CN103816780B - 一种低温烟气脱硫脱硝除氨一体化工艺 - Google Patents
一种低温烟气脱硫脱硝除氨一体化工艺 Download PDFInfo
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- CN103816780B CN103816780B CN201410087513.0A CN201410087513A CN103816780B CN 103816780 B CN103816780 B CN 103816780B CN 201410087513 A CN201410087513 A CN 201410087513A CN 103816780 B CN103816780 B CN 103816780B
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- Prior art keywords
- ammonia
- denitration
- except
- flue
- flue gas
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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 220
- 239000003546 flue gases Substances 0.000 title claims abstract description 87
- UGFAIRIUMAVXCW-UHFFFAOYSA-N carbon monoxide Chemical compound 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[O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 title claims abstract description 85
- 280000739435 Integral Process companies 0.000 title claims abstract description 19
- 239000003054 catalysts Substances 0.000 claims abstract description 68
- 281000066869 Coke (fuel) companies 0.000 claims abstract description 61
- 230000003009 desulfurizing Effects 0.000 claims abstract description 38
- 239000004744 fabrics Substances 0.000 claims abstract description 31
- 239000007789 gases Substances 0.000 claims abstract description 28
- 238000000034 methods Methods 0.000 claims abstract description 28
- 239000002131 composite materials Substances 0.000 claims abstract description 27
- 238000006477 desulfuration reactions Methods 0.000 claims abstract description 25
- 238000007599 discharging Methods 0.000 claims abstract description 14
- 238000005243 fluidization Methods 0.000 claims abstract description 14
- 241000196324 Embryophyta Species 0.000 claims abstract description 11
- 230000000694 effects Effects 0.000 claims abstract description 11
- 238000000746 purification Methods 0.000 claims abstract description 9
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- 239000000843 powders Substances 0.000 claims description 42
- 238000005507 spraying Methods 0.000 claims description 35
- 239000002956 ash Substances 0.000 claims description 34
- 235000011114 ammonium hydroxide Nutrition 0.000 claims description 24
- 239000002245 particles Substances 0.000 claims description 24
- 239000011734 sodium Substances 0.000 claims description 23
- 239000000428 dust Substances 0.000 claims description 20
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- UIIMBOGNXHQVGW-UHFFFAOYSA-M NaHCO3 Chemical compound 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N.N.OS(O)(=O)=O BFNBIHQBYMNNAN-UHFFFAOYSA-N 0.000 description 2
- 229910052921 ammonium sulfate Inorganic materials 0.000 description 2
- 235000011130 ammonium sulphate Nutrition 0.000 description 2
- 238000001704 evaporation Methods 0.000 description 2
- 239000011901 water Substances 0.000 description 2
- OKTJSMMVPCPJKN-UHFFFAOYSA-N carbon Chemical compound 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- NINIDFKCEFEMDL-UHFFFAOYSA-N sulfur Chemical compound 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[S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 1
- 239000002699 waste materials Substances 0.000 description 1
Abstract
本发明涉及一种低温烟气脱硫脱硝除氨一体化工艺，适用于烟气温度大于180℃，SO2含量小于150mg/Nm3的焦炉烟道废气脱硫脱硝，根据流态化原理在脱硝之前先干法脱硫，采用焦化厂蒸氨工段产生的剩余氨水蒸发出来的氨气作为还原剂，利用布袋-除氨催化剂复合结构作为除尘及脱硝手段，高效脱硫脱硝的同时，可控制氨逃逸量低于国家排放标准值。与现有技术相比，本发明的有益效果是：1）一体化脱硫脱硝除氨效率高；2）脱硝方式独特，设备结构形式先进；3）清灰简单；4）节省能源，降低运行费用及一次投资；5）充分回收利用煤气净化工艺中的剩余氨水；6）充分回收利用余热。
Description
技术领域
[0001] 本发明涉及低温烟气无害化处理技术领域，尤其涉及一种低温烟气脱硫脱硝除氨一体化工艺。
背景技术
[0002] NH3-SCR法(选择性催化还原法)脱硝技术成熟、可靠，已在电厂得到广泛应用。电厂烟气温度在350°C〜400°C之间，在此温度工况下的脱硝效率可达90%，且由于烟气温度高，在催化剂作用下SO2转化成SO 3的量很少，SO 2对脱硝效率的影响微乎其微。电厂一般采用先脱硝、烟气余热回收、后低温脱硫工艺。
[0003] 焦化厂焦炉烟道废气温度一般在180°C〜250°C之间；S02含量一般为60〜150mg/Nm3，对于原料煤中有机硫含量比较高的企业，其焦炉烟道废气中的SCV#量可达350mg/Nm35NOx含量在600〜1200mg/Nm3之间；氧含量较低，约为6% ;含水量随焦炉加热介质变化，采用焦炉煤气加热时约为17.25%，采用混合煤气加热时约为6.6%。为满足焦化行业对N0X& SO 2的排放浓度要求，必须对焦炉烟道废气采取脱硫脱硝措施。
[0004] 焦炉烟道废气温度较低，采用常规NH3-SCR法脱硝，其效率仅为50〜70 %，经过脱硝后的NOr^度无法满足国家排放标准要求，同时会有大量的氨逃逸，产生新的大气污染。在此温度区间内，SO2在催化剂催化作用下极易转化成SO 3，503与NH 3反应生成硫酸铵盐，硫酸铵盐粘结在催化剂表面，不仅降低脱硝效率，还会减少催化剂使用寿命。如果在脱硝装置前加入传统的脱硫工艺，则由于烟气温度随之降低，会进一步降低脱硝效率。上述问题虽然可以通过加热焦炉烟道废气来解决，但会造成能源浪费，同时增加一次投资及运行费用。目前为止，还没有针对焦炉烟道废气脱硝技术的公开信息。
发明内容
[0005] 本发明提供了一种低温烟气脱硫脱硝除氨一体化工艺，脱硝方式独特，设备结构形式先进，充分回收利用煤气净化工艺中的剩余氨水，高效脱硫脱硝的同时，可控制氨逃逸量低于国家排放标准值。
[0006] 为了达到上述目的，本发明采用以下技术方案实现:
[0007] 一种低温烟气脱硫脱硝除氨一体化工艺，适用于烟气温度大于180°C，SO2含量小于150mg/Nm3的焦炉烟道废气脱硫脱硝，根据流态化原理，在脱硝之前先进行干法脱硫，采用焦化厂蒸氨工段产生的剩余氨水蒸发出来的氨气作为还原剂，利用布袋-除氨催化剂复合结构作为除尘及脱硝手段，高效脱硫脱硝的同时，可控制氨逃逸量低于国家排放标准值。具体步骤如下:
[0008] I)低温烟气在脱硝之前先采取脱硫措施，在除氨脱硝设备烟道气入口管道上设脱硫催化剂喷入口，贮存在干粉贮存槽中的NaHCO3细粉脱硫剂通过压缩空气及干粉流态化设备流化后，由脱硫剂喷入口喷入焦炉烟道废气输送管道；流态化NaHCO3细粉与焦炉烟道废气接触后，在热烟气中多数分解生成细度更小、比表面积更大、活性度更高的Na2CO3, NaHCO3及Na2CO3细粉均与SO 2反应生成Na2SO3,脱除烟气中的SO2;
[0009] 2)脱硫后的烟道废气输送管道上设有喷氨格栅及静态混合器，焦化厂煤气净化工艺蒸氨工序产生的剩余氨水存放在氨水贮罐中，经过氨喷淋蒸发器被蒸发成氨气，与一部分烟气混合后通过喷氨格栅均匀喷入烟气中，通过静态混合器与焦炉烟道废气均匀混合；
[0010] 3)与氨气均匀混合后的焦炉烟道废气进入除氨脱硝设备进行脱硝除氨；烟气从除氨脱硝设备侧底部进入，经过脱硝除氨的烟气由除氨脱硝设备侧顶部或顶部流出；进入除氨脱硝设备的烟气首先与布袋复合催化剂接触，脱硫过程中生成的Na2SO3细粉、未参加反应的NaHC03& Na 2C03细粉、烟气中含有的粉尘均被滤袋过滤在滤袋外表面，烟气则在引风机的负压作用下强制性穿过滤袋，进入并穿过除氨催化剂层；除氨催化剂呈细颗粒状，低硫、低温烟气环境中，在除氨催化剂的催化作用下，NH3优先与NO x等强氧化气体反应，将NO x还原成N2;随着滤袋表面颗粒附着物的增加，除氨脱硝设备阻力也会增加，利用压缩空气通过清灰装置对布袋复合催化剂进行脉冲清灰，除下的颗粒物落入除氨脱硝设备底部灰仓；烟气穿过滤袋外表面颗粒物层时，烟气中残留的302与NaHCO3及Na2CO3细粉继续发生反应，进一步提尚脱硫效率；
[0011] 4)经过脱硫脱硝除氨全过程处理后的烟道废气达到国家排放标准，返回焦炉烟囱排放；除氨脱硝设备收集的颗粒物通过出灰口排出，通过刮板输送机及链斗式提升机输送至颗粒物贮仓，定期外运销售。
[0012] 所述除氨脱硝设备采用脉冲袋式除尘器结构形式，布袋复合催化剂外表面为耐高温滤袋，中间为除氨催化剂层，里层为滤料骨架；滤袋用于滤除颗粒物及粉尘，除氨催化剂用于高效脱硝除氨；通过清灰装置脉冲反吹清灰，不仅可以清掉滤袋外表面附着的颗粒物，同时可以清除除氨催化剂颗粒之间夹杂的粉尘，提高除氨催化剂的使用效率及使用寿命。
[0013] 所述除氨脱硝设备焦炉烟道废气入口处设气流分布板，将气流均布至布袋复合催化剂，同时由于布袋复合催化剂层具有一定的阻力，具有一定的均压作用，利于设备内部气流场及温度场均布。
[0014] 所述除氨脱硝设备出灰口设密闭排料锁气阀，防止由于室外空气通过出料口渗透进设备中降低处理烟气温度。
[0015] 所述引风机配有变频电机，通过对引风机进行变频调速，并调节烟道气入口风量调节阀，既可以保证焦炉正常生产所需要的负压值，也可以保证脱硫脱硝工艺系统正常工作所需要的压力值。
[0016] 所述氨水为焦化厂煤气净化工艺蒸氨工序产生的浓度为15〜18%的剩余氨水，氨水贮罐用于稳定脱硝系统氨水流量及浓度，根据焦炉烟道废气中的NOx含量，可变频调节氨水供给泵的供给量。
[0017] 所述氨喷淋蒸发器所用热媒为经过脱硫脱硝后的焦炉烟道废气，经过脱硫脱硝后的焦炉烟道废气还用于稀释氨气浓度，提高氨气温度，同时可以使喷入的氨更好的与焦炉烟道废气混合，并减少由于氨气喷入而引起的烟气温度下降。
[0018] 所述压缩空气用于除氨脱硝设备清灰、脱硫剂干粉流态化、启闭密闭排料锁气阀。
[0019] 所述引风机安装在靠近除氨脱硝设备出口附近的烟气管道上，焦炉烟囱底部两侧烟道气入口处设置烟道气入口风量调节阀；
[0020] 所述干粉贮存槽设在除氨脱硝设备烟道气入口管道旁，底部设置变频定量给料设备及干粉流态化设备，干粉流态化设备通过脱硫催化剂喷入口连接烟气管道；
[0021] 所述氨水储罐出口处设氨水定量供给泵，并通过管道依次连通氨喷淋蒸发器、氨气缓冲罐、氨气-烟气混合器，氨喷淋蒸发器的两端通过管道接入脱硫脱硝除氨处理后的烟气管道，形成回路，其位于氨喷淋蒸发器前的管路另设一管道支路依次连通氨气-烟气混合器和安装在除氨脱硝设备入口管道上的喷氨格栅，静态混合器安装在喷氨格栅位于烟气输送方向前方的烟气管道中；
[0022] 所述除氨脱硝设备底部为灰仓，灰仓出口设密闭排料锁气阀，灰仓上部设布袋复合催化剂，布袋复合催化剂侧面烟气入口处设气流分布板，布袋复合催化剂顶部设脉冲清灰装置，除氨脱硝设备侧底部连接烟道气入口，除氨脱硝设备侧顶部或顶部连接烟道气出P ；
[0023] 所述刮板输送机位于除氨脱硝设备灰仓的下方，其尾部通过管道接入链斗式提升机下部，颗粒物贮仓的上方连接链斗式提升机，下方出料口设有螺杆式插板阀；
[0024] 所述压缩空气贮存在压缩空气贮罐中，通过连接管道分别连接除氨脱硝设备脉冲清灰装置、脱硫剂干粉流态化设备和除氨脱硝设备出灰口的密闭排料锁气阀。
[0025] 与现有技术相比，本发明的有益效果是:
[0026] I) 一体化脱硫脱硝除氨效率高
[0027] 通过在烟道气输送管道中喷入流态化的NaHCO3细粉，先干法脱除烟气中的S02，S后采用除氨催化剂进行脱硝，其脱硫效率高于90%，脱硝效率高于90%，氨反应效率高于98%。
[0028] 2)脱硝方式独特，设备结构形式先进
[0029] 焦炉烟道废气直接采用除氨催化剂进行脱硝同时除氨，除氨脱硝装置采用脉冲袋式除尘器结构形式，耐高温滤袋与除氨催化剂复合，滤袋用于滤除烟气中的NaHC03、Na2C03、Na2SO3等颗粒物及粉尘，防止粉尘及颗粒物污染除氨催化剂表面，同时烟气穿过滤袋外表面颗粒物层时，烟气中的SO2会与NaHCO 3及似20)3继续反应，进一步脱除SO2，在低硫环境下，除氨催化剂对低温烟气仍有很高的脱硝效率。
[0030] 3)清灰简单
[0031] 采用压缩空气脉冲清灰方式清除滤袋外表面的颗粒物，不仅可以提高布袋滤尘效率，降低系统运行阻力，还可以吹落除氨催化剂颗粒之间夹杂的粉尘，提高除氨催化剂的除氨效率及脱硝效率，延长催化剂使用寿命。
[0032] 4)节省能源，降低运行费用及一次投资
[0033] 采用脱硫脱硝除氨一体化工艺，可在焦炉烟道废气低温工况下，直接高效干法脱硫，同时高效脱硝除氨，不需要对低温焦炉烟道废气采取加热措施，节省能源，降低运行费用及一次投资。
[0034] 5)充分回收利用煤气净化工艺中的剩余氨水
[0035] 采用煤气净化蒸氨工段中产生的浓度约为15%〜18%的剩余氨水作为还原剂，降低焦化厂外排污染物浓度，同时降低处理污染物运行成本及一次投资。
[0036] 6)充分回收利用余热
[0037] 氨蒸发及氨气混合均采用经过脱硝后的焦炉烟道废气，充分回收利用烟道废气的余热，不需另外增设加热媒，大大节约能源。
附图说明
[0038] 图1是本发明的工艺流程图。
[0039] 图2是本发明中除氨脱硝设备侧视图。
[0040]图3是本发明中布袋复合催化剂结构示意图。
[0041] 图中:1a.引风机Ib.烟道气入口风量调节阀2a.变频定量给料设备2b.干粉流态化设备 2c.干粉贮存槽 3a.氨水贮罐 3b.氨水供给泵 3c.氨喷淋蒸发器3d.氨气缓冲罐3e.氨气-烟气混合器3f.喷氨格栅3g.静态混合器4.除氨脱硝设备4a.布袋复合催化剂4a_l.滤袋4a_2.除氨催化剂层4a_3.滤料骨架4b.脉冲清灰装置4c.灰仓4d.密闭排料锁气阀4e.气流分布板5.压缩空气贮罐6a.刮板输送机6b.链斗式提升机6c.颗粒物贮仓6d.螺杆式插板阀
具体实施方式
[0042] 下面结合附图对本发明的具体实施方式作进一步说明:
[0043] 见图1，是本发明一种低温烟气脱硫脱硝除氨一体化工艺的工艺过程示意图，从焦炉烟囱开始，沿烟气流动方向，在烟气主管道上依次设置有流态化脱硫剂喷入口、喷氨格栅3f;静态混合器3g、除氨脱硝设备4、引风机la、氨制备混合用烟气入口及出口，在烟囱根部烟道废气输送管道上设烟道气入口风量调节阀lb。
[0044] 流态化脱硫剂喷入口连接干粉流态化设备2b，干粉流态化设备2b的上方是干粉贮存槽2c，其底部出料口设变频定量给料设备2a。
[0045] 喷氨格栅3f与氨制备装置连接，包括氨水贮罐3a、氨水供给泵3b、氨喷淋蒸发器3c、氨气缓冲罐3d及氨气-烟气混合器3e，氨水储罐3a出口处设氨水定量供给泵3b，并通过管道依次连通氨喷淋蒸发器3c、氨气缓冲罐3d及氨气-烟气混合器3e，氨喷淋蒸发器3c的两端通过管道接入脱硫脱硝除氨处理后的烟道废气输送管道，形成回路，其位于氨喷淋蒸发器3c前的管路另设一管道支路依次连通氨气-烟气混合器3e和安装在除氨脱硝设备入口管道上的喷氨格栅3f，静态混合器3g安装在喷氨格栅3f位于烟气输送方向前方的烟道废气输送管道中。
[0046] 除氨脱硝设备4底部为灰仓4c，灰仓4c出口设密闭排料锁气阀4d，灰仓4c上部设布袋复合催化剂4a，布袋复合催化剂4a侧面烟气入口处设气流分布板4e，布袋复合催化剂4a顶部设脉冲清灰装置4b，除氨脱硝设备4侧底部连接烟道气入口，除氨脱硝设备4侧顶部或顶部连接烟道气出口。
[0047] 刮板输送机6a位于除氨脱硝设备灰仓4c的下方，其尾部通过管道接入链斗式提升机6b下部，颗粒物贮仓6c的上方连接链斗式提升机6b，下方出料口设有螺杆式插板阀6d0
[0048] 压缩空气贮罐5通过连接管道分别连接除氨脱硝设备脉冲清灰装置4b、脱硫剂干粉流态化设备2b和除氨脱硝设备出灰口的密闭排料锁气阀4d。
[0049] 本发明一种低温烟气脱硫脱硝除氨一体化工艺，具体步骤如下:
[0050] I)低温烟气在脱硝之前先采取脱硫措施，贮存在干粉贮存槽2c中的NaHCO3细粉脱硫剂通过压缩空气及干粉流态化设备2b流化后，由脱硫剂喷入口喷入焦炉烟道废气输送管道；流态化NaHCO3细粉与焦炉烟道废气接触，发生如下化学反应:
[0051 ] 2NaHC03->Na2C03+H20+C02 ；
[0052] Na2C03+S02->Na2S03+C02；
[0053] 2NaHC03+S02->Na2S03+H20+2C02。
[0054] 多数NaHCO3细粉在热烟气中分解生成细度更小、比表面积更大、活性度更高的Na2CO3，提尚SO2脱除效率。
[0055] 2)将煤气净化工艺蒸氨工序产生的浓度为15〜18%的剩余氨水用管道输送至氨水贮罐3a中贮存，氨水贮罐3a还用于稳定脱硝系统氨水流量及浓度。氨水定量供给泵3b将氨水贮罐3a中的氨水喷入氨喷淋蒸发器3c进行蒸发，蒸发后一定压力的氨气先进入氨缓冲罐3d，然后进入氨气-烟气混合器3e与一部分脱硝后的排气混合，混合后的氨气由喷氨格栅3f均匀喷入脱硫后的焦炉烟道废气输送管道中，喷氨格栅3e后面设置静态混合器3g，使氨气与烟气中的氮氧化合物充分混合。
[0056] 根据焦炉烟道废气中NOx含量及NO x排放浓度要求，可调节氨水供给泵3b的供给量，以满足脱硝系统氨用量要求。
[0057] 氨喷淋蒸发器3c的热源来自脱硝后的焦炉烟道废气，充分利用烟气的余热，不需另外增设加热系统。
[0058] 混合器3e起到稀释氨气浓度，提高氨气温度的作用，可以使喷入的氨气更好的与焦炉烟道废气混合，并减少由于氨气喷入而引起的烟气温度下降。与氨气混合的介质采用经过脱硫脱硝处理的焦炉烟道废气。
[0059] 经过模拟后设计的喷氨格栅3f用于在焦炉烟道废气中均匀喷入氨气，而静态混合器3g则可以使氨气与焦炉烟道废气进一步充分混合均匀。
[0060] 3)见图2，是除氨脱硝设备4的侧视图；与氨气均匀混合后的焦炉烟道废气进入除氨脱硝设备4进行脱硝除氨；烟气从除氨脱硝设备4侧底部进入，经过脱硝除氨的烟气由除氨脱硝设备4侧顶部或顶部流出；进入除氨脱硝设备4的烟气经过气流分布板4e均布气流后，首先与布袋复合催化剂4a接触。见图3，是布袋复合催化剂结构示意图，布袋复合催化剂4a外表面为耐高温滤袋4a_l，中间为除氨催化剂层4a_2，里层为滤料骨架4a_3。脱硫过程中生成的Na2SO3细粉、未参加反应的NaHCO 3及Na 2C03细粉、烟气中含有的粉尘均被滤袋4a-l过滤在滤袋外表面，烟气则在引风机Ia的负压作用下强制性穿过滤袋，进入并穿过除氨催化剂层4a_2 ;除氨催化剂呈细颗粒状，焦炉烟道废气中的氧含量较低，约为6%，低硫、低温烟气环境中，在除氨催化剂的催化作用下，NH3优先与NOx等强氧化气体反应，将顯!£还原成N2;低温工况下的脱硝效率高达90%，同时氨也与少部分氧反应生成N2和水，除氨催化剂催化作用下的氨反应效率高达98%。
[0061] 滤袋4a_l用于滤除颗粒物及粉尘，随着滤袋4a_l表面颗粒附着物的增加，除氨脱硝设备4阻力也会增加，利用压缩空气通过脉冲清灰装置4b对布袋复合催化剂4a进行脉冲清灰，除下的颗粒物落入除氨脱硝设备4底部灰仓4c ;烟气穿过滤袋4a_l外表面颗粒物层时，烟气中残留的SO# NaHCO 3及Na 2C03细粉继续发生反应，进一步提高脱硫效率。
[0062] 引风机Ia配有变频电机。通过对引风机Ia进行变频调速，并调节烟道气入口风量调节阀lb，既可以保证焦炉正常生产所需要的负压值，也可以保证脱硫脱硝工艺系统正常工作所需要的压力值。
[0063] 除氨脱硝设备焦炉烟道废气入口处设气流分布板4e，将气流均布至布袋复合催化剂4a，同时由于布袋复合催化剂层具有一定的阻力，具有一定的均压作用，利于设备内部气流场及温度场均布。
[0064] 通过脉冲清灰装置4b反吹清灰，不仅可以清掉滤袋4a_l外表面附着的颗粒物，同时可以清除除氨催化剂颗粒之间夹杂的粉尘，提高除氨催化剂的使用效率及使用寿命。
[0065] 灰仓4出口设密闭排料锁气阀4d，防止外部空气由出灰口不严密处渗入，降低烟气温度。
[0066] 4)经过脱硫脱硝除氨全过程处理后的焦炉烟道废气达到国家排放标准，返回焦炉烟囱排放；除氨脱硝设备4中收集的颗粒物及粉尘通过密闭排料锁气阀4d排料后，由刮板输送机6a、链斗式提升机6b输送至颗粒物IC仓6c 存，并定期外运出售。
[0067] 压缩空气用于除氨脱硝设备清灰、脱硫剂干粉流态化、启闭密闭排料锁气阀。
[0068] 本发明一种低温烟气脱硫脱硝除氨一体化工艺，适用于烟气温度大于180°C，SO2含量小于150mg/Nm3的焦炉烟道废气脱硫脱硝。
Claims (9)
1.一种低温烟气脱硫脱硝除氨一体化工艺，其特征在于，适用于烟气温度大于180°c，SCV#量小于150mg/Nm3的焦炉烟道废气脱硫脱硝及同时除氨；该工艺根据流态化原理，在脱硝之前先进行干法脱硫，采用焦化厂蒸氨工段产生的剩余氨水蒸发出来的氨气作为还原剂，利用布袋-除氨催化剂复合结构作为除尘及脱硝手段，高效脱硫脱硝的同时，能够控制氨逃逸量低于国家排放标准值；具体步骤如下: 1)低温烟气在脱硝之前先采取脱硫措施，在除氨脱硝设备烟道气入口管道上设脱硫催化剂喷入口，贮存在干粉贮存槽中的NaHCO3细粉脱硫剂通过压缩空气及干粉流态化设备流化后，由脱硫剂喷入口喷入焦炉烟道废气输送管道；流态化NaHC0#H粉与焦炉烟道废气接触后，在热烟气中多数分解生成细度更小、比表面积更大、活性度更高的Na2CO3, NaHC03与似20)3细粉均与SO 2反应生成Na 2S03，脱除烟气中的SO2; 2)脱硫后的烟道废气输送管道上设有喷氨格栅及静态混合器，焦化厂煤气净化工艺蒸氨工序产生的剩余氨水存放在氨水贮罐中，经过氨喷淋蒸发器被蒸发成氨气，与一部分烟气混合后通过喷氨格栅均匀喷入烟气中，通过静态混合器与焦炉烟道废气均匀混合； 3)与氨气均匀混合后的焦炉烟道废气进入除氨脱硝设备进行脱硝除氨；烟气从除氨脱硝设备侧底部进入，经过脱硝除氨的烟气由除氨脱硝设备侧顶部或顶部流出；进入除氨脱硝设备的烟气首先与布袋复合催化剂接触，脱硫过程中生成的Na2SO3细粉、未参加反应的NaHC03& Na2CO3细粉、烟气中含有的粉尘均被滤袋过滤在滤袋外表面，烟气则在引风机的负压作用下强制性穿过滤袋，进入并穿过除氨催化剂层；除氨催化剂呈细颗粒状，低硫、低温烟气环境中，在除氨催化剂的催化作用下，NH3优先与NOx等强氧化气体反应，将顯!£还原成N2;随着滤袋表面颗粒附着物的增加，除氨脱硝设备阻力也会增加，利用压缩空气通过清灰装置对布袋复合催化剂进行脉冲清灰，除下的颗粒物落入除氨脱硝设备底部灰仓；烟气穿过滤袋外表面颗粒物层时，烟气中残留的302与NaHCO 3及Na 2C03细粉继续发生反应，进一步提尚脱硫效率； 4)经过脱硫脱硝除氨全过程处理后的焦炉烟道废气达到国家排放标准，返回焦炉烟囱排放；除氨脱硝设备收集的颗粒物通过出灰口排出，通过刮板输送机及链斗式提升机输送至颗粒物贮仓，定期外运销售。
2.根据权利要求1所述的一种低温烟气脱硫脱硝除氨一体化工艺，其特征在于，所述除氨脱硝设备采用脉冲袋式除尘器结构形式，布袋复合催化剂外表面为耐高温滤袋，中间为除氨催化剂层，里层为滤料骨架；滤袋用于滤除颗粒物及粉尘，除氨催化剂用于高效脱硝除氨；通过清灰装置脉冲反吹清灰，不仅可以清掉滤袋外表面附着的颗粒物，同时可以清除除氨催化剂颗粒之间夹杂的粉尘，提高除氨催化剂的使用效率及使用寿命。
3.根据权利要求1或2所述的一种低温烟气脱硫脱硝除氨一体化工艺，其特征在于，所述除氨脱硝设备焦炉烟道废气入口处设气流分布板，将气流均布至布袋复合催化剂，同时由于布袋复合催化剂层具有一定的阻力，具有一定的均压作用，利于设备内部气流场及温度场均布。
4.根据权利要求1或2所述的一种低温烟气脱硫脱硝除氨一体化工艺，其特征在于，所述除氨脱硝设备出灰口设密闭排料锁气阀，防止由于室外空气通过出料口渗透进设备中降低处理烟气温度。
5.根据权利要求1所述的一种低温烟气脱硫脱硝除氨一体化工艺，其特征在于，所述引风机配有变频电机，通过对引风机进行变频调速，并调节烟道气入口风量调节阀，既可以保证焦炉正常生产所需要的负压值，也可以保证脱硫脱硝工艺系统正常工作所需要的压力值。
6.根据权利要求1所述的一种低温烟气脱硫脱硝除氨一体化工艺，其特征在于，所述氨水为焦化厂煤气净化工艺蒸氨工序产生的浓度为15〜18%的剩余氨水，氨水贮罐用于稳定脱硝系统氨水流量及浓度，根据焦炉烟道废气中的NOx含量，可变频调节氨水供给泵的供给量。
7.根据权利要求1所述的一种低温烟气脱硫脱硝除氨一体化工艺，其特征在于，所述氨喷淋蒸发器所用热媒为经过脱硫脱硝后的焦炉烟道废气，经过脱硫脱硝后的焦炉烟道废气还用于稀释氨气浓度，提高氨气温度，同时可以使喷入的氨更好的与焦炉烟道废气混合，并减少由于氨气喷入而引起的烟气温度下降。
8.根据权利要求1所述的一种低温烟气脱硫脱硝除氨一体化工艺，其特征在于，所述压缩空气用于除氨脱硝设备清灰、脱硫剂干粉流态化、启闭密闭排料锁气阀。
9.根据权利要求1所述的一种低温烟气脱硫脱硝除氨一体化工艺，其特征在于，所述引风机安装在靠近除氨脱硝设备出口附近的烟气管道上，焦炉烟囱底部两侧烟道气入口处设置烟道气入口风量调节阀； 所述干粉贮存槽设在除氨脱硝设备烟道气入口管道旁，底部设置变频定量给料设备及干粉流态化设备，干粉流态化设备通过脱硫催化剂喷入口连接烟气管道； 所述氨水储罐出口处设氨水定量供给泵，并通过管道依次连通氨喷淋蒸发器、氨气缓冲罐、氨气-烟气混合器，氨喷淋蒸发器的两端通过管道接入脱硫脱硝除氨处理后的烟气管道，形成回路，其位于氨喷淋蒸发器前的管路另设一管道支路依次连通氨气-烟气混合器和安装在除氨脱硝设备入口管道上的喷氨格栅，静态混合器安装在喷氨格栅位于烟气输送方向前方的烟气管道中； 所述除氨脱硝设备底部为灰仓，灰仓出口设密闭排料锁气阀，灰仓上部设布袋复合催化剂，布袋复合催化剂侧面烟气入口处设气流分布板，布袋复合催化剂顶部设脉冲清灰装置，除氨脱硝设备侧底部连接烟道气入口，除氨脱硝设备侧顶部或顶部连接烟道气出口 ； 所述刮板输送机位于除氨脱硝设备灰仓的下方，其尾部通过管道接入链斗式提升机下部，颗粒物贮仓的上方连接链斗式提升机，下方出料口设有螺杆式插板阀； 所述压缩空气贮存在压缩空气贮罐中，通过连接管道分别连接除氨脱硝设备脉冲清灰装置、脱硫剂干粉流态化设备和除氨脱硝设备出灰口的密闭排料锁气阀。
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Effective date of registration: 20180802 Address after: 116085 128 high energy street, Qixian Ling high tech Industrial Park, Dalian, Liaoning Patentee after: ACRE Coking And Refractory (Dalian) Engineering Consulting Corp., MCC Address before: 116085 128 high energy street, Qixian Ling high tech Industrial Park, Dalian, Liaoning Patentee before: ACRE Coking and Refractory Engineering Consulting Corporation, MCC |