CN101402019B - 均流场内回流循环流化床烟气脱硫反应器 - Google Patents
均流场内回流循环流化床烟气脱硫反应器 Download PDFInfo
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- CN101402019B CN101402019B CN2008102255669A CN200810225566A CN101402019B CN 101402019 B CN101402019 B CN 101402019B CN 2008102255669 A CN2008102255669 A CN 2008102255669A CN 200810225566 A CN200810225566 A CN 200810225566A CN 101402019 B CN101402019 B CN 101402019B
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- flue gas
- reactor
- gas desulfurization
- absorbent
- flue
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- UGFAIRIUMAVXCW-UHFFFAOYSA-N carbon monoxide Chemical compound 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[O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 title claims abstract description 71
- 239000003546 flue gases Substances 0.000 title claims abstract description 67
- 238000006477 desulfuration reactions Methods 0.000 title claims abstract description 25
- 230000003009 desulfurizing Effects 0.000 title claims abstract description 22
- 244000171263 Ribes grossularia Species 0.000 title claims description 16
- 230000002745 absorbent Effects 0.000 claims abstract description 33
- 239000002250 absorbents Substances 0.000 claims abstract description 33
- 239000003570 air Substances 0.000 claims abstract description 15
- 239000007787 solids Substances 0.000 claims abstract description 14
- 239000002956 ash Substances 0.000 claims description 19
- AXCZMVOFGPJBDE-UHFFFAOYSA-L Calcium hydroxide Chemical compound data:image/svg+xml;base64,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 data:image/svg+xml;base64,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 [OH-].[OH-].[Ca+2] AXCZMVOFGPJBDE-UHFFFAOYSA-L 0.000 claims description 9
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- 229910001861 calcium hydroxide Inorganic materials 0.000 claims description 9
- 239000011257 shell materials Substances 0.000 claims description 9
- 230000004913 activation Effects 0.000 claims description 8
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Abstract
本发明涉及一种均流场内回流循环流化床烟气脱硫技术。其核心设备——反应器的结构，由下至上依次为：直流流线型底部进气口、导流板、中心内置式吸收剂分配器、烟气加速器、增湿活化喷嘴、旋流板气固分离器以及反应器筒体上部的中心出口烟道。反应器进口烟道内设有双片圆弧式烟气均布导流板，反应器内设有中心内置式吸收剂分配器、仿“拉伐尔喷嘴”式烟气加速器、两级双流体增湿活化喷嘴、旋流板气固分离器。本发明配置合理，使反应器的烟气获得理想稳定的均匀流场和温度场；吸收剂获得高循环倍率和高利用率；两级增湿可有效提高吸收剂的反应活性，还可有效避免湿壁、结垢、塌床；确保脱硫效率；同时明显降低了出口烟道的含尘量，大大减轻了后部袋式除尘器负荷，解决了半干法循环流化床烟气脱硫技术中的技术难题。
Description
均流场内回流循环流化床烟气脱硫反应器
技术领域
[0001] 本发明涉及烟气脱硫技术和设备，具体涉及一种适用于中小机组燃煤电厂和垃圾焚烧电厂的半干法循环流化床烟气脱硫技术。
背景技术
[0002] 半干法循环流化床烟气脱硫技术，投资省（仅为湿法的50%以下）、占地少、无废水排放、不会造成二次污染、脱硫效率高、运行成本低、系统基本不腐蚀、可用一般碳钢制造，符合我国国情，因而受到青睐。但其核心设备一反应器仍存在三大技术难题：（I).流场不均匀，甚至严重偏流或局部涡流；（2).脱硫灰粘壁、结块、塌床、堵塔多有发生；（3).出口烟气粉尘浓度太高（800〜1000g/Nm3)，使后部的袋式除尘器负荷过重，阻力降大。这三大难题成了制约该技术的瓶颈。 发明内容
[0003] 本发明的目的，在于克服现有技术中的上述不足，提供一种结构合理，烟气流场、温度场、压力场非常均匀的内回流循环流化床烟气脱硫反应器。
[0004] 本发明的目的是通过以下技术方案实现的。
[0005] 本发明“均流场内回流循环流化床烟气脱硫技术”的核心设备一反应器，由下至上的结构依次为：直流流线型底部进气口、作为进气机构一部分的导流板、中心内置式吸收剂分配器、烟气加速器、增湿活化喷嘴、旋流板气固分离器以及反应器筒体顶部的中心出口烟道，还有与中心内置式吸收剂分配器相连接的消石灰和循环灰进口。
[0006] 所述的直流流线型底部进气烟道，为方形变截面结构。
[0007] 所述的作为进气烟道结构一部分的导流板为双片圆弧式均布导流板。
[0008] 所述的中心内置式吸收剂分配器为6个出口，分别对准烟气加速器的6个入口端。
[0009] 所述的烟气加速器为仿“拉伐尔喷嘴”式烟气加速器。
[0010] 所述的增湿活化喷嘴采用两级双流体喷嘴，位于反应器的中心部位。
[0011] 所述的旋流板气固分离器设在反应器筒体上部。
[0012] 本发明采用实际工程的数据，经过严谨的工艺计算，并运用Fluent软件进行流场分析加以验证，效果十分理想。
[0013] 本发明配置合理，使反应器的烟气与吸收剂充分混合；并获得稳定均匀的流场和温度场；吸收剂获得高循环倍率和高利用率；两级增湿可有效提高吸收剂的反应活性，还可有效避免湿壁、结垢、塌床；确保脱硫效率；同时明显降低了出口烟道的含尘量，大大减轻了后部袋式除尘器负荷，解决了半干法循环流化床烟气脱硫技术中的技术难题。
附图说明
[0014] 图I为本发明“均流场内回流循环流化床烟气脱硫技术”的核心设备一反应器的结构示意图。[0015] 图中：1.进气口，2.导流板，3.吸收剂分配器，4.烟气加速器，5.增湿活化喷嘴，
6.气固分离器，7.反应器筒体，8.中心出口烟道，9.消石灰及循环灰入口通道。
具体实施方式
[0016] 参见图I，“均流场内回流循环流化床烟气脱硫技术”的核心设备一反应器，其由下至上的结构依次为：直流流线型底部进气口 I、导流板2、中心内置式吸收剂分配器3、烟气加速器4、增湿活化喷嘴5、旋流板气固分离器6、反应器筒体7上部的中心出口烟道8、以及与中心内置式吸收剂分配器3相连接的消石灰及循环灰入口通道9。增湿活化喷嘴5采用两级双流体喷嘴，位于反应器的中心部位。作为进气机构一部分的导流板2为双片圆弧式均布导流板。烟气加速器4为仿“拉伐尔喷嘴”式烟气加速器。
[0017] 直流流线型底部进气烟道、双片园弧式均布导流板及中心内置式吸收剂分配器为本发明的独创结构。
[0018] 燃煤电厂或垃圾焚烧发电厂锅炉的出口烟气，从本反应器底部直流流线型进气烟道I进入反应器，经过双片圆弧式气流均布导流板2分成三等分，继续向上运动；新鲜消石灰及循环灰由入口通道9进入中心内置式吸收剂分配器3，并将其分成六等分，注入反应器内，与上升的烟气混合，进入仿“拉伐尔喷嘴”式烟气加速器4 ;烟气与吸收剂通过烟气加速器4，气、固两相充分接触、混合，瞬间流速可提高三倍以上，并形成圆筒状烟气高速区；增湿水通过双流体喷嘴5，以极细的水雾（40〜60μπι)喷入反应器内，水分迅速蒸发，使吸收剂增湿，使烟气降温，提高反应活性，实现脱硫反应。
[0019] 带有大量吸收剂及反应产物的烟气，经过设在反应器上部的旋流板气、固分离器6，由于旋流板的离心分离作用，固相（吸收剂及反应产物）被甩向器壁，又靠重力沿器壁向下滑落，形成内回流。被分离出一部分吸收剂及反应产物的烟气，经过设在反应器顶部中心部位的烟气出口 8，进入本烟气脱硫工艺后部的袋式除尘器，进行气、固分离。经除尘器净化了的烟气，通过引风机送进烟囱，排入大气。被分离出的固相（即循环灰），大部分循环回去，进反应器继续参加脱硫反应。少部分送到灰库，另行处理。反应器烟气中较大的颗粒或团块，气流无法带动，将会下落，进入下灰斗，定期排出。
[0020] 本发明的优点在于：
[0021] I)直流流线型底部进气结构（包括灰斗及扩散段），符合烟气流动的自然流线，可实现烟气的稳定流动，并有利于再调节；流体阻力小。该结构优于WulfT的双侧进气结构，优于Lurgi的直流式（两个135°弯头）进气结构，更优于国内传统的单侧正交进气结构。
[0022] 2)双片圆弧式气流均布导流板，可有效实现烟气流场均布，阻力降很小；导流板下部（直板段）可根据烟气量变化调整角度，并可使积存在导流板上的粉尘滑落，掉入灰斗中排出。
[0023] 3)中心内置式吸收剂分配器，将新鲜消石灰和循环灰（统称吸收剂）输入位于反应器中心的本分配器，再重新均匀分配入反应器。
[0024] 分配器六个出灰口，定向对准6个烟气加速器入口端，可实现吸收剂等量、定向分配；出料口设在烟气高速区，可准确有效的与上升烟气混合进入烟气加速器；新鲜消石灰、循环灰提前与SO2接触，被烟气加热，使其快速干燥；消石灰和Cr在100°C以上反应，生成吸潮性较差、颗粒较细、不易凝结的碱式氯化钙〔CaCl2 ^Ca(OH)2 · H2O)，可大大减少粘壁、结垢的现象；新鲜消石灰及循环灰的颗粒硬度远远低于锅炉烟气中的粉尘硬度，混合后将大大减弱对烟气加速器入口的冲击磨损；合理利用空间。
[0025] 吸收剂分配器3位于塔中心，吸收剂被均匀分配，烟气流速高、动能大，易于将其带走。而Lurgi的单侧下进灰结构,Wulff和国内许多公司的单侧上进灰结构,循环灰进口均开在器壁单侧，循环灰在整个塔截面分布不可能均匀。
[0026] 4)六个“拉伐尔喷嘴”式烟气加速器：可有效提高烟气流速，可降低反应器的高度，可有效提高气、固混合的均匀度。因喉口的直段很短，进气段及扩散段夹角较小，其压力降比Lurgi、Wulff、AE等国外技术的文丘里管低得多，并可有效强化烟气入口段气固接触、传质、传热，提高脱硫反应效率。烟气加速器入口段可采用耐磨钢或耐磨涂料。
[0027] 5)双流体喷嘴两级增湿活化：水雾粒径很细（40〜60 μ m)，水雾处于烟气湍动能最大、颗粒密度最大的区域，水分能完全蒸发；与传统单级喷雾相比，明显降低了反应器内的平均反应温度和出口烟温；使反应器内温度场分布更均匀；可有效避免因局部喷水过量造成的湿壁效应；雾化水可有效降低烟气温度（要控制在烟气露点温度以上10〜 20V),增湿效果好，使SO2与Ca (OH) 2转化为可瞬间完成的离子型反应，有效提高脱硫效率。第二级喷嘴主要用于调节出口烟气的温度。
[0028] 采用本喷嘴可有效提高Ca的利用率，降低运行成本；系统运行更加稳定可靠；投资比高压回流式喷嘴低30%以上；第一级喷嘴的水、压缩空气管布置于烟气加速器上板面下部，可避免发生因侧向悬臂伸入，喷嘴的水、气入口管路被烟气粉尘颗粒磨穿的情况。
[0029] 6)旋流板气、固分离器设在反应器筒体上部。
[0030] 脱硫灰通过该装置随烟气流动突然改变方向，使颗粒获得惯性离心力，被甩向器壁，又靠重力作用沿器壁向下滑落，形成内回流；脱硫灰在这种运动中相互碰撞，与器壁摩擦，加速吸收剂的表面更新；有效提高吸收剂的循环倍率（可达100〜150)，延长吸收剂在反应器内的停留时间，提高吸收剂的利用率；可使反应器出口烟气粉尘含量显著降低（可降低50%以上），大大减轻袋式除尘器的负荷。可提高袋式除尘器的气布比，减少过滤面积，节省投资；该分离器结构简单，分离效率高，压力损失很小（低于150pa)。
[0031] 反应器筒体包括筒体下部扩散段。烟气出口 8为设在反应器顶部中心部位的矩形烟道，有利于整个反应器流场分布均匀，有利于吸收剂内回流。
Claims (5)
1. 一种均流场内回流循环流化床烟气脱硫反应器。其特征在于：由下至上的结构依次为，直流流线型底部进气口（I)、作为进气机构一部分的导流板（2)、中心内置式吸收剂分配器（3)、烟气加速器（4)、增湿活化喷嘴（5)、旋流板气固分离器（6)以及反应器筒体（7)上部的中心出口烟道（8)，与中心内置式吸收剂分配器（3)相连接的消石灰及循环灰入口通道（9)。
2.根据权利要求I所述的内回流循环流化床烟气脱硫反应器，其特征在于：所述的直流流线型进气口（I)为方形变截面结构，进气口内的导流板（2)为双片圆弧式均布导流板，且下部设有可调角度的直板段。
3.根据权利要求I所述的内回流循环流化床烟气脱硫反应器，其特征在于：所述的中心内置式吸收剂分配器（3)，设有6个出灰口，分别对准6个烟气加速器（4)的入口端。
4.根据权利要求I所述的内回流循环流化床烟气脱硫反应器，其特征在于：所述的增湿活化喷嘴（5)共2个，设在反应器中心不同高度，为双流体喷嘴。
5.根据权利要求I所述的内回流循环流化床烟气脱硫反应器，其特征在于：所述的旋流板式气固分离器（6)设在反应器筒体（7)上部中心处，为反向旋流板结构。
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| WO2015113627A1 (en) * | 2014-01-31 | 2015-08-06 | Amec Foster Wheeler Energia Oy | A method of and a scrubber for removing pollutant compounds from a gas stream |
| EP3581258A1 (en) | 2018-06-14 | 2019-12-18 | Doosan Lentjes GmbH | Reactor for cleaning flue gas by a dry or quasi-dry sorption process |
| EP3663647A1 (en) | 2018-12-07 | 2020-06-10 | Doosan Lentjes GmbH | Incineration plant with a nozzle, reactor for cleaning flue gases with a nozzle and respective nozzle |
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| CN101596398B (zh) * | 2009-05-08 | 2012-05-23 | 朱学智 | 一种基于循环流化床锅炉烟道的再脱硫方法 |
| EP2263780B1 (de) * | 2009-06-18 | 2017-12-06 | ENVIROSERV GmbH | Rauchgasreinigungsanlage mit Düsenvariation |
| EP2263779B1 (de) * | 2009-06-18 | 2015-03-11 | ENVIROSERV GmbH | Rauchgasreinigunsanlage mit Auslasseinheit |
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| CN101920164B (zh) * | 2010-06-12 | 2012-09-19 | 北京科技大学 | 一种卧式密相循环流化干塔脱硫装置 |
| CN102441324A (zh) * | 2010-10-15 | 2012-05-09 | 北京博朗环境工程技术股份有限公司 | 下行循环流化床烟气脱硫反应器 |
| CN102389706A (zh) * | 2011-10-24 | 2012-03-28 | 浙江菲达脱硫工程有限公司 | 一种用于半干法脱硫反应器的灰气混合装置 |
| CN103721484A (zh) * | 2012-10-15 | 2014-04-16 | 北京博朗环境工程技术股份有限公司 | 同轴短程快速循环协同脱除多种污染物的半干法烟气净化技术 |
| PL3099398T3 (pl) | 2014-01-31 | 2018-01-31 | Amec Foster Wheeler Energia Oy | METHOD AND TOWER RINSE TO REMOVE POLLUTION COMPOUNDS FROM THE GAS STREAM |
| CN106215538B (zh) * | 2016-08-24 | 2018-03-13 | 北京北科环境工程有限公司 | 一种用于烧结/球团湿法脱硫烟气深度治理系统 |
| CN108273375A (zh) * | 2017-12-29 | 2018-07-13 | 铜陵铜冠神虹化工有限责任公司 | 硫化钠生产中热化炉烟气除硫装置及工艺 |
| EP3738667A1 (en) | 2019-05-13 | 2020-11-18 | Doosan Lentjes GmbH | Nozzle in a reactor comprising an outlet insert |
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| EP3663647A1 (en) | 2018-12-07 | 2020-06-10 | Doosan Lentjes GmbH | Incineration plant with a nozzle, reactor for cleaning flue gases with a nozzle and respective nozzle |
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