CN205007792U - 湿法脱硫烟气处理机构 - Google Patents
湿法脱硫烟气处理机构 Download PDFInfo
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- CN205007792U CN205007792U CN201520646369.XU CN201520646369U CN205007792U CN 205007792 U CN205007792 U CN 205007792U CN 201520646369 U CN201520646369 U CN 201520646369U CN 205007792 U CN205007792 U CN 205007792U
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- Prior art keywords
- flue gas
- wet
- heat exchanger
- type phase
- pipe heat
- Prior art date
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- UGFAIRIUMAVXCW-UHFFFAOYSA-N carbon monoxide Chemical compound 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- 239000003546 flue gas Substances 0.000 title claims abstract description 114
- 238000006477 desulfuration reaction Methods 0.000 title claims abstract description 59
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- 238000009833 condensation Methods 0.000 claims abstract description 70
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- 238000000034 method Methods 0.000 description 21
- RAHZWNYVWXNFOC-UHFFFAOYSA-N sulfur dioxide Inorganic materials 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O=S=O RAHZWNYVWXNFOC-UHFFFAOYSA-N 0.000 description 18
- 238000001816 cooling Methods 0.000 description 15
- AKEJUJNQAAGONA-UHFFFAOYSA-N Sulfur trioxide Chemical compound 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O=S(=O)=O AKEJUJNQAAGONA-UHFFFAOYSA-N 0.000 description 14
- MWUXSHHQAYIFBG-UHFFFAOYSA-N nitric oxide Inorganic materials 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- 239000002002 slurry Substances 0.000 description 3
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound 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- 230000002745 absorbent Effects 0.000 description 2
- 238000010521 absorption reaction Methods 0.000 description 2
- 239000000443 aerosol Substances 0.000 description 2
- 230000002079 cooperative Effects 0.000 description 2
- 238000004134 energy conservation Methods 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- GQPLMRYTRLFLPF-UHFFFAOYSA-N nitrous Oxide Chemical compound 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[O-][N+]#N GQPLMRYTRLFLPF-UHFFFAOYSA-N 0.000 description 2
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- NINIDFKCEFEMDL-UHFFFAOYSA-N sulfur Chemical compound 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- 239000011593 sulfur Substances 0.000 description 1
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Abstract
本实用新型公开了一种湿法脱硫烟气处理机构，旨在解决现有的脱硫烟气处理后经烟囱排入大气易形成“白烟”现象，同时湿式电除尘消耗电功率消耗大，投资、运行费用高的不足。该实用新型包括沿着烟气流动方向依次设置的静电除尘器、湿法脱硫塔、湿式相变冷凝除尘器、烟囱，静电除尘器和湿法脱硫塔之间安装有引风机，湿式相变冷凝除尘器下端设有排液口，排液口通过管道连接到湿法脱硫塔上。脱硫烟气处理后经烟囱排入大气不易形成“白烟”现象，整个处理系统功耗低，降低了投资、运行费用，处理系统能够有效回收工业用水。
Description
技术领域
[0001] 本实用新型涉及一种烟气处理技术，更具体地说，它涉及一种高效的湿法脱硫烟气处理机构。
背景技术
[0002] 锅炉及各类炉窑内燃料燃烧后将产生大量的携带粉尘、二氧化硫、氮氧化物的烟气，为实现清洁达标排放，目前一般对氮氧化物采用SCR脱硝、对粉尘采用静电、布袋等除尘、对二氧化硫采用湿法脱硫处理。高温含硫烟气进入湿法脱硫吸收塔时，与吸收剂浆液反应，并释放大量的热，同时被吸收剂浆液冷却到50摄氏度左右，吸收塔浆液中的大量水分蒸发成水蒸汽，随烟气经烟囱排入大气后形成“白烟”现象，同时湿式电除尘消耗电功率消耗大，湿式电除尘投资、运行费用高。
[0003] 中国专利公告号CN103861419A，公开了一种湿法脱硫烟气综合处理方法，将脱硫后烟气的温度进行降温处理，在喷淋塔出口，降温用循环水和从烟气中冷凝下来的回收水分构成降温后热水，利用热栗系统将降温后热水冷却，同时热栗系统加热热网的回水或是电厂冷凝水；降温热水由热栗冷却后的水部分用作降温用循环水，部分用作回收水；回收水部分用作脱硫系统的用水或部分外供；从喷淋降温塔降温后的烟气，通过湿式静电除尘器，脱除脱硫后烟气中的PM2.5颗粒、硫酸雾。实现燃煤电厂的节水、节能及污染物的终端把关。但是处理后的烟气经烟囱排入大气后形成“白烟”现象，同时湿式电除尘消耗电功率消耗大，投资、运行费用高。
实用新型内容
[0004] 本实用新型克服了现有的脱硫烟气处理后经烟囱排入大气易形成“白烟”现象，同时湿式电除尘消耗电功率消耗大，投资、运行费用高的不足，提供了一种湿法脱硫烟气处理机构，脱硫烟气处理后经烟囱排入大气不易形成“白烟”现象，整个处理系统功耗低，降低了投资、运行费用，处理系统能够有效回收工业用水。
[0005] 为了解决上述技术问题，本实用新型采用以下技术方案:一种湿法脱硫烟气处理机构，包括沿着烟气流动方向依次设置的静电除尘器、湿法脱硫塔、湿式相变冷凝除尘器、烟囱，静电除尘器和湿法脱硫塔之间安装有引风机，湿式相变冷凝除尘器下端设有排液口，排液口通过管道连接到湿法脱硫塔上。
[0006] 烟气处理时先经过静电除尘器，去除烟气中99%以上的粉尘，温度基本保持不变；随后烟气进入湿法脱硫塔中进行脱硫处理，去除90%以上的二氧化硫，温度降低至50摄氏度左右，形成湿饱和状态的烟气；之后烟气进入湿式相变冷凝除尘器中，烟气进一步冷却至40摄氏度左右，在烟气冷却过程中，烟气仍处于湿饱和状态，烟气中水分被大量冷凝下来，同时烟气中粉尘被进一步清除，粉尘等污染物去除率到80%以上，冷凝水回收利用到湿法脱硫塔中；在去除烟气中的大量水份的过程，协同去除烟气中三氧化硫，三氧化硫除着回收水重新回到脱硫塔中二次循环吸收，有利于减少烟气排放中的三氧化硫。最后烟气从烟囱排出。湿式相变冷凝除尘器将烟气温度降低到40摄氏度以下，烟气在冷却过程中，烟气中的水分可大量凝结，在凝结过程中，烟气中的粉尘、气溶胶以及其他溶于水的物质被水滴吸收，随水分被清除，平均除尘效率大于80%，除尘效率高，保证了粉尘的达标排放，又省去了湿式电除尘装置的投资，降低了投资成本，缩短了工作流程，烟气降温后流量及阻力减小，使整个处理系统的耗电量显著减少，实现了节能减排的协同效应。脱硫烟气处理后含水量大幅降低，经烟囱排入大气不易形成浓浓的“白烟”现象，整个系统功耗低，降低了投资、运行费用，处理系统能够有效回收工业用水。。
[0007] 作为优选，还包括管式换热器，管式换热器包括降温段和升温段，管式换热器的降温段设置在静电除尘器的前端，管式换热器的升温段设置在湿式相变冷凝除尘器的后端，管式换热器的降温段和升温段之间连接循环栗。
[0008] 经过湿式相变冷凝除尘器后的烟气绝对湿度大幅减少，烟气经过管式换热器的升温段再加热后温度为50-65摄氏度左右，烟气中的水蒸气分压小于该温度对应的水蒸气饱和分压，水蒸气烟气以较低的温度、较小的相对湿度排放，有效防止烟囱出口烟气在空气中冷却时产生二次凝露过程，消除烟囱冒白汽及“烟囱雨”现象，消除视觉污染。管式换热器的降温段将烟气从130摄氏度左右降低到90-110摄氏度左右，烟气中的热量被管式换热器内的循环水吸收，由循环栗输送至管式换热器的升温段。
[0009] 另一种方案，还包括管式换热器，管式换热器包括降温段和升温段，管式换热器的降温段设置在静电除尘器和引风机之间，管式换热器的升温段设置在湿式相变冷凝除尘器的后端，管式换热器的降温段和升温段之间连接循环栗。
[0010] 烟气经过静电除尘器去除99%以上的粉尘后再通过管式换热器的降温段进行降温，大大减少了管式换热器外壁粉尘的沉积，保证了管式换热器的换热效果，延长使用寿命ο
[0011] 作为优选，引风机和湿法脱硫塔之间设置有前级湿式相变冷凝除尘器，前级湿式相变冷凝除尘器下端设有出液口，出液口通过管道连接到湿法脱硫塔上。前级湿式相变冷凝除尘器和湿式相变冷凝除尘器均对烟气中的水分和粉尘进行冷凝清除，烟气通过两级的水分和粉尘冷凝清除，效果更加明显。
[0012] 作为优选，湿式相变冷凝除尘器和前级湿式相变冷凝除尘器下端均设有集液斗，排液口和出液口分别设置在两集液斗下端。集液斗便于冷凝水的收集和排放。
[0013] 与现有技术相比，本实用新型的有益效果是:(1)脱硫烟气处理后经烟囱排入大气不易形成“白烟”现象，整个系统功耗低，降低了投资、运行费用，处理系统能够有效回收工业用水；(2)湿式相变冷凝除尘器使烟气在冷却过程中，烟气中的水分可大量凝结，在凝结过程中，烟气中粉尘、气溶胶、三氧化硫以及其他溶于水的物质被水滴吸附，随水分被去除，平均除尘效率大于80%，既保证了粉尘的达标排放，又可以省去湿式电除尘的投资，降低了项目投资，缩短了工作流程、烟气降温后流量及阻力减少，使整个处理系统的耗电量显著减少，实现了节能与减排的协同效应；(3)在低烟气温度、低环境温度下，经烟尘排出的烟气温度低，减少或不需在管式换热器中增加外部热源辅助加热，节能效益显著。
附图说明
[0014] 图1是本实用新型的实施例1的结构示意图；
[0015] 图2是本实用新型的实施例2的结构示意图；
[0016] 图3是本实用新型的实施例3的结构示意图；
[0017] 图中:1、静电除尘器，2、湿法脱硫塔，3、湿式相变冷凝除尘器，4、烟囱，5、引风机，
6、排液口，7、管式换热器，8、降温段，9、升温段，10、循环栗，11、前级湿式相变冷凝除尘器，12、出液口，13、集液斗。
具体实施方式
[0018] 下面通过具体实施例，并结合附图，对本实用新型的技术方案作进一步的具体描述:
[0019] 实施例1:一种湿法脱硫烟气处理机构(参见附图1)，包括沿着烟气流动方向依次设置的静电除尘器1、湿法脱硫塔2、湿式相变冷凝除尘器3、烟囱4，静电除尘器和湿法脱硫塔之间安装有引风机5，湿式相变冷凝除尘器下端设有排液口 6，湿式相变冷凝除尘器下端设有集液斗13，排液口设置在集液斗下端，排液口通过管道连接到湿法脱硫塔上；湿式相变冷凝除尘器内设有冷凝管，冷凝管一端连接有循环进液管，冷凝管另一端连接有循环出液管，循环进液管和循环出液管均延伸到湿式相变冷凝除尘器外部。还包括管式换热器7，管式换热器包括降温段8和升温段9，管式换热器的降温段设置在静电除尘器的前端，管式换热器的升温段设置在湿式相变冷凝除尘器的后端，管式换热器的降温段和升温段之间连接循环栗10，通过循环栗使管式换热器的降温段和升温段之间的液体循环使用。
[0020] 燃烧产生的烟气中含有粉尘、二氧化硫、氮氧化物等污染。烟气处理时先进入管式换热器的降温段，将烟气从130摄氏度左右降低到90-110摄氏度左右，烟气中的热量被管式换热器内的循环水吸收，由循环栗输送到管式换热器的升温段。然后烟气经过静电除尘器，去除烟气中99%以上的粉尘，温度基本保持不变；随后烟气进入湿法脱硫塔中进行脱硫处理，去除90%以上的二氧化硫，温度降低至50摄氏度左右，形成湿饱和状态的烟气，水分含量约为0.039千克/立方米；之后烟气进入湿式相变冷凝除尘器中，烟气进一步冷却至40摄氏度左右，在烟气冷却过程中，烟气仍处于湿饱和状态，水分含量约为0.026千克/立方米，烟气中水分被大量冷凝下来，每台600MW发电机组满负荷每小时可冷凝约80-100吨水，每台1000MW发电机组满负荷每小时可冷凝约100-150吨水。同时烟气中粉尘、三氧化硫等被进一步清除，粉尘污染物去除率到80%以上，冷凝水回收利用到湿法脱硫塔中；从湿式相变冷凝除尘器排出的烟气经过管式换热器升温段进行升温，将烟气温度升高至50-65摄氏度左右，最后通过烟囱排出。
[0021] 实施例2:—种湿法脱硫烟气处理机构(参见附图2)，包括沿着烟气流动方向依次设置的静电除尘器1、湿法脱硫塔2、湿式相变冷凝除尘器3、烟囱4，静电除尘器和湿法脱硫塔之间安装有引风机5，湿式相变冷凝除尘器下端设有排液口 6，湿式相变冷凝除尘器下端设有集液斗13，排液口设置在集液斗下端，排液口通过管道连接到湿法脱硫塔上；湿式相变冷凝除尘器内设有冷凝管，冷凝管一端连接有循环进液管，冷凝管另一端连接有循环出液管，循环进液管和循环出液管均延伸到湿式相变冷凝除尘器外部。还包括管式换热器，管式换热器包括降温段和升温段，管式换热器的降温段设置在静电除尘器和引风机之间，管式换热器的升温段设置在湿式相变冷凝除尘器的后端，管式换热器的降温段和升温段之间连接循环栗，通过循环栗使管式换热器的降温段和升温段之间的液体循环使用。
[0022] 燃烧产生的烟气中含有粉尘、二氧化硫、氮氧化物等污染。烟气先经过静电除尘器，去除烟气中99%以上的粉尘，温度基本保持不变；然后进入管式换热器的降温段，将烟气从130摄氏度左右降低到90-110摄氏度左右，烟气中的热量被管式换热器内的循环水吸收，由循环栗输送到管式换热器的升温段。随后烟气进入湿法脱硫塔中进行脱硫处理，去除90%以上的二氧化硫，温度降低至50摄氏度左右，形成湿饱和状态的烟气，水分含量约为0.039千克/立方米；之后烟气进入湿式相变冷凝除尘器中，烟气进一步冷却至40摄氏度左右，在烟气冷却过程中，烟气仍处于湿饱和状态，水分含量约为0.026千克/立方米，烟气中水分被大量冷凝下来，每台600MW发电机组满负荷每小时可冷凝约80-100吨水，每台1000丽发电机组满负荷每小时可冷凝约100-150吨水。同时烟气中粉尘、三氧化硫等污染物被进一步清除，其中粉尘污染物去除率到80%以上，冷凝水回收利用到湿法脱硫塔中；从湿式相变冷凝除尘器排出的烟气经过管式换热器升温段进行升温，将烟气温度升高至50-65摄氏度左右，最后通过烟囱排出。
[0023] 实施例3:—种湿法脱硫烟气处理机构(参见附图3)，包括沿着烟气流动方向依次设置的静电除尘器1、湿法脱硫塔2、湿式相变冷凝除尘器3、烟囱4，静电除尘器和湿法脱硫塔之间安装有引风机5，湿式相变冷凝除尘器下端设有排液口 6，排液口设置在集液斗下端，排液口通过管道连接到湿法脱硫塔上；湿式相变冷凝除尘器内设有冷凝管，冷凝管一端连接有循环进液管，冷凝管另一端连接有循环出液管，循环进液管和循环出液管均延伸到湿式相变冷凝除尘器外部。还包括管式换热器7，管式换热器包括降温段8和升温段9，管式换热器的降温段设置在静电除尘器的前端，管式换热器的升温段设置在湿式相变冷凝除尘器的后端，管式换热器的降温段和升温段之间连接循环栗10，通过循环栗使管式换热器的降温段和升温段之间的液体循环使用。引风机和湿法脱硫塔之间设置有前级湿式相变冷凝除尘器11，前级湿式相变冷凝除尘器下端设有出液口 12，出液口通过管道连接到湿法脱硫塔上。湿式相变冷凝除尘器和前级湿式相变冷凝除尘器下端均设有集液斗13，排液口和出液口分别设置在两集液斗下端。
[0024] 燃烧产生的烟气中含有粉尘、二氧化硫、氮氧化物等污染。烟气处理时先进入管式换热器的降温段，将烟气从130摄氏度左右降低到90摄氏度左右，烟气中的热量被管式换热器内的循环水吸收，由循环栗输送到管式换热器的升温段。然后烟气经过静电除尘器，去除烟气中99%以上的粉尘，温度基本保持不变；之后烟气进入前级湿式相变冷凝除尘器进行前级冷凝除尘，冷凝水回收利用到湿法脱硫塔中，烟气冷却至35摄氏度左右；随后烟气进入湿法脱硫塔中进行脱硫处理，去除90%以上的二氧化硫，温度到达36-37摄氏度左右，形成湿饱和状态的烟气，水分含量约为0.021千克/立方米；之后烟气进入湿式相变冷凝除尘器中，烟气进一步冷却至30摄氏度左右，在烟气冷却过程中，烟气仍处于湿饱和状态，水分含量约为0.015千克/立方米，烟气中水分被大量冷凝下来，每台600MW发电机组满负荷每小时可冷凝约40-60吨水，每台1000MW发电机组满负荷每小时可冷凝约50-80吨水。同时烟气中粉尘、三氧化硫等污染物被进一步清除，其中粉尘污染物去除率到80%以上，冷凝水回收利用到湿法脱硫塔中；从湿式相变冷凝除尘器排出的烟气经过管式换热器升温段进行升温，将烟气温度升高至50-65摄氏度左右，最后通过烟囱排出。
[0025] 以上所述的实施例只是本实用新型的三种较佳的方案，并非对本实用新型作任何形式上的限制，在不超出权利要求所记载的技术方案的前提下还有其它的变体及改型。
Claims (5)
1.一种湿法脱硫烟气处理机构，其特征是，包括沿着烟气流动方向依次设置的静电除尘器、湿法脱硫塔、湿式相变冷凝除尘器、烟囱，静电除尘器和湿法脱硫塔之间安装有引风机，湿式相变冷凝除尘器下端设有排液口，排液口通过管道连接到湿法脱硫塔上。
2.根据权利要求1所述的湿法脱硫烟气处理机构，其特征是，还包括管式换热器，管式换热器包括降温段和升温段，管式换热器的降温段设置在静电除尘器的前端，管式换热器的升温段设置在湿式相变冷凝除尘器的后端，管式换热器的降温段和升温段之间连接循环栗Ο
3.根据权利要求1所述的湿法脱硫烟气处理机构，其特征是，还包括管式换热器，管式换热器包括降温段和升温段，管式换热器的降温段设置在静电除尘器和引风机之间，管式换热器的升温段设置在湿式相变冷凝除尘器的后端，管式换热器的降温段和升温段之间连接循环栗。
4.根据权利要求1或2或3所述的湿法脱硫烟气处理机构，其特征是，引风机和湿法脱硫塔之间设置有前级湿式相变冷凝除尘器，前级湿式相变冷凝除尘器下端设有出液口，出液口通过管道连接到湿法脱硫塔上。
5.根据权利要求4所述的湿法脱硫烟气处理机构，其特征是，湿式相变冷凝除尘器和前级湿式相变冷凝除尘器下端均设有集液斗，排液口和出液口分别设置在两集液斗下端。
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| CN105688582A (zh) * | 2016-04-07 | 2016-06-22 | 国电环境保护研究院 | 一种凝变湿电复合烟气净化工艺 |
| CN105709573A (zh) * | 2016-03-01 | 2016-06-29 | 上海锅炉厂有限公司 | 冷凝法烟气水回收消白烟系统 |
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| CN109432936A (zh) * | 2018-12-04 | 2019-03-08 | 中冶南方都市环保工程技术股份有限公司 | 烧结烟气处理方法及处理系统 |
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| CN108981416A (zh) * | 2018-08-07 | 2018-12-11 | 中国能源建设集团广东省电力设计研究院有限公司 | 洗涤塔尾气降温装置及气体净化系统 |
| CN108981416B (zh) * | 2018-08-07 | 2020-10-09 | 中国能源建设集团广东省电力设计研究院有限公司 | 洗涤塔尾气降温装置及气体净化系统 |
| CN109432936A (zh) * | 2018-12-04 | 2019-03-08 | 中冶南方都市环保工程技术股份有限公司 | 烧结烟气处理方法及处理系统 |
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