CN205412654U - 一种烧结机烟气氨法h2o2氧化脱硝装置 - Google Patents
一种烧结机烟气氨法h2o2氧化脱硝装置 Download PDFInfo
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- CN205412654U CN205412654U CN201520944512.3U CN201520944512U CN205412654U CN 205412654 U CN205412654 U CN 205412654U CN 201520944512 U CN201520944512 U CN 201520944512U CN 205412654 U CN205412654 U CN 205412654U
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- spray gun
- flue gas
- ammonia
- oxidation
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- 238000000034 method Methods 0.000 title claims abstract description 49
- QGZKDVFQNNGYKY-UHFFFAOYSA-N ammonia Chemical compound data:image/svg+xml;base64,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 data:image/svg+xml;base64,PD94bWwgdmVyc2lvbj0nMS4wJyBlbmNvZGluZz0naXNvLTg4NTktMSc/Pgo8c3ZnIHZlcnNpb249JzEuMScgYmFzZVByb2ZpbGU9J2Z1bGwnCiAgICAgICAgICAgICAgeG1sbnM9J2h0dHA6Ly93d3cudzMub3JnLzIwMDAvc3ZnJwogICAgICAgICAgICAgICAgICAgICAgeG1sbnM6cmRraXQ9J2h0dHA6Ly93d3cucmRraXQub3JnL3htbCcKICAgICAgICAgICAgICAgICAgICAgIHhtbG5zOnhsaW5rPSdodHRwOi8vd3d3LnczLm9yZy8xOTk5L3hsaW5rJwogICAgICAgICAgICAgICAgICB4bWw6c3BhY2U9J3ByZXNlcnZlJwp3aWR0aD0nODVweCcgaGVpZ2h0PSc4NXB4JyB2aWV3Qm94PScwIDAgODUgODUnPgo8IS0tIEVORCBPRiBIRUFERVIgLS0+CjxyZWN0IHN0eWxlPSdvcGFjaXR5OjEuMDtmaWxsOiNGRkZGRkY7c3Ryb2tlOm5vbmUnIHdpZHRoPSc4NS4wJyBoZWlnaHQ9Jzg1LjAnIHg9JzAuMCcgeT0nMC4wJz4gPC9yZWN0Pgo8dGV4dCB4PSczNS4wJyB5PSc1My42JyBjbGFzcz0nYXRvbS0wJyBzdHlsZT0nZm9udC1zaXplOjIzcHg7Zm9udC1zdHlsZTpub3JtYWw7Zm9udC13ZWlnaHQ6bm9ybWFsO2ZpbGwtb3BhY2l0eToxO3N0cm9rZTpub25lO2ZvbnQtZmFtaWx5OnNhbnMtc2VyaWY7dGV4dC1hbmNob3I6c3RhcnQ7ZmlsbDojNDI4NEY0JyA+TjwvdGV4dD4KPHRleHQgeD0nNTEuMCcgeT0nNTMuNicgY2xhc3M9J2F0b20tMCcgc3R5bGU9J2ZvbnQtc2l6ZToyM3B4O2ZvbnQtc3R5bGU6bm9ybWFsO2ZvbnQtd2VpZ2h0Om5vcm1hbDtmaWxsLW9wYWNpdHk6MTtzdHJva2U6bm9uZTtmb250LWZhbWlseTpzYW5zLXNlcmlmO3RleHQtYW5jaG9yOnN0YXJ0O2ZpbGw6IzQyODRGNCcgPkg8L3RleHQ+Cjx0ZXh0IHg9JzY3LjAnIHk9JzYyLjknIGNsYXNzPSdhdG9tLTAnIHN0eWxlPSdmb250LXNpemU6MTVweDtmb250LXN0eWxlOm5vcm1hbDtmb250LXdlaWdodDpub3JtYWw7ZmlsbC1vcGFjaXR5OjE7c3Ryb2tlOm5vbmU7Zm9udC1mYW1pbHk6c2Fucy1zZXJpZjt0ZXh0LWFuY2hvcjpzdGFydDtmaWxsOiM0Mjg0RjQnID4zPC90ZXh0Pgo8L3N2Zz4K N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 title claims abstract description 43
- 238000005245 sintering Methods 0.000 title claims abstract description 39
- UGFAIRIUMAVXCW-UHFFFAOYSA-N carbon monoxide Chemical compound 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[O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 title claims abstract description 34
- 239000003546 flue gas Substances 0.000 title claims abstract description 34
- 238000007254 oxidation reaction Methods 0.000 title claims abstract description 33
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- 238000006243 chemical reaction Methods 0.000 claims abstract description 61
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- MWUXSHHQAYIFBG-UHFFFAOYSA-N nitric oxide Chemical compound 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O=[N] MWUXSHHQAYIFBG-UHFFFAOYSA-N 0.000 abstract description 11
- 229910052813 nitrogen oxide Inorganic materials 0.000 abstract description 3
- 239000000463 material Substances 0.000 abstract description 2
- NLXLAEXVIDQMFP-UHFFFAOYSA-N Ammonium chloride Substances 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[NH4+].[Cl-] NLXLAEXVIDQMFP-UHFFFAOYSA-N 0.000 abstract 1
- VHUUQVKOLVNVRT-UHFFFAOYSA-N ammonium hydroxide Chemical compound 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[NH4+].[OH-] VHUUQVKOLVNVRT-UHFFFAOYSA-N 0.000 abstract 1
- 235000011114 ammonium hydroxide Nutrition 0.000 abstract 1
- 229910000831 Steel Inorganic materials 0.000 description 8
- 239000010959 steel Substances 0.000 description 8
- 230000000694 effects Effects 0.000 description 7
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- 239000002994 raw material Substances 0.000 description 3
- 239000002253 acid Substances 0.000 description 2
- 238000004458 analytical method Methods 0.000 description 2
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- 238000001311 chemical methods and process Methods 0.000 description 2
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- ZAMOUSCENKQFHK-UHFFFAOYSA-N chlorine atom Chemical compound 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[Cl] ZAMOUSCENKQFHK-UHFFFAOYSA-N 0.000 description 2
- 150000001875 compounds Chemical class 0.000 description 2
- 238000010276 construction Methods 0.000 description 2
- 238000005260 corrosion Methods 0.000 description 2
- 238000000354 decomposition reaction Methods 0.000 description 2
- 239000003517 fume Substances 0.000 description 2
- 229910052742 iron Inorganic materials 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- 239000002184 metal Substances 0.000 description 2
- 229910052751 metal Inorganic materials 0.000 description 2
- 125000001477 organic nitrogen group Chemical group 0.000 description 2
- 150000002927 oxygen compounds Chemical class 0.000 description 2
- 238000011084 recovery Methods 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- 239000002912 waste gas Substances 0.000 description 2
- 239000002918 waste heat Substances 0.000 description 2
- CAMXVZOXBADHNJ-UHFFFAOYSA-N Ammonium nitrite Chemical compound 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Abstract
本实用新型公开了一种烧结机烟气氨法H2O2氧化脱硝装置,包括:一氧化剂双流体喷射装置,所述氧化剂双流体喷射装置包括一H2O2溶液储罐,一压缩空气储罐,以及一连通所述H2O2溶液储罐和压缩空气储罐的第一双流体喷枪和第二双流体喷枪;一反应吸收装置,所述反应吸收装置包括一反应氧化反应烟道,所述第一双流体喷枪从上端深入反应氧化反应烟道内;一进行氨吸收的绿色反应塔,所述反应氧化反应烟道通过管道将初处理的烧结机烟气送至一绿色反应塔的底部,所述第二双流体喷枪从侧端深入绿色反应塔内,且所述绿色反应塔的上端连接一设置有喷枪的氨水溶液储罐;以及一废物排放收集装置。本实用新型能够高效的降低烧结烟气氮氧化物排放,实现无污染零排放。
Description
技术领域
[0001] 本实用新型涉及氨法氧化脱硝技术领域,具体涉及一种烧结机烟气氨法H202氧化 脱硝装置。
背景技术
[0002] 大多数的工业烟气中含有N0X,它们大量排放到大气中,不仅形成酸雨,破坏臭氧 层,并造成温室效应导致全球变暖。钢铁行业作为国家工业的一个重要组成部分,国家对其 环保要求也日益严格。研究表明,钢铁行业中各种设备放出的N0 X总量在污染物排放固定发 生源中占第二位,仅次于S02的排放量。其中,烧结生产过程N0 X排放量约占钢铁行业N0X排放 总量的一半左右,随着钢铁企业的快速发展,烧结矿产量大幅度增加, N〇x排放量随之增大, 烧结厂环境保护的压力也随之增加。因此,对烧结机烟气N0X排放量的严格控制,在日益严 峻的环保压力下,逐渐提上环保工作日程。
[0003] 烧结过程是一个高温燃烧条件下的复杂物理化学过程,被抽入料层的空气与混合 料中的燃料发生燃烧反应,燃烧释放的热量保证烧结物理化学过程的进行,燃烧的烟气作 为废气排放。钢铁烧结行业中氮主要以硝酸盐和有机氮的形式存在,硝酸盐主要来自于铁 矿粉,而有机氮则主要来自于固体燃料。在烧结过程中以单质或化合物形式存在的氮通常 在氧化反应中以气态氧化物的形式释放,而以酸式盐形式存在的氮则在分解反应中以气态 氧化物的形式释放。
[0004] c
[0005] 目前,烟气中N0J兑除方式主要分为燃烧过程脱除和燃烧后脱除两种方式。燃烧脱 除技术主要为低N0X燃烧技术,包括低氮燃烧器,分级燃烧等。燃烧后脱除目前燃煤电厂采 用选择性催化还原法(SCR)和选择性非催化还原法(SNCR)。但针对于烧结行业,这些方法都 具有明显的不足和不适应性。烧结行业的燃烧器和燃烧分配方式具有其自身的特点,传统 的低氮燃烧器和分级燃烧技术不适用于烧结机行业。而烧结机后部烟道空间有限,无法布 置SCR工艺中的催化剂,且烧结烟气成分中重金属含量很高,极易造成催化剂失活;SNCR反 应温度窗口为850~1100 °C,此温度窗口在烧结行业中难以实现,因为在烧结机中,此温度 位于烧结机内部,由于其自身结构特点,不可能向烧结机内部喷入氨气。因此针对烧结机急 需开发新型的N0J兑除工艺,以确保其污染物排放符合环保相关规定。
[0006] 公布号为CN102343212A的中国实用新型专利中提到了一种臭氧与过氧化氢协同 氧化结合湿法吸收的脱硝工艺,采用臭氧与过氧化氢协同反应虽然能够增强两者的氧化 性,对于氮氧化物和硫氧化物的氧化脱除均有帮助,但臭氧与过氧化氢氧化氮氧化物反应 温度区间是不同的,同时反应难以达到很好的效果,并且该工艺会生成含硝酸盐废水,后续 处理极大增加成本。同时,臭氧的引入会增加制氧设备,臭氧发生器等一系列设备投资,运 行电耗也相当之高,极大降低了该工艺的经济性。
[0007] 公布号为CN103191634A的中国实用新型专利提到了一种低成本的氧化脱硝新工 艺,该工艺将石灰水和氯气为原料配制为氧化剂和吸收剂,氧化氮氧化物,利用碱液性质吸 收。该工艺虽然流程简单,操作费用较低,但存在较大的问题是喷入了大量氯气,氯离子腐 蚀将会对金属结构造成非常严重的腐蚀,在实际工程运用中几乎不具有可操作性。 实用新型内容
[0008] 本实用新型要解决的技术问题是提供一种烧结机烟气氨法H202氧化脱硝装置,能 够高效的降低烧结烟气氮氧化物排放,实现无污染零排放,良好适应烧结行业烟气成分复 杂;同时,通过合理控制反应发生条件,控制反应发生方式与过程,极大节约了H 2〇2用量,提 高工艺经济性。
[0009] 为达到上述目的,本实用新型的技术方案如下:
[0010] -种烧结机烟气氨法H202氧化脱硝装置,包括:
[0011] 一氧化剂双流体喷射装置,所述氧化剂双流体喷射装置包括一 H2〇2溶液储罐,一压 缩空气储罐,以及一连通所述H2〇 2溶液储罐和压缩空气储罐的第一双流体喷枪和第二双流 体喷枪,
[0012] -反应吸收装置,所述反应吸收装置包括一反应氧化反应烟道,所述第一双流体 喷枪从上端深入反应氧化反应烟道3内;
[0013] -进行氨吸收的绿色反应塔,所述反应氧化反应烟道通过管道将初处理的烧结机 烟气送至一绿色反应塔的底部,所述第二双流体喷枪从侧端深入绿色反应塔内,且所述绿 色反应塔的上端连接一设置有喷枪的氨水溶液储罐;
[0014]以及一废物排放收集装置,所述废物排放收集装置包括一与绿色反应塔底部连接 的吸收液收集池,以及一与绿色反应塔连接的用于排放标准的洁净烟气的烟囱。
[0015]在本实用新型的一个优选实施例中,所述h2〇2溶液储罐中的H 2〇2质量浓度范围为 10% ~50%〇
[0016] 在本实用新型的一个优选实施例中,所述反应氧化反应烟道中的烟气反应温度为 400~500。。。
[0017] 在本实用新型的一个优选实施例中,绿色反应塔中,氨水溶液从反应塔上部通过 喷淋装置雾化喷出,烟气从反应塔下部进入反应塔,氨水与烟气逆向流动,使反应充分进 行,反应塔内温度控制为50°C ±5°C。
[0018] 在本实用新型的一个优选实施例中,所述氨水溶液储罐中的氨水质量浓度1 %~ 30% 〇
[0019] 通过上述技术方案,本实用新型的有益效果是:
[0020] 本实用新型能够高效的降低烧结烟气氮氧化物排放,实现无污染零排放,良好适 应烧结行业烟气成分复杂;同时,新工艺通过合理控制反应发生条件,控制反应发生方式与 过程,极大节约了 H202用量,提高工艺经济性。
附图说明
[0021] 为了更清楚地说明本实用新型实施例或现有技术中的技术方案,下面将对实施例 或现有技术描述中所需要使用的附图作简单地介绍,显而易见地,下面描述中的附图仅仅 是本实用新型的一些实施例,对于本领域普通技术人员来讲,在不付出创造性劳动的前提 下,还可以根据这些附图获得其他的附图。
[0022]图1为本实用新型的结构不意图。
具体实施方式
[0023]为了使本实用新型实现的技术手段、创作特征、达成目的与功效易于明白了解,下 面结合具体图示,进一步阐述本实用新型。
[0024]参照图1,一种烧结机烟气氨法H202氧化脱硝装置,包括:氧化剂双流体喷射系统, 反应吸收系统,废物排放收集系统三个部分。
[0025]氧化剂双流体喷射系统主要由H202溶液储罐1,压缩空气供应装置,如压缩空气储 罐2,双流体喷枪4及相关栗阀门仪表组成,通过调节适当的溶液与空气流量比例,使两者流 经双流体喷枪并良好雾化。H2〇 2具有强腐蚀性,因此H2〇2溶液储罐、输送管道应采用能有效 防腐蚀材料,如玻璃钢、聚乙烯、304不锈钢等。
[0026] 反应吸收系统包括反应氧化反应烟道3、氨水溶液储罐5和绿色反应塔6,其中氧化 反应烟道3中烟气温度窗口为400~500°C,该温度下,H 2〇2能够与N0良好反应生成N〇2,获得 较高的转化率,减小H2〇2使用量,提高经济性。对于反应烟道的选取,在钢铁行业烧结机中, 该温度窗口主要位于烧结机冷却机高温段废气烟道处。绿色反应塔中,氨水溶液从反应塔 上部通过喷淋装置雾化喷出,烟气从反应塔下部进入反应塔,氨水与烟气逆向流动,使反应 充分进行,反应塔内温度控制为50°C±5°C,保证反应充分高效进行。同时,在反应塔内部通 过双流体喷枪喷入一定量的H 2〇2,防止3N〇2+H20--2HN03+N0反应大量发生、N〇2向NO转化、 降低脱除效率。绿色反应塔不仅是N0 X脱除的反应设备,同时,对于固体微小颗粒等其他污 染物的脱除也有良好的促进作用。
[0027] 废物排放收集系统用于排出净化后烟气和收集氨水吸收溶液,该系统包含氨水吸 收液收集池和烟肉,经过绿色反应塔与烟气进行反应完成后的液体从反应塔下部排出后由 氨水吸收液收集池收集,并在收集池内进行无害化处理后排放;反应塔上部排出的达到排 放标准的洁净烟气经烟肉排放。
[0028] 本工艺按如下工艺过程及反应机理如下:
[0029] l、H2〇2与压缩空气雾化
[0030] H2〇2能否与N0充分反应,保证一个较高的反应效率,良好的雾化效果是必要的保 证,本工艺中,压缩空气压力为0.4~0.6Mpa,与H2〇2经过双流体喷枪后能够实现良好雾化, 平均粒径为80~200μπι随着烟气含尘量差异,最佳粒径亦有差别。
[0031] 作为优选,Η2〇2溶液质量浓度为27.5 %,浓度较低时,喷入Η2〇2溶液量大,会影响烧 结机后部冷却机及其他余热回收装置的效率,浓度过高,Η2〇2溶液成本迅速提高,降低本工 艺的经济性。
[0032] 表1Η202溶液质量浓度同烧结机效率降低,脱硝成本对照
[0034]通过表1实验结果可看出,随着Η202溶液质量浓度提高,烧结机后部冷却机及其他 余热回收装置的效率逐渐降低,但脱硝成本大幅提高,综合两项实验结果/计算可得,作为 优选,H2〇2溶液质量浓度为27.5 %时,本工艺综合收益最高。
[0035] 27.5 %浓度H202溶液广泛运用于各工业过程,可同时减少其他混合过程,降低工艺 复杂程度。
[0036] 2、N0氧化过程
[0037] 经双流体喷枪良好雾化后的H2〇2喷入400~500°C烟道中,将N0氧化为N〇2,该温度 区间为氧化效果最好的温度窗口,能够实现H2〇290 %以上的反应效率,其反应总体方程式如 下:
[0038] H2O2+NO--NO2+H2O
[0039] 该氧化过程通过控制H202反应量将需要脱除的NOx氧化50%,而非完全氧化,这是 本工艺的特点所在。氧化过程之后烟气进入下一反应过程。
[0040] 3、氨吸收反应过程
[0041]烟气进入绿色吸收塔后,在氨水喷淋作用下,Ν0、Ν02与氨水发生下述吸收反应:
[0042] NO+N〇2+2NH3 · H2O--2NH4NO2+H2O
[0043] 该反应发生温度为50°C±5°C,根据《元素化学》中对于相关反应的理论,以及在一 些化学工艺过程中的运用可知该反应进行迅速,反应转化率高,能够保证95%以上的N0 X被 氨水吸收。
[0044] 此外此处喷入氨水对S02有一定的吸收作用,能够减小烟气中酸性污染物含量。
[0045] 作为优选,氨水浓度为10~20%,该氨水浓度能够在保持较好的吸收效率的前提 下减小污染物泄露可能带来的危害,同时该浓度范围氨水价格较为便宜,能够保证较高的 经济性。(如表2所示)
[0046] 表2选用氨水浓度同吸收效率,泄露危害对照表
[0048] 4、NH4N〇2 分解过程
[0049] ΝΗ4Ν02化合物特性为:干燥低温易保存,易溶于水,加热至50°C左右发生强烈分解 反应,反应过程如下:
[0050] NH4NO2--Ν2Ϊ+2Η2Ο
[0051 ]该过程在绿色吸收塔下部反应迅速,能实现NH4N02完全分解,反应生成物为N2和 水,做到无害化处理。
[0052] 5、染物排放收集过程
[0053]经处理后的洁净烟气随后进入烟囱排放,吸收反应后的吸收液由吸收液收集池收 集,随后进行净化处理或循环使用。
[0054]本实用新型工艺与其他脱硝工艺相比,具有的优势为:经济性较高,设备投资小, 运行维护简单;脱硝效率高,能够实现90 %以上脱硝效率;工艺适应性强,该工艺反应温度 窗口低,结构简单,除了能够很好的适应烧结烟气的特点,对于其他烟气脱硝也适用;真正 实现零污染排放,需要转化的N0 X最终转变为N2和水,对环境无危害。
[0055]本实用新型工艺与其他工艺性能及经济性对比如表3所示。
[0056]表3各种脱硝方法性能及经济性对比
[0059]采用如图1所示的工艺系统实现本实用新型新型氨法H202氧化脱硝工艺,一定浓度 氨水1~30%,优选浓度范围为10~20%和压缩空气优选压力为0.4~0.6Mpa经双流体喷枪 混合雾化作用后,喷入400~500°C烟气烟道,在烟道内部实现N0氧化反应,随后烟气经过其 他部件后进入绿色吸收塔,吸收塔内部温度控制为50°C ± 5°C,在吸收塔喷入氨水优选浓度 10~20 %吸收反应下转化为NH4NO2,随后NH4NO2发生分解反应,生成N2和水,实现零污染排 放。
[0060] 实施例1
[0061 ] 以某项目烟气量500000Nm3/h,N0x含量300mg/Nm3,脱硝目标效率为60%,利用绿色 吸收塔喷入氨水吸收方式,对一种针对钢铁行业烧结机烟气氨法H202氧化脱硝工艺进行分 析。采用新工艺时原料消耗如表4所示,经济性分析如表4所示。
[0062] 表4H2〇2新型氧化法原料消耗
[0064] 表5H2〇2新型氧化法经济性分析
[0065]
[0066] 实践表明,采用该工艺时脱硝效率可达到60%以上,满足目标要求。从设备投资和 运行成本上,新工艺亦低于其他脱硝工艺。
[0067]以上显示和描述了本实用新型的基本原理和主要特征和本实用新型的优点。本行 业的技术人员应该了解,本实用新型不受上述实施例的限制,上述实施例和说明书中描述 的只是说明本实用新型的原理,在不脱离本实用新型精神和范围的前提下,本实用新型还 会有各种变化和改进,这些变化和改进都落入要求保护的本实用新型范围内。本实用新型 要求保护范围由所附的权利要求书及其等效物界定。
Claims (1)
1. 一种烧结机烟气氨法H2〇2氧化脱硝装置,其特征在于,包括: 一氧化剂双流体喷射装置,所述氧化剂双流体喷射装置包括一 H2〇2溶液储罐,一压缩空 气储罐,以及一连通所述H2〇2溶液储罐和压缩空气储罐的第一双流体喷枪和第二双流体喷 枪, 一反应吸收装置,所述反应吸收装置包括一反应氧化反应烟道,所述第一双流体喷枪 从上端深入反应氧化反应烟道内; 一进行氨吸收的绿色反应塔,所述反应氧化反应烟道通过管道将初处理的烧结机烟气 送至一绿色反应塔的底部,所述第二双流体喷枪从侧端深入绿色反应塔内,且所述绿色反 应塔的上端连接一设置有喷枪的氨水溶液储罐; 以及一废物排放收集装置,所述废物排放收集装置包括一与绿色反应塔底部连接的吸 收液收集池,以及一与绿色反应塔连接的用于排放标准的洁净烟气的烟囱。
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