CN106000068A - 一种so2超低排放微变温节能消烟系统 - Google Patents
一种so2超低排放微变温节能消烟系统 Download PDFInfo
- Publication number
- CN106000068A CN106000068A CN201610557606.4A CN201610557606A CN106000068A CN 106000068 A CN106000068 A CN 106000068A CN 201610557606 A CN201610557606 A CN 201610557606A CN 106000068 A CN106000068 A CN 106000068A
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- desulfurizing tower
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- RAHZWNYVWXNFOC-UHFFFAOYSA-N sulphur dioxide Chemical compound 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[S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 claims description 3
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- 239000011593 sulfur Substances 0.000 claims description 3
- 229910001069 Ti alloy Inorganic materials 0.000 claims description 2
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- 229910052755 nonmetal Inorganic materials 0.000 claims description 2
- 150000002843 nonmetals Chemical class 0.000 claims description 2
- SCKXCAADGDQQCS-UHFFFAOYSA-N performic acid Chemical compound 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OOC=O SCKXCAADGDQQCS-UHFFFAOYSA-N 0.000 claims description 2
- UGFAIRIUMAVXCW-UHFFFAOYSA-N carbon monoxide Chemical compound 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- 238000004458 analytical method Methods 0.000 description 1
- OKTJSMMVPCPJKN-UHFFFAOYSA-N carbon Chemical compound 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- B01D53/34—Chemical or biological purification of waste gases
- B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
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Abstract
本发明开发设计一种SO2超低排放微变温节能消烟系统，该系统用于高、低双pH喷淋装置脱硫塔内，该系统主要包括降温均流器、相变深度净化器、微热升温消烟器，以及泵和连接管路；降温均流器设置在脱硫塔的入口烟道内；相变深度净化器设置在高pH喷淋装置上方的一级除雾器与二级除雾器之间；微热升温消烟器设置在脱硫塔的出口烟道内；降温均流器的换热介质和微热升温消烟器的换热介质经由循环泵和连接管路形成循环回路，该循环回路又通过控制阀与开式冷源连接。该系统主要用于燃煤烟气高效脱硫并消除脱硫后烟气烟羽问题，以实现SO2超低排放和消除烟羽的目的。
Description
一种S〇2超低排放微变温节能消烟系统
[0001 ]
技术领域： 本发明提供一种S02超低排放微变温节能消烟系统，属资源环境烟气净化技术领域。
[0002]
背景技术： 随着火电厂大气污染物控制进入超低排放阶段，火电烟气二氧化硫排放浓度控制要求 从国家标准GB13223-2011的200mg/m3降至35mg/m3以下，也就是超低排放，部分地方标准甚 至要求采取措施消除烟羽。目前，应用的常规石灰石一石膏脱硫工艺采用单塔喷淋单pH值 控制，脱硫效率一般为95%，依靠单纯的放大保守设计，已经难以满足新的排放控制要求，而 且单纯采用保守设计存在建设及运行不经济，工况适应性差等问题。关于消除烟羽，原来采 用的回转式GGH换热技术因为设备漏风、S0 2逃逸、故障率高等问题，近年来已经基本淘汰， 且因漏风问题难以满足超低排放需求。而传统直接再热技术加热耗能高、也增加烟风系统 阻力，增加机组引风机功耗，经济性差。因此，迫切需要开发一种既能高效脱硫满足超低排 放，又能经济性解决烟囱烟羽、消除白烟视觉困扰的新型多功能低能耗脱硫装置，以适应当 前环保要求。
[0003] 此外，根据对脱硫机理的深入研究及分析，当脱硫塔内浆液pH值控制在低区间时， 可提高液相反应速率，加速吸收剂一一石灰石的溶解、促进副产物石膏氧化和结晶，利于洗 涤后二氧化硫的稳定固化和成盐转化，促进脱硫。当pH值控制在高区间时可以提高浆液对 烟气中二氧化硫的洗涤吸收速率。传统的单塔单pH值控制只能在高低pH之间找一个相对折 中的控制范围，无法彻底解决此矛盾。目前，国内使用的单塔双循环脱硫塔采用圆锥底收集 碗与浆液导流板，烟气通流阻断冲击效应明显，气流过渡不够顺畅、分布均匀性差，导致烟 气通流阻力大，烟风系统能耗大幅增加。因此，需要开发一种能够将高、低pH值分区控制同 时兼顾，均化流场以降低烟气通流阻力，实现进一步脱硫低能耗提效、S02超低排放且可以 消除湿法脱硫后烟羽的技术及装备，以适应新的环保排放要求。
[0004]
发明内容： 本发明开发设计一种既高效脱硫实现s〇2超低排放，又能够消除脱硫后烟气烟羽的系 统，主要用于烟气脱硫及脱硫后烟羽消除，以实现二氧化硫超低排放及烟囱不冒有色烟羽 的目的。
[0005] 本发明的具体技术方案如下： 一种S〇2超低排放微变温节能消烟系统，该系统用于高、低双pH喷淋装置脱硫塔内，该 系统主要包括降温均流器、相变深度净化器、微热升温消烟器，以及栗和连接管路；降温均 流器设置在脱硫塔的入口烟道内；相变深度净化器设置在高pH喷淋装置上方的一级除雾器 与二级除雾器之间；微热升温消烟器设置在脱硫塔的出口烟道内；降温均流器的换热介质 和微热升温消烟器的换热介质经由循环栗和连接管路形成循环回路，该循环回路又通过控 制阀与开式冷源连接。
[0006] 本发明的进一步设计在于： 还包括设置在脱硫塔内的高、低pH喷淋装置之间的双pH喷淋脱硫塔双向整流导液装 置，该装置包括壁流引流环和钵型积液盘； 所述壁流引流环由上、下分配弧环和振动分液环组合而成，上、下分配弧环形状相当且 背向对称设置，凹面朝外，两环外缘分别安装在脱硫塔内壁上，两环外缘相抵且连接，并在 内缘的内圈连接所述振动分液环； 所述钵型积液盘设置在壁流引流环的正下方，并通过支撑架安装在脱硫塔内，钵型积 液盘上部敞口，底部经浆液管道连接至高pH衆液池。
[0007] 本发明的进一步设计在于： 上、下分配弧环径向投影内口半径较0.618R小0.1~0.5m，外口半径与脱硫塔相适配， 上、下分配弧环的弧度角为1°~30°，弧半径为0.3 R~0.6R;钵型积液盘上口与壁流引流环 的上、下分配弧环连接处的间距为0.382R±0.5m;钵型积液盘内口径较0.618 R大0. lm~ 〇. 5m;振动分液环外口径与上、下分配弧环内口径相当，内口径较钵型积液盘的口径小0.1 ~1.5m;其中R为脱硫塔半径。
[0008] 振动分液环向脱硫塔下方带有锥度，与水平方向呈1°~30°角；厚度为0.02~ 0.3mm〇
[0009] 上、下分配弧环之间经由限位板定位连接;钵型积液盘表面采用流线型设计;振动 分液环内圈呈齿状。
[0010] 上、下分配弧环与钵型积液盘采用耐腐蚀耐磨合金、玻璃钢材质或采用碳钢衬镀 防腐耐磨涂层。
[0011] 为了实现壁流引流环的浆液振动分散，振动分液环采用弹性合金或非金属耐腐耐 磨薄片材质;如薄金属钛合金、双相合金钢、PC、PET、PFA等。
[0012] 本发明相比现有技术具有以下有益效果： 1、本发明的微变温节能排放消烟系统，与双pH喷淋脱硫塔有机组合，回收利用烟气余 热消除白烟，无需额外增加能耗，双pH分区高效脱硫实现S02超低排放，想变凝聚，多污染物 深度净化，减少吸收塔水份蒸发，降低脱硫水耗，消除脱硫后石膏雨、烟雨、有色烟羽及白 烟。
[0013] 2、降温均流器具有余热回收、均化化吸收塔流场、降低吸收塔处理烟气量、降低脱 硫水耗的功能。通过回收吸收塔入口干烟气中的余热用于吸收塔脱硫后烟气加热消烟，余 热利用，没有增加消烟能耗;降低了进塔烟气温度，吸收塔处理的工况烟气量下降，延长了 烟气在吸收塔内洗涤区的停留时间，利于提高脱硫效率，也减少了吸收塔水汽蒸发量，降低 了脱硫系统水耗。
[0014] 3、相变深度净化器具有细微颗粒物和雾滴凝聚、多污染物深度净化、脱水功能，通 过冷却介质对脱硫后经过一级除雾器除雾的携带有一定量浆液雾滴的过饱和湿烟气降温 和产生相变，促进细微颗粒和雾滴相变凝聚，凝结过饱和的烟气，产生大量可去除液滴，通 过相变深度净化器以及后续的二级除雾器脱除，将烟气中大量水和污染物脱除。
[0015] 4、微热升温消烟器利用吸收塔入口烟气回收的余热将脱硫后经过深度净化和脱 水的饱和湿烟气微升温，使得烟气进入不饱和区后排放就彻底消除的视觉白烟。
[0016] 5、双pH喷淋脱硫塔双向整流导液装置，用于将高pH值洗液与低pH值洗液分开回 收，具有结构独特，脱硫效率高、吸收塔阻力小等特点。双pH分区设置，将吸收塔分为302高 pH洗涤区和低pH洗涤区，本装置或实现高、低pH值分区调控的功能。
[0017] 6、研究验证表明，对于S02低pH洗涤区，洗涤吸收大量S02的同时，通过低pH值调控， 可促进吸收剂石灰石迅速彻底溶解，提高了吸收剂溶解及参与化学反应的速率，并更利于 副产物石膏氧化和结晶析出；对于S02高pH洗涤区，通过高pH值调控，进一步实现S02提效;相 比常规单塔喷淋单pH控制技术双pH控制可以在更低液气比条件下可实现更高的脱硫效率， 脱硫效率尚达99%以上，提尚吸收剂利用率接近100%，排放指标可以满足超低排放35mg/m 3 要求。
[0018] 7、同时，本发明的采用将大大提高吸收塔对输入条件(煤种、吸收剂、工况)的适应 性，提高脱硫效率的同时，均化了吸收塔内流场，降低了烟气通流阻力。
[0019]
附图说明： 图1为本发明的结构示意图。
[0020] 图2为壁流引流环的局部放大图。
[0021 ]图中：1-脱硫塔;2-高pH喷淋装置;21-搅拌器;22-高pH衆液池;23-氧化喷枪;24-高pH循环栗；3-低pH喷淋装置;31-搅拌器;32-低pH衆液池;33-氧化喷枪;34-低pH循环栗； 4-壁流引流环;41-上分配弧环;42-下分配弧环;43-限位板;44-振动分液环；5-钵型积液 盘;51-高pH浆液引出管路;52-支撑架;6--级除雾器;7-二级除雾器;81-降温均流器;82-相变深度净化器;83-微热升温消烟器;84-循环栗;85-旁通阀。
[0022]图3为现有的单塔双循环脱硫塔圆锥。
[0023]图3中：1-脱硫塔;2-高pH喷淋装置;21-搅拌器;22-高pH衆液池;23-氧化喷枪;24-高pH循环栗；3-低pH喷淋装置;31-搅拌器;32-低pH衆液池;33-氧化喷枪;34-低pH循环栗； 4-塔壁导流环;5-圆锥形托盘;51-高pH衆液引出管路;52-支撑钢架;6--级除雾器;7-二级 除雾器。
[0024]
具体实施方式： 下面结合附图对本发明作进一步的阐述： 实施例一： 本发明单塔双pH脱硫系统:包括布置在脱硫塔1内的高pH喷淋装置2和低pH喷淋装置3， 连接管路以及高pH衆液悬浮氧化器、低pH衆液悬浮氧化器、高pH衆液池22和低pH衆液池32。 高pH衆液池22和低pH衆液池32分割开来，设置在塔底部。
[0025]高pH喷淋装置2和低pH喷淋装置3均设有多层喷淋头;高、低pH浆液悬浮氧化器包 括搅拌器、氧化喷枪、滤网及容器等。
[0026]双pH脱硫系统特点是将烟气分区洗涤，布置在下层的第一级为低pH洗涤区、pH控 制范围4-5.4;布置在上层的第二级为高pH洗涤区，pH控制范围5.4-6.5。
[0027]如图1所示，本发明的双pH喷淋脱硫塔微变温节能排放消烟系统:主要包括降温均 流器81、相变深度净化器82、微热升温消烟器83,以及栗和连接管路(如图1中部分所示），该 系统设置在实施例一的单塔双pH脱硫系统中。降温均流器设置在脱硫塔的入口烟道内；相 变深度净化器设置在高pH喷淋装置上方的一级除雾器与二级除雾器之间；微热升温消烟器 设置在脱硫塔的出口烟道内；降温均流器的换热介质和微热升温消烟器的换热介质经由循 环栗和连接管路形成循环回路，该循环回路又通过控制阀与开式冷源连接。
[0028] 原烟气经降温均流器81与微热升温消烟器83之间由介质循环栗84、阀和连接管路 组成，管内介质可以为水等热媒，介质（如水)经过脱硫塔入口的原烟气由降温均流器81吸 热升温后栗送至微热升温消烟器83,用于加热烟道内流经微热升温消烟器的净烟气，加热 后净烟气温度升高l-l〇°C，升温前净烟气为饱和湿烟气，升温后变为不饱和烟气，进入烟囱 排放至后看不到白烟。而原烟气经过降温均流器后温度下降、流场更加均匀，原烟气烟温降 低，减少了脱硫塔要处理的工况烟气量，降低的塔内运行流速，有利于提高脱硫效率 相变深度净化器82安装在吸收塔内一级除雾器6上方，二级除雾器7下方，介质为冷却 水，温度0-30°C，用于将吸收塔内的烟气温度降低0-KTC，烟气降温使得携带大量液滴的饱 和湿烟气进一步凝聚，脱出大量的水，同时烟气冷却、冷凝已经相变过程伴随着细微雾滴、 细微颗粒的热凝聚和相变凝聚，利于细微雾滴和颗粒物的凝聚和洗涤。当介质冷却水采用 开式循环运行方式时，来水由开式循环栗经过过滤器后送入相变深度净化器，冷却烟气后 排出，送至电厂工业用水箱。如果采用闭式循环，则来水经过净化为软水，再栗送至相变多 功能深度净化器，介质在系统内循环使用，水温升高后，可通过增设成熟的空冷系统降温， 该方式运彳丁能耗偏尚。
[0029] 实施例三： 如图1所示，本发明双pH喷淋脱硫塔双向整流导液装置设置在脱硫塔内的高、低pH喷淋 装置之间，包括壁流引流环和钵型积液盘。
[0030] 如图2所示，壁流引流环4由上分配弧环41、下分配弧环41和振动分液环44组合而 成，上、下分配弧环形状相当且背向对称设置，凹面朝外，两环外缘分别安装在脱硫塔内壁 上，两环外缘相抵且连接，并在内缘的内圈连接所述振动分液环44;上、下分配弧环之间经 由限位板43定位连接。
[0031] 钵型积液盘5设置在壁流引流环4的正下方，并通过支撑架52安装在脱硫塔1内，钵 型积液盘5上部敞口，底部经浆液管道连接至高pH衆液池22,钵型积液盘5表面采用流线型 设计。
[0032] 上、下分配弧环径向投影内口半径较0.618R小0.1~0.5m，外口半径与脱硫塔相适 配，上、下分配弧环的弧度角为8° (1°~30°之间），弧半径为0.5R(0.3R~0.6R);钵型积液盘 5上口与壁流引流环4的上、下分配弧环连接处的间距为0.382R±0.5m;钵型积液盘5内口径 较0.618 R大0. lm~0.5m;振动分液环44外口径与上、下分配弧环内口径相当，内口径较钵 型积液盘5的口径小0.5 m(0.1~1.5m);其中R为脱硫塔半径。
[0033]振动分液环44向脱硫塔下方带有锥度，与水平方向呈20° (1°~30°之间均可）角； 厚度为0.02~0.3mm;宽度为5~300mm(该宽度为锥形的母线），振动分液环44内圈呈齿状， 用于撕裂液滴。
[0034] 上、下分配弧环与钵型积液盘5采用耐腐蚀耐磨合金、玻璃钢材质或采用碳钢衬镀 防腐耐磨涂层。
[0035] 本发明so2超低排放微变温节能消烟系统各部分的具体功能如下： 1、本发明的双pH喷淋脱硫塔微变温节能排放消烟系统与脱硫塔内构件组合使用，先通 过一级除雾器初步除雾，初步分离喷淋层浆液携带;接着利用降温均流器（相变深度净化 器)降温、相变、凝聚细微雾滴、细微颗粒、凝结水汽，析出烟气中大量的水;然后利用二级除 雾器除尘除雾后，烟气变为超净的含少量饱和水汽的烟气，既改善了脱硫塔的流场、又提高 了脱硫塔内除雾器的除雾效率，吸收塔出口雾滴含量5~25mg/m 3,远低于常规除雾器吸收 塔细微浆液雾滴携带量75 mg/m3;再利用微热升温器加热烟气变为不饱和气体，就消除了 烟羽、石膏雨，烟囱看不到白烟。
[0036] 2、降温均流器具有余热回收、均化化吸收塔流场、降低吸收塔处理烟气量、降低脱 硫水耗的功能。通过回收吸收塔入口干烟气中的余热用于吸收塔脱硫后烟气加热消烟，余 热利用，没有增加消烟能耗;降低了进塔烟气温度，吸收塔处理的工况烟气量下降，延长了 烟气在吸收塔内洗涤区的停留时间，利于提高脱硫效率，也减少了吸收塔水汽蒸发量，降低 了脱硫系统水耗。
[0037] 3、相变深度净化器具有细微颗粒物和雾滴凝聚、多污染物深度净化、脱水功能，通 过冷却介质对脱硫后经过一级除雾器除雾的携带有一定量浆液雾滴的过饱和湿烟气降温 和产生相变，促进细微颗粒和雾滴相变凝聚，凝结过饱和的烟气，产生大量可去除液滴，通 过相变深度净化器以及后续的二级除雾器脱除，将烟气中大量水和污染物脱除。
[0038] 4、微热升温消烟器利用吸收塔入口烟气回收的余热将脱硫后经过深度净化和脱 水的饱和湿烟气微升温，使得烟气进入不饱和区后排放就彻底消除的视觉白烟。
[0039] 5、壁流引流环用于将上层喷淋挂壁的浆液引离吸收塔塔壁，导入到钵型积液盘， 同时将挂壁液膜分配到振动分液环上，由振动分液环通过振动将挂壁汇流的浆液再次撕割 破裂分散成为液滴用于烟气洗涤，以提高脱硫有效液气比。
[0040] 6、振动分液环为连接在上、下两弧环接合连接处的内侧开条状齿口的合金薄层， 内端在气流和喷淋液滴的击打下产生震动，将沿壁流而下的浆液撕裂成分散的液滴。振动 分液环的材料可以采用合金、碳钢覆盖防腐耐磨涂层、也可以采用耐腐耐磨非金属材质(如 玻璃钢），振动源为气流、液流或下落浆液的冲击引起。
[0041 ] 7、钵型积液盘:呈钵盂体流线结构，上部敞口，用于收集高pH洗涤区下来的浆液， 底部连接浆液管道，将收集的高pH浆液导出吸收塔外的高pH浆池，从而与吸收塔内低pH浆 池的有效隔离，实现双pH值控制分区功能。钵型积液盘的流线设计有利于将从下而上的烟 气圆滑过渡与分流，最大限度减少烟气通流的阻力。同时流线型设计表面光洁，可利用饱和 湿烟气凝结析出的冷凝水滴对烟气携带可能碰撞粘附的浆液及细颗粒进行清洗，实现自清 洁功能。
[0042] 8、钵型积液盘的容积为上层喷淋浆液0~100S停留时间容积，积液盘底部设置高 pH衆液引出管路，管径需要与积液盘容积匹配避免积液盘浆液溢流。
[0043] 试验案例一： 某处理烟气量5万m3/h脱硫试验装置，吸收塔喷淋层数配置相同，进行了以下几种情形 的试验比较； 情形一:空塔，3层喷淋，单pH值控制，两级除雾器； 情形二:采用实施例二的双pH喷淋脱硫塔双向整流导液装置，实现pH值分区，装置上方 高pH喷淋装置设置一层，下方低pH喷淋装置设置两层，两级除雾器之间增设相变深度净化 器，脱硫塔入口设降温均流器，出口设微热升温消烟器。
[0044] 情形三:采用图3所示现有的单塔双循环脱硫塔圆锥(采用圆锥形托盘，塔壁导流 环为板式结构），两级除雾器。
[0045] 其余试验条件类似，试验测试结果如下表：
注:情形二中，脱硫入口烟气经过降温均流器温度从122.5°C降至103°C，经过高、低pH 洗涤区后再经过一级除雾器除雾后，由相变深度净化器降温4°C相变凝聚深度净化后，再微 热升温3 °C，出口终端排放47.9 °C。
[0046]由上表可见，本发明设计的S02超低排放微变温节能消烟系统具有脱硫效率高、流 场更均化、吸收塔阻力小、烟气超低排放、排放无白色烟羽的特点。
Claims (10)
1. 一种S02超低排放微变温节能消烟系统，该系统用于高、低双pH喷淋装置脱硫塔内，其 特征在于:该系统主要包括降温均流器、相变深度净化器、微热升温消烟器，以及栗和连接 管路；降温均流器设置在脱硫塔的入口烟道内；相变深度净化器设置在高pH喷淋装置上方 的一级除雾器与二级除雾器之间；微热升温消烟器设置在脱硫塔的出口烟道内；降温均流 器的换热介质和微热升温消烟器的换热介质经由循环栗和连接管路形成循环回路，该循环 回路又通过控制阀与开式冷源连接。
2. 根据权利要求1所述S02超低排放微变温节能消烟系统，其特征在于:还包括设置在脱 硫塔内的高、低pH喷淋装置之间的双pH喷淋脱硫塔双向整流导液装置，该装置包括壁流引 流环和钵型积液盘； 所述壁流引流环由上、下分配弧环和振动分液环组合而成，上、下分配弧环形状相当且 背向对称设置，凹面朝外，两环外缘分别安装在脱硫塔内壁上，两环外缘相抵且连接，并在 内缘的内圈连接所述振动分液环； 所述钵型积液盘设置在壁流引流环的正下方，并通过支撑架安装在脱硫塔内，钵型积 液盘上部敞口，底部经浆液管道连接至高pH衆液池。
3. 根据权利要求2所述S02超低排放微变温节能消烟系统，其特征在于;上、下分配弧环 径向投影内口半径较〇. 618R小0.1~0.5m，外口半径与脱硫塔相适配，上、下分配弧环的弧 度角为1°~30°，弧半径为0.3 R~0.6R;钵型积液盘上口与壁流引流环的上、下分配弧环连 接处的间距为〇 · 382R±0 · 5m;钵型积液盘内口径较0 · 618 R大0 · lm~0 · 5m;振动分液环外口 径与上、下分配弧环内口径相当，内口径较钵型积液盘的口径小0.1~1.5m;其中R为脱硫塔 半径。
4. 根据权利要求2或3所述S02超低排放微变温节能消烟系统，其特征在于;振动分液环 向脱硫塔下方带有锥度，与水平方向呈1°~30°角；厚度为0.02~0.3mm;振动分液环最外边 口径沿环板面距离最里边口径距离50~300mm。
5. 根据权利要求4所述S02超低排放微变温节能消烟系统，其特征在于;上、下分配弧环 之间经由限位板定位连接。
6. 根据权利要求4所述S02超低排放微变温节能消烟系统，其特征在于;钵型积液盘表面 采用流线型设计。
7. 根据权利要求4所述S02超低排放微变温节能消烟系统，其特征在于;振动分液环内圈 呈齿状。
8. 根据权利要求4所述S02超低排放微变温节能消烟系统，其特征在于;上、下分配弧环 与钵型积液盘采用耐腐蚀耐磨合金、玻璃钢材质或采用碳钢衬镀防腐耐磨涂层。
9. 根据权利要求1所述S02超低排放微变温节能消烟系统，其特征在于;振动分液环采用 弹性合金或非金属耐腐耐磨薄片材质。
10. 根据权利要求9所述S02超低排放微变温节能消烟系统，其特征在于:振动分液环采 用薄金属钛合金、双相合金钢、PC、PET或PFA材料制成。
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