化工进展 ›› 2024, Vol. 43 ›› Issue (5): 2324-2342.DOI: 10.16085/j.issn.1000-6613.2023-1945
• 化石能源的清洁高效转化利用 • 上一篇
高凡翔1(), 刘阳1, 张贵泉2, 秦锋3, 姚建涛2, 金辉1, 师进文1()
收稿日期:
2023-11-06
修回日期:
2024-03-14
出版日期:
2024-05-15
发布日期:
2024-06-15
通讯作者:
师进文
作者简介:
高凡翔(2000—),男,硕士研究生,研究方向为碳捕集和利用。E-mail:gfx2284217583@stu.xjtu.edu.cn。
基金资助:
GAO Fanxiang1(), LIU Yang1, ZHANG Guiquan2, QIN Feng3, YAO Jiantao2, JIN Hui1, SHI Jinwen1()
Received:
2023-11-06
Revised:
2024-03-14
Online:
2024-05-15
Published:
2024-06-15
Contact:
SHI Jinwen
摘要:
燃煤烟气中SO2和CO2的处理逐渐向协同脱除方向发展,基于湿法脱硫和脱碳的组合技术因此获得了广泛关注。本文首先系统梳理了梯级(依次)脱硫脱碳技术的重点研究方向,认为SO2的胺降解作用是该类技术面对的核心问题,但其影响机理尚未形成统一共识。从控制排放和预防降解两个角度出发,分析了强化脱硫技术和胺降解抑制剂对缓解SO2不利影响的作用。与梯级处理相比,联合(同步)脱硫脱碳技术可基于单一溶剂实现循环吸收-解吸。然后总结了钙法、氨法、胺法等联合脱硫脱碳(联脱)技术的最新进展,梳理并对比了各类吸收体系的原理和工艺设计,其中基于氨水的联脱工艺研究最为成熟。还简述了两类协同脱除技术的优缺点和发展前景。最后,建议对于梯级脱硫脱碳技术未来应重点关注SO2的胺降解机理及其在开发预防降解措施中的作用,对于联脱技术应加强反应理论和集成工艺建模研究等。
中图分类号:
高凡翔, 刘阳, 张贵泉, 秦锋, 姚建涛, 金辉, 师进文. 燃煤烟气湿法协同脱硫脱碳技术研究进展[J]. 化工进展, 2024, 43(5): 2324-2342.
GAO Fanxiang, LIU Yang, ZHANG Guiquan, QIN Feng, YAO Jiantao, JIN Hui, SHI Jinwen. Research progress of wet process synergistic desulfurization and decarbonization technology for coal-fired flue gas[J]. Chemical Industry and Engineering Progress, 2024, 43(5): 2324-2342.
改造类型 | 改造项目或地点 | 改造方案 | SO2排放浓度(标准)/mg·m-3 | 脱硫效率/% | 完工时间 /年 | ||
---|---|---|---|---|---|---|---|
改造前 | 改造后 | 改造前 | 改造后 | ||||
喷淋层 | 攀枝花某企业小型锅炉[ | 增设一层冲洗水层,缩短喷嘴与除雾器间距,优化冲洗水管及相关配套设施等 | 78~126 | 98.5~99.0 | 2016 | ||
魏家峁电厂[ | 采用一层旋流和三层喷淋,增加每层喷淋喷嘴数等 | 130 | <23 | >95 | >99 | 2017 | |
托盘塔 | 某660MW超临界燃煤 机组[ | 采用双托盘,拆除回转式烟气换热器(GGH),增加液气比等 | 111 | <35 | 91.5~92.5 | 2012 | |
华能集团滇东电厂3号和4号机组[ | 采用双托盘,增设喷淋层,拆除GGH,布置3级高效屋脊式除雾器及冲洗水系统等 | — | <35 | — | — | 2018 | |
单塔双区 | 某公司二期630MW电厂[ | 对吸收塔两段环切加高,优化改进配套设备等 | 100 | 96 | 2018 | ||
单塔双循环 | 山西某超低排放项目[ | 升级原塔,新建塔外循环塔和配套的浆液循环泵等 | <35 | 2015 | |||
某1000MW燃煤电厂[ | 拆除原塔并建新塔和一座循环浆液槽 | 100~175 | 95 | 2016 | |||
双塔双循环 | 大唐集团河北某600MW发电厂[ | 新建一级吸收塔与原吸收塔(二级)串联 | 110~170 | <35 | 95 | >99 | 2014 |
国电谏壁发电厂8号机组[ | 利用7号机组旧塔与8号机组旧塔组合形成双塔双循环 | >50 | 22.43 | 95 | >99.3 | 2014 | |
任丘2×300MW燃煤电厂[ | 新建二级吸收塔与原吸收塔(一级)串联 | 163.49 | 20.65 | 93.07 | 99.47 | 2018 | |
某350MW燃煤电厂[ | 新建二级吸收塔与原吸收塔(一级)串联 | 107 | 27 | 96.5 | 99.3 | 2018 | |
华能集团滇东电厂1号和2号机组[ | 新建二级吸收塔与原吸收塔(一级)串联 | <35 | — | 99.53 | 2018 | ||
其他 | 宁夏某2×350MW燃煤 电厂[ | 增大塔壁板高度,增加喷淋层,扩大浆池容积等 | >50 | 35 | >98.675 | >99.08 | 2020 |
某3×50MW抽凝式发电 机组[ | 新建塔形成“一炉一塔”,原塔新增脱硫增效协同除尘设置,改用三级屋脊式高效除雾器及冲洗水系统等 | 89.6 | 9.7 | — | 98.8~99.7 | 2022 | |
某2×600MW燃煤电厂[ | 新增浆液再循环装置,差异化布置喷嘴,升级除雾器等 | > 45 | <35 | — | >95 | 2022 | |
兰州石化公司燃煤锅炉[ | 新建塔形成“一炉一塔”,原塔喷淋层增设湍流器和偏转环 | — | 99 | 2023 |
表1 燃煤电厂石灰石/石膏湿法FGD系统超低排放改造项目
改造类型 | 改造项目或地点 | 改造方案 | SO2排放浓度(标准)/mg·m-3 | 脱硫效率/% | 完工时间 /年 | ||
---|---|---|---|---|---|---|---|
改造前 | 改造后 | 改造前 | 改造后 | ||||
喷淋层 | 攀枝花某企业小型锅炉[ | 增设一层冲洗水层,缩短喷嘴与除雾器间距,优化冲洗水管及相关配套设施等 | 78~126 | 98.5~99.0 | 2016 | ||
魏家峁电厂[ | 采用一层旋流和三层喷淋,增加每层喷淋喷嘴数等 | 130 | <23 | >95 | >99 | 2017 | |
托盘塔 | 某660MW超临界燃煤 机组[ | 采用双托盘,拆除回转式烟气换热器(GGH),增加液气比等 | 111 | <35 | 91.5~92.5 | 2012 | |
华能集团滇东电厂3号和4号机组[ | 采用双托盘,增设喷淋层,拆除GGH,布置3级高效屋脊式除雾器及冲洗水系统等 | — | <35 | — | — | 2018 | |
单塔双区 | 某公司二期630MW电厂[ | 对吸收塔两段环切加高,优化改进配套设备等 | 100 | 96 | 2018 | ||
单塔双循环 | 山西某超低排放项目[ | 升级原塔,新建塔外循环塔和配套的浆液循环泵等 | <35 | 2015 | |||
某1000MW燃煤电厂[ | 拆除原塔并建新塔和一座循环浆液槽 | 100~175 | 95 | 2016 | |||
双塔双循环 | 大唐集团河北某600MW发电厂[ | 新建一级吸收塔与原吸收塔(二级)串联 | 110~170 | <35 | 95 | >99 | 2014 |
国电谏壁发电厂8号机组[ | 利用7号机组旧塔与8号机组旧塔组合形成双塔双循环 | >50 | 22.43 | 95 | >99.3 | 2014 | |
任丘2×300MW燃煤电厂[ | 新建二级吸收塔与原吸收塔(一级)串联 | 163.49 | 20.65 | 93.07 | 99.47 | 2018 | |
某350MW燃煤电厂[ | 新建二级吸收塔与原吸收塔(一级)串联 | 107 | 27 | 96.5 | 99.3 | 2018 | |
华能集团滇东电厂1号和2号机组[ | 新建二级吸收塔与原吸收塔(一级)串联 | <35 | — | 99.53 | 2018 | ||
其他 | 宁夏某2×350MW燃煤 电厂[ | 增大塔壁板高度,增加喷淋层,扩大浆池容积等 | >50 | 35 | >98.675 | >99.08 | 2020 |
某3×50MW抽凝式发电 机组[ | 新建塔形成“一炉一塔”,原塔新增脱硫增效协同除尘设置,改用三级屋脊式高效除雾器及冲洗水系统等 | 89.6 | 9.7 | — | 98.8~99.7 | 2022 | |
某2×600MW燃煤电厂[ | 新增浆液再循环装置,差异化布置喷嘴,升级除雾器等 | > 45 | <35 | — | >95 | 2022 | |
兰州石化公司燃煤锅炉[ | 新建塔形成“一炉一塔”,原塔喷淋层增设湍流器和偏转环 | — | 99 | 2023 |
地点 | 名称 | 规模 | 溶剂类型 | 能耗/GJ·t-1 | 时间/年 |
---|---|---|---|---|---|
美国 | Warrior Run示范项目 | 150t/d | MEA | — | 2000 |
Petro Nova碳捕集项目 | 1.4×106t/a | KS-1 | 2.4 | 2017 | |
德国 | Staudinger电站中试项目 | — | 氨基酸 | 2.7 | 2009 |
Wilhelmshaven电站中试项目 | 70t/d | 二甘醇胺 | 2.7 | 2012 | |
加拿大 | Boundary Dam项目 | 1×106t/a | MEA | — | 2014 |
澳大利亚 | Hazelwood电站中试项目 | 1t/d | 碳酸钾 | 2.5 | 2011 |
中国 | 华能北京热电厂中试项目 | 3000t/a | MEA | — | 2008 |
华能上海石洞口示范项目 | 1.2×105t/a | MEA | 3 | 2009 | |
胜利发电厂100t/a CO2捕集纯化工程 | 100t/d | 新型MSA复合吸收剂 | 5.95 | 2012 | |
长春热电厂相变型碳捕集工业装置 | 1000t/a | 相变吸收剂 | 2.3 | 2020 | |
国能锦界1.5×105t/a CCUS示范项目 | 1.5×105t/a | 复合胺(多氨基胺及位阻胺) | 2.4 | 2021 | |
齐鲁石化-胜利油田百万吨级CCUS项目 | 1t/a | 新型MSA复合吸收剂 | — | 2022 |
表2 国内外运行中的燃煤烟气CCUS项目
地点 | 名称 | 规模 | 溶剂类型 | 能耗/GJ·t-1 | 时间/年 |
---|---|---|---|---|---|
美国 | Warrior Run示范项目 | 150t/d | MEA | — | 2000 |
Petro Nova碳捕集项目 | 1.4×106t/a | KS-1 | 2.4 | 2017 | |
德国 | Staudinger电站中试项目 | — | 氨基酸 | 2.7 | 2009 |
Wilhelmshaven电站中试项目 | 70t/d | 二甘醇胺 | 2.7 | 2012 | |
加拿大 | Boundary Dam项目 | 1×106t/a | MEA | — | 2014 |
澳大利亚 | Hazelwood电站中试项目 | 1t/d | 碳酸钾 | 2.5 | 2011 |
中国 | 华能北京热电厂中试项目 | 3000t/a | MEA | — | 2008 |
华能上海石洞口示范项目 | 1.2×105t/a | MEA | 3 | 2009 | |
胜利发电厂100t/a CO2捕集纯化工程 | 100t/d | 新型MSA复合吸收剂 | 5.95 | 2012 | |
长春热电厂相变型碳捕集工业装置 | 1000t/a | 相变吸收剂 | 2.3 | 2020 | |
国能锦界1.5×105t/a CCUS示范项目 | 1.5×105t/a | 复合胺(多氨基胺及位阻胺) | 2.4 | 2021 | |
齐鲁石化-胜利油田百万吨级CCUS项目 | 1t/a | 新型MSA复合吸收剂 | — | 2022 |
技术类型 | 优点 | 缺点 |
---|---|---|
梯级脱硫脱碳技术 | 1.技术成熟,工程经验丰富 | 1.占地空间大,不易维护 |
2.易于在已有电站改造(无论是否有FGD系统) | 2.能耗高 | |
3.脱硫和脱碳系统便于各自调控实现高脱除率 | 3.烟气成分对脱碳剂的影响大 | |
联合脱硫脱碳技术 | 1.节能潜力大 | 1.技术不成熟,工程经验极少 |
2.占地空间小,运行维护方便 | 2.不适合已有FGD系统的电站改造 | |
3.单一吸收剂的用量更大,使吸收效率受影响,设备更易腐蚀、胺损耗更严重等 |
表3 不同协同脱硫脱碳技术的对比
技术类型 | 优点 | 缺点 |
---|---|---|
梯级脱硫脱碳技术 | 1.技术成熟,工程经验丰富 | 1.占地空间大,不易维护 |
2.易于在已有电站改造(无论是否有FGD系统) | 2.能耗高 | |
3.脱硫和脱碳系统便于各自调控实现高脱除率 | 3.烟气成分对脱碳剂的影响大 | |
联合脱硫脱碳技术 | 1.节能潜力大 | 1.技术不成熟,工程经验极少 |
2.占地空间小,运行维护方便 | 2.不适合已有FGD系统的电站改造 | |
3.单一吸收剂的用量更大,使吸收效率受影响,设备更易腐蚀、胺损耗更严重等 |
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