CN105944631A - 一种流化床合成气甲烷化装置 - Google Patents

一种流化床合成气甲烷化装置 Download PDF

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CN105944631A
CN105944631A CN201610559584.5A CN201610559584A CN105944631A CN 105944631 A CN105944631 A CN 105944631A CN 201610559584 A CN201610559584 A CN 201610559584A CN 105944631 A CN105944631 A CN 105944631A
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高振
侯建国
宋鹏飞
侯海龙
姚辉超
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China National Offshore Oil Corp CNOOC
CNOOC Gas and Power Group Co Ltd
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Abstract

本发明公开了一种流化床合成气甲烷化装置。它包括依次相连通的主反应段、辅反应段和沉降回收段，且所述主反应段、所述辅反应段和所述沉降回收段沿轴向变径设置；所述主反应段的底部设有工艺气主进口，所述主反应段的下部的横截面上设有气体分布板，所述气体分布板上设有与所述主反应段的腔壁相连通的催化剂卸料口；所述辅反应段和/或所述沉降回收段上设有催化剂入口；所述沉降回收段的内部设有内置旋风分离器，所述内置旋风分离器与所述沉降回收段的腔壁相连通的产品气出口相连接。本发明装置的结构简单，其传质传热效率高。

Description

一种流化床合成气甲烷化装置
技术领域
本发明涉及一种流化床合成气甲烷化装置，属于化工领域。
背景技术
我国化石能源以煤炭为主要资源，煤炭贮量极为丰富，目前已探明的保有贮量高达1.28万亿吨以上。石油、天然气资源则相对贫乏，国内油气产量远不能满足国民经济高速发展的需要，必须依靠大量进口来支撑我国经济的发展。我国进口原油已由2000年的0.7亿吨增长到2011年的2.5亿吨，2012年对境外石油进口依存度达到55.2％。2009年我国天然气产量为830×108Nm3，与2008年相比增长7.7％。表观消费量为874.5×108Nm3，同比增长11.5％。与国内产量相比，国内天然气供需缺口达40多亿立方米。2010年我国天然气同比增长12.1％，达到944.8×108Nm3。到2020年天然气需求量将超过2000×108Nm3左右，而产量仅有1000×108Nm3，另外的50％将依赖进口或者其他替代能源。逐年递增的油气需求，必将成为制约我国经济发展的瓶颈。因此，充分利用我国丰富的煤炭资源优势，大力发展煤化工高新技术产业，生产煤制天然气，对于优化我国能源结构，保证我国能源安全，保证国民经济的可持续发展，迫在眉睫，势在必行。可以预见未来无论是国内还是国外对天然气的需求都存在很大缺口，因此利用煤炭资源生产合成天然气将是一种现实的天然气补充来源。
发明内容
本发明的目的是提供一种流化床合成气甲烷化装置，本发明装置的结构简单，其传质传热效率高。
本发明提供的流化床合成气甲烷化装置，其特征在于：它包括依次相连通的主反应段、辅反应段和沉降回收段，且所述主反应段、所述辅反应段和所述沉降回收段沿轴向变径设置；
所述主反应段的底部设有工艺气主进口，所述主反应段的下部的横截面上设有气体分布板，所述气体分布板上设有与所述主反应段的腔壁相连通的催化剂卸料口；
所述辅反应段和/或所述沉降回收段上设有催化剂入口；
所述沉降回收段的内部设有内置旋风分离器，所述内置旋风分离器与所述沉降回收段的腔壁相连通的产品气出口相连接。
本发明装置中，所述催化剂入口具体设置在所述辅反应段中部。
上述的装置中，所述辅反应段设置至少一对辅反应段工艺气进口。
上述的装置中，所述主反应段、所述辅反应段和所述沉降回收段的直径比可为1：1～5：1～8。
上述的装置中，所述主反应段、所述辅反应段和所述沉降回收段的高度比可为1：1～10：1～20。
上述的装置中，所述主反应段的上部与所述辅反应段连接处的腔壁设为漏斗形连接区1，所述漏斗形连接区1与所述主反应段的腔壁横截面的夹角可为20°～80°。
上述的装置中，所述辅反应段的上部与所述沉降回收段连接处的腔壁设为漏斗形连接区2，所述漏斗形连接区2与所述辅反应段的腔壁横截面的夹角可为20°～80°。
本发明装置应用时，所述工艺气主进口与原料气管道相连通，且所述原料气管道上设有原料气控制阀。
本发明装置应用时，所述工艺气主进口与所述原料气控制阀之间的所述原料气管道上可根据需要设置一个旁路管道总管，所述旁路管道总管与所述辅反应段工艺气进口相连通；
所述旁路管道总管设有旁路阀；所述旁路管道设有分流阀。
本发明具有以下优点：
本发明装置的结构简单，反应器内部流场完整顺畅、传质传热效率高，结合“一种新型流化床合成气工艺”，原料气中含有大量水蒸气和循环产品气，易于整个装置的温度控制，具有可操作性高、有利于保护催化剂、热量利用高的等优点。
附图说明
图1为本发明流化床合成气甲烷化装置的结构示意图。
图中标记如下：
1工艺气主进口；2气体分布板；3催化剂卸料口；4内置旋风分离器；5产品气出口；6、7辅反应段工艺气进口；8催化剂入口；V1原料气控制阀；V2旁路阀；V3分流阀；h1、d1分别为主反应段的高度和直径；h2、d2分别为辅反应段的高度和直径；h3、d3分别为沉降回收段的高度和直径。
具体实施方式
下述实施例中所使用的实验方法如无特殊说明，均为常规方法。
下述实施例中所用的材料、试剂等，如无特殊说明，均可从商业途径得到。
实施例、流化床合成气甲烷化装置
如图1所示，为本发明流化床合成气甲烷化装置，它包括三段，分别是依次相连通的主反应段、辅反应段、沉降回收段，三段沿轴向变径设置，主反应段的底部设有工艺气主进口1，主反应段的下部的横截面上设有气体分布板2，气体分布板2上设有与主反应段的腔壁相连通的催化剂卸料口3，所述辅反应段中部设有催化剂入口8；辅反应段上设有辅反应段工艺气进口6和7；沉降回收段的内部无换热和复杂内件，其内设有内置旋风分离器4。内置旋风分离器4把产品气中携带的少量固体颗粒分离，并返回主反应段或辅反应段，反应后的产品经过内置旋风分离器4后，经过与其相连通且与沉降回收段的腔壁相连通的产品气出口5离开装置。
主反应段、辅反应段、沉降回收段的直径关系为辅反应段的直径d2是主反应段的直径d1的3倍，沉降回收段的直径d3是主反应段的直径d1的5倍；三段高度关系为辅反应段的高度h2是主反应段的高度h1的3倍，沉降回收段的高度h3是主反应段的高度h1的5倍，主反应段的漏斗形连接区1与辅反应段连接处与水平面夹角S1为50°，辅反应段的漏斗形连接区2和沉降回收段连接处与水平面夹角S2为50°。主反应段承担90％的主要反应负荷；辅反应段承担10％的反应负荷；沉降回收段基本不承担反应负荷或承担微量反应负荷。
使用本发明装置时，原料气通过位于主反应段的工艺气主进口1和辅反应段工艺气进口6、7加入反应器中，原料气总量通过阀门V1控制，工艺气主进口1的流量控制通过阀门V2，辅反应段工艺气进口6和7的流量分配控制用阀门V3。工艺气主进口1进入的原料气以一定温度通过位于主反应段底部的气体分布板2后，均匀进入并与流化床甲烷化催化剂(通过催化剂入口8加入)均匀混合，实现催化剂的流化态并迅速发生甲烷化反应。气流经过主反应段后已经反应了大部分，进入辅反应段后气流速度下降，与来自辅反应段工艺气进口6和7喷入的原料气混合并发生化学反应，一部分催化剂开始沉降，向上的气流与沉降的催化剂逆流接触，加深了反应深度；经过辅反化段的气流继续向上进入沉降回收段，气流速度进一步下降，大部分的催化剂开始沉降，仅有少量反应发生，产品气经过内置旋风分离器4后把携带的小颗粒催化剂回收，返回至主反应段或辅反应段。由催化剂卸料口可实现催化剂的间歇性回收。产品气从产品气出口5离开装置，此时产品气中含有较高浓度的甲烷，并携带大量热量。

Claims (6)

1.一种流化床合成气甲烷化装置，其特征在于：它包括依次相连通的主反应段、辅反应段和沉降回收段，且所述主反应段、所述辅反应段和所述沉降回收段沿轴向变径设置；
所述主反应段的底部设有工艺气主进口，所述主反应段的下部的横截面上设有气体分布板，所述气体分布板上设有与所述主反应段的腔壁相连通的催化剂卸料口；
所述辅反应段和/或所述沉降回收段上设有催化剂入口；
所述沉降回收段的内部设有内置旋风分离器，所述内置旋风分离器与所述沉降回收段的腔壁相连通的产品气出口相连接。
2.根据权利要求1所述的装置，其特征在于：所述辅反应段设置至少一对辅反应段工艺气进口。
3.根据权利要求1或2所述的装置，其特征在于：所述主反应段、所述辅反应段和所述沉降回收段的直径比为1：1～5：1～8。
4.根据权利要求1-3中任一项所述的装置，其特征在于：所述主反应段、所述辅反应段和所述沉降回收段的高度比为1：1～10：1～20。
5.根据权利要求1-4中任一项所述的装置，其特征在于：所述主反应段的上部与所述辅反应段连接处的腔壁设为漏斗形连接区1，所述漏斗形连接区1与所述主反应段的腔壁横截面的夹角为20°～80°。
6.根据权利要求1-5中任一项所述的装置，其特征在于：所述辅反应段的上部与所述沉降回收段连接处的腔壁设为漏斗形连接区2，所述漏斗形连接区2与所述辅反应段的腔壁横截面的夹角为20°～80°。
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