CN106955586A - 一种燃煤烟气的多污染物协同控制的超低排放处理系统 - Google Patents
一种燃煤烟气的多污染物协同控制的超低排放处理系统 Download PDFInfo
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- CN106955586A CN106955586A CN201710122118.5A CN201710122118A CN106955586A CN 106955586 A CN106955586 A CN 106955586A CN 201710122118 A CN201710122118 A CN 201710122118A CN 106955586 A CN106955586 A CN 106955586A
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- UGFAIRIUMAVXCW-UHFFFAOYSA-N carbon monoxide Chemical compound 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[O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 title claims abstract description 73
- 239000003546 flue gases Substances 0.000 title claims abstract description 70
- 239000003344 environmental pollutants Substances 0.000 title claims abstract description 19
- 239000000428 dust Substances 0.000 claims abstract description 42
- 239000010410 layers Substances 0.000 claims abstract description 37
- 239000003054 catalysts Substances 0.000 claims abstract description 25
- 238000006477 desulfuration reactions Methods 0.000 claims abstract description 20
- 230000001131 transforming Effects 0.000 claims abstract description 16
- 238000005054 agglomeration Methods 0.000 claims abstract description 14
- 230000002776 aggregation Effects 0.000 claims abstract description 14
- 239000003570 air Substances 0.000 claims abstract description 9
- 239000000779 smoke Substances 0.000 claims abstract description 8
- QSHDDOUJBYECFT-UHFFFAOYSA-N mercury Chemical compound 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[Hg] QSHDDOUJBYECFT-UHFFFAOYSA-N 0.000 claims description 37
- 229910052753 mercury Inorganic materials 0.000 claims description 37
- 239000007789 gases Substances 0.000 claims description 12
- 239000003463 adsorbents Substances 0.000 claims description 10
- 238000002347 injection Methods 0.000 claims description 10
- 239000007924 injections Substances 0.000 claims description 10
- 238000005507 spraying Methods 0.000 claims description 9
- 239000011901 water Substances 0.000 claims description 7
- 230000002745 absorbent Effects 0.000 claims description 4
- 239000002250 absorbents Substances 0.000 claims description 4
- 239000004809 Teflon Substances 0.000 claims description 3
- 229910010250 TiO2—V2O5 Inorganic materials 0.000 claims description 3
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- 229920001343 polytetrafluoroethylenes Polymers 0.000 claims description 3
- 229910001886 silicon monoxide Inorganic materials 0.000 claims description 3
- 230000001869 rapid Effects 0.000 claims description 2
- 229910001890 sulfur dioxide Inorganic materials 0.000 abstract description 6
- RAHZWNYVWXNFOC-UHFFFAOYSA-N sulphur dioxide Chemical compound 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- 229910001385 heavy metals Inorganic materials 0.000 abstract description 3
- 239000002245 particles Substances 0.000 description 12
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- 239000004776 ESP Substances 0.000 description 1
- XHJBQVYOOVZIRA-UHFFFAOYSA-N [S+2].[O-2].[O-2].[Ti+4] Chemical compound 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- B01D53/34—Chemical or biological purification of waste gases
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- B01D53/02—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography
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Abstract
本发明提供一种燃煤烟气的多污染物协同控制的超低排放处理系统。包括沿烟气流向依次布置的：内部设有一协同脱汞催化剂层的脱硝反应器；一空预器；降低微细颗粒含量的一相变团聚装置；一除尘装置；具有湍流装置和二次除雾装置的一脱硫吸收塔。锅炉烟气首先进入具有协同脱汞功能的SCR脱硝反应器实现脱硝，然后通过团聚装置后再经过除尘器，最后进入脱硫除尘一体化装置，从而实现重金属汞、二氧化硫和粉尘的协同处理及超低排放。
Description
一种燃煤烟气的多污染物协同控制的超低排放处理系统
技术领域
[0001] 本发明涉及环境保护技术领域，尤其涉及燃煤烟气净化，具体涉及一种燃煤烟气 的多污染物协同控制的超低排放处理系统。
背景技术
[0002] 2014年9月三部委联合下发了《煤电节能减排升级与改造行动计划》，行动计划对 燃煤发电机组排放标准提出了新的要求。随后，各省又根据自身情况制定了相应的排放标 准。目前，燃煤火电厂进行超低排放改造已经成为了共识。
[0003] 目前，实现超低排放的关键是实现二氧化硫和粉尘的超低排放，为了实现二氧化 硫超低排放，需要增加喷淋层或者采用串塔技术，这种方法虽然可以提高脱硫效率，但是造 价比较高，尤其对于改造工程，实施难度较大。为了实现粉尘超低排放，现有技术增加了湿 式电除尘技术，该技术系统复杂，运行成本较高。
[0004] 在燃煤烟气处理设备中，现有脱硫除尘技术协同除尘效率低,通常在50-70%，因 此对脱硫吸收塔入口烟气中粉尘浓度要求比较高，需要增加额外设备或措施进行除尘处 理，否则，一旦入口烟气中的粉尘浓度超过3〇mg/Nm3，粉尘出口浓度就达不到5mg/Nm3以下的 要求，不符合排放标准。
[0005] 此外，燃煤烟气重金属汞污染也已经成为又一大社会关注热点。2011年，中国环境 保护部颁布的新版《火电厂大气污染物排放标准》规定，从2015年开始执行燃煤电厂烟气汞 排放限值30yg/m3的标准。
[0006] 利用现有污染物控制装置脱汞，即选择性催化还原脱硝装置(SCR)、电除尘器/布 袋除尘器(ESP/FF)和湿法脱硫装置(WFGD)等对烟气中各形态汞(气态元素态汞HgO (g)、气 态氧化态汞Hg2+ (g)、颗粒态汞Hg (p))实现不同程度的转化、富集和脱除;通常燃煤电厂污染 物控制装置对汞的协同脱除效率为40%。
[0007] 采用烟气喷射吸附剂脱汞，在空预器与除尘器之间设置专门脱汞吸附剂(活性炭 等)烟气喷射装置，吸附剂能够在2秒停留时间内高效吸附脱除烟气中汞蒸气，或将其催化 氧化成易于脱除的氧化态汞，最后由除尘器捕集脱汞后的吸附剂。烟气喷射脱汞是目前燃 煤电厂最实用的脱汞技术，效率可达90%以上，可满足美国的汞排放标准，但采用活性炭作 为吸附剂时，其成本高达2.5〜6.0万美元每脱除1镑烟气汞(〇.45kg)。如此高的运行成本在 中国恐难以推广。
[0008] 因此，本技术领域亟需对于现有燃煤烟气处理设备改进，使其具备协同处理功能， 并力求在一定程度上降低处理成本。
发明内容
[0009] 针对上述问题，本发明提供一种燃煤烟气的多污染物协同控制的超低排放处理系 统。锅炉烟气首先进入具有协同脱汞功能的SCR脱硝反应器实现脱硝，然后通过团聚装置后 再经过除尘器，最后进入脱硫除尘一体化装置，从而实现重金属汞、二氧化硫和粉尘的协同 处理及超低排放。
[0010]为达上述目的，本发明采取的具体技术方案是：
[0011] 一种燃煤烟气的多污染物协同控制的超低排放处理系统，包括沿烟气流向依次布 置的：
[0012] 一脱硝反应器，其内部设有一协同脱汞催化剂层，用以将通过的烟气中的零价汞 转化为二价汞；
[0013] —空预器；
[0014] 一相变团聚装置包括:依次连接的一入口整流段、一相变换热段及一出口段;所述 相变换热段内布置有换热器，用以供换热介质流通；
[0015] —除尘装置；
[0016] 一脱硫吸收塔，包括：
[0017]作为烟气通路的一塔体，具有一烟气入口及一烟气出口；
[0018] 在所述塔体内，沿烟气流向依次布置有:一湍流装置，用以使烟气通过之后形成湍 流状态;一喷淋层;一第一除雾层;一第二除雾层；
[0019] 其中，所述第一除雾层布置有若干层屋脊式除雾器，所述第二除雾层布置有旋流 式电除雾器；
[0020] 所述旋流式电除雾器包括多个二次除雾单元，每个所述二次除雾单元包括一阳极 筒体，所述阳极筒体具有一烟气进口，该烟气进口设有一旋流板;所述阳极筒体的中心固设 与其绝缘的极芯，所述极芯电连接一高压直流电源。
[0021] 进一步地，所述入口整流段设置有若干导流板，用以使通过入口整流段的烟气流 场均匀;所述相变换热段内的换热器为氟塑料换热器;所述换热介质为水。
[0022] 进一步地，所述除尘装置为电除尘器。
[0023] 进一步地，所述协同脱汞催化剂层布置有催化剂，所述催化剂选自添加Ce元素和 Zr元素的Si02-Ti02-V20_K剂或溴化物催化剂。
[0024]进一步地，所述空预器及除尘器之间设有喷射吸附装置，所述喷射吸附装置内设 有喷射汞吸附剂的喷头。
[0025]进一步地，所述湍流装置包括:沿烟气流量依次布置若干层管列，各管列中包括多 根平行布置的湍流管，任一管列中的各湍流管与其他管列中的湍流管平行交错或投影交 叉。
[0026] 进一步地，所述管列在其所在塔体的水平截面内的开孔率为65%-78%。
[0027]进一步地，所述高压直流电源连接一控制装置，该控制装置接入一控制系统。
[0028]进一步地，所述控制装置为一自动开关，所述控制系统为脱硫系统分布式控制系 统(DCS) 0
[0029]进一步地，所述湍流装置与喷淋层之间的距离为1.8-3.2米;所述第一除雾层与第 二除雾层之间的间距为1.2-2.5米。
[0030]通过采取上述技术方案，烟气进入相变团聚装置，经过换热后温度降低10-20度， 烟气体积减小，烟气粒径在团聚作用下变大，烟气比电阻增加，由于后续采用电除尘器，比 电阻降低可以提高电除尘器效率。颗粒粒径增大，可以提高除尘器以及脱硫吸收塔对细小 颗粒的捕集效率。而湍流装置和二次除雾结构，都可以进一步提高除尘效率，实现脱硫处理 过程中，实现协同除尘，可以保证二氧化硫达到超低排放标准，脱硫效率可以达到99.95 %， 且协同除尘效率高，能够是烟气含尘量降低至<5mg/Nm3;在脱硝反应器中利用汞催化剂将 零价汞氧化成二价汞从而在脱硫吸收塔中协同脱除，并且在经团聚处理后，二价汞也更易 在除尘装置及脱硫吸收塔中协同脱除，脱汞效率达84 • 2-93.1 %。并且，无需采用消耗较高 的湿式除尘器，运行成本较低，节能效果显著。
[0031]并且具有运行成本低的优点，要达到同样的除尘效果，传统工艺需增加额外的烟 气入口前除尘设备，与其相比，本发明能够使相关运行成本降低约4〇%。要达到同样的脱汞 效果，较好的工艺是采用活性炭作为吸附剂，与其相比，本发明能够将相关运行成本降低约 65% 〇
附图说明
[0032]图1为本发明一实施例中烟气处理系统的布置示意图。
[0033]图2为本发明一实施例中相变团聚装置的结构示意图。
[0034]图3为本发明一实施例中经图2所示的相变团聚装置团聚前后的烟气中颗粒粒径 分布示意图。
[0035]图4为本发明一实施例中脱硫吸收塔的结构示意图。
[0036]图5为本发明一实施例中二次除雾单元的结构示意图。
具体实施方式
[0037]下面将结合本发明实施例中的附图，对本发明实施例中的技术方案进行清楚、完 整的描述。
[0038]如图1所示，为一实施例中烟气后处理系统，包括沿烟气流向依次连接的：锅炉！、 SCR脱硝反应器2、空预器3、相变团聚装置4、除尘装置5、脱硫吸收塔6及烟囱7;
[0039]其中，SCR脱硝反应器2、空预器3、相变团聚装置4、除尘装置5及脱硫吸收塔6;共同 组合为燃煤烟气的多污染物协同控制的超低排放处理系统。
[0040]其中，脱硝反应器2为SCR脱硝反应器，其内部在设置常规脱硝催化剂的基础上，增 设有协同脱汞催化剂层21。协同脱汞催化剂层21布置有催化剂，催化剂选自添加Ce元素和 Zr元素的Si〇2-Ti〇2_V2〇5催化剂或溴化物催化剂。燃煤烟气中汞主要分为三种形式，一种为 零价汞，颗粒汞，和二价汞。零价汞不溶于水较难脱除。颗粒汞在经过除尘器时可以协同脱 除。二价汞溶于水，在湿法脱硫塔内可以脱除大部分。本实施例通过对脱汞催化剂进行改 性，提高汞氧化性能，将零价汞氧化成二价汞从而在湿法脱硫装置协同脱除，采用的改性催 化剂，能够提高催化剂汞氧化性能。改性后催化剂汞氧化能力提高30-40%，整体脱汞效率 达到80%以上，可以满足目前标准要求。
[0041]在另外的实施例中，空预器和除尘器之间增加一个喷射汞吸附剂的装置，效果最 好的是活性炭，但是成本较高，在一些烟气中汞含量极高或对于排放要求极高的运行环境 下，可考虑同步采用上述设置。
[0042]如图2所示，相变团聚装置4包括:依次连接的入口整流段41、相变换热段42及出口 段43;相变换热段42内布置有换热器，用以供换热介质流通;连通换热器两端的介质入口 44 及介质出口 45。入口整流段41设置有若干导流板，用以使通过入口整流段41的烟气流场均 匀;相变换热段42内的换热器为氟塑料换热器;换热介质为水。当然，在其他一些实施例中， 换热介质也可替换为其他，例如液态石蜡等。
[0043]如图4所示，脱硫吸收塔6，包括:作为烟气通路的塔体61，具有烟气入口 62及烟气 出口 67;在塔体ei内，沿烟气流向依次布置有:湍流装置63，用以使烟气通过之后形成湍流 状态;喷淋层64;第一除雾层65;第二除雾层66;
[0044]其中，第一除雾层65布置有若干层屋脊式除雾器，第二除雾层66布置有旋流式电 除雾器;旋流式电除雾器包括多个二次除雾单元，如图5所示，每个二次除雾单元包括阳极 筒体6价，阳极筒体册1具有一烟气进口，该烟气进口设有旋流板662;阳极筒体661的中心固 设与其绝缘的极芯663,极芯663电连接一高压直流电源（图未示）。高压直流电源连接一控 制装置，例如为自动开关，该控制装置接入一控制系统，例如为脱硫系统分布式控制系统 (DCS)。即可通过DCS实现根据系统负荷进行通断电的自动控制。
[0045]除尘装置5为电除尘器。
[0046]湍流装置63包括:沿烟气流量依次布置若干层管列，各管列中包括多根平行布置 的湍流管，任一管列中的各湍流管与其他管列中的湍流管平行交错或投影交叉。所述管列 在其所在塔体的水平截面内的开孔率为65%-78%。所述湍流管为圆形或类圆形。具体结构 可参考申请人已获得授权的相关系列专利（专利号：ZL 201420330458.9等），在此不再赘 述。
[0047]与申请人之前公开的专利相比，管列在其所在塔体的水平截面内的开孔率为 65 % -78 %，依据此开孔率，获得较佳的协同除尘及脱汞效果。
[0048] 此外，湍流装置与喷淋层之间的距离为1.8-3.2米。
[0049] 锅炉后排出的烟气首先进入SCR脱硝反应器，经过相变团聚装置，然后进入除尘装 置，除尘装置出口粉尘控制在30mg/Nm3，最后进入湿法脱硫装置即脱硫吸收塔，依次经过湍 流装置、喷淋层和高效除雾装置，然后通过烟囱排出。
[0050] 烟气流动过程中，相变团聚装置主要通过适当降低烟气温度，使烟气中液滴冷凝， 液滴附着在细小粉尘颗粒表面，从而实现粉尘颗粒团聚，增大大颗粒粉尘所占比例，如图3 所示，经团聚室团聚前后的烟气中颗粒粒径分布变化。图中横坐标为颗粒粒径，单位为M1， 纵坐标为相应粒径颗粒所占的百分比，团聚前的颗粒主要为lwn以下的小颗粒，团聚后曲线 波峰向右移动，lwii以上的颗粒占到总数的96%，表明颗粒长大效果显著，大颗粒更利于后 续电除尘器脱除。相变团聚的同时还能降低烟气比电阻，从而提高除尘器效率和脱硫塔协 同除尘效率。
[0051] 如上述实施例描述的处理提供，在SCR脱硝反应器中采用具有协同脱汞催化剂，用 以将烟气中的零价汞转化为二价汞，以提高湿法脱硫系统对二价汞的洗涤效率，在保证氮 氧化物实现超低排放的同时，提高汞氧化率，从而可以提高后续设备汞脱除能力。最终实现 脱汞效率达82• 2-90 • 1 %。同时，湍流装置和二次除雾的设置可以保证二氧化硫脱除效率 99.95 %以上，粉尘脱除效率83%以上。电除尘器主要对烟气中粉尘进行初步脱除，保证粉 尘浓度降到30mg/Nm3以内，可以为后续设备协同脱除粉尘提供基础。
[0052] 而脱硫吸收塔内增加了湍流装置，可以实现烟气均布和增加气液接触时间，从而 明显提高脱硫塔脱硫效率和协同除尘脱汞效果。旋流式电除雾装置可以提高协同除尘脱汞 性能。旋流式除雾装置分为上下两个区域，烟气由下而上，烟气入口处设置一个旋流式除雾 器，上部是湿式电除雾器。主要通过烟气量或者锅炉蒸发量确定高负荷或者低负荷，通常烟 气量或者锅炉蒸发量在额定70%以上算高负荷，70%以下认为低负荷。在负荷高的情况下， 阳极筒体下部的旋流板叶片引导高速烟气切向旋流，烟气旋流产生的离心力将雾滴和烟尘 甩到阳极筒体内表面，阳极筒体表面的液膜将这些雾滴捕获，捕获的粉尘雾滴随液膜掉入 下部吸收塔达到收尘的效果。在锅炉负荷低时，入口旋流装置不能达到最佳除尘效率时，以 自动控制方式开启直流高压电源，也可以通过人工操作实现电源开启与闭合。烟气经旋流 板进入阳极筒体后，烟气中的颗粒物和水滴中荷电带负离子，带负离子的这些颗粒物和雾 滴被吸引到带正电的收尘极上，当雾滴、颗粒被吸引到收尘极后，通过喷淋冲水，使其掉落 至下方脱硫塔内，从而达到<5mg/Nm3的收尘效果。该装置克服了单独采用旋流式除雾器和 单独采用湿式电除雾器的缺点，具有运行成本低、负荷适应性好等优点。并且随着液滴去除 率的提高，其中附着的二价汞也能够以较高的效率的被脱除，从而获得协同脱汞的效果。 [0053]实际工程应用表明，湍流装置和二次除雾的设置可以保证二氧化硫脱除效率 99 • 95 %以上，粉尘脱除效率83 %以上。
[0054] 显然，所描述的实施例仅是本发明一部分实施例，而不是全部的实施例。基于本发 明中的实施例，本领域普通技术人员在没有做出创造性劳动前提下所获得的所有其他实施 例，都属于本发明保护的范围。
Claims (10)
1. 一种燃煤烟气的多污染物协同控制的超低排放处理系统，其特征在于，包括沿烟气 流向依次布置的： 一脱硝反应器，其内部设有一协同脱汞催化剂层，用以将通过的烟气中的零价汞转化 为二价汞； 一空预器； 一相变团聚装置包括:依次连接的一入口整流段、一相变换热段及一出口段;所述相变 换热段内布置有换热器，用以供换热介质流通； 一除尘装置； 一脱硫吸收塔，包括： 作为烟气通路的一塔体，具有一烟气入口及一烟气出口； 在所述塔体内，沿烟气流向依次布置有:一湍流装置，用以使烟气通过之后形成湍流状 态;一喷淋层;一第一除雾层;一第二除雾层； 其中，所述第一除雾层布置有若干层屋脊式除雾器，所述第二除雾层布置有旋流式电 除雾器;所述旋流式电除雾器包括多个二次除雾单元，每个所述二次除雾单元包括一阳极 筒体，所述阳极筒体具有一烟气进口，该烟气进口设有一旋流板;所述阳极筒体的中心固设 与其绝缘的极芯，所述极芯电连接一高压直流电源。
2. 如权利要求1所述的燃煤烟气的多污染物协同控制的超低排放处理系统，其特征在 于，所述入口整流段设置有若干导流板，用以使通过入口整流段的烟气流场均匀;所述相变 换热段内的换热器为氟塑料换热器;所述换热介质为水。
3. 如权利要求1所述的燃煤烟气的多污染物协同控制的超低排放处理系统，其特征在 于，所述除尘装置为电除尘器。
4. 如权利要求1所述的燃煤烟气的多污染物协同控制的超低排放处理系统，其特征在 于，所述协同脱汞催化剂层布置有催化剂，所述催化剂选自添加Ce元素和Zr元素的Si02-Ti〇2_V2〇5催化剂或溴化物催化剂。
5. 如权利要求1所述的燃煤烟气的多污染物协同控制的超低排放处理系统，其特征在 于，所述空预器及除尘器之间设有喷射吸附装置，所述喷射吸附装置内设有喷射汞吸附剂 的喷头。
6. 如权利要求1所述的燃煤烟气的多污染物协同控制的超低排放处理系统，其特征在 于，所述湍流装置包括:沿烟气流量依次布置若千层管列，各管列中包括多根平行布置的湍 流管，任一管列中的各湍流管与其他管列中的湍流管平行交错或投影交叉。
7. 如权利要求6所述的燃煤烟气的多污染物协同控制的超低排放处理系统，其特征在 于，所述管列在其所在塔体的水平截面内的开孔率为65%_78%。
8. 如权利要求1所述的燃煤烟气的多污染物协同控制的超低排放处理系统，其特征在 于，所述高压直流电源连接一控制装置，该控制装置接入一控制系统。
9. 如权利要求8所述的燃煤烟气的多污染物协同控制的超低排放处理系统，其特征在 于，所述控制装置为一自动开关，所述控制系统为脱硫系统分布式控制系统。
10. 如权利要求1所述的燃煤烟气的多污染物协同控制的超低排放处理系统，其特征在 于，所述湍流装置与喷淋层之间的距离为丨.8—3.2米;所述第一除雾层与第二除雾层之间的 间距为1.2-2.5米。
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