CN101844037A - 一种均匀布风湿法烟气脱硫塔装置 - Google Patents
一种均匀布风湿法烟气脱硫塔装置 Download PDFInfo
- Publication number
- CN101844037A CN101844037A CN 201010201012 CN201010201012A CN101844037A CN 101844037 A CN101844037 A CN 101844037A CN 201010201012 CN201010201012 CN 201010201012 CN 201010201012 A CN201010201012 A CN 201010201012A CN 101844037 A CN101844037 A CN 101844037A
- Authority
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- China
- Prior art keywords
- flue gas
- tower
- slurry
- desulfurization
- humidifying
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- 230000003009 desulfurizing Effects 0.000 title claims abstract description 89
- UGFAIRIUMAVXCW-UHFFFAOYSA-N carbon monoxide Chemical compound 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[O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 title claims abstract description 69
- 239000003546 flue gas Substances 0.000 title claims abstract description 68
- 238000006477 desulfuration reaction Methods 0.000 title claims abstract description 41
- 239000002002 slurry Substances 0.000 claims abstract description 89
- 235000019738 Limestone Nutrition 0.000 claims abstract description 27
- 239000006028 limestone Substances 0.000 claims abstract description 27
- 239000007921 spray Substances 0.000 claims abstract description 24
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- 238000007254 oxidation reaction Methods 0.000 claims abstract description 10
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- 238000010521 absorption reaction Methods 0.000 abstract description 2
- GBAOBIBJACZTNA-UHFFFAOYSA-L Calcium sulfite Chemical compound 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[Ca+2].[O-]S([O-])=O GBAOBIBJACZTNA-UHFFFAOYSA-L 0.000 abstract 1
- 235000010261 calcium sulphite Nutrition 0.000 abstract 1
- 239000003595 mist Substances 0.000 abstract 1
- OKTJSMMVPCPJKN-UHFFFAOYSA-N carbon Chemical compound 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- OYPRJOBELJOOCE-UHFFFAOYSA-N calcium Chemical compound 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[Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 description 2
- 239000011575 calcium Substances 0.000 description 2
- 229910052791 calcium Inorganic materials 0.000 description 2
- 238000007599 discharging Methods 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 239000002737 fuel gas Substances 0.000 description 2
- 239000002245 particle Substances 0.000 description 2
- 239000011505 plaster Substances 0.000 description 2
- 238000010248 power generation Methods 0.000 description 2
- 238000004088 simulation Methods 0.000 description 2
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Abstract
本发明公开一种均匀布风的湿法烟气脱硫塔装置，脱硫塔的顶部有烟气出口，底部有脱硫剂浆液池，在脱硫剂浆液池和顶部烟气出口自下而上依次有向下倾斜的烟气入口、文丘里导流管区、浆液喷淋区、除雾器区，脱硫剂浆液池与浆液喷淋区之间通过外置浆液循环泵相连；脱硫剂浆液池连接有石灰石浆液外部补给装置和氧化空气系统。烟气进入脱硫塔后，经文丘里导流管形成均匀向上的湍流，再经交错布置的浆液喷淋区，使烟气中的SO2转化成CaSO3，随吸收浆液液滴落入塔下方的浆液池内，最后被氧化成石膏。该装置与传统脱硫塔相比，气液传质效率可以提高20～30％，脱硫效率可达97％以上，液气比可以降低3～5L/m2，结构较简单，成本低。
Description
一种均匀布风湿法烟气脱硫塔装置
技术领域
[0001] 本发明涉及对燃煤电站锅炉所排放烟气的净化处理技术，具体涉及一种均勻布风 湿法脱硫塔装置。
背景技术
[0002] 在我国的一次能源构成中，煤占有绝对性的主导地位。以燃煤为主的火力发电但 煤燃烧时会产生大量污染物质，是目前我国大气污染排放最大的污染源，其危害性已成为 共识。燃煤带来的SO2和酸雨污染不仅是中国大气环境污染的主要问题，目前还是制约经 济协调稳定发展的重要环境因素。一般来说，SO2排放总量和烟气中SO2浓度增加率与燃煤 量及燃煤的含硫量有关。电力工业作为燃煤大户，消耗的煤炭数量占全国煤炭总产量半数 以上，而且多年来我国电力结构中火电所占比例居高不下，始终稳定在80%左右。因此，电 力行业是我国SO2的最重要排放源，控制发电过程中的SO2排放，对于解决日益严重的酸雨 污染问题具有重要的意义。
[0003] 目前来说，常用的火电厂烟气脱硫工艺主要有湿法、干法和半干法等。其中，湿法 烟气脱硫工艺由于具有运行可靠性好、脱硫效率高、煤种适应性强等优点，已成为主流的烟 气脱硫工艺。在湿法烟气脱硫工艺中，脱硫塔是整个工艺的核心部件，常用的脱硫塔主要有 喷淋塔、液柱塔、鼓泡塔和双回路塔等。在这些塔型中，喷淋塔具有结构简单、阻力小等优 点，获得了广泛的应用。
[0004] 但是，对于目前的传统脱硫塔来说，由于烟气从侧向进入塔内而后转向向上流动， 这就造成了塔内气液两相流速分布的不均勻，这样就会使得塔内压降增大，脱硫效率降低。
发明内容
[0005] 本发明的目的就是要提供一种均勻布风湿法烟气的脱硫方法及其能够均勻分布 气液两相流场的脱硫塔装置。
[0006] 本发明的技术方案
[0007] 一种均勻布风湿法烟气脱硫塔装置
[0008] 一种均勻布风湿法烟气脱硫塔装置，包括脱硫塔8，所述的脱硫塔8包括烟气入口 3、烟气出口 7、脱硫产物排浆口 1、浆液喷淋区5、除雾器区6、脱硫剂浆液池9、石灰石浆液外 部补给装置10、氧化空气系统11和浆液循环泵2及文丘里导流管区4 ；
[0009] 烟气出口 7开在脱硫塔8的顶部，脱硫剂浆液池9设在脱硫塔8的底部，脱硫剂浆 液池9底部侧边开有脱硫产物排浆口 1 ；
[0010] 石灰石浆液外部补给装置10和氧化空气系统11分别与脱硫剂浆液池9连接；
[0011] 脱硫塔8的底部脱硫剂浆液池9和顶部烟气出口 7自下而上依次设有向下倾斜的 烟气入口 3、文丘里导流管区4、浆液喷淋区5、除雾器区6，浆液池9与浆液喷淋区5之间通 过外置的浆液循环泵2相连；
[0012] 烟气入口 3与水平面之间的倾斜角度为10〜20°，烟气入口 3的上方的文丘里导流管区4区设有两层分别与烟气入口中心面成45°和135°角的文丘里导流管层，文丘里 导流管层的层间距为0. 9m，每层由外径为0. 2m,内径为0. 16m的平行不锈钢空心圆形管排 组成，相邻两空心管的中心间距为0. 4m ；
[0013] 浆液喷淋区5设有3层交错布置的石灰石浆液喷淋层；
[0014] 脱硫塔8的上部除雾器区6可以除去烟气中的液滴。
[0015] 一种均勻布风湿法烟气脱硫塔装置的应用
[0016] 采用上述的一种均勻布风湿法烟气脱硫塔装置进行脱硫，其脱硫的工艺过程如 下：
[0017] 对需要脱硫的烟气首先经过除尘预处理，将经过预除尘处理的烟气经脱硫塔下部 入口以向下倾斜的角度送入脱硫塔，而后烟气转向向上旋涡流动，再经过两层文丘里导流 管进行整流以使得烟气流场分布均勻，然后烟气流经脱硫塔中上方交错布置的喷淋层，与 喷淋层喷出的石灰石浆液液滴逆流接触，其中所含的SO2被吸收形成CaSO3,此时烟气由于 受到浆液的喷淋整流而使得其流场分布更为均勻，同时也强化了烟气和浆液之间的气液传 质，促进了 SO2W吸收。
[0018] 石灰石浆液吸收SO2形成CaSO3后，含有CaSO3落入脱硫塔底部的浆液池内，与空 气发生充分的氧化反应，所生成的副产品石膏在浆液池底部经石膏浆液泵排出，同时，脱硫 后的净烟气流经脱硫塔上部区域的除雾器，脱除烟气中所携带的液滴，所得的洁净烟气从 脱硫塔顶部出口引出排入烟囱。
[0019] 其中入口烟气最好以与水平面成10〜20°的向下角度引入脱硫塔中，这样可以 使烟气进入脱硫塔后流程增长，一方面使得烟气对对侧塔壁的冲击减弱，且使得烟气流向 发生偏转整理的时间延长，有利于烟气流场的均勻分布；另一方面也延长了气液两相在塔 内的接触时间，有利于脱硫反应的进行。
[0020] 上述脱硫塔浆液池内的石灰石浆液pH值控制在5. 4〜5. 6为宜。这样，可以确保 石灰石具有适当的的溶解速率以提供与SO2反应的C032_和HC03_，以使得烟气中的SO2与石 灰石浆液始终处于最佳化学反应状态，以进一步提高SO2的脱除效率。
[0021] 上述工艺中，SO2首先溶于水，生成H2SO3,而后与石灰石浆液中溶解的CaCO3反应 生成CaSO3，其化学反应式为：
[0022]
SO2+H2O O H2SO3 (1)
[0023]
CaCO3 f H2SO3 O CaSO3 +H20 + C02 (2)
[0024] 同时，从浆液池内鼓入的空气不断地与CaSO3反应生成CaSO4，其化学反应式为：
[0025]
CaS03+1/202oCaS04 (3)
[0026] 石膏浆液在浆液池底部经石膏浆液泵排出，通过水力旋流分离器和真空皮带脱水 机脱除其中所含的水分，最终得到副产品石膏。
[0027] 本发明的有益效果
[0028] 与传统脱硫塔比，本发明具有如下优点：[0029] (1)在传统脱硫塔内，烟气进入喷淋塔后，冲击入口对侧塔壁区域，而后分别形成一个顺时针和一个逆时针方向旋转的旋涡盘旋向上流动。由于烟气流向的转变，一方面增 大了塔内压降，另一方面也使得烟气流速分布不均勻，而烟气流速分布的不均勻又造成了 浆液流速空间分布的不均勻性，脱硫效率仅为90-95%。通过安装文丘里导流管层，烟气流 至这一区域时，由于文丘里管的阻挡、导流作用，使得烟气向塔中心区域聚拢，烟气流所形 成的两个旋涡体积缩小，在塔纵剖面上的烟气流速逐渐趋于均勻，从而优化了塔内气液两 相流场分布，强化了气液传质，提高脱硫效率至97%以上，完全符合S02排放的国家标准。
[0030] (2)由于塔内流场分布均勻，脱硫效果较好，可以有效地减少脱硫剂用量，降低脱 硫塔运行费用。
附图说明
[0031] 图1、均勻布风烟气脱硫装置结构示意图
[0032] 图2、数值模拟传统脱硫塔纵剖面烟气流场速度矢量图
[0033] 图3、数值模拟均勻布风烟气脱硫塔纵剖面烟气流场速度矢量图
具体实施方式
[0034] 下面针对一台燃煤锅炉机组所排放的烟气结合附图1对本发明的工艺及其装置 进行进一步说明。
[0035] 实施例1
[0036] 如图1所示的均勻布风烟气脱硫塔
[0037] 一种均勻布风湿法烟气脱硫塔装置，包括脱硫塔8，所述的脱硫塔8包括烟气入口 3、烟气出口 7、脱硫产物排浆口 1、浆液喷淋区5、除雾器区6、脱硫剂浆液池9、石灰石浆液外 部补给装置10、氧化空气系统11和浆液循环泵2及文丘里导流管区4 ；
[0038] 烟气出口 7开在脱硫塔8的顶部，脱硫剂浆液池9设在脱硫塔8的底部，
[0039] 脱硫剂浆液池9底部侧边开有脱硫产物排浆口 1 ；
[0040] 石灰石浆液外部补给装置10和氧化空气系统11分别与脱硫剂浆液池9连接；
[0041] 脱硫塔8的底部脱硫剂浆液池9和顶部烟气出口 7自下而上依次设有向下倾斜的 烟气入口 3、文丘里导流管区4、浆液喷淋区5、除雾器区6，浆液池9与浆液喷淋区5之间通 过外置的浆液循环泵2相连；
[0042] 烟气入口 3与水平面之间的倾斜角度为10〜20°，烟气入口 3的上方的文丘里导 流管区4区设有两层分别与烟气入口中心面成45°和135°角的文丘里导流管层，文丘里 导流管层的层间距为0. 9m，每层由外径为0. 2m,内径为0. 16m的平行不锈钢空心圆形管排 组成，相邻两空心管的中心间距为0. 4m ；
[0043] 浆液喷淋区5设有3层交错布置的石灰石浆液喷淋层；
[0044] 脱硫塔上部设有除雾器区6以除去烟气中的液滴。
[0045] 实施例2
[0046] 采用传统的非均勻布风的烟气脱硫塔进行脱硫
[0047] 从锅炉排出的烟气，其中SO2浓度为1500mg/m3，经过经电除尘器除尘后通过增压 风机选择烟气流速为6785m3/L经脱硫塔8的烟气入口 3送入脱硫塔8内，烟气分成两路，分别形成一个顺时针和一个逆时针方向的旋涡向上流动，并继续向上流动，穿过交错布置 在脱硫塔8中上方的喷淋区5，浆液池9内的石灰石浆液经石灰石浆液循环泵2以流速为 67. 85m3/L不断输送到喷淋区5，经喷嘴喷出，与烟气逆流接触，从而完成脱硫。同时，石灰石 浆液补给装置10不断的向浆液池9内补给石灰石浆液，维持其pH值介于5. 4〜5. 6之间； 同时氧化空气系统11则不断的向浆液池9内供给空气，将CaSO3氧化为CaSO4,生成的石膏 浆液则由脱硫副产物排浆口 1排出，经脱水后形成副产品石膏，烟气出口处利用德图350XL 烟气分析仪测量出口 SO2浓度，计算可得脱硫效率为93. 7%。
[0048] 所用的石灰石浆液中的石灰石粒径为30〜50μ m，浆液含固率为20wt%，进口 SO2 浓度为 1500mg/m3。
[0049] 实施例3
[0050] 本发明的采用均勻布风的烟气脱硫塔进行脱硫
[0051] 从锅炉排出的烟气，其中SO2浓度为1500mg/m3，经过经电除尘器除尘后通过增压 风机选择烟气流速为6785m3/L经脱硫塔8的烟气入口 3送入脱硫塔8内，烟气分成两路，分 别形成一个顺时针和一个逆时针方向的旋涡向上流动，经文丘里导流管4整流形成均勻分 布的烟气湍流，并继续向上流动，穿过交错布置在脱硫塔8中上方的喷淋区5，浆液池9内的 石灰石浆液经石灰石浆液循环泵2以流速为67. 85m3/L不断输送到喷淋区5，经喷嘴喷出， 与烟气逆流接触，从而完成脱硫。同时，石灰石浆液补给装置10不断的向浆液池9内补给 石灰石浆液，维持其PH值介于5. 4〜5. 6之间；同时氧化空气系统11则不断的向浆液池9 内供给空气，将CaSO3氧化为CaSO4,生成的石膏浆液则由脱硫副产物排浆口 1排出，经脱水 后形成副产品石膏，烟气出口处利用德图350XL烟气分析仪测量出口 SO2浓度，计算可得脱 硫效率为97.4%。
[0052] 所用的石灰石浆液中的石灰石粒径为30〜50 μ m，浆液含固率为20wt%，进口 SO2 浓度为 1500mg/m3。
[0053] 图2为实施例2的传统的非均勻布风的烟气脱硫塔进行脱硫烟的脱硫塔横截面上 的烟气流场速度云图（单位：m/s)的CFD模拟结果。
[0054] 图3为实施例3的本发明的均勻布风的烟气脱硫塔进行脱硫的脱硫塔横截面上的 烟气流场速度云图（单位：m/s)的CFD模拟结果。
[0055] 从图2和图3中可以直观的看出，与传统脱硫塔相比，均勻布风脱硫塔内的烟气流 速分布的均勻性得到了明显的改善，这也从理论上验证了该发明的合理性。
[0056] 以上所述内容仅为本发明构思下的基本说明，而依据本发明的技术方案所做的任 何等效变换，均应属于本发明的保护范围。
Claims (6)
- 一种均匀布风湿法烟气脱硫塔装置，包括脱硫塔(8)，所述的脱硫塔(8)包括烟气入口(3)、烟气出口(7)、脱硫产物排浆口(1)、浆液喷淋区(5)、除雾器区(6)、脱硫剂浆液池(9)、石灰石浆液外部补给装置(10)、氧化空气系统(11)和浆液循环泵(2)，其特征在于还包括文丘里导流管区(4)；所述的烟气出口(7)开在脱硫塔(8)的顶部，脱硫剂浆液池(9)设在脱硫塔(8)的底部，脱硫剂浆液池(9)底部侧边开有脱硫产物排浆口(1)；所述的脱硫剂浆液池(9)和顶部烟气出口(7)之间自下而上依次设有烟气入口(3)、文丘里导流管区(4)、浆液喷淋区(5)及除雾器区(6)；其中脱硫剂浆液池(9)与浆液喷淋区(5)之间通过外置的浆液循环泵(2)相连；石灰石浆液外部补给装置(10)和氧化空气系统(11)分别与脱硫剂浆液池(9)连接。
- 2.如权利要求1所述的一种均勻布风湿法烟气脱硫塔装置，其特征在于所述的文丘里 导流管区（4)区设有两层分别与烟气入口中心面成45°和135°角的文丘里导流管层。
- 3.如权利要求2所述的一种均勻布风湿法烟气脱硫塔装置，其特征在于所述的文丘里 导流管层，层间距为0. 9m，每层由外径为0. 2m,内径为0. 16m的平行不锈钢空心圆形管排组 成，相邻两空心管的中心间距为0. 4m。
- 4.如权利要求1所述的一种均勻布风湿法烟气脱硫塔装置，其特征在于所述的烟气入 口（3)向下与水平面之间的倾斜角度为10〜20°。
- 5.如权利要求1所述的一种均勻布风湿法烟气脱硫塔装置，其特征在于所述的浆液喷 淋区（5)设有交错布置的喷淋层。
- 6.如权利要求2所述的一种均勻布风湿法烟气脱硫塔装置，其特征在于所述的浆液喷 淋区（5)设有交错布置的喷淋层为3层。
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