CN102580431B - 烟气除尘、脱硫一体化工艺 - Google Patents
烟气除尘、脱硫一体化工艺 Download PDFInfo
- Publication number
- CN102580431B CN102580431B CN201110099028.1A CN201110099028A CN102580431B CN 102580431 B CN102580431 B CN 102580431B CN 201110099028 A CN201110099028 A CN 201110099028A CN 102580431 B CN102580431 B CN 102580431B
- Authority
- CN
- China
- Prior art keywords
- tower
- wet
- particle
- flue gas
- oxidation
- Prior art date
Links
- 238000000034 methods Methods 0.000 title claims abstract description 48
- 239000000779 smoke Substances 0.000 title abstract description 8
- 239000002245 particles Substances 0.000 claims abstract description 92
- 230000003647 oxidation Effects 0.000 claims abstract description 37
- 238000007254 oxidation reactions Methods 0.000 claims abstract description 37
- 239000007788 liquids Substances 0.000 claims abstract description 32
- 239000007787 solids Substances 0.000 claims abstract description 26
- UGFAIRIUMAVXCW-UHFFFAOYSA-N carbon monoxide Chemical compound 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[O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims description 71
- 239000003546 flue gases Substances 0.000 claims description 65
- 239000011901 water Substances 0.000 claims description 23
- 230000003009 desulfurizing Effects 0.000 claims description 19
- 239000000428 dust Substances 0.000 claims description 19
- LVGQIQHJMRUCRM-UHFFFAOYSA-L Calcium bisulfite Chemical compound 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[Ca+2].OS([O-])=O.OS([O-])=O LVGQIQHJMRUCRM-UHFFFAOYSA-L 0.000 claims description 17
- 235000010260 calcium hydrogen sulphite Nutrition 0.000 claims description 17
- 238000004062 sedimentation Methods 0.000 claims description 16
- 238000006477 desulfuration reactions Methods 0.000 claims description 15
- 239000007921 sprays Substances 0.000 claims description 15
- OKTJSMMVPCPJKN-UHFFFAOYSA-N carbon Chemical compound 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Abstract
烟气除尘脱硫一体化工艺是向大气环保领域提供一种烟气净化工艺技术和设备。工艺是由；湿法变相工艺(一)上部垂直串接湿法增大可吸入颗粒工艺(二)。下部垂直串接地面的液体氧化，固体浓缩工艺(三)工艺设备是湿法变相塔(1)上部垂直串接湿法静电塔(2)，再串接升温塔(4)。底部垂直串接氧化，浓缩塔(3)构成的。烟气净化和排放与一体的新“烟塔合一”的技术和设备-环保烟囱。
Description
[0001] 技术领域:本发明工艺，烟气除尘、脱硫一体化工艺是向环保领域提供一种烟气净化新工艺。
[0002] 背景技术:目前烟气净化分两次。1，先除尘。2，后脱硫。
[0003] 1，除尘；烟气流速V # 0，静电除尘振打吸附极板，烟尘颗粒100%脱离吸附极板，又回到流动的烟气中。由于流动烟气有悬浮力，较大颗粒沉降脱离流动烟气，达到净化目的。较小的可吸入烟尘颗粒不能沉降，悬浮在流动烟气中排放进大气。造成固体可吸入颗粒物在空气中悬浮污染。在辽宁省环保局大气悬浮物可吸入颗粒物分析报告中说；大气中可吸入颗粒物85%是燃煤电厂静电除尘器排放进大气。
[0004] 布袋除尘是烟气流动中，烟颗粒100 %悬浮进布袋，较大颗粒在悬浮通过布袋孔时被布袋孔过滤出来，达到净化除尘。较小的可吸入颗粒悬浮通过布袋孔，直接排放进大气，造成固体可吸入颗粒物在空气中悬浮污染。
[0005] 2，脱硫；在半干法和湿法/脱硫后，含有大量SO2次生物-亚硫酸氢钙水溶液雾滴的雾状烟气直接排放进大气。亚硫酸氢钙水溶液雾滴在大气中氧化成极小可吸入2水石膏颗粒悬浮在大气中，构成可吸入颗粒悬浮污染。
[0006] 以上净化工艺仅仅是将I种次生物污染变成另一种次生物污染的过程。并减少污染。所以是一种不健全、不完善的净化工艺。
[0007] 发明特征:本发明与一般烟气净化工艺最大不同处；
[0008] ①，烟气原来分两次净化；1，先干法除尘。2，后再湿法脱硫。
[0009] 本发明是烟气除尘、脱硫同时在环保烟囱内I次湿法净化完成。
[0010] ②原烟气通过脱硫塔内I次沉降分离出较大烟尘颗粒和亚硫酸氢钙水溶液颗粒。没有再将悬浮的可吸入烟尘颗粒和SO2次生物雾滴颗粒再分离。
[0011] 本发明增加，将悬浮的可吸入烟尘颗粒和SO2次生物雾滴颗粒增大到几百倍大于可吸入烟尘和亚硫酸氢钙水溶液的颗粒，在流动中完成第二次沉降。达到净化固体、液体各种粒径颗粒的效率100%。是本发明最大特征。
[0012] ③，原来烟气净化，烟气流速V都# O。特别是湿法脱硫，V都大于2米。烟气在2米/秒流速中100%可吸入级固体、液体颗粒100%悬浮不沉降。
[0013] 本发明是烟气流速V #0，VS 2米/秒。大于2米/秒，本发明就失效，不能工作。
[0014] ④，原烟气由气、固两相流，经喷淋变成气、液、固三相流雾状烟气排放(含可吸入液体和固体颗粒)。
[0015] 本发明是烟气经喷淋后，气固两相流烟气变成气、液、固三相流雾状烟气。再经湿法增大可吸入颗粒工艺(二)，将100%可吸入颗粒，沉降分离出来。变成气体一相流无色透明烟气排放。
[0016] ⑤，原来烟气中SO/变成亚硫酸氢钙水溶液用鼓风机鼓空气进氧化池氧化。
[0017] 本发明改成用亚硫酸氢钙水溶液薄膜液层垂直流动，接触空气直接氧化技术过程。废弃鼓风机鼓空气进氧化池氧化。
[0018] ⑥，原来水循环是；喷淋浆液落到增湿变相塔内底部循环池，用泵I次提升到塔外氧化池，再用泵2次提升进浓缩池，再用泵第3次提升进脱水机脱水。再用泵第四次提升进制浆池加脱硫剂后，再用泵第五次提升到塔内循环池。再用循环泵第六次提升进增湿变相塔内喷淋烟气。
[0019] 本发明水循环是；喷淋后的浆液垂直落进氧化、浓缩塔(3)内的浓缩池出)。浓缩池(6)。底流完成I次浓缩后进脱水机(7) 2次脱水制备出潮湿固体颗粒排放。浓缩池(6)澄清液溢流，沿氧化、浓缩塔(3)墙壁垂直流，完成SO2次生物接触空气达到氧化，氧化出2水石膏颗粒并还原出水进氧化、浓缩塔(3)内地面循环池(9)。进用循环泵(5)第一提升进增湿变相塔(I)喷淋。
[0020] ⑦由于湿法静电塔将烟气中唯一的可吸入雾滴颗粒100%分离出来。所以:烟气中无任何污染物就不需原来高200米烟囱飘散污染物。净化后烟气直接排放的新烟塔合一技术。
[0021] 本发明专利；烟气除尘脱硫工艺的目的；
[0022] 1，将烟气中烟尘颗粒100%分离出来。
[0023] 2，将烟气中S02100%变成次生物的各种粒径的颗粒，再100%分离出来。本发明专利；烟气除尘脱硫工艺的实施方案；
[0024] 烟气除尘脱硫一体化工艺；湿法变相工艺(一)上部垂直串接湿法增大可吸入颗粒工艺(二)，下部垂直串接液体氧化，固体浓缩工艺(三)组成的。
[0025] 湿法变相工艺(一)；
[0026] 烟气在湿法变相塔(I)内用循环泵(5)雾状喷淋脱硫剂浆，烟尘颗粒100%变成被液体包裹的各种粒径的导电颗粒。SO2100 %变成各种粒径的亚硫酸氢钙水溶液导电液滴颗粒，
[0027] 烟气在流速VS 2米/秒，沉降临界粒径是可吸入颗粒d。烟气在湿法变相塔(I)内流动，大于可吸入颗粒d的颗粒，(包括被液体包裹的烟尘导电颗粒和亚硫酸氢钙水溶液导电液滴颗粒)100%垂直降落进底部的氧化、浓缩塔(3)内的浓缩池出)。完成第一次污染物沉降净化过程的湿法变相工艺(一)。第第一次沉降分离出100%大于可吸入颗粒d的颗粒
[0028] 湿法增大可吸入颗粒工艺(二)；
[0029] 剩余100可吸入颗粒d的颗粒(被液体包裹的烟尘导电颗粒和亚硫酸氢钙水溶液导电雾滴颗粒)，悬浮进湿法静电塔(2)。导电雾滴颗粒被吸附极吸附、汇聚、增大、增重变成大于可吸入颗粒d的颗粒，垂直流出湿法静电塔(2)，过增湿变相塔(I)进氧化、浓缩塔内⑶的浓缩池(6)。第二次将剩余100%彡可吸入颗粒d的颗粒增大后再100%沉降分离出来。
[0030] 二次沉降完成净化过程的湿法变相工艺(一)和湿法增大可吸入颗粒工艺(二)。达到烟气中100%任何粒径的固体颗粒、SO2次生物亚硫酸氢钙水溶液液滴颗粒100%被分离出来。达到除尘效率100%，脱硫效率100%、回收液体雾滴颗粒效率100%。。
[0031] 液体氧化，固体浓缩工艺(三)
[0032] 喷淋浆在增湿变相塔⑴内喷淋后垂直落进氧化、浓缩塔(3)的浓缩池(6)。浓缩池(6)底流浓浆进搅龙(7)(或脱水机(7))最后排放潮湿固体颗粒。(脱水机(7)分离出水回流进循环池(9))。
[0033] 浓缩池(6)澄清液溢流，过内挡水板(11)，过溢流孔，沿氧化、浓缩塔(3)墙壁与外挡水板(12)之间间隙垂直流进氧化、浓缩塔(3)内地面循环池(9)。完成scy欠生物接触空气达到氧化和热交换的液体氧化，固体浓缩工艺(三)。
[0034] 湿法静电塔(2)分离出100%可吸入液体和固体颗粒后的烟气是无色透明饱和烟气进升温塔(4)，变成不饱和烟气直接排放。这就是烟气除尘、脱硫、排放的“烟塔合一”技术。
[0035] 设备是地面的氧化、浓缩塔(3)垂直串接湿法变相塔(I)再垂直串接湿法静电塔
(2)再垂直串接升温塔(4)的环保烟囱。
[0036] 说明书附图；图2，烟气除尘脱硫一体化工艺流程图
[0037] 液体氧化，固体浓缩工艺(三)垂直串接湿法变相工艺(一)再垂直串接湿法增大可吸入颗粒工艺(二)的工艺流程图。
[0038] 说明书附图；图1，烟气除尘脱硫一体化流程图和设备
[0039] 湿法变相塔⑴，上部垂直串接湿法静电塔⑵，湿法静电塔⑵再串接升温塔(4)
[0040] 湿法变相塔⑴底部垂直串接氧化、浓缩塔(3)的环保烟囱图。
[0041] 烟气进湿法变相塔(I)，在湿法变相塔(I)，内用循环泵(5)泵出液体或浆体雾状喷淋烟气。喷淋后液体或浆体落到氧化、浓缩塔(3)的浓缩池(6)
[0042] 雾状烟气进湿法静电塔(2)分离出固体和液体落到氧化、浓缩塔(3)的浓缩池(6)内，
[0043] 循环液在浓缩池(6)溢流进循环池(9)
[0044] 浓缩池(6)底流进脱水机(7)脱出潮湿固体颗粒排放，脱出水回流进循环池(9)
[0045] 循环泵(5)泵出液体或浆体在湿法变相塔(I)内雾状喷淋烟气，烟气变成雾状烟气。进湿法静电塔(2)
[0046] 湿法静电塔(2)分离出无色透明饱和烟气进升温塔后按一直接排放。
[0047] 湿法静电塔(2)分离出较大液滴过湿法变相塔(I)落进氧化、浓缩塔(3)的浓缩池⑶。
[0048] 摘要附图；图1
[0049] 具体实施案例
[0050] 烟气；含SO2的燃煤烟气
[0051] 烟气除尘、脱硫一体化工艺过程。
[0052] I，烟气“湿法变相工艺；
[0053] 烟气流速V= I。2米/秒，按一进增湿变相塔(1)，在增湿变相塔⑴内用循环泵
(5)雾状喷淋石灰石浆。烟气在增湿变相塔(I)内滞留14秒。烟气变成雾状烟气。
[0054] 302在14秒内100%变成亚硫酸氢钙水溶液各种粒径的液滴颗粒，悬浮在烟气中。
[0055] 烟尘颗粒变成被水和亚硫酸氢钙水溶液包裹的含烟尘颗粒的各种粒径的导电液滴颗粒，悬浮在烟气中。
[0056] 烟气流速在V = I。2米/秒，100%大于可吸入液滴颗粒10微米的颗粒，垂直沉降进浓缩池¢)内。
[0057] 小于10微米的可吸入颗粒，100%悬浮进湿法静电塔⑵内。
[0058] 2，湿法增大可吸入颗粒工艺；
[0059] 含100%小于10微米粒径的可吸入液滴颗粒和被液体包裹的烟尘颗粒的雾状烟气。在流速V= I。2米/秒，悬浮进湿法静电塔(2)内，滞留大于3秒。将小于10微米可吸入液滴颗粒和被液体包裹的烟尘颗粒，100%变成大于10微米粒径的液滴颗粒，垂直流出静电场，进增湿变相塔⑴内。因颗粒增大几百倍，在增湿变相塔⑴内不能悬浮，就100%沉降进浓缩池(6)
[0060] 静电后不含任何种液体雾滴、烟尘颗粒的净化后气体是饱和、无色透明烟气按a—出湿法静电塔(2)过升温塔，变成不饱和、无色透明烟气排放。
[0061] 3，液体氧化，固体浓缩工艺(三)
[0062] 浓缩池¢)中水和亚硫酸氢钙水溶液的澄清液，溢流过氧化、浓缩塔(3)外壁垂直流进循环池(7)，在墙壁接触空气氧化，产出2水石膏颗粒，还原出水进地面环形循环池⑵。
[0063] 浓缩池¢)中2水石膏颗粒与烟尘颗粒与还原出的水和亚硫酸氢钙水溶液浓缩，经底部排放口进脱水机(7)。脱出水进地面环形循环池(9)，脱出潮湿固体颗粒排放。
[0064] 在循环池(9)加脱硫剂石灰，经搅拌机(8)搅拌。再经循环泵(5)进增湿变相塔
(I)内雾状喷淋烟气。
[0065] 经天津市环保局检测，达到；除尘效率99。9 %，脱硫效率99 %，烟气黑度小于I级，无色透明。
Claims (1)
1.烟气除尘脱硫一体化工艺，由湿法变相工艺(一)上部垂直串接湿法增大可吸入颗粒 工艺(二)，下部垂直串接液体氧化，固体浓缩工艺(三)组成； 湿法变相工艺(一)； 烟气在湿法变相塔(I)内用循环泵(5)雾状喷淋脱硫剂浆，烟尘颗粒100%变成被液体 包裹的各种粒径的导电颗粒；SO210 %变成各种粒径的亚硫酸氢钙水溶液导电雾滴颗粒， 烟气在流速V =1.2米/秒，烟气在增湿变相塔(I)内滞留14秒，沉降临界粒径是可吸入颗粒d;烟气在湿法变相塔(I)内流 动，大于可吸入颗粒d的颗粒，包括被液体包裹的烟尘导电颗粒和亚硫酸氢钙水溶液导电 液滴颗粒，100%垂直降落进底部的氧化、浓缩塔(3)内的浓缩池¢);完成第一次污染物 沉降净化过程； 湿法变相工艺(一)完成第一次沉降分离出100%大于可吸入颗粒d的颗粒；湿法增大 可吸入颗粒工艺(二)； 剩余100%<可吸入颗粒d的颗粒，被液体包裹的烟尘导电颗粒和亚硫酸氢钙水溶液导电雾滴颗粒，流速V = 1.2米/秒，悬浮进湿法静电塔(2)，滞留大于3秒；导电雾滴颗粒被吸附极吸附、汇聚、增大、增重变 成大于可吸入颗粒d的颗粒，垂直流出湿法静电塔(2)，过增湿变相塔(I)落进氧化、浓缩塔 (3)内的浓缩池¢);第二次将剩余100%<可吸入颗粒d的颗粒增大后再100%沉降分离 出来； 湿法增大可吸入颗粒工艺(二)完成第二次沉降分离出100%小于可吸入颗粒d的颗 粒；两次沉降完成烟气中100%任何粒径的固体颗粒、S02次生物亚硫酸氢钙水溶液液滴颗粒 被分离出来；达到除尘效率100%，脱硫效率100%、回收液体雾滴颗粒效率100% ； 液体氧化，固体浓缩工艺(三) 脱硫浆剂在湿法变相塔(I)内喷淋后垂直落进氧化、浓缩塔(3)的浓缩池¢);浓缩池 (6)底流浓浆进绞龙或脱水机后排放潮湿固体颗粒；绞龙或脱水机分离出水回流 进循环池(9); 浓缩池¢)澄清液溢流，过内挡水板(11)，过溢流孔，在沿氧化、浓缩塔(3)墙壁与外挡 水板(12)之间间隙垂直流进氧化、浓缩塔(3)内地面循环池(9);完成SO 2次生物接触空 气达到氧化和热交换的液体氧化，固体浓缩工艺(三)； 湿法静电塔(2)分离出100%可吸入液体和固体颗粒后的烟气是无色透明饱和烟气，饱和烟气进 升温塔(4)，变成不饱和烟气直接排放；这就是烟气除尘、脱硫、排放的“烟塔合一”技术； 设备是地面的氧化、浓缩塔(3)垂直串接湿法变相塔(I)再垂直串接湿法静电塔(2) 再垂直串接升温塔(4)的环保烟囱。
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| CN102580432A (zh) * | 2011-04-21 | 2012-07-18 | 庄建中 | 烟气除尘、脱硫、脱氮一体化工艺 |
| CN103263821A (zh) * | 2013-05-22 | 2013-08-28 | 庄建中 | 燃煤烟气脱氮氧化物成套设备 |
| CN104759182B (zh) * | 2015-02-12 | 2016-05-18 | 济南信邦信息工程有限公司 | 一种净化室外大气中细颗粒物的方法及装置 |
| CN105688590B (zh) * | 2016-04-19 | 2018-01-30 | 庄建中 | 燃烧垃圾烟气净化设备及净化工艺 |
| CN107648965A (zh) * | 2016-07-25 | 2018-02-02 | 庄建中 | 一种燃烧垃圾的烟气综合净化工艺与设备 |
| CN108159814A (zh) * | 2016-12-08 | 2018-06-15 | 天津市嘉腾环保设备有限公司 | 一种布袋除尘装置 |
| CN109173552A (zh) * | 2018-10-15 | 2019-01-11 | 中石化（洛阳）科技有限公司 | 一种烟气净化方法及系统 |
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