CN101745305B - 一种脱除烟气中气态多种污染物的方法 - Google Patents
一种脱除烟气中气态多种污染物的方法 Download PDFInfo
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- CN101745305B CN101745305B CN2010101000091A CN201010100009A CN101745305B CN 101745305 B CN101745305 B CN 101745305B CN 2010101000091 A CN2010101000091 A CN 2010101000091A CN 201010100009 A CN201010100009 A CN 201010100009A CN 101745305 B CN101745305 B CN 101745305B
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- Prior art keywords
- absorption
- absorption tower
- active
- flue gas
- smoke gas
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- 239000003344 environmental pollutants Substances 0.000 title claims abstract description 27
- 239000007789 gases Substances 0.000 title claims abstract description 25
- 239000000779 smoke Substances 0.000 title claims abstract description 23
- 231100000719 pollutant Toxicity 0.000 title claims abstract description 21
- 238000010521 absorption reactions Methods 0.000 claims abstract description 100
- 230000003009 desulfurizing Effects 0.000 claims abstract description 28
- 238000006477 desulfuration reactions Methods 0.000 claims abstract description 27
- 238000007254 oxidation reactions Methods 0.000 claims abstract description 21
- 238000005261 decarburization Methods 0.000 claims abstract description 20
- 239000007800 oxidant agents Substances 0.000 claims abstract description 16
- 238000005192 partition Methods 0.000 claims abstract description 6
- AHKZTVQIVOEVFO-UHFFFAOYSA-N oxide(2-) Chemical compound data:image/svg+xml;base64,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 data:image/svg+xml;base64,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 [O-2] AHKZTVQIVOEVFO-UHFFFAOYSA-N 0.000 claims abstract description 3
- 239000003546 flue gases Substances 0.000 claims description 60
- UGFAIRIUMAVXCW-UHFFFAOYSA-N carbon monoxide Chemical compound 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[O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims description 57
- 239000007788 liquids Substances 0.000 claims description 56
- QSHDDOUJBYECFT-UHFFFAOYSA-N mercury Chemical compound 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[Hg] QSHDDOUJBYECFT-UHFFFAOYSA-N 0.000 claims description 21
- 229910052753 mercury Inorganic materials 0.000 claims description 21
- CBENFWSGALASAD-UHFFFAOYSA-N ozone Chemical group 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- 238000005507 spraying Methods 0.000 abstract description 4
- CURLTUGMZLYLDI-UHFFFAOYSA-N carbon dioxide Chemical compound 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O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 abstract description 3
- 229910002092 carbon dioxides Inorganic materials 0.000 abstract description 3
- 229910001890 sulfur dioxide Inorganic materials 0.000 abstract description 3
- RAHZWNYVWXNFOC-UHFFFAOYSA-N sulphur dioxide Chemical compound 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- 239000006227 byproducts Substances 0.000 description 5
- MWUXSHHQAYIFBG-UHFFFAOYSA-N nitric oxide Chemical compound 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O=[N] MWUXSHHQAYIFBG-UHFFFAOYSA-N 0.000 description 5
- 229910001874 nitric oxide Inorganic materials 0.000 description 5
- 239000003513 alkali Substances 0.000 description 4
- HZAXFHJVJLSVMW-UHFFFAOYSA-N ethanolamine Chemical compound 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NCCO HZAXFHJVJLSVMW-UHFFFAOYSA-N 0.000 description 4
- 229910052813 nitrogen oxides Inorganic materials 0.000 description 4
- OKTJSMMVPCPJKN-UHFFFAOYSA-N carbon Chemical compound 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[C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 3
- 238000004140 cleaning Methods 0.000 description 3
- 238000007599 discharging Methods 0.000 description 3
- 229910000132 mercury(II) oxide Inorganic materials 0.000 description 3
- DVARTQFDIMZBAA-UHFFFAOYSA-O Ammonium nitrate Chemical compound 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- 239000002699 waste materials Substances 0.000 description 2
- BFNBIHQBYMNNAN-UHFFFAOYSA-N Ammonium sulfate Chemical compound 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- 280000420903 Energy Agency companies 0.000 description 1
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- LSNNMFCWUKXFEE-UHFFFAOYSA-L Sulphite Chemical compound 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[O-]S([O-])=O LSNNMFCWUKXFEE-UHFFFAOYSA-L 0.000 description 1
- 229910052921 ammonium sulfate Inorganic materials 0.000 description 1
- 235000011130 ammonium sulphate Nutrition 0.000 description 1
- OYPRJOBELJOOCE-UHFFFAOYSA-N calcium Chemical compound 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- 239000004071 soot Substances 0.000 description 1
- NINIDFKCEFEMDL-UHFFFAOYSA-N sulfur Chemical compound 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[S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 1
- 229910052717 sulfur Inorganic materials 0.000 description 1
- 239000011593 sulfur Substances 0.000 description 1
- 229910052815 sulfur oxides Inorganic materials 0.000 description 1
Classifications
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
- Y02A50/00—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE in human health protection, e.g. against extreme weather
- Y02A50/20—Air quality improvement or preservation, e.g. vehicle emission control or emission reduction by using catalytic converters
Abstract
Description
一种脱除烟气中气态多种污染物的方法技术领域[0001] 本发明涉及一种烟气净化方法,特别是脱除电站锅炉和工业锅炉烟气气态多种污 染物的方法,属烟气净化技术领域。背景技术[0002] 众所周知,化石燃料燃烧过程排放的二氧化硫(SO2)和氮氧化物(NOx),形成酸雨 和其他二次污染物,已严重影响到人类的生产和生活。因此,SO2和NOx的控制和净化迫在 眉睫,关系到国民经济的发展和人类的生存。[0003] 烟气脱硫(FGD)是目前世界上开展的惟一大规模商业化应用的脱硫方法,是控制 酸雨和SO2污染最为有效和主要的技术手段。其主流的技术是湿式石灰石石膏洗涤法,其技 术比较成熟、脱除效率高、工艺可靠性好,但却存在设备投资高、系统复杂、易于堵塞、结垢、 腐蚀、泄漏以及淤泥的后处理等问题。这些因素使得湿法脱硫在经济性、运行维护方面出现 一定的局限性。酸雨前体物SO2被大量脱除后,在环保要求较高的地区,NOx将成为酸雨前体 物减排的主要控制目标。烟气脱硝是当前治理NOx中最重要的方法。现行的NOx治理技术主 要是采用选择性催化还原法脱硝(SCR),SCR法脱硝投资巨大,运行成本高。除了酸雨问题, 最近温室效应越来越引起人们的关注。二氧化碳等温室气体的大量排放已引起全球温度不 断升高,全球气候变化是当前最紧迫的环境压力之一。据经济合作发展组织和国际能源署 数据显示,燃煤电厂是CO2的主要来源,现有电厂CO2年排放量约106亿吨,占全世界排放总 量的40. 6 %。这就要求采用碳捕获和存储(CCS)等技术控制CO2的排放。上述各种独立的烟 气污染物控制技术(FGD、SCR、CCS)虽然都能达到各自理想的脱除和捕集效率,但如果分别 脱除,几种设备同时运行必然给电厂带来巨大的经济压力,这就要求发展气态多种污染物 同时脱除技术,以简化工艺系统,降低脱除成本,提高脱除效率。而传统的烟气脱硫脱硝工 艺需要分级进行,存在投资高、占地面积大、系统复杂等缺点。中国专利CN200910095344. 4 号公开了一种臭氧氧化结合双塔洗涤对烟气同时脱硫脱硝的技术,该技术使用的装置包括 烟道、与烟道依次相连的换热器、碱液洗涤塔A、碱液洗涤塔B,利用该装置可同时对烟气脱 硫脱硝。但该技术的目标脱除物不包括CO2,而且存在双吸收塔结构复杂、占地面积大等问 题,另外,该专利的臭氧加入到碱液洗涤塔A下部的液相区,参与脱硫浆液中的亚硫酸盐的 氧化,势必增加臭氧消耗,增大系统地运行成本。中国专利200810197731. 4号公开了一种 燃煤烟气多污染物脱除工艺及其设备。该工艺先用SCR脱硝法脱除烟气中的NOx,而后用除 尘器脱除烟气中的粉尘灰粒,然后用湿式钙基脱硫法消除烟气中的SO2,最后再用一乙醇胺 (MEA)脱碳法吸收烟气中的CO2。该技术采用MEA脱碳存在成本高昂、MEA损失较大、CO2吸 收容量低、腐蚀速率高等问题。另外,由于其工艺系统复杂,不适合在大烟气量的电厂应用。[0004] 综上所述,研发工艺简单、可靠、经济实用的烟气气态多种污染物控制方法具有十 分重要的意义。发明内容[0005] 本发明所要解决的问题是提供一种使用设备简单、系统集成度高、运行费用低的 脱除烟气中气态多种污染物的方法。[0006] 本发明所称问题是由以下技术方案解决的:[0007] 一种脱除烟气中气态多种污染物的方法,它利用一个吸收塔对烟气中S02、N0X、$ 蒸气以及CO2进行全面脱除,所述吸收塔下部设置吸收浆液池,中部设置喷淋管、上部设有 氧化剂管,吸收塔沿纵向设有隔板,隔板下部探入吸收浆液池中,隔板将吸收塔分隔为脱硫 工作段和脱硝脱碳工作段,吸收塔上部为连通的氧化区;烟气由吸收塔进口进入脱硫工作 段逆流向上,经与喷淋管喷射的吸收液接触,完成SO2和氯化氢的脱除;烟气继续向上进入 氧化区,在氧化区NOx被氧化剂管喷出的氧化剂氧化成易溶于水的高价态氧化物后进入脱 硝脱碳工作段,所述氧化剂为臭氧、二氧化氯、过氧化氢气体或其混合物;在脱硝脱碳工作 段烟气顺流向下经喷淋管喷出的吸收液洗涤,完成N0X、$ (Hg)蒸气及CO2脱除,净化后的 烟气由吸收塔出口排出。[0008] 上述脱除烟气中气态多种污染物的方法,所述喷淋管在两工作段间连通,或在各 工作段内分置,喷淋管经吸收液循环泵及管路连通吸收浆液池。[0009] 上述脱除烟气中气态多种污染物的方法,所述吸收浆液池在两工作段下部连通, 或由隔板分置为分别对应两工作段的独立池。[0010] 上述脱除烟气中气态多种污染物的方法,所述吸收塔旁设有吸收液补充罐,吸收 液补充罐经吸收液补充泵和管路连通吸收液池;所述吸收浆液池外设有吸收液排出泵,吸 收液排出泵经管路连通吸收液池;所述塔吸收浆液池内设有与鼓风装置相连的氧化空气管。[0011] 上述脱除烟气中气态多种污染物的方法,所述吸收塔出口依次设有冲洗水装置和除雾器。[0012] 本发明针对现有燃煤电厂烟气气态多污染物治理技术的局限性进行了改进,提供 了一种新的治理方法,该方法解决了烟气污染物分别治理的问题,并且突破了现有技术烟 气中气态多污染物同时脱除设备复杂、运行成本高的技术瓶颈,其工艺方法和装置具有独 特的创新性。本发明在吸收塔内添加臭氧(O3)等强氧化剂,将锅炉烟气中一氧化氮(NO) 氧化成为易溶于水的高价态N0X,如N02、NO3或N2O5,然后采用传统的碱液水洗涤锅炉烟气, 脱除烟气中的S02、N0x以及C02。同时该工艺还具有较高的脱汞性能,可以达到95%以上的 脱硫率和85%以上的脱硝和脱碳率。本发明利用一个吸收塔内同时去除NOx,SOx,氯化氢 (HCl),汞蒸气和CO2,而且可以回收有价值的副产品。此工艺不仅可以满足目前环保的需 要,而且可以满足未来环保标准提高的要求(比如对汞和CO2的脱除)。具有系统简单,脱 除成本低,易于实现,回收率高等特点。附图说明[0013] 图1是本发明实施例I示意图;[0014] 图2是本发明实施例2示意图[0015] 图3是本发明实施例3示意图。[0016] 图中标号含义如下:1.吸收浆液池;2.吸收塔进口 ;3.脱硫工作段;4.臭氧发生 器;5.氧化剂管;6.吸收塔;7.氧化区;8.隔板;9.喷淋管;10.脱硝脱碳工作段;11.冲洗水装置;12.除雾器;13.吸收塔出口 ;14.吸收液补充罐;15.吸收液补充泵;16.吸收液循环泵;17.氧化空气管;18.吸收液排出泵。具体实施方式
[0017] 本发明利用一个吸收塔完成对烟气中S02、NOx、汞蒸气以及CO2等的全面脱除,以下结合实施例对此作进一步说明:[0018] 实施例1:参看图1,吸收塔6下部设置吸收浆液池I ;中部设置喷淋管9,喷淋管由吸收液循环泵16及管路与吸收液池连通,吸收浆液池中吸收液pH值维持在5〜7,吸收液采用氨水;吸收塔上部设有氧化剂管5,氧化剂为臭氧,臭氧以气相的方式加入氧化区7, 由于绝大部分SO2在脱硫工作段3被脱除,减少了由于SO2氧化所消耗的臭氧量,从而降低了系统对臭氧的消耗,氧化剂管连通臭氧发生器4,加入的臭氧与烟气中的NOx摩尔比(O3/ NO)控制在O. 5〜2. O范围内,本实施例中NOx摩尔比03/N0为O. 5。氧化剂并不仅限于臭氧,其他氧化剂,比如次氯酸钠、过氧化氢等也可以代替或者以一定比例与臭氧混合作为氧化剂。吸收塔沿纵向设有隔板8,隔板两侧分别为脱硫工作段3和脱硝脱碳工作段10,为防止烟气从隔板底部泄露,隔板下部要探入吸收浆液池中,吸收塔上部为将两工作段连通的氧化区7。本实施例烟气脱除过程如下:[0019] (1)90-120°C烟气由吸收塔进口 2进入脱硫工作段3,在该工作段主要完成SO2和 HCl的脱除,在脱硫工作段烟气逆流向上,经与喷淋管9喷射的吸收液接触反应,温度降至 50〜100°C,并完成SO2和HCl的脱除,吸收反应原理如下:[0020] S02+NH3+H20 = NH4HSO3[0021] HCI+NH3 = NH4Cl[0022] (2)脱除了 SOjPHCl的烟气继续向上进入氧化区7,在此区域烟气中NO被氧化剂管喷出的臭氧氧化成更高氧化态的NOx,基本反应原理如下:[0023] N0+03 — N02+02[0024] N02+03 — N03+02[0025] N03+N02 — N2O5[0026] 氧化区加入的氧化剂同时也将烟气中元素汞氧化成二价汞,二价汞溶于水,易在后续的洗涤过程中被去除。基本反应原理如下:[0027] Hg+03 — Hg0+02[0028] Hg+N03 — Hg0+N02[0029] Hg0+2H+ — Hg2++H20[0030] 本发明烟气先经过逆流洗涤,而后加入臭氧氧化,由于绝大部分SO2在脱硫段被脱除,因而可以减少由于SO2氧化所消耗的臭氧量。[0031] (3)经氧化的烟气继续下行进入脱硝脱碳工作段10,在此工作段烟气中高氧化态的NOx、二价汞及CO2与喷淋管9喷出吸收液反应,主要完成NOx、汞蒸气及CO2脱除,也可以脱除未被完全利用的氨和臭氧。此工作段烟气温度降至30〜50°C,氨水在此温度区间脱碳可减少氨的挥发损失。[0032] 脱硝基本反应原理如下:[0033] 2N02+H20 — ΗΝ03+ΗΝ02[0034] Ν205+Η20 — 2HN03[0035] 脱碳基本反应原理如下:[0036] CO2+ NH3 石NH2COOH[0037] NH2COOH+ NH3 <~~> NH2COONH4[0038] NH2COONH4 + H2O <> NH4HCO3+NH3[0039] ΝΗ3+Η20 <-> NH4OH[0040] NH4HCO3+NH4OH <~~~> (NH4)2C03+H20[0041] (NH4)2C03+C02+H20 <~~> 2NH4HC03 [0042] 脱硝过程生成的HNO3被碱性物质氨水中和生成稳定产物。二价汞进入脱除废液中,可在后续的废液固分离过程中可以采用目前烟气脱硫工艺中常用的加入有机硫试剂 TMT-15的方法予以去除。[0043] (4)脱除多污染物以后的清洁烟气由吸收塔出口 13排出。为防止氨泄漏,在烟气出口部位加装冲洗水装置11,在其后面安装有除雾器,以除去烟气中携带的小水滴。[0044] 在吸收塔旁设有吸收液补充罐,吸收液补充罐经吸收液补充泵和管路连通吸收液池。吸收液补充罐中氨水浓度在10〜25%,吸收液池中吸收液的pH由补加的氨水流量来调节。为保持吸收液池中的吸收液离子含量不超过限定值,部分吸收液由吸收液排出泵18 抽出。为得到硫酸铵、硝酸铵以及碳酸氢铵的混合氨态肥料,吸收浆液池内设有与鼓风装置相连的氧化空气管17。[0045] 实施例2 :参看图2,90_120°C烟气由吸收塔进口 2进入脱硫工作段3,在该工作段完成SO2和HCl的脱除,在脱硫工作段烟气逆流向上,经与喷淋管9喷射的吸收液(氨水) 接触反应,温度降至50〜100°C,完成SO2和HCl的脱除;烟气继续向上进入氧化区,在此区域烟气中NO被氧化剂管喷出的臭氧氧化成更高氧化态的N0X,同时元素汞氧化成二价汞,本实施例中NOx摩尔比03/N0为1. O ;烟气继续下行进入脱硝脱碳工作段10,在此工作段烟气中高氧化态的NOx、二价汞及CO2与喷淋管9喷出吸收液反应,完成NOx、汞蒸气及CO2脱除。 此工作段烟气温度降至30〜50°C,氨水在此温度区间脱碳可减少氨的挥发损失;脱除多污染物以后的清洁烟气由吸收塔烟气排出口排出。本实施烟气脱除过程的各步骤基本反应原理同实施例I。与实施例I的不同之处在于,为了控制脱硫工作段与脱硝脱碳工作段不同的液气比,喷淋管9在各工作段内分置,并设置了两个分别与各工作段喷淋管连通的吸收液循环泵16。[0046] 实施例3,参看图3,90_120°C烟气由吸收塔进口 2进入脱硫工作段3,在该工作段完成SO2和HCl的脱除,在脱硫工作段烟气逆流向上,经与喷淋管9喷射的吸收液接触反应, 温度降至50〜100°C,完成SO2和氯化氢的脱除;烟气继续向上进入氧化区7,在此区域烟气中NO被臭氧氧化成更高氧化态的N0X,同时元素汞氧化成二价汞,本实施例NOx摩尔比O3/ NO为2. O ;烟气继续下行进入脱硝脱碳工作段10,在此工作段烟气中高氧化态的NOx、二价汞及CO2与喷淋管9喷出吸收液反应,完成NOx、汞蒸气及CO2脱除。脱除多污染物以后的清洁烟气由吸收塔出口 13排出。本实施喷淋管仍采用如实施例2在两工作段分置方式,与实施例2的不同之处在于,吸收塔内隔板8直接插入到吸收塔底部,由隔板将吸收液池分置为分别对应两工作段的独立池。含有脱除副产品的吸收液分别由两个吸收液排出泵18排出, 该设置脱硫工作段和脱硝脱碳工作段可以根据市场的需要来提供不同的副产品。本实施例中,脱硫工作段采用石灰石作为吸收液,脱硫工作段的副产品是石膏;脱硝脱 碳工作段采用氨水为吸收液,其副产品是硝酸铵与碳酸氢铵。
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