CN105709585A - 一种双塔高效湿法脱硫装置 - Google Patents
一种双塔高效湿法脱硫装置 Download PDFInfo
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- CN105709585A CN105709585A CN201610054487.0A CN201610054487A CN105709585A CN 105709585 A CN105709585 A CN 105709585A CN 201610054487 A CN201610054487 A CN 201610054487A CN 105709585 A CN105709585 A CN 105709585A
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- desulfurizing tower
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- 239000002002 slurries Substances 0.000 claims abstract description 119
- 230000003647 oxidation Effects 0.000 claims abstract description 88
- 238000007254 oxidation reactions Methods 0.000 claims abstract description 88
- 229910052602 gypsum Inorganic materials 0.000 claims abstract description 58
- 239000010440 gypsum Substances 0.000 claims abstract description 58
- 239000003570 air Substances 0.000 claims abstract description 50
- UGFAIRIUMAVXCW-UHFFFAOYSA-N carbon monoxide Chemical compound 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- 239000003546 flue gases Substances 0.000 claims abstract description 34
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- 230000003009 desulfurizing Effects 0.000 claims description 128
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- OKTJSMMVPCPJKN-UHFFFAOYSA-N carbon Chemical compound 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[C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 5
- 238000000034 methods Methods 0.000 description 5
- 230000033116 oxidation-reduction process Effects 0.000 description 4
- 238000004140 cleaning Methods 0.000 description 3
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- GBAOBIBJACZTNA-UHFFFAOYSA-L Calcium sulfite Chemical compound 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- 229910002089 NOx Inorganic materials 0.000 description 1
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound 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- LSNNMFCWUKXFEE-UHFFFAOYSA-M bisulfite Chemical compound 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- 239000007787 solids Substances 0.000 description 1
- NINIDFKCEFEMDL-UHFFFAOYSA-N sulfur Chemical compound 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[S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 1
- 235000011149 sulphuric acid Nutrition 0.000 description 1
- 239000001117 sulphuric acid Substances 0.000 description 1
- 230000001131 transforming Effects 0.000 description 1
- 238000010792 warming Methods 0.000 description 1
Classifications
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—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
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/46—Removing components of defined structure
- B01D53/48—Sulfur compounds
- B01D53/50—Sulfur oxides
- B01D53/501—Sulfur oxides by treating the gases with a solution or a suspension of an alkali or earth-alkali or ammonium compound
- B01D53/502—Sulfur oxides by treating the gases with a solution or a suspension of an alkali or earth-alkali or ammonium compound characterised by a specific solution or suspension
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—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
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/46—Removing components of defined structure
- B01D53/48—Sulfur compounds
- B01D53/50—Sulfur oxides
- B01D53/501—Sulfur oxides by treating the gases with a solution or a suspension of an alkali or earth-alkali or ammonium compound
- B01D53/504—Sulfur oxides by treating the gases with a solution or a suspension of an alkali or earth-alkali or ammonium compound characterised by a specific device
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2258/00—Sources of waste gases
- B01D2258/02—Other waste gases
- B01D2258/0283—Flue gases
Abstract
本发明公开了一种双塔高效湿法脱硫装置，它包括SO2吸收系统、浆液供应系统、氧化空气系统及石膏脱水系统四个子系统；其中，SO2吸收系统由结构相同的主脱硫塔和副脱硫塔构成，主脱硫塔和副脱硫塔为串联连接，主脱硫塔和副脱硫塔共用一套浆液供应系统和氧化空气系统，副脱硫塔的石膏浆液输送到主脱硫塔内，主脱硫塔的石膏通过石膏脱水系统排出塔外。本发明具有脱硫效率高、适用范围广、运行稳定及方便维护检修等特点。通过本脱硫装置净化后的烟气能够满足国家日益严格的SO2超低排放标准，同时通过将废弃的氧化空气与净化烟气隔离，有利于提高后续CO2净化系统的捕获效率。
Description
技术领域
[0001 ]本发明涉及烟气处理技术领域，尤其涉及一种双塔高效湿法脱硫装置。
背景技术
[0002]随着工业的快速发展，酸雨等大气环境问题日益突出，严重威胁人类生命健康和财产安全。近年来，酸雨问题引起广大民众的极大关注，国家环保法规及政策对烟气302的排放限值要求日益严格，如《火电厂大气污染物排放标准》(GB13223-2011)进一步降低了燃煤电厂大气污染物的排放限值，其中重点控制地区，要求302排放限制为50mg/m3;《煤电节能减排升级与改造行动计划(2014〜2020年)》要求东部地区新建燃煤机组302排放基本达到燃气轮机组污染物排放限值，即基准氧含量6 %条件下，SO2排放浓度不高于35mg/m3，同时对中部和西部地区也提出了要求。
[0003] 石灰石一石膏湿法脱硫工艺因其技术成熟稳定且脱硫效率高而广泛应用于烟气脱硫。目前工业上应用的主流技术是单塔喷淋脱硫系统，随着国家环保法规及政策对烟气SO2排放要求的逐步落实，对于中高含硫煤燃烧烟气，要求系统的脱硫效率必须高于98%，有时甚至要求脱硫效率高于99%才能使烟气达标排放，此时采用单塔喷淋脱硫系统很难保证如此高的脱硫效率。而且，单塔喷淋脱硫系统内部结构简单，部分烟气容易沿塔壁直接流出系统外，形成烟气短路导致脱硫效率降低。此外，单塔喷淋脱硫系统内的喷淋浆液直接掉落到塔底的浆液池中，当锅炉燃烧工况发生改变，如烟气含氧量升高或SO2浓度降低时，尽管停止浆液池内部的氧化空气供应，烟气中的氧足以使浆液中的亚硫酸发生过度氧化，使浆液氧化还原电位高于设计值。当浆液氧化还原电位高于设计值时，将会导致石膏着色、浆液PH测量仪器故障、喷嘴堵塞、石膏脱水机堵塞等系列故障，影响系统的稳定运行。
[0004]全球气候变暖是人类面临的另外一个严峻问题，中国电力行业CO2排放量约占全国总排放量的一半左右，因此，推进电力行业碳减排对中国实现碳减排目标和绿色循环生产具有重要的意义。CO2捕获和封存技术可以减少火力发电站80 %〜95 %的0)2排放量，是国际上公认的拥有巨大减排潜力的技术。目前应用的湿法脱硫系统普遍采用强制氧化法，浆液池排出的氧化空气被初期溶解于浆液中的C02、H20、Hg、N0x、S02等气体饱和。当锅炉采用富氧燃烧方式时，燃烧产物中的CO2含量将达到75%〜90%以上，若浆液池排出的废弃氧化空气混入到烟气中，将高浓度CO2气流稀释，会导致后续CO2净化系统的捕获效率下降。
[0005]综上所述，为使排放烟气满足日益严格的502排放标准以及利于CO2捕获和封存技术的应用，需对现有脱硫系统进行提效改造。
发明内容
[0006]本发明所要解决的技术问题是提供一种双塔高效湿法脱硫装置，该装置的脱硫效率高、能满足302排放标准以及能提高后续CO2净化系统的捕获效率。
[0007]本发明以如下技术方案解决上述技术问题:
[0008]本发明一种双塔高效湿法脱硫装置，它包括SO2吸收系统、浆液供应系统、氧化空气系统及石膏脱水系统四个子系统;其中，SO2吸收系统由结构相同的主脱硫塔和副脱硫塔构成，主脱硫塔和副脱硫塔为串联连接，主脱硫塔和副脱硫塔共用一套浆液供应系统和氧化空气系统，副脱硫塔的石膏浆液输送到主脱硫塔内，主脱硫塔的石膏通过石膏脱水系统排出塔外。
[0009]进一步地，所述主脱硫塔和副脱硫塔的塔体从上至下分别依次设有烟气出口、除雾器、喷淋层、集液槽、烟气入口、氧化风隔离板、浆液池;浆液池与喷淋层之间由浆液循环管连接，并在浆液循环管上设有浆液循环栗;所述烟气出口连接湿式电除尘器，湿式电除尘器连接CO2捕集系统。
[0010]进一步地，所述集液槽呈螺旋状设置，并沿主脱硫塔和副脱硫塔的内壁安装，集液槽的最低点处设置有液体流出口，液体流出口经管道与浆液池相连通，通过集液槽将沿塔壁直接流下的浆液收集并排回浆液池，同时对浆液进行辅助搅拌。
[0011]进一步地，所述集液槽以向上环绕角度为3°〜6°的坡度进行设置，沿塔内壁环绕一周。
[0012]进一步地，所述氧化风隔离板设置在烟气入口下方、浆液池液位上方，将氧化空气系统从下方喷入的氧化空气与烟气进行隔离。
[0013]进一步地，所述氧化风隔离板为平板或波纹板，以1:0.596〜1:0.565的锥度由塔壁向塔中心倾斜，中心设置有喷淋浆液下降管，下降管的插入深度低于氧化空气的喷入点。
[0014]进一步地，所述氧化风隔离板的侧边分别设置一个氧化空气出口，废弃的氧化空气经氧化空气出口排出并经碱液处理后排入大气中。
[0015]进一步地，所述主脱硫塔和副脱硫塔分别设置有检修旁路，检修旁路上设置检修阀；主脱硫塔的检修旁路一端连接主脱硫塔的烟气入口，另一端连接副脱硫塔的烟气入口，副脱硫塔的检修旁路一端连接副脱硫塔的烟气出口，另一端接入主脱硫塔的检修旁路，并与主脱硫塔的烟气出口相连通。
[0016]进一步地，所述浆液供应系统由浆液箱、浆液箱搅拌器、浆液栗组成;浆液箱中的吸收浆液经浆液栗分两路输出，一路输送至主脱硫塔的浆液池，另一路输送至副脱硫塔的浆液池，主脱硫塔和副脱硫塔的浆液池之间设置连通管路，以维持两个塔的浆液池液位平衡。
[0017]进一步地，所述氧化空气系统由氧化风机、氧化喷嘴、侧进式搅拌器组成;氧化喷嘴和侧进式搅拌器设置在主脱硫塔和副脱硫塔的浆液池内，氧化风机的输出管路分两路，一路输送至主脱硫塔的氧化喷嘴，另一路输送至副脱硫塔的氧化喷嘴。
[0018]进一步地，所述石膏脱水系统由石膏排出栗、旋流器、真空皮带脱水机、石膏输送管路及石膏浆液输送栗构成；主脱硫塔和副脱硫塔的浆液池下部分别连接石膏排出栗，石膏排出栗分别连接旋流器，旋流器的稀浆液输出返回至浆液池，接副脱硫塔的旋流器的浓浆液输出至主脱硫塔的浆液池，接主脱硫塔的旋流器的浓浆液输出至真空皮带脱水机经脱水处理后排放，主脱硫塔和副脱硫塔的浆液池之间设有石膏输送管路，并在该管路上设有石膏浆液输送栗。
[0019]本发明的有益效果是:
[0020] 1.本发明采用主塔与副塔二级串联的脱硫系统，延长烟气与脱硫浆液的接触时间，提高整体脱硫效率，适用范围广，能够满足燃料含硫量高及锅炉负荷波动大的烟气脱硫要求。
[0021] 2.相比于单塔脱硫系统，本发明采用主塔与副塔二级串联，当双塔中的某一个出现临时故障需检修时可以通过另外一个进行脱硫，而单塔系统出现故障时必须停止整个脱硫系统的运行方可进行检修。
[0022] 3.本发明主塔和副塔喷淋层下方沿塔壁四周分别设置环状集液槽，沿塔壁直接流下的浆液经集液槽的收集后返回到各自的浆液池中，对浆液池中的浆液进行辅助搅拌，可节省浆液池侧进式搅拌器电耗的1/3左右;此外，集液槽的设置可以聚拢烟气向塔体中心的有效喷淋区域流动，有效防止烟气沿塔壁流出造成的烟气短路，从而提高脱硫效率。
[0023] 4.本发明主塔和副塔浆液池液位上方设置氧化风隔离板，喷淋浆液下落时先与氧化风隔离板接触碰撞再进入浆液池，液滴携带的氧气在碰撞的过程中被除去，当烟气含氧量降低或SO2浓度降低时，浆液的自然氧化不影响系统的氧化还原电位，即消除了自然氧化对强制氧化系统的影响，脱硫系统运行稳定，易生成高品质的石膏副产物。
[0024] 5.本发明主塔和副塔浆液池液位上方设置氧化风隔离板，可以有效隔离氧化空气进入到处理烟气中，降低净化后烟气的氧含量；当采用富氧燃烧时，高浓度CO2因与氧化空气隔离而不被稀释，有利于提高后续CO2净化系统的捕获效率。
附图说明
[0025]图1为本发明的结构不意图；
[0026]图2为集液槽的俯视结构示意图；
[0027]图3为集液槽的主视结构示意图。
[0028]图中:
[0029] A、主脱硫塔;B、副脱硫塔；1、主塔浆液循环栗;2、主塔浆液循环管;3、主塔喷淋层；
4、主塔除雾器;5、主塔烟气入口 ；6、主塔烟气出口；7、副塔烟气入口 ；8、副塔烟气出口；9、湿式电除尘器；10、原烟气；11、连通管道；12、主塔石膏排出栗；13、主塔旋流器；14、主塔旋流器稀浆液；15、主塔旋流器浓浆液；16、真空皮带脱水机；17、副塔浆液循环栗；18、副塔浆液循环管；19、副塔喷淋层;20、副塔除雾器;21、副塔石膏排出栗;22、副塔旋流器;23、副塔旋流器浓浆液；24、副塔旋流器稀浆液；25、石膏浆液输送栗；26、浆液箱；27、浆液箱搅拌器；28、浆液栗;29、浆液供应管道;30、氧化风机;31、氧化空气管道;32、主塔氧化喷嘴;33、副塔氧化喷嘴;34、主塔侧进式搅拌器;35、副塔侧进式搅拌器;36、主塔浆液池;37、副塔浆液池；38、主塔氧化风隔离板;39、副塔氧化风隔离板;40、主塔喷淋浆液下降管;41、副塔喷淋浆液下降管;42、主塔氧化空气出口； 43、副塔氧化空气出口； 44、主塔集液槽;45、主塔集液槽液体流出口；46、副塔集液槽;47、副塔集液槽液体流出口；48、浆液池连通管路;49、石膏输送管路;50、主塔检修旁路;51、副塔检修旁路;52、CO2捕集系统。
具体实施方式
[0030]下面结合附图及具体实施例对本发明的技术方案做进一步的阐述。为使附图简洁，图中仅示意性的表示出与本发明相关的部分，而且图中具有相同结构或功能的部件，仅示意性的标示出了其中的一个。
[0031]如图1所示，本发明双塔高效湿法脱硫装置，包括SO2吸收系统、浆液供应系统、氧化空气系统及石膏脱水系统四个子系统；其中，SO2吸收系统由结构相同的主脱硫塔A和副脱硫塔B构成，主脱硫塔A和副脱硫塔B为串联连接，主脱硫塔和副脱硫塔共用一套浆液供应系统和氧化空气系统，副脱硫塔的石膏浆液输送到主脱硫塔内，主脱硫塔的石膏通过石膏脱水系统排出塔外。
[0032]主脱硫塔的宽度为副脱硫塔的1.1倍左右，主脱硫塔的塔体从上至下分别依次设有主塔烟气出口 6、主塔除雾器4、主塔喷淋层3、主塔集液槽44、主塔烟气入口 5、主塔氧化风隔离板38、主塔浆液池36，主塔浆液池36与主塔喷淋层3之间由主塔浆液循环管2连接，并在主塔浆液循环管2上设有主塔浆液循环栗I。副脱硫塔的塔体从上至下分别依次设有副塔烟气出口 8、副塔除雾器20、副塔喷淋层19、副塔集液槽46、副塔烟气入口、副塔氧化风隔离板39、副塔浆液池37，副塔浆液池37与副塔喷淋层19之间由副塔浆液循环管18连接，并在副塔浆液循环管18上设有副塔浆液循环栗17。主脱硫塔A和副脱硫塔B的烟气出口经管路汇集后连接湿式电除尘器9，湿式电除尘器9连接⑶2捕集系统52，C02捕集系统52处理后经烟囱排放。
[0033]如图2和图3所示，本发明采用的主塔集液槽44和副塔集液槽46均呈螺旋状排布，并以向上环绕角度为3°〜6°的坡度进行设置，沿塔内壁环绕一周固定安装。主塔集液槽44和副塔集液槽46在最低点处分别设置有主塔集液槽液体流出口 45和副塔集液槽液体流出口47，主塔集液槽液体流出口 45和副塔集液槽液体流出口47分别经管道与主塔浆液池36和副塔浆液池37相连通，集液槽用于收集沿塔壁直接流下的浆液以及阻止烟气沿塔壁流动，收集的浆液沿着浆液池内浆液旋转的切线方向返回至浆液池中，辅助维持浆液的旋转与搅拌，降低浆液侧进搅拌器的能耗。
[0034]本发明采用的主塔氧化风隔离板38和副塔氧化风隔离板39分别设置在主塔烟气入口 5和副塔烟气入口 7的下方、浆液池液位上方，将氧化空气系统从下方喷入的氧化空气与烟气进行隔离。
[0035]采用的主塔氧化风隔离板38和副塔氧化风隔离板39可为平板或波纹板，以1:
0.596〜1: 0.565的锥度由塔壁向塔中心倾斜，主塔氧化风隔离板38和副塔氧化风隔离板39的中心分别设置有主塔喷淋浆液下降管40和副塔喷淋浆液下降管41，下降管的插入深度低于氧化空气的喷入点。喷淋层落下的浆液首先与氧化空气隔离板碰撞，增强喷淋液中溶解氧气的释放，以消除烟气中的氧对浆液池氧化还原电位的影响，接着降落的浆液从氧化空气隔离板中心的浆液下降管进入到浆液池中，与喷入的氧化空气接触混合后，浆液中的亚硫酸钙被氧化生成石膏。
[0036]主塔氧化风隔离板38和副塔氧化风隔离板39的侧边分别设置有主塔氧化空气出口 42和副塔氧化空气出口 43，废弃的氧化空气经氧化空气出口排出并经碱液处理后排入大气中。
[0037]本发明装置工作时，原烟气10经主塔烟气入口 5进入主脱硫塔内部，主脱硫塔内部设置4层喷淋层3，循环浆液的停留时间为4.5〜5.5min，通过主塔浆液循环喷淋可脱除原烟气中65〜80%的S02，未达到排放标准的烟气通过主塔除雾器4除雾后由主塔烟气出口 6排出主塔，接着经连通管道11进入到副脱硫塔中；副脱硫塔内部设置2层喷淋层19，循环浆液的停留时间为4.5〜5.5min，烟气在副脱硫塔内与循环喷淋楽液接触进一步脱除剩余S02的90〜98%，净化达标后的烟气经副塔除雾器20除雾及湿式电除尘器9进一步脱除硫酸烟雾和细颗粒物后，进入到CO2捕集系统52脱除C02，最后通过烟囱排入大气。
[0038]本发明在主脱硫塔和副脱硫塔的侧边分别设置有主塔检修旁路50和副塔检修旁路51，主塔检修旁路50和副塔检修旁路51上设置有检修阀。主塔检修旁路50—端连接主脱烟气入口 5，另一端连接副塔烟气入口 7，副塔检修旁路51—端连接副塔烟气出口 8，另一端接入主塔检修旁路50，并与主塔烟气出口 6之间通过连通管道11连接。
[0039]当主脱硫塔出现临时故障时，为了便于对主脱硫塔进行临时检修，烟气通过主塔检修芳路50直接进入副脱硫塔内脱硫，当副脱硫塔出现临时故障时，为了便于对副脱硫塔进行临时检修，烟气经主脱硫塔脱硫后由副塔检修旁路51直接进入到湿式电除尘器9中。
[0040]本发明所述的浆液供应系统由浆液箱26、浆液箱搅拌器27、浆液栗28及浆液供应管道29组成;浆液箱26中的吸收浆液通过浆液栗28抽出并分两路由浆液供应管道29输送至浆液池36和浆液池37中以补充脱硫系统浆液，补充的浆液量根据主脱硫塔与副脱硫塔中浆液的PH值来调节;主脱硫塔与副脱硫塔的浆液池中部设置连通管路48，以维持二塔浆液池液位平衡。
[0041]本发明所述的氧化空气系统由氧化风机30、主脱硫塔的氧化喷嘴32和副脱硫塔的氧化喷嘴33、主脱硫塔的侧进式搅拌器34和副脱硫塔的侧进式搅拌器35以及氧化空气管道31组成;来自氧化风机30的氧化空气经氧化空气管道31分别输送至安装在浆液池中部的氧化喷嘴32和氧化喷嘴33，经氧化喷嘴连续喷入浆液池中，并通过安装在氧化喷嘴附近的侧进式搅拌器34和侧进式搅拌器35搅拌，以进一步加强氧化空气的扩散，促进浆液中亚硫酸钙的氧化。
[0042]本发明所述的石膏脱水系统由主塔石膏排出栗12和副塔石膏排出栗21、主塔旋流器13和副塔旋流器22、真空皮带脱水机16、石膏浆液管道49及石膏浆液输送栗25构成;主塔石膏排出栗12和副塔石膏排出栗21分别安装在主脱硫塔和副脱硫塔的浆液池下部，主塔石膏排出栗12和副塔石膏排出栗21分别连接主塔旋流器13和副塔旋流器22，副塔旋流器22的稀浆液输出返回至副脱硫塔的浆液池，副塔旋流器22的浓浆液输出至主脱硫塔的浆液池，主塔旋流器13的稀浆液输出返回至主脱硫塔的浆液池，主塔旋流器13的浓浆液输出至真空皮带脱水机16。
[0043]工作时，副脱硫塔的石膏浆液通过副塔石膏排出栗21输送至副塔旋流器22，副塔旋流器22分离的稀浆液经管道24返回至副塔浆液池37，浓浆液经管道23输送至主塔浆液池36，主脱硫塔与副脱硫塔的底部设置石膏输送管路49，通过石膏浆液输送栗21将副塔浆液池底部的石膏浆液输送至主塔浆液池底部;主脱硫塔的石膏浆液通过主塔石膏排出栗12输送至主塔旋流器13，主塔旋流器分离的稀浆液经管道14返回至主塔浆液池36，浓浆液经管道15输送至真空皮带脱水机16进一步浓缩脱水，最终得到固含率大于90%的石膏副产物。
[0044]以上所述之实施例只是本发明的较佳实施方式而己，并非用来限制本发明实施范围，如权利要求书所记载的内容，在不脱离本发明主要思想情况下进行的各种变更，均包括于本发明申请专利范围内。
Claims (11)
1.一种双塔高效湿法脱硫装置，其特征在于:它包括SO2吸收系统、浆液供应系统、氧化空气系统及石膏脱水系统四个子系统;其中，SO2吸收系统由结构相同的主脱硫塔和副脱硫塔构成，主脱硫塔和副脱硫塔为串联连接，主脱硫塔和副脱硫塔共用一套浆液供应系统和氧化空气系统，副脱硫塔的石膏浆液输送到主脱硫塔内，主脱硫塔的石膏通过石膏脱水系统排出塔外。
2.根据权利要求1所述的双塔高效湿法脱硫装置，其特征在于:所述主脱硫塔和副脱硫塔的塔体从上至下分别依次设有烟气出口、除雾器、喷淋层、集液槽、烟气入口、氧化风隔离板、浆液池;浆液池与喷淋层之间由浆液循环管连接，并在浆液循环管上设有浆液循环栗；所述烟气出口连接湿式电除尘器，湿式电除尘器连接CO2捕集系统。
3.根据权利要求2所述的双塔高效湿法脱硫装置，其特征在于:所述集液槽呈螺旋状设置，并沿主脱硫塔和副脱硫塔的内壁安装，集液槽的最低点处设置有液体流出口，液体流出口经管道与浆液池相连通，通过集液槽将沿塔壁直接流下的浆液收集并排回浆液池，同时对浆液进行辅助搅拌。
4.根据权利要求3所述的双塔高效湿法脱硫装置，其特征在于:所述集液槽以向上环绕角度为3°〜6°的坡度进行设置，沿塔内壁环绕一周。
5.根据权利要求2所述的双塔高效湿法脱硫装置，其特征在于:所述氧化风隔离板设置在烟气入口下方、浆液池液位上方，将氧化空气系统从下方喷入的氧化空气与烟气进行隔离。
6.根据权利要求5所述的双塔高效湿法脱硫装置，其特征在于:所述氧化风隔离板为平板或波纹板，以1: 0.596〜1: 0.565的锥度由塔壁向塔中心倾斜，中心设置有喷淋浆液下降管，下降管的插入深度低于氧化空气的喷入点。
7.根据权利要求5所述的双塔高效湿法脱硫装置，其特征在于:所述氧化风隔离板的侧边分别设置一个氧化空气出口，废弃的氧化空气经氧化空气出口排出并经碱液处理后排入大气中。
8.根据权利要求2所述的双塔高效湿法脱硫装置，其特征在于:所述主脱硫塔和副脱硫塔分别设置有检修旁路，检修旁路上设置检修阀；主脱硫塔的检修旁路一端连接主脱硫塔的烟气入口，另一端连接副脱硫塔的烟气入口，副脱硫塔的检修旁路一端连接副脱硫塔的烟气出口，另一端接入主脱硫塔的检修旁路，并与主脱硫塔的烟气出口相连通。
9.根据权利要求1所述的双塔高效湿法脱硫装置，其特征在于:所述浆液供应系统由浆液箱、浆液箱搅拌器、浆液栗组成;浆液箱中的吸收浆液经浆液栗分两路输出，一路输送至主脱硫塔的楽■液池，另一路输送至副脱硫塔的楽■液池，主脱硫塔和副脱硫塔的楽■液池之间设置连通管路，以维持两个塔的浆液池液位平衡。
10.根据权利要求1所述的双塔高效湿法脱硫装置，其特征在于:所述氧化空气系统由氧化风机、氧化喷嘴、侧进式搅拌器组成;氧化喷嘴和侧进式搅拌器设置在主脱硫塔和副脱硫塔的浆液池内，氧化风机的输出管路分两路，一路输送至主脱硫塔的氧化喷嘴，另一路输送至副脱硫塔的氧化喷嘴。
11.根据权利要求1所述的双塔高效湿法脱硫装置，其特征在于:所述石膏脱水系统由石膏排出栗、旋流器、真空皮带脱水机、石膏输送管路及石膏浆液输送栗构成;主脱硫塔和副脱硫塔的浆液池下部分别连接石膏排出栗，石膏排出栗分别连接旋流器，旋流器的稀浆液输出返回至浆液池，接副脱硫塔的旋流器的浓浆液输出至主脱硫塔的浆液池，接主脱硫塔的旋流器的浓浆液输出至真空皮带脱水机经脱水处理后排放，主脱硫塔和副脱硫塔的浆液池之间设有石膏输送管路，并在该管路上设有石膏浆液输送栗。
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