CN201840979U - 一种烟气综合处理系统 - Google Patents
一种烟气综合处理系统 Download PDFInfo
- Publication number
- CN201840979U CN201840979U CN2010205970317U CN201020597031U CN201840979U CN 201840979 U CN201840979 U CN 201840979U CN 2010205970317 U CN2010205970317 U CN 2010205970317U CN 201020597031 U CN201020597031 U CN 201020597031U CN 201840979 U CN201840979 U CN 201840979U
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- CN
- China
- Prior art keywords
- absorber
- flue gas
- comprehensive treatment
- absorption tower
- communicated
- Prior art date
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- 239000000779 smoke Substances 0.000 title claims abstract description 26
- 239000007789 gases Substances 0.000 title abstract description 12
- 238000010521 absorption reactions Methods 0.000 claims abstract description 46
- 239000006096 absorbing agents Substances 0.000 claims abstract description 42
- UGFAIRIUMAVXCW-UHFFFAOYSA-N carbon monoxide Chemical compound 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[O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims description 54
- 239000003546 flue gases Substances 0.000 claims description 54
- 239000003463 adsorbents Substances 0.000 claims description 28
- 238000006243 chemical reactions Methods 0.000 claims description 24
- 230000003009 desulfurizing Effects 0.000 claims description 18
- 239000000953 sodium hydroxide Substances 0.000 claims description 17
- 229910001856 sodium hydroxide Inorganic materials 0.000 claims description 17
- 235000011121 sodium hydroxide Nutrition 0.000 claims description 17
- 239000003513 alkali Substances 0.000 claims description 16
- 239000007921 sprays Substances 0.000 claims description 10
- 230000001603 reducing Effects 0.000 claims description 6
- 238000001816 cooling Methods 0.000 claims description 3
- 239000000428 dust Substances 0.000 abstract description 17
- OKTJSMMVPCPJKN-UHFFFAOYSA-N carbon Chemical compound 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[C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 abstract description 14
- 239000011521 glasses Substances 0.000 abstract description 7
- 238000000746 purification Methods 0.000 abstract description 7
- 239000003245 coal Substances 0.000 abstract description 3
- 238000000034 methods Methods 0.000 description 11
- 229910052799 carbon Inorganic materials 0.000 description 8
- 239000011901 water Substances 0.000 description 7
- 238000006477 desulfuration reactions Methods 0.000 description 6
- 239000000126 substances Substances 0.000 description 6
- 238000010531 catalytic reduction reactions Methods 0.000 description 5
- GRYLNZFGIOXLOG-UHFFFAOYSA-N nitric acid Chemical compound 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Abstract
Description
一种烟气综合处理系统
技术领域
[0001] 本实用新型涉及环保技术领域,尤其涉及一种烟气综合处理系统。 背景技术
[0002] 随着现代工业的迅速发展,环境保护问题逐渐成为各类工业领域的一个热点问 题,现有的烟气净化处理主要包括除尘、脱硫和脱硝处理。
[0003] 烟气除尘技术主要包括干式除尘法和湿式除尘法,其中干式除尘采用重力沉降 室、惯性除尘器、电除尘器、布袋除尘器、旋风除尘器等设备除尘,湿式除尘采用喷淋塔、冲 击式除尘器、文丘里洗涤剂、泡沫除尘器和水膜除尘器等设备除尘。
[0004] 烟气脱硫技术主要分为干法、半干法和湿法三大类。其中干法和半干法脱硫的效 率低,燃料变化时难以达到环保要求,湿法脱硫,效率较高,完全能达到环保要求,且对HF 和HCl等酸性气体完全吸收。
[0005] 烟气脱氮(脱硝)技术主要包括催化还原法、液体吸收法和固体吸附法等三类措 施。催化还原法包含非选择性催化还原法和选择性催化还原法两种,前者用NH3作还原剂 将NHx催化还原为N2,烟气中的氧很少与NH3反应,因此放热量小,后者用CH4、H2、CO及其 它燃料气体作为还原剂与NOx进行催化还原反应,废气中的氧参加反应,因此放热量大。液 体吸收法包含水吸收法、稀硝酸吸收法、碱性溶液吸收法、氧化-吸收法、吸收-还原法和 络合吸收法六种,其中水吸收法用水作吸收剂对NOx进行吸收,吸收效率低,仅可用于气量 小、净化要求不高的场合,不能净化NO含量较大的烟气;稀硝酸吸收法用稀硝酸作吸收剂 对NOx进行物理吸收与化学吸收,吸收效率高,但消耗动力较大;碱性溶液吸收法用NaOH、 Na2CO3^ Ca (OH) 2、NH4OH等碱溶液作吸收剂对NOx进行化学吸收,对于含NO较多的烟气净化 效率低;氧化-吸收法对于含NO较多的烟气用浓硝酸、03、KMnO4等作氧化剂,先将NO部分 氧化成NO2,然后再用碱溶液吸收,使净化效率提高;吸收-还原法将NOx吸收至溶液中,与 (NH4)2SO3^ (NH4)HSO3^ Na2SO3等还原剂反应,NOx被还原为N2,净化效率较好;络合吸收法利 用络合吸收剂I^eSOp !^ (II)-EDTA及!^ (II)-EDTA-Na2SO3等直接同NO反应,NO生成的络 合物加热时重新释放出N0,从而使NO能回收。固体吸附法才用丝光沸石分子筛、泥煤、风化 煤等吸附废气中的NOx从而起到脱硝的作用。
[0006] 燃煤锅炉、玻璃窑炉等各种窑炉排出的高温、高污染性烟气中,含有大量的粉尘、 硫氧化合物和氮氧化合物,如果直接排放,会对大气造成严重危害,目前,国家制订的排放 标准日益严格,规定烟气排放必须达到一定标准才能排放至大气中。而现有的大多数烟气 净化装置的功能相对比较单一,例如以上所述的各种烟气净化方式主要用于去除粉尘、硫 氧化物或者氮氧化物中的一种有害物质,因此综合处理能力较差,如果用于处理燃煤锅炉 或玻璃窑炉等排放的高温、高污染性烟气,则治理效率尚待提高,难以达到排放标准。
实用新型内容
[0007] 本实用新型要解决的主要技术问题是,提供一种综合处理能力强、净化效率高的烟气综合处理系统。
[0008] 为解决上述技术问题,本实用新型提供一种烟气综合处理系统,包括依次连接的 文丘里脱硫除尘器、一体反应器和吸附器;所述文丘里脱硫除尘器包括烟气进入管、文丘里 管和吸收塔,所述文丘里管一端与所述烟气进入管连通,另一端与所述吸收塔连通,所述吸 收塔与所述一体反应器连通。
[0009] 所述烟气进入管内设置至少一排喷淋方向与烟气的进入方向相逆的降温喷头。
[0010] 优选地,所述烟气进入管水平延伸,所述文丘里管竖直延伸,且所述文丘里管的上 端与所述烟气进入管连通,下端与所述吸收塔连通。
[0011] 所述吸收塔可为立式吸收塔。
[0012] 优选地,所述吸收塔内设有至少一排喷淋方向向下的碱液喷头。
[0013] 一种实施例中,所述一体反应器包括腔体,所述腔体两端分别设置用于连通所述 文丘里脱硫除尘器的进烟口,和用于连通所述吸附器的出烟口 ;所述腔体内的底部包括碱 液容置区,所述碱液容置区的上方设有用于烟气通过的喉口、以及第一反应腔和第二反应 腔,所述第一反应腔与所述第二反应腔之间通过所述喉口相互连通,所述进烟口和出烟口 分别位于所述第一反应腔和第二反应腔的顶部。
[0014] 优选地,所述吸附器包括分别工作在主备模式下的主用吸附器和备用吸附器。
[0015] 一种实施方式中,所述吸附器内设有至少一个用于支撑吸附剂床层的吸附剂下料 透气斗,所述吸附剂下料透气斗自上而下缩口设置,其底部设有向下通往所述吸附器外部 的出料管,所述出料管上安装锁气器。
[0016] 进一步地,所述吸附器顶部设有吸附剂进料口,两个相对的侧壁上分别设有进烟 口和出烟口 ;所述进烟口位于所述吸附剂下料透气斗下方,所述出烟口位于所述吸附剂下 料透气斗与所述吸附剂进料口之间。
[0017] 还包括与所述吸附器相连的烟囱,以及连接在所述烟囱与所述吸附器之间的引风 机。
[0018] 本实用新型的有益效果是:本实用新型烟气综合处理系统具有良好的除尘、脱硫、 脱硝综合处理能力,净化效率高,尤其适用于燃煤锅炉或玻璃窑炉等排放的高温、高污染性 烟气的净化处理。
附图说明
[0019] 图1为本实用新型一种实施例的烟气综合处理系统示意图;
[0020] 图2为本实用新型一种实施例的文丘里脱硫除尘器示意图;
[0021] 图3为图2中烟A-A方向的截面图。
具体实施方式
[0022] 下面通过具体实施方式结合附图对本实用新型作进一步详细说明。
[0023] 请参考图1,本实施例的烟气综合处理系统包括依次连接的文丘里脱硫除尘器1、 一体反应器2、吸附器3、引风机4和烟囱5。其中,如图2和图3所示,文丘里脱硫除尘器1 由烟气进入管11、文丘里管14和吸收塔15连接形成,文丘里管14的一端与烟气进入管11 连通,另一端与吸收塔15连通。[0024] 本实施例的文丘里脱硫除尘器1中,烟气进入管11水平延伸,文丘里管14竖直延 伸,且文丘里管14的上端与进入管11连通,下端与吸收塔15连通使烟气从上向下流动。吸 收塔15采用立式吸收塔,不仅便于对烟气进行有效脱硫处理,而且节省了空间,布局更加 合理。当然各个组成部分的延伸方向和连接位置也可根据具体需要进行设置。
[0025] 燃煤锅炉或玻璃窑炉等设备的高温烟气首先通过烟气进入管11进入文丘里脱硫 除尘器1进行处理,烟气进入管11内设置至少一排降温喷头12,其喷淋方向与烟气的进入 方向相逆,能够喷出碱性液体或者水,与烟气发生热交换后对其进行有效降温以便后续处 理。例如,来自玻璃窑炉的400°C的烟气在烟气进入管11中实现降温处理后,温度可降至 180 "C。
[0026] 文丘里管14的中部具有缩口状的喉部13,使冲入文丘里管14的烟气在喉部13产 生低压,这个低压使流入的高速烟气切向喷出文丘里管14并进入吸收塔15中并产生较大 的离心力。吸收塔15内设有至少一排喷淋方向向下的碱液喷头16,高速烟气中的尘粒被不 断喷入的碱液浸湿,并在离心力的作用下脱离烟气;同时,烟气与吸收塔15内碱液形成的 水雾大界面接触,形成气液两相之间的传质,使烟气中的硫氧化物与碱性雾液发生充分的 中和反应,同时脱出大部分重金属以及HCI,HF气体,烟气的温度进一步降低后,通过烟气 出口 17进入一体反应器2。吸收塔15内分离的尘粒落在吸收塔5底部,吸收硫氧化物的碱 液也落在底部并被排出回收。
[0027] —体反应器2包括一个较大的腔体,腔体两端分别设置用于连通文丘里脱硫除尘 器1的进烟口,和用于连通吸附器3的出烟口。腔体内的底部包括碱液容置区,能够容纳一 定量的碱液。碱液容置区的上方设有喉口、和由隔板隔开的第一反应腔、第二反应腔,第一 反应腔与第二反应腔之间通过隔板底部的喉口相互连通,进烟口和出烟口分别位于第一反 应腔和第二反应腔的顶部。经文丘里脱硫除尘器1进行初步处理的烟气从进烟口进入一体 反应器2后,高速向下冲入碱液,并在喉口处改变运动方向而形成湍流,这一过程中,烟气 与碱液产生的水滴充分接触,烟气中的硫氧化物、氮氧化物等再次与碱液发生中和反应而 被去除,同时进一步减少了烟气中的尘粒。
[0028] 吸附器3利用包含具有强吸附能力的活性炭等物质对烟气进行进一步净化处理, 在吸附器3中,活性炭颗粒堆积成可供烟气透过的吸附剂床层作为脱硫吸附剂和脱硝催化 剂,首先将烟气中的有害物质吸附在活性炭的内表面,再在内表面上活性点的催化作用下, 将SA催化氧化为S03,并进一步与水合成硫酸储存在活性炭的微孔中。NOx在活性炭催化 作用下与加入的NH3反应生成无害物质N2和H2O ;烟气在穿过吸附剂床层的过程中,粉尘被 活性炭颗粒过滤清除。吸附器3可设置一个,为了方便使用,也可包括分别工作在主备模式 下的主用吸附器和备用吸附器,两个吸附器3都通过阀门与一体反应器2相连,当主用吸 附器发生故障或者需要检修时,关闭其阀门,并打开备用吸附器的阀门使其与一体反应器2 连通。
[0029] 根据需要,吸附器3可灵活选用对流式或者错流式吸附器,一种实例例中,吸附器 3内设有至少一个用于支撑吸附剂床层的吸附剂下料透气斗,吸附剂下料透气斗自上而下 缩口设置,其底部设有向下通往吸附器3外部的出料管,出料管上还安装允许吸附剂通过 而避免漏气的锁气器。对于对流式吸附器,吸附器3的两个相对的侧壁上分别设有进烟口 和出烟口 ;进烟口位于吸附剂下料透气斗下方,出烟口位于吸附剂下料透气斗与吸附剂进料口之间,烟气从吸附器3底部向上流动,透过吸附剂下料透气斗与活性炭进行吸附反应, 新鲜的活性炭从吸附器3顶部的吸附剂进料口输入,使吸附剂床层中的活性炭的吸附量由 下向上依次减小,达到饱和的活性炭首先通过出料管排出,能够实现均勻的补料和排料,不 仅提高了活性炭的利用率,减小了循环量,而且由于吸附剂床层的厚度均勻,对烟气形成均 勻的阻力,显著提高了净化效率。
[0030] 经吸附器3处理的烟气经引风机4引出,并通过烟囱5排出大气。
[0031] 据测试,本实施例烟气综合处理系统的除尘效率> 99%,脱硫率> 95%,脱硝效 率>65%,可广泛用于多种工业领域的废气治理,尤其适用于处理燃煤锅炉或玻璃窑炉等 排放的高温、高污染性烟气,能够对其中的各种有害物质进行综合处理,治理效率高。
[0032] 以上内容是结合具体的实施方式对本实用新型所作的进一步详细说明,不能认定 本实用新型的具体实施只局限于这些说明。对于本实用新型所属技术领域的普通技术人员 来说,在不脱离本实用新型构思的前提下,还可以做出若干简单推演或替换,都应当视为属 于本实用新型的保护范围。
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