CN107051064A - 一种焚烧尾气除尘及硫回收系统及其使用方法 - Google Patents
一种焚烧尾气除尘及硫回收系统及其使用方法 Download PDFInfo
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- CN107051064A CN107051064A CN201710058599.8A CN201710058599A CN107051064A CN 107051064 A CN107051064 A CN 107051064A CN 201710058599 A CN201710058599 A CN 201710058599A CN 107051064 A CN107051064 A CN 107051064A
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- Prior art keywords
- sulfur
- liquid
- bearing
- gas
- desorption reaction
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- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 title claims abstract description 86
- 229910052717 sulfur Inorganic materials 0.000 title claims abstract description 73
- 239000011593 sulfur Substances 0.000 title claims abstract description 73
- 238000011084 recovery Methods 0.000 title claims abstract description 23
- 238000000034 method Methods 0.000 title claims description 16
- 239000007788 liquid Substances 0.000 claims abstract description 122
- 238000003795 desorption Methods 0.000 claims abstract description 61
- 238000006243 chemical reaction Methods 0.000 claims abstract description 59
- 239000007789 gas Substances 0.000 claims abstract description 52
- 239000003054 catalyst Substances 0.000 claims abstract description 50
- 239000003513 alkali Substances 0.000 claims abstract description 43
- 238000002347 injection Methods 0.000 claims abstract description 43
- 239000007924 injection Substances 0.000 claims abstract description 43
- 239000006096 absorbing agent Substances 0.000 claims abstract description 41
- 238000001179 sorption measurement Methods 0.000 claims abstract description 37
- RAHZWNYVWXNFOC-UHFFFAOYSA-N Sulphur dioxide Chemical compound O=S=O RAHZWNYVWXNFOC-UHFFFAOYSA-N 0.000 claims abstract description 30
- 239000003546 flue gas Substances 0.000 claims abstract description 30
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims abstract description 26
- 238000010521 absorption reaction Methods 0.000 claims abstract description 21
- 239000000428 dust Substances 0.000 claims abstract description 20
- 238000011069 regeneration method Methods 0.000 claims abstract description 12
- 230000008929 regeneration Effects 0.000 claims abstract 3
- 238000003672 processing method Methods 0.000 claims abstract 2
- HEMHJVSKTPXQMS-UHFFFAOYSA-M sodium hydroxide Inorganic materials [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 claims description 72
- AZQWKYJCGOJGHM-UHFFFAOYSA-N 1,4-benzoquinone Chemical compound O=C1C=CC(=O)C=C1 AZQWKYJCGOJGHM-UHFFFAOYSA-N 0.000 claims description 12
- 229910021645 metal ion Inorganic materials 0.000 claims description 12
- 239000005864 Sulphur Substances 0.000 claims description 11
- 239000000126 substance Substances 0.000 claims description 10
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 claims description 8
- 238000004581 coalescence Methods 0.000 claims description 8
- 239000000779 smoke Substances 0.000 claims description 8
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 5
- 229910052760 oxygen Inorganic materials 0.000 claims description 5
- 239000001301 oxygen Substances 0.000 claims description 5
- CDBYLPFSWZWCQE-UHFFFAOYSA-L Sodium Carbonate Chemical compound [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 claims description 4
- 229910021529 ammonia Inorganic materials 0.000 claims description 4
- 239000003795 chemical substances by application Substances 0.000 claims description 4
- 238000000926 separation method Methods 0.000 claims description 4
- 239000000243 solution Substances 0.000 claims description 4
- 239000007921 spray Substances 0.000 claims description 4
- 238000001816 cooling Methods 0.000 claims description 3
- 239000008187 granular material Substances 0.000 claims description 3
- 150000008442 polyphenolic compounds Chemical class 0.000 claims description 3
- 235000013824 polyphenols Nutrition 0.000 claims description 3
- 230000001105 regulatory effect Effects 0.000 claims description 3
- 239000002699 waste material Substances 0.000 claims description 3
- KWYUFKZDYYNOTN-UHFFFAOYSA-M Potassium hydroxide Chemical compound [OH-].[K+] KWYUFKZDYYNOTN-UHFFFAOYSA-M 0.000 claims description 2
- 230000003647 oxidation Effects 0.000 claims description 2
- 238000007254 oxidation reaction Methods 0.000 claims description 2
- 229910000029 sodium carbonate Inorganic materials 0.000 claims description 2
- 238000004804 winding Methods 0.000 claims description 2
- 238000006555 catalytic reaction Methods 0.000 claims 2
- 239000000203 mixture Substances 0.000 claims 1
- 238000006477 desulfuration reaction Methods 0.000 abstract description 9
- 230000023556 desulfurization Effects 0.000 abstract description 9
- 238000012546 transfer Methods 0.000 abstract description 3
- 238000005520 cutting process Methods 0.000 abstract description 2
- 230000005484 gravity Effects 0.000 abstract description 2
- 238000012423 maintenance Methods 0.000 abstract description 2
- 230000002045 lasting effect Effects 0.000 abstract 1
- 238000012545 processing Methods 0.000 description 6
- 230000000694 effects Effects 0.000 description 4
- 239000000463 material Substances 0.000 description 3
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 2
- GWEVSGVZZGPLCZ-UHFFFAOYSA-N Titan oxide Chemical compound O=[Ti]=O GWEVSGVZZGPLCZ-UHFFFAOYSA-N 0.000 description 2
- 230000003197 catalytic effect Effects 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 239000001257 hydrogen Substances 0.000 description 2
- 229910052739 hydrogen Inorganic materials 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 238000004073 vulcanization Methods 0.000 description 2
- PEDCQBHIVMGVHV-UHFFFAOYSA-N Glycerine Chemical compound OCC(O)CO PEDCQBHIVMGVHV-UHFFFAOYSA-N 0.000 description 1
- 238000003916 acid precipitation Methods 0.000 description 1
- 238000012271 agricultural production Methods 0.000 description 1
- 239000000809 air pollutant Substances 0.000 description 1
- 231100001243 air pollutant Toxicity 0.000 description 1
- 235000011114 ammonium hydroxide Nutrition 0.000 description 1
- BFNBIHQBYMNNAN-UHFFFAOYSA-N ammonium sulfate Chemical group N.N.OS(O)(=O)=O BFNBIHQBYMNNAN-UHFFFAOYSA-N 0.000 description 1
- 229910052921 ammonium sulfate Inorganic materials 0.000 description 1
- 235000011130 ammonium sulphate Nutrition 0.000 description 1
- 238000000889 atomisation Methods 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000004523 catalytic cracking Methods 0.000 description 1
- 235000019504 cigarettes Nutrition 0.000 description 1
- 238000010276 construction Methods 0.000 description 1
- 230000003009 desulfurizing effect Effects 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 239000003337 fertilizer Substances 0.000 description 1
- 239000003500 flue dust Substances 0.000 description 1
- 230000002779 inactivation Effects 0.000 description 1
- 239000002563 ionic surfactant Substances 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 239000003595 mist Substances 0.000 description 1
- 239000002245 particle Substances 0.000 description 1
- 239000002243 precursor Substances 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 239000000376 reactant Substances 0.000 description 1
- 238000011160 research Methods 0.000 description 1
- 210000001533 respiratory mucosa Anatomy 0.000 description 1
- 239000002689 soil Substances 0.000 description 1
- 239000004071 soot Substances 0.000 description 1
- 238000003860 storage Methods 0.000 description 1
- 239000004408 titanium dioxide Substances 0.000 description 1
- 238000005406 washing Methods 0.000 description 1
Classifications
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Abstract
本发明公开了一种焚烧尾气除尘及硫回收系统,其包括吸附单元和脱附‑再生单元,所述吸附单元包括旋流喷射吸附器、气液分离器、碱液缓冲罐和吸附液泵;所述脱附‑再生单元包括过滤器、含硫液贮存罐、含硫液泵、脱附反应器和催化剂再生器。本发明还公开了所述焚烧尾气除尘及硫回收系统的焚烧尾气处理方法。含尘含硫的焚烧尾气进入所述旋流喷射吸附器后可切向高速旋转形成超重力场,持续切割径向喷入的流线型吸附液,烟气和吸附液之间的传质得到强化,吸附液对粉尘和二氧化硫的吸附和反应效率大大提高。所述旋流喷射吸附器可同时进行除尘和脱硫,结构更加简单、占地面积大大减小、成本低且易于装配维修。
Description
本发明申请要求名称为“一种高效硫化氢气体吸收装置”,申请日是2016年9月21日,申请号是201610494578.6的发明,作为本发明中旋流喷射吸附器结构的优先权。
技术领域
本发明属于石油化工与环保领域,涉及一种焚烧尾气除尘及硫回收系统及其使用方法。
背景技术
我国大气污染物排放量巨大。据统计,我国SO2年排放量超过2000万吨,烟尘排放量超过1200万吨,居世界首位。SO2是酸雨的前体物之一,人体吸入后对眼及呼吸道粘膜有强烈的刺激作用,烟尘的直接排空使雾霾天气日益严重。
研究发现,氨液对二氧化硫有较好的吸收效果,同时吸收产生的副产物为硫酸铵可作为化肥用于农业生产,不但可以给电厂带来经济效益,弥补烟气污染控制费用支出,还能实现二氧化硫的土壤和生物固定。
目前常用的除尘脱硫方法,是将脱硫与除尘两种工艺分开进行的。使得工艺流程较为复杂,设备台数较多,操作难度较大,占地空间大,前期投资高,转化速度慢,副产物多,不适用于小规模的气体处理装置。
发明内容
因此,针对现有技术中的焚烧尾气的脱硫与除尘设备结构复杂、占地面积大、成本高的技术问题,本发明的目的在于提供一种结构简单、占地面积小的脱硫与除尘同时进行的焚烧尾气除尘及硫回收系统。
本发明的焚烧尾气除尘及硫回收系统包括:
吸附单元,所述吸附单元包括旋流喷射吸附器、气液分离器、碱液缓冲罐和吸附液泵,所述旋流喷射吸附器上部为旋流圆筒体,所述旋流圆筒体顶部设有切向接入的烟气入口;所述旋流圆筒体内部沿着中心轴线设有一排气套管,所述排气套管顶端作为含液烟气出口伸出所述旋流喷射吸附器,所述含液烟气出口与所述气液分离器的入口接通;所述旋流圆筒体侧壁外设有圆柱形外夹套,所述圆柱形外夹套与所述旋流筒体外壁连接构成水力喷射雾化室,所述旋流圆筒体侧壁上均匀开有小孔,所述圆柱形外夹套上端设有一个碱液入口,所述碱液入口与所述碱液缓冲罐出口接通;所述旋流喷射吸附器底部设有含硫含尘液出口;所述吸附液泵安装在所述碱液入口和所述碱液缓冲罐出口之间;所述气液分离器的气体出口排空,所述气液分离器的液体出口与所述碱液缓冲罐入口接通;
脱附-再生单元,所述脱附-再生单元包括过滤器、含硫液贮存罐、含硫液泵、脱附反应器和催化剂再生器,所述过滤器、所述含硫液贮存罐、所述含硫液泵和所述脱附反应器依次连接在所述含硫含尘液出口的下游,所述脱附反应器侧壁设有含硫液入口和催化剂入口,所述脱附反应器顶部设有硫磺出口,所述脱附反应器底部设有脱附反应物出口,所述催化剂再生器侧壁设有脱附反应物入口、空气入口和催化剂出口,所述催化剂再生器底部设有废液出口,所述脱附反应物出口与所述脱附反应物入口接通,所述催化剂出口与所述催化剂入口接通。
较佳的,所述吸附液泵下游、所述含硫液泵下游和所述含液烟气出口下游分别设有调节阀,分别用于调节碱液进入所述旋流喷射吸附器的流量、含硫吸附液进入脱附反应器的流量以及含液烟气进入所述气液分离器的流量,以此保证吸附液的用量适中能够对烟气进行充分的除尘和脱硫同时避免用量过大而浪费,调整所述气压分离器和所述脱附反应器的工作负荷。
较佳的,所述排气套管侧壁外设有圆柱形内夹套,所述圆柱形内夹套与所述排气套管侧壁连接也构成水力喷射雾化室,所述圆柱形内夹套外层均匀开有小孔;所述圆柱形内夹套上端也设有一个碱液入口。
较佳的,所述小孔孔径为0.5~5mm。
较佳的,所述的旋流喷射吸附器为单级,或者为多级串连和/或并联。
较佳的,所述气液分离器为气液聚结分离器。
本发明的另一目的在于提供所述的焚烧尾气除尘及硫回收系统的焚烧尾气处理方法,其包括:
(a)焚烧尾气中粉尘、二氧化硫的吸附分离:含尘含硫的焚烧烟气降温后进入所述旋流喷射吸附器,同时所述碱液贮存罐中的碱液作为吸附液经所述吸附液泵送入所述旋流喷射吸附器,含尘含硫的烟气从所述旋流喷射吸附器入口高速切向进入,碱液从所述旋流圆筒体上的小孔径向喷入,径向喷入的流线型吸附液被切向高速旋转的烟气持续切割,形成无数吸附液雾滴;吸附液雾滴吸附聚并烟气中的粉尘颗粒,同时与烟气中的二氧化硫快速反应将二氧化硫从烟气中分离出来,含尘含硫的吸附液在离心力的作用下沿着所述旋流喷射吸附器的边壁流下自所述含硫液出口流出再进入所述过滤器;含少量吸附液的气体从所述旋流喷射吸附器的顶部流出进入所述气液分离器,聚结回收的吸附液流回碱液贮存罐,净化后的气体排入大气;
(b)产物脱附:含尘含硫的吸附液经所述过滤器过滤后粉尘被去除,含硫的吸附液经所述含硫液泵送至所述脱附反应器中,所述脱附反应器中利用金属离子催化剂脱附出产物硫,金属离子催化剂被还原,产物硫从所述脱附反应器顶部离开,送入后续设备,分离回收单质硫,脱附反应流出物从所述脱附反应器底部流出;
(c)催化剂再生:脱附反应流出物同空气一起进入所述催化剂再生器,所述催化剂再生器中的多酚物质与空气中的氧气结合生成醌,醌将金属离子催化剂氧化复活,恢复氧化脱硫能力,由所述催化剂再生器顶部催化剂出口离开,进入所述脱附反应器,完成工艺的脱硫—再生循环。
较佳的,所述的碱液为液氨、氢氧化钠溶液、氢氧化钾溶液或碳酸钠溶液。
较佳的,所述金属离子催化剂为离子型表面活性物质,可为市售产品。
较佳的,通入的焚烧烟气的流量为50000~200000Nm3/h,优选100000~130000Nm3/h;初始温度为60~160℃,优选70~80℃;压力为3000~7000Pa,优选5000Pa。
本发明的有益效果在于:
1、本发明的焚烧尾气除尘及硫回收系统中,所述旋流喷射吸附器中利用了超重力场强化传质的原理,即含尘含硫的焚烧尾气进入所述旋流喷射吸附器后切向高速旋转形成超重力场,可持续切割径向喷入的流线型吸附液,烟气和吸附液之间的传质得到强化,吸附液对粉尘和二氧化硫的吸附和反应效率大大提高。而且所述旋流喷射吸附器同时进行除尘和脱硫,相比于传统的除尘和脱硫分开的组合设备,结构更加简单、占地面积大大减小、成本低且易于装配维修。
2、烟气中的粉尘和二氧化硫被吸附液洗涤、吸附、反应后,含少量吸附液的气体应该所述气液分离器聚结后净化气体排入大气,聚结的碱液流回所述碱液贮存罐重新利用。而含尘含硫吸附液经过所述过滤器后进入所述脱附反应器,在催化剂的作用下富集出单质硫,与此同时,含有失活的催化剂的脱附反应流出物(溶液)进入所述催化剂再生器,在氧气的作用下,催化剂复活后再次进入所述脱附反应器,如此循环,不仅可以高效的实现硫的回收,而且金属离子催化剂可重复利用,有效降低生产成本。
附图说明
图1为本发明的焚烧尾气除尘及硫回收系统的示意图;
图2为本发明的旋流喷射吸附器的示意图。
附图标记
气液分离器1、风机2、焚烧炉3、碱液缓冲罐4、吸附液泵5、喷射吸附器6、过滤器7、含硫液贮存罐8、含硫液泵9、脱附反应器10、催化剂再生器11。
具体实施方式
以下结合具体实施例,对本发明作进一步说明。应理解,以下实施例仅用于说明本发明而非用于限定本发明的范围。
实施例1
图1所示为本发明一较佳实施例的焚烧尾气除尘及硫回收系统,其包括连接在焚烧炉3和风机2下游的吸附单元和脱附-再生单元。
吸附单元包括旋流喷射吸附器6、气液分离器1、碱液缓冲罐4和吸附液泵5,本发明中旋流喷射吸附器结构,可参见名称为“一种高效硫化氢气体吸收装置”,申请日是2016年9月21日,申请号是201610494578.6的发明。如图2所示,旋流喷射吸附器6上部为旋流圆筒体,旋流圆筒体顶部设有切向接入的烟气入口,烟气入口与风机2的出口接通;旋流圆筒体内部沿着中心轴线设有排气套管,排气套管顶端作为含液烟气出口伸出旋流喷射吸附器,含液烟气出口与气液分离器1的入口接通;旋流圆筒体侧壁外设有圆柱形外夹套,圆柱形外夹套与旋流筒体外壁连接构成水力喷射雾化室,旋流圆筒体侧壁上均匀开有小孔,圆柱形外夹套上端设有一个碱液入口,碱液入口与碱液缓冲罐出口接通;旋流喷射吸附器6底部设有含硫含尘液出口;吸附液泵5安装在旋流喷射吸附器6的碱液入口和碱液缓冲罐4的出口之间;气液分离器的1气体出口与排空管道接通,气液分离器1的液体出口与碱液缓冲罐4入口接通。
脱附-再生单元包括过滤器7、含硫液贮存罐8、含硫液泵9、脱附反应器10和催化剂再生器11,过滤器7、含硫液贮存罐8、含硫液泵9和脱附反应器10依次连接在旋流喷射吸附器6的含硫含尘液出口下游,脱附反应器10侧壁设有含硫液入口和催化剂入口,脱附反应器10顶部设有硫磺出口,脱附反应器10底部设有脱附反应物出口,催化剂再生器11侧壁设有脱附反应物入口、空气入口和催化剂出口,催化剂再生器11底部设有废液出口,其中,脱附反应物出口与脱附反应物入口接通,催化剂出口与催化剂入口接通。
较佳的,吸附液泵5下游、含硫液泵9下游以及旋流喷射吸附器6的含液烟气出口下游分别设有调节阀。
较佳的,该系统中还可增设多个旋流喷射吸附器,可以是串联、并联,还可以是串联和并联相结合,可根据烟气中含硫气体的含量选择。
实施例1技术效果
某在石化公司的2#催化装置焚烧CO焚烧锅炉烟气的处理中,通过本发明的焚烧尾气除尘及硫回收系统,对烟气进行中的催化剂粉尘、SO2进行去除回收,其具体运作过程及效果描述如下:
在某石化公司的催化装置焚烧CO焚烧锅炉烟气的处理中,对烟气进行中的进行除尘和硫回收处理,物料性质及相关参数为:
1、物料性质及相关参数
催化裂化CO焚烧锅炉烟气的流量为128761Nm3/h,初始温度为160℃,压力为5000Pa,NOX为350mg/Nm3,SO2为1500mg/Nm3,粉尘颗粒物的浓度为200mg/Nm3,H2O为10.1%。
2、处理过程
吸附(除尘和脱硫):含尘含二氧化硫的焚烧尾气降温后进入旋流喷射吸附器6,同时碱液贮存罐4中的碱液(液氨)作为吸附液经吸附液泵5送入旋流喷射吸附器6。含二氧化硫烟气从旋流喷射吸附器6顶部的烟气入口高速切向进入,碱液(液氨)从旋流圆筒体上的小孔径向喷入;径向喷入的流线型吸附液被切向高速旋转的烟气持续切割,形成无数吸附液雾滴;一方面,吸附液雾滴吸附聚并烟气中的粉尘颗粒,在离心力的作用下,含尘液滴沿旋流喷射吸附器的边壁流下至底部碱液出口,经过滤器7后溶液中的粉尘被去除。另一方面,碱液雾滴与烟气中的二氧化硫快速反应,经吸收后富含硫的吸附液从旋流喷射吸附器的底部流出,经过滤器后流入含硫吸附液缓冲罐;含少量吸附液的气体从旋流喷射吸附器6的顶部流出进入气液分离器1,聚结回收的吸附液流入碱液贮存罐4,净化后的气体排入大气。
脱附:含硫液经含硫液泵9抽送至脱附反应器10中,脱附反应器10中利用金属离子催化剂脱附出产物硫,金属离子催化剂被还原,产物硫从脱附反应器10顶部离开,送入后续设备,分离回收单质硫;脱附反应流出物从脱附反应器10底部流出。
催化剂再生:脱附反应流出物同空气一起进入催化剂再生器11,催化剂再生器11中的多酚物质与空气中的氧气结合生成醌,醌将金属离子催化剂氧化复活,恢复氧化脱硫能力,由催化剂再生器11顶部溢流口离开,进入脱附反应器10,完成工艺的脱硫—再生循环。
3、处理结果分析
通过使用本法发明的焚烧尾气除尘及硫回收系统处理,烟气中的SO2浓度由1500mg/Nm3及以上降低至40mg/Nm3以下,脱硫总体效率在97%以上,粉尘浓度由200mg/Nm3及以上降低20mg/Nm3以下,粉尘的去除效率在90%以上,大大提高了除尘脱硫的效果与处理量。采用可再生循环的金属离子催化剂,使硫磺单质回收率极大提高。和其他工艺及装置相比,本发明的工艺及装置简化了系统,节省了成本,能产生极大的经济效益。
以上已对本发明创造的较佳实施例进行了具体说明,但本发明创造并不限于实施例,熟悉本领域的技术人员在不违背本发明创新的前提下还可作出种种的等同的变型或替换,这些等同的变型或替换均包含在本申请权利要求所限定的范围内。
Claims (8)
1.一种焚烧尾气除尘及硫回收系统,其特征在于,其包括:
吸附单元,所述吸附单元包括旋流喷射吸附器、气液分离器、碱液缓冲罐和吸附液泵,所述旋流喷射吸附器上部为旋流圆筒体,所述旋流圆筒体顶部设有切向接入的烟气入口;所述旋流圆筒体内部沿着中心轴线设有一排气套管,所述排气套管顶端作为含液烟气出口伸出所述旋流喷射吸附器,所述含液烟气出口与所述气液分离器的入口接通;所述旋流圆筒体侧壁外设有圆柱形外夹套,所述圆柱形外夹套与所述旋流筒体外壁连接构成水力喷射雾化室,所述旋流圆筒体侧壁上均匀开有小孔,所述圆柱形外夹套上端设有一个碱液入口,所述碱液入口与所述碱液缓冲罐出口接通;所述旋流喷射吸附器底部设有含硫含尘液出口;所述吸附液泵安装在所述碱液入口和所述碱液缓冲罐出口之间;所述气液分离器的气体出口排空,所述气液分离器的液体出口与所述碱液缓冲罐入口接通;
脱附-再生单元,所述脱附-再生单元包括过滤器、含硫液贮存罐、含硫液泵、脱附反应器和催化剂再生器,所述过滤器、所述含硫液贮存罐、所述含硫液泵和所述脱附反应器依次连接在所述含硫含尘液出口的下游,所述脱附反应器侧壁设有含硫液入口和催化剂入口,所述脱附反应器顶部设有硫磺出口,所述脱附反应器底部设有脱附反应物出口,所述催化剂再生器侧壁设有脱附反应物入口、空气入口和催化剂出口,所述催化剂再生器底部设有废液出口,所述脱附反应物出口与所述脱附反应物入口接通,所述催化剂出口与所述催化剂入口接通。
2.如权利要求1所述的焚烧尾气除尘及硫回收系统,其特征在于,所述吸附液泵下游、所述含硫液泵下游和所述含液烟气出口下游分别设有调节阀。
3.如权利要求1所述的焚烧尾气除尘及硫回收系统,其特征在于,所述排气套管侧壁外设有圆柱形内夹套,所述圆柱形内夹套与所述排气套管侧壁连接也构成水力喷射雾化室,所述圆柱形内夹套外层均匀开有小孔;所述圆柱形内夹套上端也设有一个碱液入口。
4.如权利要求3所述的焚烧尾气除尘及硫回收系统,其特征在于,所述小孔孔径为0.5~5mm。
5.如权利要求1所述的焚烧尾气除尘及硫回收系统,其特征在于,所述的旋流喷射吸附器为单级,或者为多级串连和/或并联。
6.如权利要求1所述的焚烧尾气除尘及硫回收系统的焚烧尾气处理方法,其特征在于,其包括:
(a)焚烧尾气中粉尘、二氧化硫的吸附分离:含尘含硫的焚烧烟气降温后进入所述旋流喷射吸附器,同时所述碱液贮存罐中的碱液作为吸附液经所述吸附液泵送入所述旋流喷射吸附器,含尘含硫的烟气从所述旋流喷射吸附器入口高速切向进入,碱液从所述旋流圆筒体上的小孔径向喷入,径向喷入的流线型吸附液被切向高速旋转的烟气持续切割,形成无数吸附液雾滴;吸附液雾滴吸附聚并烟气中的粉尘颗粒,同时与烟气中的二氧化硫快速反应将二氧化硫从烟气中分离出来,含尘含硫的吸附液在离心力的作用下沿着所述旋流喷射吸附器的边壁流下自所述含硫液出口流出再进入所述过滤器;含少量吸附液的气体从所述旋流喷射吸附器的顶部流出进入所述气液分离器,聚结回收的吸附液流回碱液贮存罐,净化后的气体排入大气;
(b)产物脱附:含尘含硫的吸附液经所述过滤器过滤后粉尘被去除,含硫的吸附液经所述含硫液泵送至所述脱附反应器中,所述脱附反应器中利用金属离子催化剂脱附出产物硫,金属离子催化剂被还原,产物硫从所述脱附反应器顶部离开,送入后续设备,分离回收单质硫,脱附反应流出物从所述脱附反应器底部流出;
(c)催化剂再生:脱附反应流出物同空气一起进入所述催化剂再生器,所述催化剂再生器中的多酚物质与空气中的氧气结合生成醌,醌将金属离子催化剂氧化复活,恢复氧化脱硫能力,由所述催化剂再生器顶部催化剂出口离开,进入所述脱附反应器,完成工艺的脱硫—再生循环。
7.如权利要求6所述的方法,其特征在于,所述的碱液为液氨、氢氧化钠溶液、氢氧化钾溶液或碳酸钠溶液。
8.如权利要求6所述的方法,其特征在于,通入的焚烧烟气的流量为50000~200000Nm3/h,初始温度为60~160℃,压力为3000~7000Pa。
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CN106823576A (zh) | 2017-06-13 |
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CN106731482A (zh) | 2017-05-31 |
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CN106833758A (zh) | 2017-06-13 |
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