CN103894051B - 一种烟气湿法脱硫脱硝一体化系统及方法 - Google Patents
一种烟气湿法脱硫脱硝一体化系统及方法 Download PDFInfo
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- CN103894051B CN103894051B CN201210585718.2A CN201210585718A CN103894051B CN 103894051 B CN103894051 B CN 103894051B CN 201210585718 A CN201210585718 A CN 201210585718A CN 103894051 B CN103894051 B CN 103894051B
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- tower
- denitration
- flue gas
- circulating pump
- smoke
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- 230000003009 desulfurizing Effects 0.000 title claims abstract description 58
- 238000006477 desulfuration reactions Methods 0.000 title claims abstract description 37
- 239000007789 gases Substances 0.000 title claims description 18
- UGFAIRIUMAVXCW-UHFFFAOYSA-N carbon monoxide Chemical compound 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[O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims abstract description 37
- 239000003546 flue gases Substances 0.000 claims abstract description 36
- 239000011901 water Substances 0.000 claims abstract description 23
- 239000007788 liquids Substances 0.000 claims abstract description 9
- 239000003595 mist Substances 0.000 claims abstract description 8
- 239000003570 air Substances 0.000 claims abstract description 6
- 238000005406 washing Methods 0.000 claims abstract description 6
- 238000005507 spraying Methods 0.000 claims abstract description 5
- 239000003795 chemical substances by application Substances 0.000 claims description 41
- 238000000034 methods Methods 0.000 claims description 24
- 280000739435 Integral Process companies 0.000 claims description 13
- 241001081830 Degeneriaceae Species 0.000 claims description 10
- 239000007921 sprays Substances 0.000 claims description 9
- 238000000746 purification Methods 0.000 claims description 7
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[O-]S([O-])(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-L 0.000 description 1
- 231100000889 vertigo Toxicity 0.000 description 1
Abstract
本发明涉及一种烟气脱硫脱硝一体化系统及方法，系统包括引风机和脱硫脱硝塔，脱硫脱硝塔底部为水洗段、中部为脱硫段、上部为脱硝段；水洗段的第一喷淋管与水循环系统相连；脱硫段的第二喷淋管与脱硫液循环系统相连；脱硝段的第三喷淋管与脱硝液循环系统相连；脱硫脱硝塔顶部设有捕雾器，脱硫脱硝塔顶部通过管道与换热器相连。方法包括引风机将烟气经换热后送入水洗段，与洗涤水逆流接触降温，接着进入脱硫段，与喷洒下来的脱硫液逆向接触进行脱硫；然后烟气再进入脱硝段，与喷洒下来的脱硝液逆流接触脱硝，脱硝后的烟气经捕雾器除去夹带液滴送入换热器，净烟气经烟道由烟囱排入大气中。
Description
技术领域
[0001] 本发明涉及烟气处理技术领域，特别是涉及一种烟气湿法脱硫脱硝一体化工艺方法。
背景技术
[0002] SOjP NOx均是大气中主要污染物之一，是形成酸雨、酸雾的主要原因之一。除此之外，NOx还参与大气臭氧层的破坏，是一种温室气体。随着《大气污染物综合排放标准》和《火电厂大气污染物排放标准》的相继实施，国家对SOjP NOx排放的要求趋于严格。
[0003] 脱硫脱硝一体化工艺方法可分为同时脱硫脱硝技术和联合脱硫脱硝技术。
[0004] 同时脱硫脱硝技术是指用一种反应剂在一个过程内将烟气中的SOjP NOx同时脱除的技术。如专利200610012525.2提及的液相烟气脱硫脱硝净化方法、电子束法脱硫脱硝技术、脉冲电子晕脱硫脱硝技术以及臭氧脱硫脱硝技术，但该类技术由于成本太高故在工业装置上没有获得推广。
[0005] 联合脱硫脱硝技术是指单独脱硫和单独脱硝通过整合后而形成的一体化技术，如活性炭/活性焦联合脱硫脱硝工艺、B&W公司开发的SNRB脱硫脱硝技术、海尔德-托普索公司开发的SN0X工艺。但活性炭/活性焦法脱硫容量低；SNRB技术脱硫技术较高时才能达到80%，烟气S02含量较高时达不到排放要求；SN0X工艺的能耗大、投资费用高。这些技术自身的缺点限制了其工业应用的普适性。
发明内容
[0006] 本发明所要解决的技术问题是提供一种烟气湿法脱硫脱硝一体化工艺方法，能够稳定、高效、低成本且能满足国家排放标准。
[0007] 本发明解决其技术问题所采用的技术方案是:提供一种烟气湿法脱硫脱硝一体化工艺方法，主要设备包括换热器、脱除塔、脱硝剂循环栗、脱硫剂循环栗和水循环栗，所述脱除塔底部和水循环栗之间、脱除塔中段和脱硫剂循环栗之间、脱除塔上段和脱硝剂循环栗之间分别形成自循环系统；该工艺方法包括以下步骤:
[0008] (1)将烟气经换热器引入到脱除塔内；
[0009] (2)在脱除塔底部通过水喷雾除尘降温；
[0010] (3)在脱除塔中段采用脱硫剂逆流接触进行脱硫；
[0011] (4)在脱除塔上段采用脱硝剂逆流接触进行脱硝；
[0012] (5)在塔内经捕雾器净化后的烟气经换热器与烟气进行换热升温至露点以上时排入烟囱放空。
[0013] 所述步骤(1)中烟气采用引风机增压输送，经换热器换热降温至70-95 V后进入脱除塔，且在换热器与脱除塔相连的管道上还设有补氧管路，可根据需要补充空气、氧气、臭氧或气/汽态氧化剂。
[0014] 所述步骤(2)中烟气进入脱除塔底部并经水喷雾除尘降温至30-65°C，所述水喷雾为工业水，当水洗段出现温度超标时，打开工业水进水阀补水降温并用循环水栗排出等量的废液。
[0015] 所述步骤(3)中烟气经除尘降温之后进入脱除塔中段与脱硫剂逆流接触，脱硫过程采用填料塔或者空塔喷淋。
[0016] 所述脱硫剂在脱除塔中段、脱硫剂循环栗组成的自循环系统内循环，直至达到工艺设定值后将脱硫剂引出自循环系统外。
[0017] 所述步骤(4)中烟气脱硫之后进入脱除塔上段与脱硝剂逆流接触，脱硝过程采用填料塔、板式塔或者空塔喷雾。
[0018] 所述脱硝剂在脱除塔上段、脱硝剂循环栗组成的系统内循环直至达到工艺设定值后将脱硝液引出系统外。
[0019] 有益效果
[0020] 由于采用了上述的技术方案，本发明与现有技术相比，具有以下的优点和积极效果:
[0021] 与传统的烟气脱硫、脱硝过程相比，本发明的脱硫脱硝工艺流程更简单，将降温、除尘、脱硫、脱硝集成在一座塔内，减少了占地面积和设备数量，节省投资和运维费用。烟道气从塔底进入，并在塔底部换热降温和洗涤粉尘，然后进入塔中段，与脱硫液逆流接触进行脱硫，最后进入塔上段，与脱硝液逆流接触进行脱硝，脱硝后的净烟气与原烟气换热后放空。
[0022] 本发明使烟气在塔中段脱硫的的同时亦能脱除部分NOx，然后再行脱硝以达到脱除NOx的目的，至烟气排放完全达标。合理地利用了脱硫技术效率高、成本低的优点，又通过两次脱硝实现减少NOx排放，达到并高于国家对污染物的排放要求。
[0023] 本发明脱除塔操作温度为38〜98°C，操作范围更宽；全塔阻力只有2.0kPa,更节能；脱硫效率稳定值在95%以上，脱硝效率稳定值在80%以上，净化后的烟气SO2含量^ 100mg/Nm3，N0x含量彡100mg/Nm3，完全达到《大气污染物综合排放标准》和《火电厂大气污染物排放标准》等规范中对SOjP NOx的排放要求。
附图说明
[0024] 图1是本发明烟气湿法脱硫脱硝一体化工艺方法流程简图。
具体实施方式
[0025] 下面结合具体实施例，进一步阐述本发明。应理解，这些实施例仅用于说明本发明而不用于限制本发明的范围。此外应理解，在阅读了本发明讲授的内容之后，本领域技术人员可以对本发明作各种改动或修改，这些等价形式同样落于本申请所附权利要求书所限定的范围。
[0026] 本发明涉及一种烟气湿法脱硫脱硝一体化工艺方法，主要设备包括换热器、脱除塔、脱硝剂循环栗、脱硫剂循环栗和水循环栗，所述脱除塔底部和水循环栗之间、脱除塔中段和脱硫剂循环栗之间、脱除塔上段和脱硝剂循环栗之间分别形成自循环系统；该工艺方法是将烟气经换热器引入到脱除塔内，然后在脱除塔底部通过水喷雾除尘降温，在脱除塔中段采用脱硫剂逆流接触进行脱硫，在脱除塔上段采用脱硝剂逆流接触进行脱硝；在塔内经捕雾器净化后的烟气经换热器与烟气进行换热升温至露点以上时排入烟囱放空。
[0027] 如图1所示，从引风机1来的约140°C原烟气经换热器2后温度降为70〜95°C，进入脱除塔3底部与雾状水逆流接触，原烟气粉尘被净化的同时温度进一步降低至30〜65°C，如果雾状水的水温超过70°C时则需要引入新的水源使水温降低。然后进入脱除塔3中段脱硫段，与喷洒下来的脱硫液逆向接触并进行化学反应，302被转化为硫酸盐，脱硫过程采用填料塔或者空塔喷淋；烟气再进脱除塔3上段，与塔顶喷淋的脱硝液逆流接触，NOx转化为硝酸盐类，脱硝过程采用填料塔、板式塔或者空塔喷雾。脱硝后烟气经捕雾器，除去夹带液滴，离开脱除塔3，经换热器2与原烟气换热后的净烟气经烟道由烟囱排入大气中。
[0028] 塔底循环洗涤水由水循环栗6抽出经过滤后返回塔内，蒸发减少的水分用工业净水补充，当烟温超标时亦通过喷洒工业水进行降温，并同时将部分废液排出；中段脱硫剂由脱硫剂循环栗5送回塔中段循环喷洒；上段脱硝剂由脱硝剂循环栗4压送至塔上段循环喷洒。当脱硫、脱硝剂分别达到工艺控制值时，从塔内引出部分失效的脱硫剂和脱硝剂并同时向塔内补充新脱硫剂和新脱硝剂。当出口烟气中S02含量无法达到排放要求时，即认为达到了工艺设定值；同理，当出口烟气中NOx含量无法达到排放要求时，即认为达到了工艺设定值。
[0029] 根据脱除塔阻力控制值，启动捕雾器清扫装置。如果脱硝效率低于75%，向烟气进口管道补充空气、氧气、臭氧或气/汽态氧化剂等以提供氧化剂，使得氧气占总烟气量的8%_15%，以确保NOx排放满足国家标准。
[0030] 本发明脱硫脱硝塔操作温度为38〜100°C，操作范围更宽；全塔阻力只有L 2kPa，更节能；脱硫效率稳定值为95%，脱硝效率稳定值为90%，净化后的烟气S02含量< lOOmg/Nm3，NOx含量< 100mg/Nm3，完全达到《大气污染物综合排放标准》和《火电厂大气污染物排放标准》中对SOjP NOx的排放要求。
Claims (7)
1.一种烟气湿法脱硫脱硝一体化工艺方法，主要设备包括换热器、脱除塔、脱硝剂循环栗、脱硫剂循环栗和水循环栗，所述脱除塔底部和水循环栗之间、脱除塔中段和脱硫剂循环栗之间、脱除塔上段和脱硝剂循环栗之间分别形成自循环系统；该工艺方法包括以下步骤: (1)将烟气经换热器引入到脱除塔内； (2)在脱除塔底部通过水喷雾除尘降温， (3)在脱除塔中段采用脱硫剂逆流接触进行脱硫， (4)在脱除塔上段采用脱硝剂逆流接触进行脱硝； 在塔内经捕雾器净化后的烟气经换热器与烟气进行换热升温至露点以上时排入烟囱放空；所述步骤(1)中烟气采用引风机增压输送，经换热器换热降温至70-95°C后进入脱除 ο
2.根据权利要求1所述的烟气湿法脱硫脱硝一体化工艺方法，其特征在于，在换热器与脱除塔相连的管道上还设有补氧管路，可根据需要补充空气、氧气、臭氧或气/汽态氧化剂。
3.根据权利要求1所述的烟气湿法脱硫脱硝一体化工艺方法，其特征在于，所述步骤(2)中烟气进入脱除塔底部并经水喷雾除尘降温至30-65°C，所述水喷雾为工业水，当水洗段出现温度超标时，打开工业水进水阀补水降温并用循环水栗排出等量的废液。
4.根据权利要求1所述的烟气湿法脱硫脱硝一体化工艺方法，其特征在于，所述步骤(3)中烟气经除尘降温之后进入脱除塔中段与脱硫剂逆流接触，脱硫过程采用填料塔或者空塔嗔淋。
5.根据权利要求4所述的烟气湿法脱硫脱硝一体化工艺方法，其特征在于，所述脱硫剂在脱除塔中段、脱硫剂循环栗组成的自循环系统内循环，直至达到工艺设定值后将脱硫剂引出自循环系统外。
6.根据权利要求1所述的烟气湿法脱硫脱硝一体化工艺方法，其特征在于，所述步骤(4)中烟气脱硫之后进入脱除塔上段与脱硝剂逆流接触，脱硝过程采用填料塔、板式塔或者空塔喷雾。
7.根据权利要求6所述的烟气湿法脱硫脱硝一体化工艺方法，其特征在于，所述脱硝剂在脱除塔上段、脱硝剂循环栗组成的系统内循环直至达到工艺设定值后将脱硝液引出系统外。
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