CN101579602B - 一种节能高品质硫酸铵回收的氨法脱硫工艺 - Google Patents
一种节能高品质硫酸铵回收的氨法脱硫工艺 Download PDFInfo
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- CN101579602B CN101579602B CN2009101468573A CN200910146857A CN101579602B CN 101579602 B CN101579602 B CN 101579602B CN 2009101468573 A CN2009101468573 A CN 2009101468573A CN 200910146857 A CN200910146857 A CN 200910146857A CN 101579602 B CN101579602 B CN 101579602B
- Authority
- CN
- China
- Prior art keywords
- ammonia
- ammonium
- ammonium sulfate
- flue gas
- desulfurizing tower
- Prior art date
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- QGZKDVFQNNGYKY-UHFFFAOYSA-N ammonia Chemical compound data:image/svg+xml;base64,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 data:image/svg+xml;base64,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 N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 title claims abstract description 35
- 238000000034 methods Methods 0.000 title claims abstract description 28
- BIGPRXCJEDHCLP-UHFFFAOYSA-N Ammonium bisulfate Chemical compound 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[NH4+].OS([O-])(=O)=O BIGPRXCJEDHCLP-UHFFFAOYSA-N 0.000 title claims abstract description 20
- 230000003009 desulfurizing Effects 0.000 claims abstract description 94
- UGFAIRIUMAVXCW-UHFFFAOYSA-N carbon monoxide Chemical compound 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[O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims abstract description 51
- 239000003546 flue gases Substances 0.000 claims abstract description 47
- PQUCIEFHOVEZAU-UHFFFAOYSA-N Ammonium sulfite Chemical compound 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[NH4+].[NH4+].[O-]S([O-])=O PQUCIEFHOVEZAU-UHFFFAOYSA-N 0.000 claims abstract description 44
- 235000011114 ammonium hydroxide Nutrition 0.000 claims abstract description 31
- 239000000047 products Substances 0.000 claims abstract description 15
- 238000002425 crystallisation Methods 0.000 claims abstract description 9
- 238000001035 drying Methods 0.000 claims abstract description 9
- 238000001914 filtration Methods 0.000 claims abstract description 7
- VHUUQVKOLVNVRT-UHFFFAOYSA-N ammonium hydroxide Chemical compound data:image/svg+xml;base64,PD94bWwgdmVyc2lvbj0nMS4wJyBlbmNvZGluZz0naXNvLTg4NTktMSc/Pgo8c3ZnIHZlcnNpb249JzEuMScgYmFzZVByb2ZpbGU9J2Z1bGwnCiAgICAgICAgICAgICAgeG1sbnM9J2h0dHA6Ly93d3cudzMub3JnLzIwMDAvc3ZnJwogICAgICAgICAgICAgICAgICAgICAgeG1sbnM6cmRraXQ9J2h0dHA6Ly93d3cucmRraXQub3JnL3htbCcKICAgICAgICAgICAgICAgICAgICAgIHhtbG5zOnhsaW5rPSdodHRwOi8vd3d3LnczLm9yZy8xOTk5L3hsaW5rJwogICAgICAgICAgICAgICAgICB4bWw6c3BhY2U9J3ByZXNlcnZlJwp3aWR0aD0nMzAwcHgnIGhlaWdodD0nMzAwcHgnIHZpZXdCb3g9JzAgMCAzMDAgMzAwJz4KPCEtLSBFTkQgT0YgSEVBREVSIC0tPgo8cmVjdCBzdHlsZT0nb3BhY2l0eToxLjA7ZmlsbDojRkZGRkZGO3N0cm9rZTpub25lJyB3aWR0aD0nMzAwJyBoZWlnaHQ9JzMwMCcgeD0nMCcgeT0nMCc+IDwvcmVjdD4KPHRleHQgZG9taW5hbnQtYmFzZWxpbmU9ImNlbnRyYWwiIHRleHQtYW5jaG9yPSJzdGFydCIgeD0nMTYuODk4JyB5PScxNTcuMjYnIHN0eWxlPSdmb250LXNpemU6NDBweDtmb250LXN0eWxlOm5vcm1hbDtmb250LXdlaWdodDpub3JtYWw7ZmlsbC1vcGFjaXR5OjE7c3Ryb2tlOm5vbmU7Zm9udC1mYW1pbHk6c2Fucy1zZXJpZjtmaWxsOiM0Mjg0RjQnID48dHNwYW4+Tkg8L3RzcGFuPjx0c3BhbiBzdHlsZT0nYmFzZWxpbmUtc2hpZnQ6c3ViO2ZvbnQtc2l6ZTozMHB4Oyc+NDwvdHNwYW4+PHRzcGFuPjwvdHNwYW4+PHRzcGFuIHN0eWxlPSdiYXNlbGluZS1zaGlmdDpzdXBlcjtmb250LXNpemU6MzBweDsnPis8L3RzcGFuPjx0c3Bhbj48L3RzcGFuPjwvdGV4dD4KPHRleHQgZG9taW5hbnQtYmFzZWxpbmU9ImNlbnRyYWwiIHRleHQtYW5jaG9yPSJlbmQiIHg9JzI4OC44ODQnIHk9JzE1Ni42JyBzdHlsZT0nZm9udC1zaXplOjQwcHg7Zm9udC1zdHlsZTpub3JtYWw7Zm9udC13ZWlnaHQ6bm9ybWFsO2ZpbGwtb3BhY2l0eToxO3N0cm9rZTpub25lO2ZvbnQtZmFtaWx5OnNhbnMtc2VyaWY7ZmlsbDojRTg0MjM1JyA+PHRzcGFuPkhPPC90c3Bhbj48dHNwYW4gc3R5bGU9J2Jhc2VsaW5lLXNoaWZ0OnN1cGVyO2ZvbnQtc2l6ZTozMHB4Oyc+LTwvdHNwYW4+PHRzcGFuPjwvdHNwYW4+PC90ZXh0Pgo8L3N2Zz4K data:image/svg+xml;base64,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 [NH4+].[OH-] VHUUQVKOLVNVRT-UHFFFAOYSA-N 0.000 claims abstract description 6
- 239000000706 filtrates Substances 0.000 claims abstract description 6
- BFNBIHQBYMNNAN-UHFFFAOYSA-N Ammonium sulfate Chemical compound 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N.N.OS(O)(=O)=O BFNBIHQBYMNNAN-UHFFFAOYSA-N 0.000 claims description 84
- 229910052921 ammonium sulfate Inorganic materials 0.000 claims description 83
- 235000011130 ammonium sulphate Nutrition 0.000 claims description 83
- 238000006477 desulfuration reactions Methods 0.000 claims description 35
- 238000007254 oxidation reactions Methods 0.000 claims description 32
- 230000003647 oxidation Effects 0.000 claims description 28
- 239000010410 layers Substances 0.000 claims description 20
- 230000008929 regeneration Effects 0.000 claims description 20
- 238000006243 chemical reactions Methods 0.000 claims description 16
- 238000005507 spraying Methods 0.000 claims description 15
- 238000003860 storage Methods 0.000 claims description 12
- ZETCGWYACBNPIH-UHFFFAOYSA-N azane;sulfurous acid Chemical compound 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- 230000002745 absorbent Effects 0.000 description 1
- 239000002250 absorbents Substances 0.000 description 1
- 238000010521 absorption reactions Methods 0.000 description 1
- 239000002253 acids Substances 0.000 description 1
- 238000005273 aeration Methods 0.000 description 1
- -1 after discharging Chemical compound 0.000 description 1
- 239000003905 agrochemicals Substances 0.000 description 1
- 239000003513 alkali Substances 0.000 description 1
- OKTJSMMVPCPJKN-UHFFFAOYSA-N carbon Chemical compound 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Abstract
Description
一种节能高品质硫酸铵回收的氨法脱硫工艺技术领域
[0001] 本发明涉及环保领域大气污染治理脱硫技术,尤其涉及一种节能高品质硫酸铵回 收的氨法脱硫工艺。背景技术
[0002] 近年来,我国二氧化硫年排放量达2000万吨以上,居全球首位,已是仅次于欧洲 和北美的第三大酸雨区。对二氧化硫如不加以控制,将造成城市大气污染加剧。因此,控制 二氧化硫排放已成为社会和经济可持续发展的迫切要求,治理二氧化硫势在必行。
[0003] 以煤或石油为燃料的锅炉或火力发电厂,以及以铁矿石为原料的钢铁厂烧结机排 放大量烟道气,烟气中SA含量通常较低,在300〜5000ppmV(1000〜15000毫克/标准立 方米)之间,但是,烟气量十分巨大。以燃煤锅炉而论,蒸汽规模从lT/h到2500T/h,发电机 组容量6丽到900MW,烟气量由1万Nm3/h到250万Nm3/h,已产生了严重的酸雨和污染。 锅炉烟气脱硫被认为是控制SO2排放行之有效的途径。目前,国内外的烟气脱硫技术主要有 干法和湿法两类。干法脱硫主要有石灰——石灰石抛弃法、循环流化床脱硫;湿法脱硫主要 有石灰石——石膏法脱硫、双碱法、氧化镁碱法、氨碱法等。氨法脱硫技术的原理是采用氨 水作为脱硫吸收剂,氨水和烟气中的反应,得到亚硫酸铵,亚硫酸铵通过用空气氧化,得 到硫酸铵,硫酸铵溶液经蒸发结晶,离心机分离脱水,干燥器干燥后即可制得硫酸铵产品。 很显然氨法脱硫技术与石灰石——石膏法脱硫和双碱法脱硫技术相比是一个“绿色技术”, 它以废弃的烟气,低廉的水和空气为原料,生产比石膏更高价值的硫酸铵化肥,无废渣废液 排放,不产生二次污染,无新增污染源,生产过程中脱硫塔不易结垢堵塞,无疑具有更好的 经济和环保效益。
[0004] 目前,通常所采用的氨法脱硫技术为氨——肥法脱硫技术,其采用氨水作为脱硫 剂,在脱硫塔内循环液PH < 6的酸性条件下,用循环泵使硫酸铵与亚硫酸铵溶液与烟气中 的SA反应,脱除SA生成副产物亚硫酸氢铵和亚硫酸铵,在脱硫塔下部利用空气曝气的方 法将亚硫酸按和亚硫酸氢铵氧化成硫酸铵,硫酸铵溶液排出后经过滤、蒸发、离心、干燥后 生产出硫酸铵晶体包装入库,完成脱硫及硫酸铵产品的回收过程。
[0005] 该方法存在着以下缺陷:
[0006] 1)循环液中含有对SO2有吸收作用的亚硫酸铵的同时,也含有大量的硫酸铵成分, 而硫酸铵对没有吸收能力,因此造成大量硫酸铵溶液参与空循环。一方面造成循环泵 动力的大量消耗,增加运行的成本;另一方面,由于大量硫酸铵溶液的循环与烟气接触,造 成净化脱硫后排放的烟气温度损失严重,排烟温度过低(< 50°c ),含水饱和的低温烟气长 期会对烟®造成严重腐蚀损害,不得不采取在脱硫后的烟气增加GGH再加热系统进行升温 到80°C左右再进入烟@,结果造成投资和运行成本的进一步加大。
[0007] 2)该技术将脱硫后产物亚硫酸铵氧化成硫酸铵是在脱硫塔内进行,由于脱硫产物 中含有大量的硫酸铵,而大量硫酸铵的存在阻碍亚硫酸铵的氧化,氧化率达到80〜90%很 困难,因此造成后级回收的硫酸铵产品中含有大量没有经过氧化的亚硫酸铵成分;硫酸铵产品作为农用化肥或复合肥的原料,具有肥效;而亚硫酸铵产品则没有任何肥效,若用于农 田,会出现烧苗,造成事故,后果严重,因此,此方法回收的硫酸铵产品品质较低。
[0008] 3)该技术方法对脱硫后产物硫酸铵溶液中水分的去除是采用常规的蒸发干燥的 方法,需要消耗大量的蒸气能源,平均每吨水蒸发约需要2吨的蒸气;按照现成本价计算约 需要100元的蒸气费用,对于大型电站锅炉长期运行的成本是一笔庞大的开支,因此,此技 术提取副产物硫酸按的运行成本很高,能耗大。发明内容
[0009] 本发明的目的是克服现有技术中的不足,提供一种节能高品质硫酸铵回收的氨法 脱硫工艺,工艺流程设计合理,占地面积小,投资小,脱硫效率高,同时还能脱除一部分氮, 回收的硫酸铵含量高,几乎不含(NH4)2SO3成分,经济价值可观,实现环保治理的“变废为 宝”,并且本工艺在脱硫的同时没有二次污染。
[0010] 本发明采用了以下技术方案:
[0011] 所述的节能高品质硫酸铵回收的氨法脱硫工艺:采用氨水作为脱硫剂,氨水与烟 气充分脱硫后生成亚硫酸铵,将亚硫酸铵在塔内强制氧化生成硫酸铵,将硫酸铵溶液过滤 除去杂质,滤液在脱硫塔内与高温烟气接触换热,使烟气降温的同时,硫酸铵溶液升温饱 和,饱和硫酸铵溶液结晶一段时间后,经离心脱水干燥制成高品质硫酸铵。
[0012] 其特征在于,包括下列工序:
[0013] ①在氨水储罐(10)内配置氨水,通过供氨泵(11)将配好的氨水送入再生储槽 ⑶;
[0014] ②再生槽(8)中的氨水经循环泵(9)及喷淋层(¾送入脱硫塔(1);
[0015] ③将除尘后的高温烟气送入脱硫塔(1),同时硫酸铵储槽(14)的稀硫酸铵溶液经 硫酸铵循环泵(1¾送入冷却喷淋层(27),雾化后在脱硫塔烟气入口与高温烟气接触换热, 烟气降温后经分布板(4)进入脱硫塔吸收段进行后续脱硫,硫酸铵溶液被高温烟气蒸发浓 缩至饱和状态后集中在脱硫塔结晶段下部的倒锥形结晶池(¾中,由高压硫酸铵泵02)送 入旋液分离器(16)中进行固液分离;
[0016] ④烟气进入脱硫塔吸收段后,与由喷淋层(¾喷入的雾化氨水接触进行脱硫,反 应生成亚硫酸氢铵,亚硫酸氢铵经溢流口 08)流入再生槽(8)中,与通过供氨泵(11)送入 的过量氨水反应,生成亚硫酸铵,再生槽(8)中的亚硫酸铵和氨水混合液由亚硫酸铵循环 泵(9)送入脱硫塔(1)内的喷淋层(5),被雾化的亚硫酸铵和氨水的混合液与烟气中的SO2 反应,进行脱硫反应,并生成硫酸氢铵,如此循环;
[0017] ⑤再生槽(8)内亚硫酸铵液经亚硫酸铵供给泵送入脱硫塔(1)内的氧化槽 (3)中,氧化风机(1¾经过曝气装置(1¾向氧化槽鼓入空气将亚硫酸铵强制充分氧化一段 时间后生成硫酸铵;
[0018] ⑥氧化生成的硫酸铵由溶液泵03)送入过滤缓冲槽(M),再由过滤进料泵05) 送入真空过滤机06)过滤,除去灰尘杂质,滤液送入硫酸铵储槽(14);
[0019] ⑦饱和硫酸铵溶液结晶一段时间后,由高压硫酸铵泵0¾送入旋液分离器(16) 中进行固液分离,分离出的硫酸铵晶体进入离心分离机(17)脱水后,再送入干燥器(18)中 干燥即为成品硫酸铵产品;[0020] ⑧脱硫后的烟气经折板式除雾器(6)除去水雾,然后通过丝网除雾器(7)除去气 溶胶,最后由脱硫塔烟气出口送入烟®达标排放。
[0021] 所述的脱硫塔(1)内部自下而上依次为:氧化槽(3)、倒锥形结晶池O)、分布板 G)、喷淋层(5)、折板除雾器(6)、丝网除雾器(7);其中氧化槽C3)底部设有曝气装置。
[0022] 所述的③中在脱硫塔结晶池内硫酸铵溶液停留时间大于lh。
[0023] 所述的⑤中亚硫酸铵溶液的pH值控制在5. 0〜6. 0。
[0024] 所述的⑤中亚硫酸铵溶液氧化时间为1〜池。
[0025] 所述的⑤中,离心分离机脱出的水中含有少量硫酸铵,将该硫酸铵溶液送入硫酸 铵储槽(14)中。
[0026] 由于采用了上述技术方案,与现有技术相比,本发明的有益效果是:脱硫效率高, 同时能够脱除部分氮;在废气中SO2达标排放的同时,氨的逃逸可以低于5ppm以下,没有废 水排放,产生的副产物为高含量的晶体硫酸铵产品,几乎不含(NH4)2SO3,设备少,占地面积 小,投资小,具有可观的经济价值,实现环保治理的“变废为宝”。本工艺技术在脱硫的同时 没有“废水、废渣”等二次污染;硫酸铵产品回收综合运行成本极低,产生可观的“正效益”, 满足循环经济的发展要求。附图说明
[0027] 图1所示为采用本发明节能高品质硫酸铵回收的湿式氨法脱硫工艺的系统及流 程示意图。
[0028] 图中标号:
[0029] 1-脱硫塔 2- 倒锥形结晶池 3- 氧化槽
[0030] 4-分布板 5- 喷淋层 6- 折板除雾器
[0031] 7-丝网除雾器 8- 再生槽 9- 亚硫酸铵循环泵
[0032] 10-氨水储槽 11- -供氨泵 12- -氧化风机
[0033] 13-曝气装置 14- -硫酸铵储槽 15- -硫酸铵循环泵
[0034] 16-旋液分离器 17- -离心脱水机 18- -干燥器
[0035] 19-加热器 20- -风机 21- -亚硫酸铵供给泵
[0036] 22-高压硫酸铵泵 23- -溶液泵 24- -过滤缓冲槽
[0037] 25-过滤进料泵 26- -过滤机 27- -冷却喷淋层
[0038] 溢流口 29- -烟囱 具体实施方式
[0039] 下面参照图1给出具体实施例。
[0040] 实施例1
[0041] 一台220T/h的燃煤热电锅炉,烟气量为270000Nm3/h,SO2含量1500mg/Nm3,烟气 含尘量为80mg/Nm3,烟气温度为140°C。脱硫塔(1)的直径为6m,高为^m。如图1所示的 一种节能高品质硫酸铵回收的氨法脱硫工艺,在氨水储罐(10)内配置4%左右的氨水,通 过供氨泵(11)将配好的氨水送入再生槽(8);再生槽(8)中的氨水经亚硫酸铵循环泵(9) 及喷淋层(¾送入脱硫塔(1);同时硫酸铵储槽(14)的4%左右的硫酸铵溶液经硫酸铵循环泵(1¾送入冷却喷淋层(27),雾化后在脱硫塔烟气入口与高温烟气接触换热,烟气降温 后经分布板(4)进入脱硫塔吸收段进行后续脱硫,硫酸铵溶液被高温烟气蒸发浓缩至饱和 状态后(浓度约为45% )集中在脱硫塔结晶段下部的倒锥形结晶池O)中,由高压硫酸铵 泵0¾送入旋液分离器(16)中进行固液分离;烟气进入脱硫塔(1)后,与由喷淋层(5)喷 入的雾化氨水接触进行脱硫,反应生成亚硫酸氢铵,亚硫酸氢铵经溢流口 08)流入再生槽(8)中,与通过供氨泵(11)送入的过量氨水反应,生成亚硫酸铵,再生槽(8)中的亚硫酸铵 和氨水混合液由循环泵(9)送入脱硫塔(1)内的喷淋层(5),被雾化的亚硫酸铵和氨水的 混合液与烟气中的SO2K应,进行脱硫反应,并生成硫酸氢铵,如此循环;再生槽(8)内亚硫 酸铵液浓度控制在4%〜5%,pH值为5. O〜6. 0,经亚硫酸铵供给泵送入脱硫塔(1) 内的氧化槽(3)中,氧化风机(1¾经过曝气装置(1¾向氧化槽鼓入空气将亚硫酸铵溶液 强制充分氧化池后生成硫酸铵。氧化生成的硫酸铵溶液由溶液泵送入过滤缓冲槽 (M),再由过滤进料泵0¾送入真空过滤机06)过滤,除去灰尘杂质,滤液送入硫酸铵储 槽(14);在倒锥形结晶槽中饱和硫酸铵溶液的浓度控制在45%〜46%,pH值控制在2. 5〜 3.0,结晶Ih后,由高压硫酸铵泵02)送入旋液分离器(16)中进行固液分离,分离出的硫 酸铵晶体进入离心分离机(17)脱水后生成含水率为3%的硫酸铵晶体,再送入干燥器(18) 中干燥为含水率为0. 5%成品硫酸铵产品。脱硫后的烟气经折板式除雾器(6)除去水雾,然 后通过丝网除雾器(7)除去气溶胶,最后由脱硫塔烟气出口送入烟@达标排放,脱硫效率 98%,氨的逃逸< 5ppm。
[0042] 实施例2
[0043] 一台670T/h的火力发电机组,即200MW,烟气量为800000Nm7n,SO2含量4200mg/ Nm3,烟气含尘量为200mg/Nm3,烟气温度为145°C。脱硫塔(1)的直径为10m,高为30m。如图 1所示的一种节能高品质硫酸铵脱硫回收的氨法脱硫工艺,在氨水储罐(10)内配置5%左 右的氨水,通过供氨泵(11)将配好的氨水送入再生槽(8);再生槽(8)中的氨水经循环泵(9)及喷淋层(¾送入脱硫塔(1);同时硫酸铵储槽(14)的5%左右的硫酸铵溶液经循环泵 (15)送入冷却喷淋层(27),被雾化的硫酸铵溶液在脱硫塔烟气入口与高温烟气接触换热, 烟气降温后经分布板(4)进入脱硫塔吸收段进行后续脱硫,硫酸铵溶液被高温烟气蒸发浓 缩至饱和状态后(浓度约为47%)集中在脱硫塔结晶段下部的倒锥形结晶池O)中;烟气 进入脱硫塔(1)后,与由喷淋层(¾喷入的雾化氨水接触进行脱硫,反应生成亚硫酸氢铵, 亚硫酸氢铵经溢流口 08)流入再生槽(8)中,与通过供氨泵(11)送入的过量氨水反应,生 成亚硫酸铵,再生槽(8)中的亚硫酸铵和氨水混合液由循环泵(9)送入脱硫塔(1)内的喷 淋层(5),被雾化的亚硫酸铵和氨水的混合液与烟气中的SO2K应生成硫酸氢铵,如此循环; 再生槽(8)内亚硫酸铵液浓度控制在5%左右,pH值为5. 8〜6. 0,经亚硫酸铵供给泵Ql) 送入脱硫塔⑴内的氧化槽⑶中,氧化风机(12)经过曝气装置(13)向氧化槽鼓入空气 将亚硫酸铵溶液强制充分氧化池后生成硫酸铵。氧化生成的硫酸铵溶液由溶液泵03)送 入过滤缓冲槽(M),再由过滤进料泵0¾送入真空过滤机06)过滤,除去灰尘杂质,滤液 送入硫酸铵储槽(14);在倒锥形结晶槽中饱和硫酸铵溶液的浓度控制在47%左右,pH值控 制在2. 5〜3. 0,结晶Ih后,由高压硫酸铵泵02)送入旋液分离器(16)中进行固液分离, 分离出的硫酸铵晶体进入离心分离机(17)脱水后生成含水率为3%的硫酸铵晶体,再送入 干燥器(18)中干燥即为含水率为0.2%成品硫酸铵产品。脱硫后的烟气经折板式除雾器(6)除去水雾,然后通过丝网除雾器(7)除去气溶胶,最后由脱硫塔烟气出口送入烟囱达标 排放,脱硫效率97%,氨的逃逸< 5ppm。
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