
对于由加压下甲醇合成、甲胺、甲醚、氨、烃类等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。其他如甲胺类合成采用绝热反应器时，沸石催化剂寿命短，当采用连续移热或分级冷却来降低触媒层温差时，则可显著提高沸石催化剂寿命。
本发明的任务是依据气—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。
发明的内容
本发明提供一种低温差放热气—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，其特征是外壳P分为带上法兰的封头P1和带下法兰的筒体P2，与隔板H连结密封，或隔板H与外壳P支承圈密封，冷管胆Cb包含有进气管a、上环管c、或者上环管c、下环管d，冷管b，冷管b是U形管，上环管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bA，U形冷管的另一端上端开口成为上行冷管bB，或者冷管b由下行冷管bA和上行冷管bB组成，上环管c连结进气管a和下行冷管bA，下环管d连结下行冷管bA和上行冷管bB，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到上环管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管外的反应气换热，然后经上行冷管中由下到上与管外反应气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冷管中的原料气换热，反应气到底部经多孔板由底部出气管2出反应器。
在本发明的一个较好实例中，反应器的冷管胆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形冷管右端上口与上环管c相连成为下行冷管，或者全部U形冷管左端上口与上环管c相连成为下行冷管。
在本发明的另一个较好的实例中，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形管左侧上端与上环管c相连，小弯头U形管右侧上端与上环管c相连，或大弯头U形管右侧为下行冷管与上环管c相连，小弯头U形管左侧管为下行冷管与上环管c相连，构成相邻二根管子中气体上下流动方向均不相同。
在本发明的另一个较好实例中，冷管胆Cb中的冷管b成同轴心的不同圈径多排冷管，每排冷管中下行冷管bA的面积与上行冷管bB的面积之比为0.5-3。
在本发明的一个实例中，出反应器后气体进入管壳式合成反应进一步反应。
在本发明的另一个实例中，反应器设有圆筒形气体分气筒E和集气筒F，分气筒E和集气筒F上开有气孔，气体经分气筒E气孔到触媒层在触媒层中径向流动到经集气筒F气孔汇集到集气筒后由底部出气管2出反应器。
附图说明
下面结合附图，作进一步说明本发明。附图中，
图1时现有技术的反应器；
图2是本发明反应器中冷管b是U形管时的合成塔示意图；
图3是冷管和上环管c连结图；
图4是本发明气体在触媒层中呈径向流动的反应器；
图5是冷胆有上环管c、下环管d和下行冷管bA、上行冷管bB的合成塔示意图；
图6为装有高压外壳合成塔内件的示意图；
较好实施方式
本发明提供一种低温差放热气—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，主要是外壳P分为带上法兰的封头P1和带下法兰的筒体P2，与隔板H连结密封，或隔板外壳支承圈密封，冷管胆Cb包含有进气管a、上环管c、冷管b，冷管b是U形管，上环管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bA，U形冷管的另一端上端开口成为上行冷管，或者冷管b由下行冷管bA和上行冷管bB组成，上环管c连结进气管a和下行冷管bA，下环管d连结下行冷管bA和上行冷管bB，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到上环管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管外的反应气换热，然后经上行冷管中由下到上与管外反应气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冷管中的原料气换热，反应气到底部经多孔板由底部出气管2出反应器。本发明中反应器出口气体可再进串联的后一反应器，例如管壳式反应器，进一步合成反应。
图2是冷管b是U形管时的合成塔示意图，图3是冷管和上环管c连结图，图2中外壳P为受内压壳体，内压为4～15MPa，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。原料气由进气口1进塔，经上部分气室分流到各冷管胆的进气管a，再经各上环管c分流到每一冷管胆的各个U形冷管b1、b2中，原料气在U形下行冷管段中由上到下流动到底部U形弯头后改变方向，进上行冷管段中由下到上流动出冷管，气体在冷管内被管外反应气加热，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为冷管和上环管c连结图，表示冷管胆中每排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上环管c相连，小弯头U形管右侧管为下行冷管与上环管c相连，冷管管径可为16～38mm。
图4为本发明的另一种结构。与图3不同之处在于在触媒层的外侧设一分气筒E，触媒层中心轴心位置设一集气筒F，E、F均为多孔筒体，气体在触媒层中经上部轴向流动反应后进入外分布筒E与壳体P的空间，然后经E的气孔到触媒层，在触媒层中由外向内流动反应并与冷管内气体错流换热，直到进入中心集气筒F后经F的气孔进入集气筒内由底部出气孔2出塔，图4中底部3为触媒卸料口。图4适用于具较高触媒层的反应器，可有效降低气体进出合成反应器压差。
图5是冷胆有上环管c、下环管d和下行冷管bA、上行冷管bB的合成塔示意图。外壳P为受内压壳体，内压为2-15MPa，外壳由带有上法兰的上封头P1和下法兰的筒体P2组成。封头P1和筒体P2通过上、下法兰与隔板H上、下面间用密封垫片L1、L2密封，并用螺栓m1、螺母m2紧固。隔板H上装有多个填料函，用作隔板和冷管Cb的进气管a密封。冷管胆有上环管c和下环管d，上环管C连结进气管a和下行冷管bA，下环管d连结下行冷管bA和上行冷管bB。
图6为装有高压外壳合成塔内件的示意图，可用于压力为10-32Mpa的氨合成等。图中P0为承受高压的合成塔外壳，内件壳体P包括上部集气室盖板Q，内件下部为换热器T，与图2一样内件有冷管胆Cb和隔板H，冷管为U形管，按图3布置，原料气主线气1由外壳上部进气口进气沿内外壳体间由上到下部换热器T管外被管内反应气加热出换热器与来自底部副线冷气2混合后进入中心管O流入上部，顶盖Q与隔板H间集气室再经冷管胆引气管a进入冷管胆内被管外反应气加热后出冷管进入催化剂层反应，出催化剂层反应气进入下部换热器被进塔原料气冷却后经底部出气管3出塔。
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。本发明中冷管用U形管时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。
下面通过实施例进一步描述本发明。
实施例1
使用图2的U形管合成塔进行低压甲醇合成，塔内径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％，CH3OH0.50％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。
实施例2
使用图4双环管的合成塔用作甲胺合成，塔直径1.5米，高9.5米，装沸石催化剂12M3，冷管面积280M2，合成压力5MPa，进塔气量900Kml/h，其中CH3OH 300Kml/h，NH3600Kml/h，触媒层热点温度280℃，温差＜10℃，甲醇转化率97％，二甲胺产量120吨/日，触媒使用寿命2年以上。
在阅读了本发明的详细描述以后，在不偏离本发明的精神和范围的情况下本领域的普通技术人员能容易地对本发明进行各种变化和改进。本发明包括在所附权利要求范围内的各种变化和改进。
Claims (6)
1.一种低温差放热气-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)，其特征在于外壳(P)分为带上法兰的封头(P1)和带下法兰的筒体(P2)，外壳(P)与隔板(H)连结密封，或隔板(H)与外壳(P)支承圈密封，冷管胆(Cb)包含有进气管(a)、上环管(c)、冷管(b)，冷管(b)是U形管，上环管(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(bA)，U形冷管的另一端上端开口成为上行冷管(bB)；或者冷管胆(Cb)包含有进气管(a)、上环管(c)、下环管(d)、冷管(b)，冷管(b)由下行冷管(bA)和上行冷管(bB)组成，上环管(c)连结进气管(a)和下行冷管(bA)，下环管(d)连结下行冷管(bA)和上行冷管(bB)；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)项部进气口进入上部分气室，经进气管(a)到上环管(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)管外的反应气换热，然后经上行冷管中由下到上与管外反应气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冷管中的原料气换热，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，其特征在于冷管胆(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形冷管右端上口与上环管(c)相连成为下行冷管，或者全部U形冷管左端上口与上环管(c)相连成为下行冷管。
3.根据权利要求1所述的反应器，其特征在于冷管胆(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形管左侧上端与上环管(c)相连，小弯头U形管右侧上端与上环管(c)相连，或大弯头U形管右侧为下行冷管与上环管(c)相连，小弯头U形管左侧管为下行冷管与上环管(c)相连，构成相邻二根管子中气体上下流动方向均不相同。
4.根据权利要求1所述的反应器，其特征在于冷管胆(Cb)中的冷管(b)成同轴心的不同圈径多排冷管，每排冷管中下行冷管(bA)的面积与上行冷管(bB)的面积之比为0.5-3。
5.根据权利要求1所述的反应器，其特征在于出反应器后气体进入管壳式合成反应器进一步反应。
6.根据权利要求1所述的反应器，其特征在于反应器设有圆筒形气体分气筒(E)和集气筒(F)，分气筒(E)和集气筒(F)上开有气孔，气体经分气筒(E)气孔到触媒层在触媒层中径向流动到经集气筒(F)气孔汇集到集气筒后由底部出气管(2)出反应器。
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| CN00105264.0 | 2000-04-24 | ||
| 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 |
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| AT (1) | ATE469695T1 (zh) |
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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 |
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| TW590792B (en) * | 2002-03-26 | 2004-06-11 | Showa Denko Kk | Reaction device with a heat-exchanger |
| 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 |
| DE202007006812U1 (de) * | 2007-05-11 | 2008-09-18 | Man Dwe Gmbh | Kühlrohrreaktor |
| CN101977677B (zh) * | 2008-01-25 | 2015-02-18 | 巴斯夫欧洲公司 | 进行高压反应的反应器,启动的方法和进行反应的方法 |
| CN103055776A (zh) * | 2013-01-22 | 2013-04-24 | 安阳盈德气体有限公司 | 草酸二甲酯的反应系统 |
| 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 |
| CN104399413B (zh) * | 2014-11-18 | 2016-03-16 | 安徽新月化工设备有限公司 | 一种可控移热反应器 |
| CN108057399B (zh) * | 2018-01-19 | 2024-06-04 | 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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| GB279819A (en) * | 1926-10-27 | 1929-02-11 | Selden Co | Catalytic apparatus |
| CN2063942U (zh) * | 1990-01-25 | 1990-10-17 | 浙江工学院 | 均温型甲醇塔 |
| CN1034070C (zh) * | 1992-05-15 | 1997-02-19 | 楼寿林 | 等压型甲醇和氨的联合生产装置 |
| CN1129205A (zh) * | 1995-02-15 | 1996-08-21 | 楼寿林 | 节能冷管型甲醇合成反应器 |
| CN1088618C (zh) * | 1996-08-21 | 2002-08-07 | 楼寿林 | 一种接近最佳温度的催化反应改进工艺及其合成反应器 |
| CN2290400Y (zh) * | 1997-02-27 | 1998-09-09 | 楼寿林 | 改进均温型气固相催化反应器 |
| CN1069626C (zh) * | 1998-11-28 | 2001-08-15 | 楼寿林 | 一种醇醚合成改进工艺及其合成反应器 |
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| CN1320478A (zh) | 2001-11-07 |
| RU2262380C2 (ru) | 2005-10-20 |
| EP1291072A1 (en) | 2003-03-12 |
| WO2001091894A1 (fr) | 2001-12-06 |
| ATE469695T1 (de) | 2010-06-15 |
| CN1426322A (zh) | 2003-06-25 |
| DE60142287D1 (de) | 2010-07-15 |
| AU6202001A (en) | 2001-12-11 |
| RU2002131458A (ru) | 2004-03-27 |
| EP1291072B1 (en) | 2010-06-02 |
| EP1291072A4 (en) | 2003-07-09 |
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