CN107349750A - 一种针对高硫煤燃煤电厂尾气so2的深度脱除及资源化利用的工艺 - Google Patents
一种针对高硫煤燃煤电厂尾气so2的深度脱除及资源化利用的工艺 Download PDFInfo
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Abstract
本发明一种针对高硫煤燃煤电厂尾气SO2的深度脱除及资源化利用的工艺,利用Na2SO3吸收烟气里的二氧化硫,不但实现了吸收剂的完全循环利用,还实现了二氧化硫的资源化利用及高附加值产品的生产。本工艺解决了现有湿法脱硫含盐废水多、易堵塞、吸收效果差等一系列的问题,同时也实现了二氧化硫的深度脱除(二氧化硫含量<35mg/m3),固体颗粒物的高度脱除(固体颗粒物<5ppm)以及二氧化碳回收率可达50%‑60%。经过回收得到的SO2经过提纯,获得符合生产氯化亚砜的高纯度,获得纯度99.6%的氯化亚砜。
Description
技术领域
本发明属于化工生产工艺领域,具体涉及一种针对高硫煤燃煤电厂尾气中二氧化硫的深度脱除及资源化利用工艺的开发。
背景技术
我国能源消费中煤的使用占60%,SO2的污染排放更是有着80%来自燃煤。因此,在现如今绿色化工、节能环保的大背景下,对烟气中二氧化硫做到深度脱除并且实现资源化利用将成为重中之重。虽然我国煤矿资源丰富而且多为低硫煤,但是煤作为一种不可再生资源,开采利用高硫煤必然会来临。
戴文军、任龙【1】对现有烟气脱硫技术进行研究,研究表明:我国现现采用的脱硫技术存在着吸收剂难以实现循环、吸收设备堵塞、烟气脱硫率低、二氧化硫难以实现资源化、烟气碳排放高等一系列问题。蒋利桥、陈恩鉴【2】也研究表明现有脱硫技术存在副产品难处理的问题。
针对现有研究结果,本专利采用回亚硫酸钠回收方法来治理锅炉二氧化硫污染,同时从中获取二氧化硫作为产品来作为氯化亚砜生产的原料。对于净化的烟气进一步处理实现低碳排放。
对回收型吸收剂的要求有:
①单位容积吸收剂吸收二氧化硫的能力较大;
②能够用加热的方法逐出其中的二氧化硫;
③吸收剂本身蒸气压小;
④吸收剂反复加热后,吸收二氧化硫的能力不会退化;
⑤在吸收过程中,二氧化硫被氧化成硫酸盐的份额要小,同时又要易于将硫酸盐从吸收
液中分离出来。
符合上述要求的吸收剂并不多。NH3是一种选择,但是其在吸收过程中产生不但会产生雾化而造成二次污染,而且所产生的副产物硫酸铵的销路也成为问题,所以其在经济上是行不通的。
本专利采用Na2SO3作为吸收剂生成NaHSO3然后加热分解回收SO2,解析后的Na2SO3返回***再次作为吸收剂,如此往复,解决了现有湿法脱硫含盐废水排放大的问题。回收得到的SO2去制备氯化亚砜实现资源化。
发明内容
本发明在于提供一种针对高硫煤燃煤电厂尾气中二氧化硫的深度脱除及资源化利用的工艺。以Na2SO3作为吸收剂生成NaHSO3然后加热分解回收SO2,解析后的Na2SO3返回***再次作为吸收剂,如此往复。回收得到的SO2去制备氯化亚砜。
一种针对高硫煤燃煤电厂尾气中二氧化硫的深度脱除及资源化利用的工艺,包括如下步骤:
1、将来自锅炉的烟气首先通过静电除尘,文丘里洗涤器洗涤,出去其中氟化物、氯化物、 SO3以及大部分的固体颗粒物。
2、将步骤1处理过的烟气送入填料吸收塔,控制吸收剂与烟气的比为0.2:1,pH为5~7,温度在55℃。
3、将步骤2净化的烟气通过聚乙二醇二甲醚的吸附,脱除回收大部分的CO2,控制吸收温度在-15℃-10℃。
4、将步骤2获得的吸收液按照3:7,一部分送去结晶回收副产物Na2SO4,另一部分送去解析获得SO2,并回收吸收剂Na2SO3。回收得到的SO2经过浅低温精馏塔等处理纯度高达99.9%。
5、硫磺和氯气在反应釜中反应产生的合成气与步骤4获得SO2气体与一起进入反应器,经过反应生成的气相进入反应精馏后被脱色。
6、步骤5获得的脱色气进入二级变压精馏塔得到产品氯化亚砜。
本发明有益效果:
本发明利用Na2SO3吸收烟气里的二氧化硫,不但实现了吸收剂的完全循环利用,还实现了二氧化硫的资源化利用及高附加值产品的生产。本工艺解决了现有湿法脱硫含盐废水多、易堵塞、吸收效果差等一系列的问题,同时也实现了二氧化硫的深度脱除(二氧化硫含量< 35mg/m3),固体颗粒物的高度脱除(固体颗粒物<5ppm)以及二氧化碳回收率可达50%-60%。经过回收得到的SO2经过提纯,获得符合生产氯化亚砜的高纯度。
附图说明
图1是二氧化硫吸收及吸收剂回收流程图。
1.二氧化硫吸收塔 2.结晶器 3.蒸发器 4.二氧化塔吸附塔 5.贫液再生罐
图2是二氧化硫提纯流程图。
1.二氧化硫干燥塔 2.压缩机 3.浅低温精馏塔 4.回流罐
图3是氯化亚砜生产流程图。
1.一级反应器 2.二级反应器 3.三级反应器 4.反应精馏塔 5.隔壁塔
具体实施方式
实施例1
1、来自锅炉的烟气一次通过静电除尘器、文丘里洗涤器,使最终进入吸收塔的温度达到 60℃。
2、烟气进入填料吸收塔,选择塑料板波纹规整填料,吸收剂用13%的亚硫酸钠溶液,保持吸收剂的量与烟气体积比为0.2:1。
实施例2
1、来自锅炉的烟气一次通过静电除尘器、文丘里洗涤器,使最终进入吸收塔的温度达到 70℃。
2、烟气进入喷淋吸收塔,吸收剂用10%的亚硫酸钠溶液,保持吸收剂的量与烟气体积比为0.4:1。
实施例3
1、来自锅炉的烟气一次通过静电除尘器、文丘里洗涤器,使最终进入吸收塔的温度达到 80℃。
2、烟气进入筛板塔,吸收剂用15%的亚硫酸钠溶液,保持吸收剂的量与烟气体积比为0.3:1。
Claims (6)
1.将来自锅炉的烟气首先通过静电除尘,文丘里洗涤器洗涤,出去其中氟化物、氯化物、SO3以及大部分的固体颗粒物。
2.将步骤1处理过的烟气送入填料吸收塔,控制吸收剂与烟气的比为0.2:1,pH为5~7,温度在55℃。
3.将步骤2净化的烟气通过聚乙二醇二甲醚的吸附,脱除回收大部分的CO2,控制吸收温度在-15℃-10℃。
4.将步骤2获得的吸收液按照3:7,一部分送去结晶回收副产物Na2SO4,另一部分送去解析获得SO2,并回收吸收剂Na2SO3。回收得到的SO2经过浅低温精馏塔等处理纯度高达99.9%。
5.硫磺和氯气在反应釜中反应产生的合成气与步骤4获得SO2气体与一起进入反应器,经过反应生成的气相进入反应精馏后被脱色。
6.步骤5获得的脱色气进入二级变压精馏塔得到产品氯化亚砜。
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CN112680256B (zh) * | 2020-12-14 | 2022-06-14 | 长春东狮科技(集团)有限责任公司 | 一种高炉煤气湿法脱氯脱硫的装置和方法 |
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Application publication date: 20171117 |