CN204365119U - 一种焦炉烟气脱硝脱硫及再热系统工艺装置 - Google Patents
一种焦炉烟气脱硝脱硫及再热系统工艺装置 Download PDFInfo
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- CN204365119U CN204365119U CN201420852405.3U CN201420852405U CN204365119U CN 204365119 U CN204365119 U CN 204365119U CN 201420852405 U CN201420852405 U CN 201420852405U CN 204365119 U CN204365119 U CN 204365119U
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- CN
- China
- Prior art keywords
- flue gas
- ammoniacal liquor
- ammonia
- desulfurizing tower
- heater
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- 230000003009 desulfurizing Effects 0.000 title claims abstract description 53
- 239000003546 flue gas Substances 0.000 title claims abstract description 45
- UGFAIRIUMAVXCW-UHFFFAOYSA-N carbon monoxide Chemical compound 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[O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 title claims abstract description 44
- 238000006477 desulfuration reaction Methods 0.000 title claims abstract description 38
- 239000000571 coke Substances 0.000 title claims abstract description 19
- 230000026676 system process Effects 0.000 title claims abstract description 8
- 235000011114 ammonium hydroxide Nutrition 0.000 claims abstract description 35
- 239000000779 smoke Substances 0.000 claims abstract description 28
- 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 claims abstract description 21
- 238000010790 dilution Methods 0.000 claims abstract description 9
- VHUUQVKOLVNVRT-UHFFFAOYSA-N ammonium hydroxide Chemical compound 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[NH4+].[OH-] VHUUQVKOLVNVRT-UHFFFAOYSA-N 0.000 claims abstract description 7
- 239000003517 fume Substances 0.000 claims abstract description 4
- 238000010438 heat treatment Methods 0.000 claims description 7
- 239000007789 gas Substances 0.000 claims description 5
- 229920002456 HOTAIR Polymers 0.000 claims description 4
- 239000008246 gaseous mixture Substances 0.000 claims description 2
- 238000005260 corrosion Methods 0.000 abstract description 5
- 239000002918 waste heat Substances 0.000 abstract description 2
- 238000000034 method Methods 0.000 description 8
- 239000003795 chemical substances by application Substances 0.000 description 4
- 239000003638 reducing agent Substances 0.000 description 4
- 238000004519 manufacturing process Methods 0.000 description 3
- MWUXSHHQAYIFBG-UHFFFAOYSA-N Nitrogen oxide Substances 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O=[N] MWUXSHHQAYIFBG-UHFFFAOYSA-N 0.000 description 2
- 239000002253 acid Substances 0.000 description 2
- 230000000607 poisoning Effects 0.000 description 2
- 231100000572 poisoning Toxicity 0.000 description 2
- RAHZWNYVWXNFOC-UHFFFAOYSA-N sulphur dioxide Chemical compound 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- NINIDFKCEFEMDL-UHFFFAOYSA-N sulfur Chemical compound 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[S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 1
- 229910052717 sulfur Inorganic materials 0.000 description 1
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Abstract
本实用新型提供一种焦炉烟气脱硝脱硫及再热系统工艺装置，由SCR脱硝反应器（1）、 GGH烟气再热器（2）、脱硫塔（3）、氨水蒸发器（4）、氨空混合器（5）、稀释风机（6）、氨水稀释罐（7）、氨水泵（8）、增压风机（9）、烟气切换阀（10）、烟囱（11）及管路相连而成，具有可充分利用厂区废氨水和烟气废热，达到脱硝脱硫目的，提高脱硝脱硫效率、降低运行成本、避免系统腐蚀等等优点。
Description
技术领域
[0001] 本实用新型属于焦炉烟气治理技术领域，涉及一种焦炉烟气脱硝脱硫及再热系统工艺装置。主要应用于焦化行业焦炉以及其它工业窑炉排放的烟气脱硝脱硫。
技术背景
[0002] 焦炉生产过程中产生的大量荒煤气，通过加热炉燃烧后排放的烟气中含有大量的二氧化硫和氮氧化物污染物污染大气环境，其他窑炉生产过程中排放的烟气也存在同样污染问题。随着国家对大气污染治理的日益重视和排放标准的提高，焦炉烟气和其他窑炉烟气污染治理迫在眉睫。由于焦炉生产的特殊性，即焦炉生产一般连续生产不能停炉停电，生产中产生大量剩余氨水、排放的烟气温度露点低等特点。以往焦炉等窑炉脱硝，一般采用炉内脱硝或煤气干法脱硝，效率低，尤其存在容易造成主炉系统堵塞等问题；脱硫一般采用烟气湿法脱硫，由于脱硫后烟气温度大幅度降低至80°C酸露点以下，会造成脱硫塔后续烟道及烟®酸腐蚀，而烟道及烟®防腐投资大、施工难度高、运行成本高，以上问题都限制了焦炉烟气脱硝脱硫装置的推广应用。
发明内容
[0003] 本实用新型将SCR脱硝工艺装置、湿法脱硫工艺装置和GGH烟气换热装置合理组合、相互补充，充分利用了高温烟气本身的热能，采用热交换原理，利用GGH再热装置，将脱硫后湿烟气再热，提供一种焦炉烟气脱硝脱硫及再热系统工艺装置，解决了焦炉烟气以往脱硝脱硫效率低、运行成本高、系统腐蚀等问题。
[0004] 本实用新型是通过以下技术方案实现:
[0005] 一种焦炉烟气脱硝脱硫及再热系统工艺装置，由SCR脱硝反应器、GGH烟气再热器、脱硫塔、氨水蒸发器、氨空混合器、稀释风机、氨水稀释罐、氨水泵、增压风机、烟气切换阀、烟囱及管路相连而成，其特征在于:所述的SCR脱硝反应器采用双反应器，与烟气管相接的管路上分别接有烟气切换阀，进氨空混合气端口与氨空混合器管路连接，氨空混合器分别与氨水蒸发器、稀释风机相接；
[0006] 所述的GGH烟气再热器的进热气口与SCR脱硝反应器的出口相连，出热气口经过增压风机与脱硫塔入口相通，氨水稀释罐、氨水泵通过管路也与脱硫塔入口相通，脱硫塔出口经管路与GGH烟气再热器的加热入气口相通，GGH烟气再热器加热出气口与烟囱管路相通；
[0007] 所述的脱硫塔为湿法脱硫塔。
[0008] 所述的氨水蒸发器为水浴式电加热的氨水蒸发器。
[0009] 装置主体包括SCR脱硝反应器、GGH烟气再热器、湿法脱硫塔等工艺装置；工艺流程首先进行烟气脱硝，脱硝后热烟气进入GGH烟气再热器后再进入湿法脱硫塔进行脱硫，脱硫后净湿烟气再进入GGH烟气再热器和热烟气换热后达到露点160°C以上进入烟囱排放；脱硝还原剂和湿法脱硫剂全部采用厂区剩余氨水，用于脱硝的氨水通过水浴式电加热器的氨水蒸发器加热成氨气后再进入脱硝反应器与烟气进行脱硝反应，用于脱硫的氨水进入氨水稀释罐稀释后泵入脱硫塔脱硫；进入脱硫塔烟气需增压风机增压后进入脱硫塔，当脱硫检修或故障停电等情况发生，脱硝后烟气通过切换阀打开直接进烟®排放。
[0010] 所述GGH烟气再热器是一种通过叶轮传动，将脱硝后280_35(TC热烟气和脱硫后70-80°C湿烟气进行换热，使得湿烟气由70-80°C升至160°C以上，热烟气由280_350°C降至150-160。。。
[0011] 所述脱硝脱硫均采用氨水，氨水采用氨水蒸发器电加热成氨气后做SCR脱硝还原齐IJ，氨水稀释后做湿法脱硫塔脱硫剂。
[0012] 所述SCR脱硝反应器采用双反应器，一备一用，通过烟气切换阀切换。其优点是避免烟气焦油等中毒后可在线再生产。
[0013] 将GGH烟气再热器放置在脱硝脱硫工艺装置之间，其好处是:
[0014] 1、可以保证进脱硫塔烟气温度在150-160°C，保证湿法脱硫烟气温度工况；
[0015] 2、提高湿烟气露点，避免脱硫后续烟道和烟囱腐蚀；
[0016] 3、保持烟囱内烟气抬升温度，在停电等事故情况下，可以达到烟气自然排放，不用临时加温烟囱，造成焦炉堵烟事故发生；
[0017] 4、采用厂区剩余氨水做脱硝还原剂和脱硫剂，以废治废。
附图说明
[0018] 附图1为本实用新型工艺装置示意图。
[0019] 图中:1、SCR脱硝反应器，2、GGH烟气再热器，3、脱硫塔，4、氨水蒸发器，5、氨空混合器，6、稀释风机，7、氨水稀释罐，8、氨水泵，9、增压风机，10、烟气切换阀，11、烟囱。
具体实施方式
[0020] 下面结合附图说明具体实施例:
[0021] 来自焦炉烟气首先进入SCR脱硝反应器I进行脱硝，脱硝后热烟气进入GGH烟气再热器2和脱硫塔3脱硫后的湿烟气进行换热，换热后热烟气由280-350°C降至150_160°C后通过增压风机9增压后进入脱硫塔3脱硫，脱硫塔3出口湿烟气进入GGH烟气再热器由70-80°C换热成160°C左右烟气进入烟囱11排放。整个系统烟气通过烟气切换阀10进行切换，即当脱硫检修或故障停电等情况发生，脱硝后烟气通过切换阀打开直接进烟® 11排放；当SCR脱硝反应器内因烟气焦油等中毒后通过烟气切换阀10切换在线再生产。
[0022] 来自厂区20%以上的废氨水一部分通过水浴式电加热的氨水蒸发器4加热成氨气后进入氨空混合器5，由稀释风机6稀释成5%左右的氨气后，做脱硝还原剂，进入SCR脱硝反应器I进行脱硝；另一部分氨水进入氨水稀释罐7稀释成6%左右的氨水由氨水泵8定期打入湿法脱硫塔3脱硫做脱硫剂进行脱硫使用。
[0023] 整套工艺装置有机结合，相互补充，充分利用厂区废氨水和烟气废热，达到脱硝脱硫目的，提高脱硝脱硫效率、降低运行成本、避免系统腐蚀等问题。
Claims (2)
1.一种焦炉烟气脱硝脱硫及再热系统工艺装置，由SCR脱硝反应器(I)、GGH烟气再热器(2)、脱硫塔(3)、氨水蒸发器(4)、氨空混合器(5)、稀释风机(6)、氨水稀释罐(7)、氨水泵(8)、增压风机(9)、烟气切换阀(10)、烟囱(11)及管路相连而成，其特征在于:所述的SCR脱硝反应器(I)采用双反应器，与烟气管相接的管路上分别接有烟气切换阀(10)，进氨空混合气端口与氨空混合器(5)管路连接，氨空混合器(5)分别与氨水蒸发器(4)、稀释风机(6 )相接；所述的GGH烟气再热器(2 )的进热气口与SCR脱硝反应器(I)的出口相连，出热气口经过增压风机(9)与脱硫塔(3)入口相通，氨水稀释罐(7)、氨水泵(8)通过管路也与脱硫塔(3)入口相通，脱硫塔(3)出口经管路与GGH烟气再热器(2)的加热入气口相通，GGH烟气再热器(2)加热出气口与烟囱(11)管路相通；所述的脱硫塔(3)为湿法脱硫塔。
2.根据权利要求1所述的一种焦炉烟气脱硝脱硫及再热系统工艺装置，其特征在于:所述的氨水蒸发器(4)为水浴式电加热的氨水蒸发器。
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| CN104548900A (zh) * | 2014-12-30 | 2015-04-29 | 大连贝斯特环境工程设备有限公司 | 一种焦炉烟气脱硝脱硫及再热系统工艺装置 |
| CN105194990A (zh) * | 2015-10-14 | 2015-12-30 | 中国华能集团清洁能源技术研究院有限公司 | 一种适用于炼焦炉的烟气综合治理系统 |
| CN105344236A (zh) * | 2015-11-13 | 2016-02-24 | 西南化工研究设计院有限公司 | 一种焦炉烟气脱硫脱硝除尘一体化工艺 |
| CN105833688A (zh) * | 2016-05-06 | 2016-08-10 | 山东岱荣节能环保科技有限公司 | 焦炉地下烟道气的节能洁净排放装置 |
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| CN104548900A (zh) * | 2014-12-30 | 2015-04-29 | 大连贝斯特环境工程设备有限公司 | 一种焦炉烟气脱硝脱硫及再热系统工艺装置 |
| CN105194990A (zh) * | 2015-10-14 | 2015-12-30 | 中国华能集团清洁能源技术研究院有限公司 | 一种适用于炼焦炉的烟气综合治理系统 |
| CN105344236A (zh) * | 2015-11-13 | 2016-02-24 | 西南化工研究设计院有限公司 | 一种焦炉烟气脱硫脱硝除尘一体化工艺 |
| CN105833688A (zh) * | 2016-05-06 | 2016-08-10 | 山东岱荣节能环保科技有限公司 | 焦炉地下烟道气的节能洁净排放装置 |
| CN105833688B (zh) * | 2016-05-06 | 2018-03-02 | 山东岱荣节能环保科技有限公司 | 焦炉地下烟道气的节能洁净排放装置 |
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