CN104941423B - 一种催化裂化再生烟气氨法脱硫脱硝除尘方法及装置 - Google Patents
一种催化裂化再生烟气氨法脱硫脱硝除尘方法及装置 Download PDFInfo
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- CN104941423B CN104941423B CN201510261073.0A CN201510261073A CN104941423B CN 104941423 B CN104941423 B CN 104941423B CN 201510261073 A CN201510261073 A CN 201510261073A CN 104941423 B CN104941423 B CN 104941423B
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- ammonia
- flue gas
- denitration
- catalytic cracking
- waste heat
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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 107
- 238000006477 desulfuration reaction Methods 0.000 title claims abstract description 45
- 230000003009 desulfurizing Effects 0.000 title claims abstract description 44
- 238000004523 catalytic cracking Methods 0.000 title claims abstract description 38
- 239000003517 fume Substances 0.000 title claims abstract description 26
- 230000008929 regeneration Effects 0.000 title claims abstract description 24
- 238000011069 regeneration method Methods 0.000 title claims abstract description 24
- 238000000034 method Methods 0.000 title claims abstract description 22
- 239000000428 dust Substances 0.000 title claims abstract description 20
- UGFAIRIUMAVXCW-UHFFFAOYSA-N carbon monoxide Chemical compound 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[O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims abstract description 70
- 239000003546 flue gas Substances 0.000 claims abstract description 69
- 239000003054 catalyst Substances 0.000 claims abstract description 34
- 239000002918 waste heat Substances 0.000 claims abstract description 28
- BFNBIHQBYMNNAN-UHFFFAOYSA-N Ammonium sulfate Chemical compound 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N.N.OS(O)(=O)=O BFNBIHQBYMNNAN-UHFFFAOYSA-N 0.000 claims abstract description 14
- 229910052921 ammonium sulfate Inorganic materials 0.000 claims abstract description 14
- 235000011130 ammonium sulphate Nutrition 0.000 claims abstract description 14
- RAHZWNYVWXNFOC-UHFFFAOYSA-N sulphur dioxide Chemical compound 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- 239000007789 gas Substances 0.000 claims abstract description 12
- 238000004140 cleaning Methods 0.000 claims abstract description 7
- 238000000746 purification Methods 0.000 claims abstract description 6
- 239000003795 chemical substances by application Substances 0.000 claims description 17
- 238000010790 dilution Methods 0.000 claims description 15
- 239000007921 spray Substances 0.000 claims description 13
- 229910002089 NOx Inorganic materials 0.000 claims description 12
- 239000007788 liquid Substances 0.000 claims description 10
- 238000006243 chemical reaction Methods 0.000 claims description 9
- 239000007787 solid Substances 0.000 claims description 9
- 238000005507 spraying Methods 0.000 claims description 9
- 238000010521 absorption reaction Methods 0.000 claims description 8
- 238000003860 storage Methods 0.000 claims description 8
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- 238000006555 catalytic reaction Methods 0.000 claims description 6
- 238000002156 mixing Methods 0.000 claims description 6
- 229910052815 sulfur oxide Inorganic materials 0.000 claims description 6
- 239000000779 smoke Substances 0.000 claims description 5
- 238000002425 crystallisation Methods 0.000 claims description 4
- 230000005712 crystallization Effects 0.000 claims description 4
- 238000001035 drying Methods 0.000 claims description 4
- 238000000926 separation method Methods 0.000 claims description 4
- 150000003462 sulfoxides Chemical class 0.000 claims description 4
- 230000005540 biological transmission Effects 0.000 claims description 3
- 238000004176 ammonification Methods 0.000 claims 1
- MWUXSHHQAYIFBG-UHFFFAOYSA-N Nitrogen oxide Substances 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O=[N] MWUXSHHQAYIFBG-UHFFFAOYSA-N 0.000 abstract description 4
- 239000006227 byproduct Substances 0.000 abstract description 3
- 238000007670 refining Methods 0.000 abstract description 3
- 229910052813 nitrogen oxide Inorganic materials 0.000 abstract description 2
- 239000000376 reactant Substances 0.000 abstract description 2
- 239000002699 waste material Substances 0.000 abstract description 2
- 238000005516 engineering process Methods 0.000 description 10
- NINIDFKCEFEMDL-UHFFFAOYSA-N sulfur Chemical compound 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- 238000011068 load Methods 0.000 description 2
- JKQOBWVOAYFWKG-UHFFFAOYSA-N molybdenum trioxide Chemical compound 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O=[Mo](=O)=O JKQOBWVOAYFWKG-UHFFFAOYSA-N 0.000 description 2
- 229910052757 nitrogen Inorganic materials 0.000 description 2
- 230000003647 oxidation Effects 0.000 description 2
- 238000007254 oxidation reaction Methods 0.000 description 2
- 239000002893 slag Substances 0.000 description 2
- KEAYESYHFKHZAL-UHFFFAOYSA-N sodium Chemical compound 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[Na] KEAYESYHFKHZAL-UHFFFAOYSA-N 0.000 description 2
- 239000011734 sodium Substances 0.000 description 2
- 229910052708 sodium Inorganic materials 0.000 description 2
- GWEVSGVZZGPLCZ-UHFFFAOYSA-N titan oxide Chemical compound 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- PNEYBMLMFCGWSK-UHFFFAOYSA-N AI2O3 Inorganic materials 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Classifications
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
- Y02A50/00—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE in human health protection, e.g. against extreme weather
- Y02A50/20—Air quality improvement or preservation, e.g. vehicle emission control or emission reduction by using catalytic converters
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
- Y02P20/129—Energy recovery, e.g. by cogeneration, H2recovery or pressure recovery turbines
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/50—Improvements relating to the production of bulk chemicals
- Y02P20/584—Recycling of catalysts
Abstract
一种催化裂化再生烟气氨法脱硫脱硝除尘方法,包括步骤:催化裂化装置来的高温含催化剂尘的催化剂再生烟气首先进入余热锅炉Ⅰ,烟气温度降到280‑430℃;烟气热量由余热锅炉Ⅰ产生蒸汽外供;280‑430℃的烟气进入脱硝装置脱硝,在脱硝反应器内在脱硝催化剂表面充分反应之后通过出口烟道进入余热锅炉Ⅱ;以氨为反应剂,脱除烟气中的二氧化硫、氮氧化物并副产硫酸铵,同时除去再生烟气中的催化剂粉尘,洁净气达标排放,无三废排放的净化方法,应用于石油炼化的催化裂化的催化剂再生烟气治理。
Description
一种催化裂化再生烟气氨法脱硫脱硝除尘方法及装置 一、
技术领域:
[0001] 本发明属环境保护领域,涉及到石油炼化行业催化裂化再生烟气二氧化硫、氮氧 化物、尘控制的工艺方法及装置。 二、
背景技术
[0002] 催化裂化是炼油过程中重要的二次加工,是提高轻质油收率,生产高辛烷值汽油, 同时又多产柴油的重要手段。催化裂化原料是重质馏分油和重油(常渣、减渣),其中含有较 多的硫、氮、氧等非烃,这些非烃元素和重金属元素,在生产过程中将转移到产品、催化剂、 工业废水中,有的随着烟气和催化剂粉尘排放到周围环境中,造成污染。
[0003] 催化裂化的催化剂烧焦产生的再生烟气,经再生器稀相段进入旋风分离器,经两 级旋风分离器分出携带的大部分催化剂,再生烟气温度很高而且含有约5%〜l〇%c〇,为了 利用其热量,不少装置设有C0锅炉,利用再生烟气产生水蒸汽。对于操作压力较高的装置, 常设有烟气能量回收系统,利用再生烟气的热能和压力作功,驱动主风机以节约电能。
[0004] 对于炼化企业来说,催化裂化再生烟气是最大的空气污染源,主要含有C0、S0x、N0x 等有害成分和催化剂粉尘颗粒,S〇2、NOx、尘是大气主要污染物,是造成雾霾的重要污染源。 尤其是SOx和NOx,随烟气排放到大气中,严重影响空气质量,还会对装置产生腐蚀,影响装置 的正常运转,因此再生烟气的处理成为环保治理中不可忽视的重点工作。
[0005] 催化裂化再生烟气通常具有以下特点:温度一般800°C以上;含有S0x、N0x的浓度 相比其他行业要高;尘:30-800mg/m3,S0X: 100-1500mg/m3,N0X: 100-1200mg/m3。尘通常为含 A1203等的催化剂颗粒。降低催化裂化再生烟气中S0X和N0X浓度有三个途径:(1)降低催化裂 化原料硫、氮含量;(2)使用转移催化剂;(3)烟气脱硫脱硝。降低催化裂化原料硫氮含量的 方法是催化原料加氢预处理,可以使催化原料硫含量降到小于0.3%,但投资高,建设310万 吨催化原料预加氢装置约需投资12亿元。转移催化剂技术国内已开发多年,单独采用此技 术难以使净烟气达标。
[0006] 催化裂化再生烟气脱硫方法主要有钠法、钙法,存在投资高、运行费用高、排放废 水等不足。
[0007] 控制催化裂化再生烟气中N0X含量的技术主要有选择性催化还原法(SCR)、选择性 非催化还原法(SNCR)、液体吸收法、固体吸附法、高能电子活化氧化法等。
[0008] CN201410590103公开了一种催化裂化烟气脱硫和除尘工艺,催化裂化烟气依次经 过烟气除尘和初脱硫、烟气脱硫和烟气除气溶胶三道工艺过程,通过动力波装置对催化裂 化烟气进行净化洗涤,烟气在吸收塔通过喷淋洗涤和机械除雾,实现湿法脱硫和除湿,最后 过电除雾方法,通过高压放电捕集雾滴,使烟气中的含尘量<30mg/Nm3,达到烟气排放标 准。采用钠碱法脱硫方法,去除炼油厂催化裂化烟气中的二氧化硫并除去烟气中夹带的高 浓度催化剂粉尘。
[0009] CN201320319032公开了一种催化裂化烟气脱硫除尘设备,包括多层喷淋吸收段和 冲洗系统,通过脱硫酸化塔上的两个吸收剂进口导入脱硫剂。烟气通过烟气进口进入脱硫 酸化塔内,以NaOH溶液为脱硫剂进行脱硫除尘,并通过喷淋吸收段除去烟气中所夹带的液 滴,达到净化烟气的作用。
[0010] CN201210108141公开一种催化裂化再生烟气脱硝净化的方法;在反应器的恒温段 中装填二个催化剂床层,上段为第一催化剂床层,下段为第二催化剂床层,中间不设置隔 层,催化裂化再生烟气自下进入反应器的催化剂床层并升温反应;第一催化剂与第二催化 剂的质量比为1:1-10;第一催化剂为纳米Ce02担载钙钛矿复合氧化物的催化剂,第二催化 剂为骨架掺杂过渡金属的分子筛,第二催化剂含有助剂;钙钛矿复合氧化物在纳米&02上 的负载量为10-50wt%;过渡金属与助剂的物质的量比为0.1-0.3;HZSM-5分子筛的硅铝摩 尔比为25-100,过渡金属在分子筛上的担载量为0. 〇5_6wt% ;
[0011]本发明提供了一种催化裂化再生烟气氨法脱硫脱硝除尘一体化技术及装置,能使 催化裂化再生烟气排放的S02控制在35mg/Nm3以下、N0X控制在40mg/Nm3以下、尘控制在5mg/ Nm3以下。本发明实现了脱硫脱硝除尘一体化控制,较常规的独立的脱硫、脱硝、除尘技术节 约投资30%以上,节省运行费用20%以上,具有明显的技术和应用优势。 三、发明内容
[0012] 本发明目的是,提出一种基于氨法脱硫脱硝的催化裂化再生烟气脱硫脱硝除尘一 体化技术及装置,从而实现催化裂化再生烟气的高效净化。且工艺流程简单,操作简便,装 置运行稳定,避免己有工艺的一些缺点。
[0013] 本发明的技术方案是:一种催化裂化再生烟气氨法脱硫脱硝除尘方法,其特征在 于包括如下步骤:
[0014] 1)催化裂化装置来的高温含催化剂尘的催化剂再生烟气首先进入余热锅炉I,烟 气温度降到280-430°C;烟气热量由余热锅炉I产生蒸汽外供;
[0015] 2) 280-430°C的烟气进入脱硝装置,按烟气流动方向依次包括脱硝进口烟道、喷氨 混合整流系统、脱硝反应器、脱硝催化剂和出口烟道;引自余热锅炉I的烟气进入脱硝进口 烟道后在喷氨处与氨气进行混合,经过喷氨混合整流系统整流后进入脱硝反应器,在脱硝 反应器内在脱硝催化剂表面充分反应之后通过出口烟道进入余热锅炉n;
[0016] 3)烟气经余热锅炉n温度降低为80-220°C,烟气热量由余热锅炉n产生蒸汽外 供;
[0017] 4)80-220°C烟气进入脱硫除尘系统,用含氨的循环吸收液吸收硫氧化物同时洗涤 催化剂尘,吸收液参数根据硫氧化物脱除量、硫氧化物浓度调整,处理后的洁净气送烟囱排 放;
[0018] 5)脱硫除尘系统产生的硫酸铵送硫酸铵处理系统,经浓缩、结晶、固液分离、干燥、 包装得到固体硫酸铵产品外供;
[0019] 6)供氨系统一般包括氨贮槽和气氨发生器。气氨发生器包括氨蒸发器、氨气缓冲 罐、稀释风机和氨-空气混合器。氨经氨蒸发器蒸发后进入氨气缓冲罐,与稀释风机来的空 气在氨-空气混合器中进行混合,稀释后的氨气经过喷氨混合系统进入烟气系统进行脱硝。 氨一部分送脱硫除尘系统作脱硫反应剂。
[0020] 7) 80-220°C烟气进入脱硫除尘系统,用循环吸收液吸收硫氧化物同时洗涤催化剂 尘,吸收液参数根据硫氧化物脱除量、硫氧化物浓度调整,处理后的洁净气温度45-65°C送 烟囱排放;脱硫除尘系统产生的硫酸铵送硫酸铵处理系统,经浓缩、结晶、固液分离、干燥、 包装得到固体硫酸铵产品外供;供氨系统负责脱硝、脱硫反应剂的贮存、配置与供应。
[0021]根据上述方法,本发明提出的装置:依次包括余热锅炉I,脱硝装置,余热锅炉n和 脱硫除尘系统,所述脱硝装置按烟气流动方向依次包括脱硝进口烟道、喷氨混合整流系统、 脱硝反应器、脱硝催化剂和出口烟道;供氨系统对喷氨混合整流系统和脱硫除尘系统供氨, 来自余热锅炉I的烟气进入脱硝进口烟道后在喷氨处与氨气进行混合,经过喷氨混合整流 系统整流后进入脱硝反应器,出口烟道;供氨系统包括氨贮槽和气氨发生器。
[0022]气氨发生器包括氨蒸发器、氨气缓冲罐、稀释风机和氨-空气混合器。氨经氨蒸发 器蒸发后进入氨气缓冲罐,与稀释风机来的空气在氨-空气混合器中进行混合,稀释后的氨 气经过喷氨混合系统进入烟气系统进行脱硝;氨一部分送脱硫除尘系统作脱硫反应剂。 [0023]用于本发明处理的催化裂化的再生烟气的温度800°c以上;颗粒物:30-800mg/m3, S0X: 100-1500mg/m3,NOx: 100-1200mg/m3。
[0024]本发明提出的处理方法,催化裂化再生烟气净化后脱硝效率多85%,脱硫效率 98%,净烟气NOx低于50mg/Nm3、S〇2低于35mg/Nm3、尘低于20mg/Nm3,副产品硫酸铵,洁净气达 标排放,同时投资低、工艺流程简单、运行成本低。
[0025]本发明的有益效果:本发明是一种催化裂化再生烟气氨法脱硫脱硝除尘一体化技 术及装置,脱硫脱硝除尘效率高,无三废排放,无二次污染,完全资源化。本发明技术优势在 于用较低的投资和运行成本实现高效脱硫脱硝除尘,确保洁净气达标排放,可满足环保高 标准的要求。工艺流程简单,操作简便,装置运行稳定。本发明脱硫、脱硝皆以一套氨系统产 生的氨为反应剂,减少了脱硫、脱硝的运行、维护工作。采用烟气加热和余热回收装置使烟 气脱硫和脱硝均在最佳的温度下进行,有利于较高的脱硫、脱硝效率。通过对烟气热量回收 利用。 四、
附图说明
[0026] 图1为一种催化裂化再生烟气氨法脱硫脱硝除尘一体化技术及装置流程框图。 五、
具体实施方式
[0027] 100万吨催化裂化装置催化剂再生烟气,烟气量135000Nm3/h,温度950 °C,水12 %, 氮氧化物360mg/Nra3,二氧化硫2300mg/Nm3,尘150mg/Nm3。脱硫剂为99 • 6 %液氣。
[0028] 1)催化裂化装置来的烟气首先进入余热锅炉I,烟气温度降到310-350°C ;烟气热 量由余热锅炉I产生蒸汽外供。
[0029] 2) 310-350。(:的烟气进入脱硝装置,按烟气流动方向依次包括进口烟道、喷氨混合 整流系统、脱硝反应器、脱硝催化剂和出口烟道。引自余热锅炉的烟气进入脱硝烟道后在喷 氨处与氨气进行混合,经过整流后进入脱硝反应器,在催化剂表面充分反应之后通过出口 烟道去余热锅炉n。
[0030] 3)烟气经余热锅炉n温度降低为115-145。(:,烟气热量由余热锅炉n产生蒸汽外 供0
[0031] 4) 115-1451:烟气进入脱硫除尘系统,用循环吸收液吸收硫氧化物同时洗漆催化 剂尘,吸收液参数根据硫氧化物脱除量、硫氧化物浓度调整,处理后的洁净气送烟肉排放;
[0032] 5)脱硫除尘系统产生的硫酸铵送硫酸铵处理系统,经浓缩、结晶、固液分离、干燥、 包装得到固体硫酸铵产品外销;
[0033] 6)供氨系统一般包括氨贮槽和气氨发生器。气氨发生器包括氨蒸发器、氨气缓冲 罐、稀释风机和氨-空气混合器。氨经氨蒸发器蒸发后进入氨气缓冲罐,与稀释风机来的空 气在氨-空气混合器中进行混合,稀释后的氨气经过喷氨混合系统进入烟气系统进行脱硝。 氨一部分送脱硫除尘系统作脱硫反应剂。
[0034] 效果:脱硝效率彡88.9%,脱硫效率98.5%,净烟气NOx38mg/Nm3、S〇232mg/Nm3、尘 低于15mg/Nm3,副产品硫酸铵含氮量20 • 8 %。
[0035]脱硫除尘系统是常规设备,包括脱硫除尘塔、循环泵(可与脱硫除尘塔一体化)、循 环槽、氧化风机、沉降池、过滤机等设备。总之,后道氨法脱硫流程及装置未涉及内容采用现 有公开技术或申请人已获授权氨法脱硫装置系列专利。如CN200510040801.1、 CN03158258.3、CN201010275966.8、CN200510040800.7、CN03158257.5等。催化剂采用以 Ti02为基材,以V205为主要活性成份,以W03、M〇03为抗氧化、抗毒化辅助成份。化剂型式可 分为三种:板式、蜂窝式和波纹板式。
[0036]以上所述的具体实施例,对本发明的目的、技术方案和有益效果进行了进一步详 细说明,所应理解的是,以上所述仅为本发明的具体实施例而已,并不用于限制本发明,凡 在本发明的精神和原则之内,所做的任何修改、等同替换、改进等,均应包含在本发明的保 护范围之内。
Claims (4)
1. 一种催化裂化再生烟气氨法脱硫脱硝除尘方法,其特征在于包括如下步骤: 催化裂化装置来的高温含催化剂尘的催化剂再生烟气首先进入余热锅炉I,烟气温度 降到310-350°C;烟气热量由余热锅炉I产生蒸汽外供; 310_35(TC的烟气进入脱硝装置,按烟气流动方向依次包括脱硝进口烟道、喷氨混合整 流系统、脱硝反应器、脱硝催化剂和出口烟道;引自余热锅炉I的烟气进入脱硝进口烟道后 在喷氨处与氨气进行混合,经过喷氨混合整流系统整流后进入脱硝反应器,烟气在脱硝反 应器内在脱硝催化剂表面充分反应之后通过出口烟道进入余热锅炉n; 烟气经余热锅炉n温度降低为115-145°C,烟气热量由余热锅炉n产生蒸汽外供; 115-145°C烟气进入脱硫除尘系统,用氨化的循环吸收液吸收硫氧化物同时洗涤催化 剂尘,吸收液参数根据硫氧化物脱除量、硫氧化物浓度调整,处理后的温度为45-65°C的洁 净气送烟囱排放; 脱硫除尘系统产生的硫酸铵送硫酸铵处理系统,经浓缩、结晶、固液分离、干燥、包装得 到固体硫酸铵产品外供;供氨系统负责脱硝、脱硫反应剂的贮存、配置与供应; 催化裂化的再生烟气的温度800 °C以上;颗粒物:30-800mg/m3, S0X: 100-1500mg/m3,N0X: 100-1200mg/m3;催化裂化再生烟气净化后脱硝效率彡85%,脱硫效率98%,净烟气N0X低于 50mg/Nm3、S〇2 低于 35mg/Nm3、尘低于 20mg/Nm3。
2. 根据权利要求1所述的催化裂化再生烟气氨法脱硫脱硝除尘方法,其特征在于脱硝 反应器与脱硫除尘系统需要的氨包括氨贮槽和气氨发生器提供;气氨发生器包括氨蒸发 器、氨气缓冲罐、稀释风机和氨-空气混合器;氨贮槽的氨经氨蒸发器蒸发后进入氨气缓冲 罐,与稀释风机来的空气在氨-空气混合器中进行混合,稀释后的氨气经过喷氨混合系统进 入烟气系统进行脱硝;氨一部分送脱硫除尘系统作为脱硫反应剂。
3.用于进行根据权利要求1或2所述方法的催化裂化再生烟气氨法脱硫脱硝装置,其特 征在于:除尘装置依次包括余热锅炉I,脱硝装置,余热锅炉n和脱硫除尘系统,所述脱硝装 置,按烟气流动方向依次包括脱硝进口烟道、喷氨混合整流系统、脱硝反应器、脱硝催化剂 和出口烟道;供氨系统对喷氨混合整流系统和脱硫除尘系统供氨,来自余热锅炉I的烟气进 入脱硝进口烟道后在喷氨处与氨气进行混合,经过喷氨混合整流系统整流后进入脱硝反应 器,出口烟道;供氨系统包括氨贮槽和气氨发生器。
4.根据权利要求3所述的催化裂化再生烟气氨法脱硫脱硝装置,其特征在于:气氨发生 巧包括氨蒸发器、氨气缓冲罐、稀释风机和氨-空气混合器,氨经氨蒸发器蒸发后进入氨气 缓冲罐,与稀释风机来的空气在氨-空气混合器中进行混合,稀释后的氨气经过喷氨混合系 统进入烟气系统进行脱硝;氨一部分送脱硫除尘系统作脱硫反应剂。
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