CN201664576U - A device for removing sulfur dioxide from flue gas by using ammonia water - Google Patents
A device for removing sulfur dioxide from flue gas by using ammonia water Download PDFInfo
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- CN201664576U CN201664576U CN2010202922345U CN201020292234U CN201664576U CN 201664576 U CN201664576 U CN 201664576U CN 2010202922345 U CN2010202922345 U CN 2010202922345U CN 201020292234 U CN201020292234 U CN 201020292234U CN 201664576 U CN201664576 U CN 201664576U
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- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 title claims abstract description 72
- 239000003546 flue gas Substances 0.000 title claims abstract description 72
- RAHZWNYVWXNFOC-UHFFFAOYSA-N Sulphur dioxide Chemical compound O=S=O RAHZWNYVWXNFOC-UHFFFAOYSA-N 0.000 title claims abstract description 40
- 235000011114 ammonium hydroxide Nutrition 0.000 title claims abstract description 15
- VHUUQVKOLVNVRT-UHFFFAOYSA-N Ammonium hydroxide Chemical compound [NH4+].[OH-] VHUUQVKOLVNVRT-UHFFFAOYSA-N 0.000 title claims abstract description 13
- 238000010521 absorption reaction Methods 0.000 claims abstract description 97
- 239000002002 slurry Substances 0.000 claims abstract description 58
- 239000007788 liquid Substances 0.000 claims abstract description 42
- 238000012856 packing Methods 0.000 claims abstract description 40
- 239000007921 spray Substances 0.000 claims abstract description 37
- 238000005273 aeration Methods 0.000 claims abstract description 11
- 239000000706 filtrate Substances 0.000 claims description 46
- BFNBIHQBYMNNAN-UHFFFAOYSA-N ammonium sulfate Chemical class N.N.OS(O)(=O)=O BFNBIHQBYMNNAN-UHFFFAOYSA-N 0.000 abstract description 37
- 229910052921 ammonium sulfate Inorganic materials 0.000 abstract description 30
- 235000011130 ammonium sulphate Nutrition 0.000 abstract description 30
- 238000006477 desulfuration reaction Methods 0.000 abstract description 12
- 230000023556 desulfurization Effects 0.000 abstract description 12
- 239000007789 gas Substances 0.000 abstract description 10
- 239000002245 particle Substances 0.000 abstract description 6
- 239000006227 byproduct Substances 0.000 abstract description 3
- 239000000243 solution Substances 0.000 description 20
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 17
- 239000000428 dust Substances 0.000 description 17
- 238000000034 method Methods 0.000 description 11
- PQUCIEFHOVEZAU-UHFFFAOYSA-N Diammonium sulfite Chemical compound [NH4+].[NH4+].[O-]S([O-])=O PQUCIEFHOVEZAU-UHFFFAOYSA-N 0.000 description 10
- AOSFMYBATFLTAQ-UHFFFAOYSA-N 1-amino-3-(benzimidazol-1-yl)propan-2-ol Chemical compound C1=CC=C2N(CC(O)CN)C=NC2=C1 AOSFMYBATFLTAQ-UHFFFAOYSA-N 0.000 description 9
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 9
- 238000005507 spraying Methods 0.000 description 8
- 229910021529 ammonia Inorganic materials 0.000 description 7
- 239000013078 crystal Substances 0.000 description 7
- 230000018044 dehydration Effects 0.000 description 5
- 238000006297 dehydration reaction Methods 0.000 description 5
- 239000000047 product Substances 0.000 description 5
- 239000007787 solid Substances 0.000 description 5
- BIGPRXCJEDHCLP-UHFFFAOYSA-N ammonium bisulfate Chemical compound [NH4+].OS([O-])(=O)=O BIGPRXCJEDHCLP-UHFFFAOYSA-N 0.000 description 4
- 229920006395 saturated elastomer Polymers 0.000 description 4
- 238000000926 separation method Methods 0.000 description 4
- 239000003337 fertilizer Substances 0.000 description 3
- 239000000945 filler Substances 0.000 description 3
- 238000005245 sintering Methods 0.000 description 3
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 description 2
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 2
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 description 2
- 239000002250 absorbent Substances 0.000 description 2
- 230000002745 absorbent Effects 0.000 description 2
- 239000012141 concentrate Substances 0.000 description 2
- 238000001035 drying Methods 0.000 description 2
- 238000005265 energy consumption Methods 0.000 description 2
- 239000003344 environmental pollutant Substances 0.000 description 2
- 238000001914 filtration Methods 0.000 description 2
- 230000005484 gravity Effects 0.000 description 2
- 229910000041 hydrogen chloride Inorganic materials 0.000 description 2
- IXCSERBJSXMMFS-UHFFFAOYSA-N hydrogen chloride Substances Cl.Cl IXCSERBJSXMMFS-UHFFFAOYSA-N 0.000 description 2
- 239000003595 mist Substances 0.000 description 2
- 231100000719 pollutant Toxicity 0.000 description 2
- AKEJUJNQAAGONA-UHFFFAOYSA-N sulfur trioxide Chemical compound O=S(=O)=O AKEJUJNQAAGONA-UHFFFAOYSA-N 0.000 description 2
- KRHYYFGTRYWZRS-UHFFFAOYSA-N Fluorane Chemical compound F KRHYYFGTRYWZRS-UHFFFAOYSA-N 0.000 description 1
- 229910000831 Steel Inorganic materials 0.000 description 1
- 239000003905 agrochemical Substances 0.000 description 1
- 238000005119 centrifugation Methods 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 239000012043 crude product Substances 0.000 description 1
- 238000002425 crystallisation Methods 0.000 description 1
- 230000008025 crystallization Effects 0.000 description 1
- 230000007423 decrease Effects 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- MHEMRIIGLWLYQA-UHFFFAOYSA-N diazanium sulfurous acid sulfate Chemical compound [NH4+].[NH4+].OS(O)=O.[O-]S([O-])(=O)=O MHEMRIIGLWLYQA-UHFFFAOYSA-N 0.000 description 1
- 229910000040 hydrogen fluoride Inorganic materials 0.000 description 1
- 229910052742 iron Inorganic materials 0.000 description 1
- 238000012423 maintenance Methods 0.000 description 1
- 230000000630 rising effect Effects 0.000 description 1
- 239000012047 saturated solution Substances 0.000 description 1
- 239000010959 steel Substances 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 238000006276 transfer reaction Methods 0.000 description 1
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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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Abstract
本实用新型涉及利用氨水脱除烟气中二氧化硫的装置，包括吸收塔由下至上为塔底浆池、喷淋层、填料层、除雾器，吸收塔中部位于喷淋层的下方、塔底浆池的上方设置有烟气入口，吸收塔顶部设置有烟气出口；所述吸收塔的塔底浆池内设置有曝气管；吸收塔外设置有循环泵，且循环泵的数量与喷淋层的层数一致，每台循环泵的出口分别与一层喷淋层中的喷淋器相连，除雾器安装在吸收塔上部，每台循环泵的进口分别与吸收塔的塔底浆池相连；并在塔外设置在线过滤器，过滤后的不饱和硫酸铵溶液作为填料层的吸收液，彻底解除填料结垢堵塞的可能。利用本实用新型脱硫具有脱硫效率高、液气比低、不容易产生结垢堵塞、出口烟气中夹带的硫酸铵颗粒和液滴含量低、副产品质量好等优点。
The utility model relates to a device for removing sulfur dioxide in flue gas by using ammonia water, which comprises an absorption tower from bottom to top consisting of a slurry pool at the bottom of the tower, a spray layer, a packing layer, and a demister. There is a flue gas inlet above the slurry tank, and a flue gas outlet is set on the top of the absorption tower; an aeration pipe is arranged in the pulp tank at the bottom of the absorption tower; a circulation pump is provided outside the absorption tower, and the number of circulation pumps is in line with the spray The number of layers is the same, the outlet of each circulating pump is connected to the sprayer in the first spray layer, the demister is installed on the upper part of the absorption tower, and the inlet of each circulating pump is respectively connected to the bottom slurry of the absorption tower. The pools are connected; and an online filter is installed outside the tower, and the filtered unsaturated ammonium sulfate solution is used as the absorption liquid of the packing layer, completely eliminating the possibility of packing fouling and clogging. The desulfurization of the utility model has the advantages of high desulfurization efficiency, low liquid-gas ratio, no fouling and blockage, low content of ammonium sulfate particles and liquid droplets entrained in the outlet flue gas, and good quality of by-products.
Description
技术领域technical field
本实用新型属于锅炉尾气、烧结机烟气处理技术领域，特别涉及一种新的利用氨水脱除烟气中二氧化硫的装置。The utility model belongs to the technical field of boiler tail gas and sintering machine flue gas treatment, in particular to a new device for removing sulfur dioxide in flue gas by using ammonia water.
背景技术Background technique
目前，氨法脱除烟气中二氧化硫主要采用喷淋吸收的方式，吸收塔主要有两种形式：一种是空塔喷淋，空塔型喷淋塔结构简单，不易产生结垢堵塞。但是该装置的不足是吸收效率较低，如果要保证脱硫系统的脱硫率，必须增加吸收液的喷淋量，即采用较大的液气比，这样势必会导致整个装置能耗增加。另外，采用空塔型喷淋塔，吸收过程中形成的微细硫酸铵颗粒以及细小液滴容易被烟气夹带，对周围环境造成二次污染。At present, the method of ammonia removal of sulfur dioxide in flue gas mainly adopts the method of spray absorption. There are two main types of absorption towers: one is empty tower spraying. The empty tower type spray tower has a simple structure and is not easy to cause scaling and blockage. However, the disadvantage of this device is that the absorption efficiency is low. If the desulfurization rate of the desulfurization system is to be guaranteed, the spraying amount of the absorption liquid must be increased, that is, a larger liquid-gas ratio is adopted, which will inevitably lead to an increase in energy consumption of the entire device. In addition, the empty tower type spray tower is adopted, and the fine ammonium sulfate particles and small droplets formed during the absorption process are easily entrained by the flue gas, causing secondary pollution to the surrounding environment.
另一种是采用填料塔，采用填料塔可以显著增加气液接触面积，提高吸收效率，减少吸收液喷淋量，使得吸收操作液气比降低，可以降低装置能耗。但是由于烟气中通常会带有大量的灰尘，加上吸收过程中形成的饱和溶液极易在填料表面形成结晶，这样就会在填料中产生结垢堵塞。实际使用的填料吸收塔，每年都必须对填料进行清理更换，检修工作量极大，严重的因为填料堵塞导致烟气流速急剧增大，将填料吹翻坍塌。The other is to use a packed tower, which can significantly increase the gas-liquid contact area, improve the absorption efficiency, reduce the spraying amount of the absorption liquid, reduce the liquid-gas ratio in the absorption operation, and reduce the energy consumption of the device. However, because the flue gas usually contains a large amount of dust, and the saturated solution formed during the absorption process is very easy to form crystals on the surface of the packing, this will cause scaling and blockage in the packing. In the actual use of the packing absorption tower, the packing must be cleaned and replaced every year, and the maintenance workload is huge. In serious cases, the flue gas flow rate increases sharply due to the blockage of the packing, and the packing is blown over and collapsed.
发明内容Contents of the invention
本实用新型的目的为了克服上述现有技术存在的不足，提供一种新的利用氨水脱除烟气中二氧化硫的装置。本实用新型提供新的利用氨水脱除烟气中二氧化硫的装置包括一种新型吸收塔，这种新型吸收塔采用空塔喷淋和填料进行合理组合，并在塔外设置在线过滤器，过滤后的不饱和硫酸铵溶液为填料层的吸收液，彻底解除填料结垢堵塞的可能。利用本装置来脱硫其脱硫效率高、液气比低、不容易产生结垢堵塞、出口烟气中夹带的硫酸铵颗粒和液滴含量低、副产品质量好等优点。The purpose of this utility model is to provide a new device for removing sulfur dioxide in flue gas by using ammonia water in order to overcome the above-mentioned deficiencies in the prior art. The utility model provides a new device for removing sulfur dioxide in flue gas by using ammonia water, which includes a new type of absorption tower. The unsaturated ammonium sulfate solution is the absorption solution of the packing layer, which completely removes the possibility of packing scaling and clogging. Using this device for desulfurization has the advantages of high desulfurization efficiency, low liquid-gas ratio, no fouling and blockage, low content of ammonium sulfate particles and droplets entrained in the outlet flue gas, and good quality of by-products.
本实用新型采取的技术方案为：The technical scheme that the utility model takes is:
利用氨水脱除烟气中二氧化硫的装置，包括吸收塔和循环泵，其特征在于：所述的吸收塔由下至上包括吸收塔的塔底浆池、喷淋层、填料层、除雾器，吸收塔中部位于喷淋层的下方、塔底浆池的上方设置有烟气入口，吸收塔顶部设置有烟气出口；所述吸收塔的塔底浆池内设置有曝气管；吸收塔外设置有循环泵，且循环泵的数量与喷淋层的层数一致，每台循环泵的出口分别与一层喷淋层中的喷淋器相连，除雾器安装在吸收塔上部，每台循环泵的进口分别与吸收塔的塔底浆池相连。The device for removing sulfur dioxide in the flue gas by using ammonia water includes an absorption tower and a circulating pump, and is characterized in that: the absorption tower includes a slurry tank at the bottom of the absorption tower, a spray layer, a packing layer, and a demister from bottom to top, The middle part of the absorption tower is located below the spray layer, a flue gas inlet is set above the slurry pool at the bottom of the tower, and a flue gas outlet is set at the top of the absorption tower; an aeration tube is installed in the slurry pool at the bottom of the absorption tower; There are circulation pumps, and the number of circulation pumps is consistent with the number of spray layers. The outlet of each circulation pump is connected to the sprayer in the spray layer of one layer. The demister is installed on the upper part of the absorption tower. The inlets of the circulating pumps are respectively connected with the slurry tanks at the bottom of the absorption tower.
本实用新型的装置还包括排出泵、旋流器、离心机、干燥器、滤液箱、过滤液泵、在线过滤器、清液泵，在吸收塔的塔底浆池的底部与排出泵进口相连，排出泵的出口与旋流器的进口相连；所述旋流器的底流管与离心机进口相连；所述旋流器的溢流管与所述离心机的滤液管相连并汇合后与滤液箱的顶部相连；所述离心机的出料管与干燥器进口相连；所述滤液箱通过滤液泵与在线过滤器相连，其中滤液泵的进口与滤液箱的底部相连，滤液泵的出口与在线过滤器的进口相连；所述在线过滤器的出口设置有清液泵，其中清液泵的进口与在线过滤器的出口相连，清液泵的出口与吸收塔的填料层相连。The device of the present invention also includes a discharge pump, a cyclone, a centrifuge, a drier, a filtrate tank, a filtrate pump, an online filter, and a clear liquid pump, which are connected to the inlet of the discharge pump at the bottom of the slurry tank at the bottom of the absorption tower , the outlet of the discharge pump is connected with the inlet of the cyclone; the underflow pipe of the cyclone is connected with the inlet of the centrifuge; the overflow pipe of the cyclone is connected with the filtrate pipe of the centrifuge and merged with the filtrate The top of the tank is connected; the discharge pipe of the centrifuge is connected with the inlet of the dryer; the filtrate tank is connected with the online filter through the filtrate pump, wherein the inlet of the filtrate pump is connected with the bottom of the filtrate tank, and the outlet of the filtrate pump is connected with the online filter. The inlet of the filter is connected; the outlet of the online filter is provided with a clear liquid pump, wherein the inlet of the clear liquid pump is connected with the outlet of the online filter, and the outlet of the clear liquid pump is connected with the packing layer of the absorption tower.
将本实用新型的装置用来利用氨水脱除烟气中二氧化硫的方法，按以下步骤进行：(1)、将锅炉来的烟气或烧结机来的烟气通过烟道从吸收塔烟气入口进入吸收塔；(2)、在吸收塔内，烟气向上通过喷淋层、填料层进行吸收处理，烟气通过喷淋层，与喷淋的吸收液进行逆流接触，发生传质与吸收反应，以脱除烟气中的SO2、SO3、HCl、HF污染物并且去除灰尘；经喷淋层除尘后的烟气在吸收塔内继续上升，进入填料层，在填料表面与吸收液继续发生传质与吸收，并吸收喷淋层产生的微细硫酸铵颗粒和液滴，最后烟气经塔顶除雾器除雾后从塔顶烟气出口排出；(3)填料层和喷淋层的吸收液向下降落，经高温烟气蒸发掉部分水分，同时使烟气降温，吸收液被蒸发水分后逐步浓缩，并析出硫酸铵、亚硫酸铵晶体；所有吸收液都汇集到吸收塔底部浆池中，在浆池中，通过曝气管通入空气、氨水或气氨，空气的作用是将亚硫酸铵氧化成硫酸铵，氨水或气氨的作用是调节溶液的PH值至5-6，使溶液中的亚硫酸氢铵、硫酸氢铵转化成亚硫酸铵、硫酸铵；(4)塔底浆池的浆液分别通过与塔底相连的循环泵打入喷淋层，循环泵与喷淋器采用单元制，每层喷淋器对应一台循环泵；(5)塔底浆池的浆液悬浮固体含量达到3％-10％时，从塔底通过排出泵打到旋流器再进行经离心机、干燥器进行脱水干燥得硫酸铵化肥成品；(6)旋流器分离出来的溢流液和离心机分离出来的滤液加水将少量的硫酸铵结晶溶解后，变成浓度为30％-40％的硫酸铵溶液，将该溶液通过滤液箱、滤液泵15进入在线过滤器进行精过滤，除去直径大于1μm的灰尘，过滤后的澄清溶液经清液泵打入吸收塔作为填料层的吸收液。The device of the present utility model is used to utilize ammoniacal liquor to remove the method for sulfur dioxide in flue gas, carry out according to the following steps: (1), the flue gas that boiler comes or the flue gas that sintering machine comes is passed flue from absorption tower flue gas entrance Enter the absorption tower; (2) In the absorption tower, the flue gas passes through the spray layer and the packing layer upward for absorption treatment, and the flue gas passes through the spray layer and contacts the sprayed absorption liquid in countercurrent, and mass transfer and absorption reactions occur , to remove SO 2 , SO 3 , HCl, and HF pollutants in the flue gas and remove dust; the flue gas after dust removal by the spray layer continues to rise in the absorption tower, enters the packing layer, and continues to mix with the absorption liquid on the packing surface. Mass transfer and absorption occur, and absorb the fine ammonium sulfate particles and droplets produced by the spray layer, and finally the flue gas is demistered by the tower top demister and then discharged from the flue gas outlet at the top of the tower; (3) packing layer and spray layer The absorption liquid falls downwards, part of the water is evaporated by the high-temperature flue gas, and the temperature of the flue gas is cooled at the same time. The absorption liquid is gradually concentrated after the water is evaporated, and ammonium sulfate and ammonium sulfite crystals are precipitated; all the absorption liquids are collected at the bottom of the absorption tower In the slurry tank, air, ammonia water or gas ammonia is introduced through the aeration pipe. The function of the air is to oxidize ammonium sulfite into ammonium sulfate. The function of ammonia water or gas ammonia is to adjust the pH value of the solution to 5- 6, the ammonium bisulfite and ammonium bisulfate in the solution are converted into ammonium sulfite and ammonium sulfate; (4) the slurry in the slurry pool at the bottom of the tower is injected into the spray layer through the circulation pump connected to the bottom of the tower respectively, and the circulation pump and the The sprayer adopts a unit system, and each layer of sprayer corresponds to a circulation pump; (5) When the suspended solid content of the slurry tank at the bottom of the tower reaches 3%-10%, it is pumped from the bottom of the tower to the cyclone through the discharge pump and then Carry out dehydration and drying through the centrifuge and drier to obtain the finished product of ammonium sulfate fertilizer; (6) add water to the overflow liquid separated by the cyclone and the filtrate separated by the centrifuge to dissolve a small amount of ammonium sulfate crystals, and become a concentration of 30 %-40% ammonium sulfate solution, the solution enters the online filter through the filtrate tank and filtrate pump 15 for fine filtration to remove dust with a diameter greater than 1 μm, and the filtered clear solution is pumped into the absorption tower through the clear liquid pump as a packing layer of the absorbent.
所述的喷淋层由喷淋器将循环的吸收液喷洒成细小的液滴，与上升的烟气逆流接触，以达到传质、吸收的目的；所述的喷淋层为1-3层，每一层的喷淋器都由联管和喷头连接而成。In the spray layer, the circulating absorbing liquid is sprayed into fine droplets by the sprinkler, and they are in countercurrent contact with the rising flue gas, so as to achieve the purpose of mass transfer and absorption; the spray layer is 1-3 layers , the showers of each layer are connected by connecting pipes and nozzles.
所述的喷淋层的吸收液由塔底浆液池中浆液通过循环泵打入，喷淋层的吸收液为含悬浮固体且质量浓度3％-10％的硫酸铵-亚硫酸铵混合浆液。The absorption liquid of the spray layer is pumped in from the slurry tank at the bottom of the tower through a circulation pump, and the absorption liquid of the spray layer is a mixed ammonium sulfate-ammonium sulfite slurry containing suspended solids and having a mass concentration of 3%-10%.
所述填料层的吸收液由塔外在线过滤器滤液打入，吸收液为质量浓度30％-40％的硫酸溶液。The absorption liquid of the packing layer is poured in by the filtrate of the online filter outside the tower, and the absorption liquid is a sulfuric acid solution with a mass concentration of 30%-40%.
所述的填料层，为一层填料。The filler layer is a layer of filler.
本实用新型中所述的喷淋器、填料层、除雾器、曝气装置、循环泵、旋流器、离心机、干燥器都选用成熟产品进行组装。The sprayer, packing layer, demister, aeration device, circulation pump, cyclone, centrifuge and dryer described in the utility model are all selected from mature products for assembly.
利用本实用新型提供的装置来脱硫具有脱硫效率高、液气比低、不容易产生结垢堵塞、出口烟气中夹带的硫酸铵颗粒和液滴含量低、副产品质量好等优点。Utilizing the device provided by the utility model for desulfurization has the advantages of high desulfurization efficiency, low liquid-gas ratio, no scaling and blockage, low content of ammonium sulfate particles and droplets entrained in the outlet flue gas, and good quality of by-products.
本实用新型提供新的利用氨水脱除烟气中二氧化硫的装置包括一种新型吸收塔，这种新型吸收塔采用空塔喷淋和填料进行合理组合，并在塔外设置在线过滤器，过滤后的不饱和硫酸铵溶液为填料层的吸收液，彻底解除填料结垢堵塞的可能。The utility model provides a new device for removing sulfur dioxide in flue gas by using ammonia water, which includes a new type of absorption tower. The unsaturated ammonium sulfate solution is the absorption solution of the packing layer, which completely removes the possibility of packing scaling and clogging.
附图说明Description of drawings
图1为本实用新型装置及工艺流程示意图。Fig. 1 is the utility model device and technological process schematic diagram.
具体实施方式Detailed ways
本实用新型是一种采用空塔喷淋和填料吸收相结合，并使用在线过滤器除灰的氨法脱硫的装置和方法，如图1所示，烟气通过吸收塔烟气入口1进入吸收塔6，烟气在吸收塔6中上升，与喷淋层2喷淋的浆液逆流接触，发生传质吸收，烟气中二氧化硫、三氧化硫、氯化氢、氟化氢等污染物大部分被吸收，烟气中的灰尘大部分被洗下来，同时高温烟气也被饱和降温，经过喷淋层2洗涤去灰尘，并饱和降温后的烟气穿过喷淋层2进入填料层3，烟气在填料层3中与填料表面吸收液发生传质吸收，达到要求的脱硫效率后继续向上通过除雾器4，除去夹带的雾滴，通过塔顶烟气出口5排出。The utility model is an ammonia desulfurization device and method which adopts the combination of empty tower spraying and packing absorption, and uses an online filter to remove ash. As shown in Figure 1, the flue gas enters the absorption tower through the flue gas inlet 1. Tower 6, the flue gas rises in the absorption tower 6 and contacts with the slurry sprayed in the spray layer 2 countercurrently, mass transfer and absorption occur, and most of the pollutants such as sulfur dioxide, sulfur trioxide, hydrogen chloride, and hydrogen fluoride in the flue gas are absorbed, and the flue gas Most of the dust in the air is washed down, and at the same time, the high-temperature flue gas is also saturated and cooled, and the dust is washed away by the spray layer 2, and the saturated and cooled flue gas passes through the spray layer 2 and enters the packing layer 3. Layer 3 undergoes mass transfer and absorption with the absorbent on the surface of the filler. After reaching the required desulfurization efficiency, it continues to pass through the demister 4 to remove entrained mist droplets, and is discharged through the flue gas outlet 5 at the top of the tower.
喷淋层和填料层的吸收液在重力作用下在塔内下降最终都汇集吸收塔塔底浆池7，吸收塔塔底浆池7内的浆液通过循环泵9打到喷淋层2循环喷淋，浆液在循环喷淋吸收的过程中，浓度不断上升，加上高温烟气不断蒸发喷淋浆液中的水分，使得吸收塔塔底浆池7内的浆液浓缩结晶，析出硫酸铵晶体。The absorption liquid in the spray layer and the packing layer descends in the tower under the action of gravity and finally gathers in the bottom slurry pool 7 of the absorption tower, and the slurry in the bottom slurry pool 7 of the absorption tower is pumped to the spray layer 2 by the circulation pump 9 and circulated for spraying. During the process of circulating spraying and absorbing, the concentration of the slurry increases continuously, and the high-temperature flue gas continuously evaporates the water in the spraying slurry, so that the slurry in the slurry tank 7 at the bottom of the absorption tower concentrates and crystallizes, and ammonium sulfate crystals are precipitated.
吸收塔塔底浆池7内的浆液中，存在硫酸铵、亚硫酸铵、硫酸氢铵、亚硫酸氢铵等多种物质，为了得到高纯度的硫酸铵化肥产品，通过吸收塔塔底浆池7内设置的曝气管8鼓入空气，使亚硫酸铵、亚硫酸氢铵氧化为硫酸铵、硫酸氢铵；同时通过该曝气管8通入氨水或气氨，调节浆液的PH值为5-6，使得硫酸氢铵、亚硫酸氢铵转化为硫酸铵、亚硫酸铵。Ammonium sulfate, ammonium sulfite, ammonium bisulfite, ammonium bisulfite and other substances exist in the slurry in the bottom slurry tank 7 of the absorption tower. The aeration pipe 8 provided in the 7 is blown into air to oxidize ammonium sulfite and ammonium bisulfite into ammonium sulfate and ammonium bisulfite; at the same time, ammonia water or gas ammonia is passed through the aeration pipe 8 to adjust the pH value of the slurry 5-6, making ammonium bisulfate and ammonium bisulfite converted into ammonium sulfate and ammonium sulfite.
吸收塔塔底浆池7内的浆液悬浮固体含量达到5％时，用排出泵10将浆液打到旋流器11进行固液分离，固液分离后的溢流进入滤液箱14收集，提浓后的底流进入离心机12进一步离心脱水，经离心机脱水后的硫酸铵含水率小于5％，然后进入干燥器13进行干燥，最终生产出满足要求的硫酸铵化肥产品。When the suspended solids content of the slurry in the slurry tank 7 at the bottom of the absorption tower reaches 5%, use the discharge pump 10 to pump the slurry to the cyclone 11 for solid-liquid separation, and the overflow after solid-liquid separation enters the filtrate tank 14 to collect and concentrate After the underflow enters the centrifuge 12 for further centrifugation and dehydration, the moisture content of ammonium sulfate after dehydration by the centrifuge is less than 5%, and then enters the drier 13 for drying, finally producing ammonium sulfate fertilizer products that meet the requirements.
旋流器11的溢流和离心机12的滤液中含有大量的灰尘和少量的硫酸铵结晶，因此，通过往滤液箱中加少量水溶解掉硫酸铵晶体，使得滤液箱中的滤液变成浓度为30％-40％的不饱和硫酸铵溶液。用滤液泵15将该含有灰尘的不饱和溶液打入在线过滤器，将溶液中悬浮的直径大于1μm的灰尘全部过滤掉，过滤后的清夜通过清液泵17打到吸收塔填料层3作为吸收液，由于吸收液为不含灰尘的不饱和硫酸铵溶液，有效地解决了填料层结垢堵塞的问题。The overflow of the cyclone 11 and the filtrate of the centrifuge 12 contain a large amount of dust and a small amount of ammonium sulfate crystals. Therefore, adding a small amount of water to the filtrate tank dissolves the ammonium sulfate crystals, so that the filtrate in the filtrate tank becomes concentrated. It is 30%-40% unsaturated ammonium sulfate solution. Use the filtrate pump 15 to pump the unsaturated solution containing dust into the online filter, filter out all the dust suspended in the solution with a diameter greater than 1 μm, and the filtered clear water is sent to the packing layer 3 of the absorption tower through the clear liquid pump 17 for absorption Since the absorption liquid is an unsaturated ammonium sulfate solution without dust, it effectively solves the problem of fouling and blockage of the packing layer.
实施例1Example 1
如图1所示，一种氨法脱硫吸收塔6、循环泵9、排出泵10、旋流器11、离心机12、干燥器13、滤液箱14、过滤液泵15、在线过滤器16、清液泵17，由下至上包括吸收塔的塔底浆池7、喷淋层2、填料层3、除雾器4，其中喷淋层2包括2层喷淋器，填料层3为一层填料；吸收塔中部位于喷淋层2的下方、塔底浆池7的上方设置有烟气入口1，吸收塔顶部设置有烟气出口5；所述吸收塔的塔底浆池7设置有曝气管8；吸收塔6外设置有2台循环泵9，每台循环泵9的出口分别与一层喷淋层2中的喷淋器相连，除雾器4安装在吸收塔上部，每台循环泵9的进口分别与吸收塔的塔底浆池7相连；，在吸收塔6的塔底浆池7的底部与排出泵10进口相连，排出泵10的出口与旋流器11的进口相连；所述旋流器11的底流管19与离心机12进口相连；所述旋流器11的溢流管18与所述离心机12的滤液管20相连并汇合后与滤液箱14的顶部相连；所述离心机12的出料管21与干燥器13进口相连；所述滤液箱14通过滤液泵15与在线过滤器16相连，其中滤液泵15的进口与滤液箱14的底部相连，滤液泵15的出口与在线过滤器16的进口相连；所述在线过滤器16的出口设置有清液泵17，其中清液泵17的进口与在线过滤器16的出口相连，清液泵17的出口与吸收塔6的填料层3相连。As shown in Figure 1, a kind of ammonia desulfurization absorption tower 6, circulation pump 9, discharge pump 10, cyclone 11, centrifuge 12, drier 13, filtrate tank 14, filtrate pump 15, in-
实施例2Example 2
其余部分与实施例1相同，不同之处在于吸收塔喷淋层2包括有3层喷淋器，与之对应的是，塔外相应设置有3台循环泵9，每台循环泵9的出口分别与喷淋层2中每层喷淋器相连，每台循环泵9的进口分别与吸收塔的塔底浆池7相连。The rest are the same as in Example 1, except that the absorption tower spray layer 2 includes 3 layers of sprayers, and correspondingly, 3 circulating pumps 9 are correspondingly arranged outside the tower, and the outlet of each circulating pump 9 They are respectively connected to each sprayer in the spraying layer 2, and the inlet of each circulation pump 9 is connected to the slurry tank 7 at the bottom of the absorption tower respectively.
实施例3Example 3
来自锅炉的温度为130℃的烟气，流量为8.0×105标准立方米/小时，烟气中二氧化硫浓度为2800mg/Nm3，灰尘含量为100mg/Nm3。该烟气从吸收塔烟气入口1进入吸收塔6，烟气在吸收塔6内上升，与喷淋层2喷淋的浆液逆流接触，发生传质吸收以及热量传递，高温烟气蒸发浆液中的水分，同时烟气迅速饱和降温至50-55℃，烟气中二氧化硫60％-70％被吸收，灰尘75％-80％被喷淋的浆液洗涤下来。降温除尘后的烟气通过喷淋层继续上升，进入填料层3，烟气与填料表面的吸收液充分接触，填料层3表面的吸收液是来自在线过滤器16过滤后的清液，是一种浓度为30％-40％，不含灰尘的不饱和硫酸铵溶液，通过清液泵17打到填料层，烟气通过填料层3后，烟气中绝大部分二氧化硫被吸收脱除，同时烟气从喷淋层夹带的微细液滴以及产生的维细硫酸铵颗粒也在填料层中被吸收洗涤一部分；烟气通过填料层后，进入吸收塔6上部的除雾器4，烟气中夹带的绝大部分液滴被除雾器拦截下来，最后洁净的烟气从吸收塔6顶部的烟气出口5排出，排出的洁净烟气中的二氧化硫浓度为110mg/Nm3，灰尘含量为20mg/Nm3。The temperature of the flue gas from the boiler is 130°C, the flow rate is 8.0×10 5 standard cubic meters per hour, the concentration of sulfur dioxide in the flue gas is 2800 mg/Nm 3 , and the dust content is 100 mg/Nm 3 . The flue gas enters the absorption tower 6 from the flue gas inlet 1 of the absorption tower, and the flue gas rises in the absorption tower 6 and contacts the slurry sprayed by the spray layer 2 in countercurrent, mass transfer absorption and heat transfer occur, and the high-temperature flue gas evaporates into the slurry At the same time, the flue gas is rapidly saturated and cooled to 50-55°C, 60%-70% of the sulfur dioxide in the flue gas is absorbed, and 75%-80% of the dust is washed down by the sprayed slurry. The flue gas after cooling and dust removal continues to rise through the spray layer and enters the packing layer 3. The flue gas fully contacts with the absorbing liquid on the packing surface. The concentration is 30%-40%, the dust-free unsaturated ammonium sulfate solution is pumped to the packing layer by the clear liquid pump 17, and after the flue gas passes through the packing layer 3, most of the sulfur dioxide in the flue gas is absorbed and removed, and at the same time The fine liquid droplets entrained by the flue gas from the spray layer and the fine ammonium sulfate particles produced are also absorbed and washed in the packing layer; after the flue gas passes through the packing layer, it enters the demister 4 on the upper part of the absorption tower 6, and the flue gas Most of the entrained liquid droplets are intercepted by the demister, and finally the clean flue gas is discharged from the flue gas outlet 5 at the top of the absorption tower 6. The sulfur dioxide concentration in the discharged clean flue gas is 110mg/Nm 3 , and the dust content is 20mg /Nm 3 .
吸收塔6内的吸收液由于重力作用最后都落入塔底浆池7，由于浆液中的水分不断被高温烟气蒸发，浆液利用烟气的热量浓缩，塔底浆池7中浆液浓度不断增加。浆液吸收二氧化硫后，浆液中的亚硫酸铵变成亚硫酸氢铵，PH降低，吸收能力减弱，再通过塔底浆池7中的曝气管8注入为质量浓度20％的浓氨水6.3m3/h，调节浆液的PH值为5-6，使浆液中亚硫酸氢铵、硫酸氢铵转化为亚硫酸铵、硫酸铵。同时从曝气管8鼓入空气，将亚硫酸铵氧化为硫酸铵；随着浆液中硫酸铵浓度不断增加，最终饱和结晶，析出硫酸铵晶体。The absorption liquid in the absorption tower 6 finally falls into the slurry tank 7 at the bottom of the tower due to gravity. Since the water in the slurry is continuously evaporated by the high-temperature flue gas, the slurry is concentrated by the heat of the flue gas, and the concentration of the slurry in the slurry tank 7 at the bottom of the tower continues to increase. . After the slurry absorbs sulfur dioxide, the ammonium sulfite in the slurry becomes ammonium bisulfite, the pH decreases, and the absorption capacity weakens, and then 6.3 m of concentrated ammonia water with a mass concentration of 20% is injected through the aeration pipe 8 in the slurry tank 7 at the bottom of the tower /h, adjust the pH value of the slurry to 5-6, so that the ammonium bisulfite and ammonium bisulfate in the slurry are converted into ammonium sulfite and ammonium sulfate. At the same time, air is blown in from the aeration pipe 8 to oxidize ammonium sulfite to ammonium sulfate; as the concentration of ammonium sulfate in the slurry increases continuously, it will eventually be saturated and crystallized, and ammonium sulfate crystals will be precipitated.
当塔底浆池7中的浆液悬浮固体浓度达到10％左右时，由排出泵10打到旋流器11进行固液分离，分离后的溢流液从旋流器11溢流管18流入滤液箱14；旋流器底流悬浮固体浓度为40％左右，底流通过底流管19流入离心机12进一步脱水。When the concentration of suspended solids in the slurry tank 7 at the bottom of the tower reaches about 10%, the discharge pump 10 is pumped into the cyclone 11 for solid-liquid separation, and the overflow liquid after separation flows into the filtrate from the overflow pipe 18 of the cyclone 11 Box 14; the concentration of suspended solids in the underflow of the cyclone is about 40%, and the underflow flows into the centrifuge 12 through the underflow pipe 19 for further dehydration.
离心机12脱水后的滤液也通过滤液管流入滤液箱14，离心过滤后的硫酸铵粗产品含水率为5％以下，通过离心机12的出料管21进入干燥器13。硫酸铵粗产品在干燥器内干燥至含水率低于1％，达到国家标准合格品的标准，作为农用化肥出售。The filtrate after the centrifuge 12 dehydration also flows into the filtrate box 14 by the filtrate pipe, and the ammonium sulfate thick product moisture content after centrifugal filtration is below 5%, enters the drier 13 by the outlet pipe 21 of the centrifuge 12. The crude product of ammonium sulfate is dried in a drier until the water content is lower than 1%, which meets the national standard qualified product, and is sold as agricultural chemical fertilizer.
旋流器11的溢流液和离心机12的滤液汇集到滤液箱14，通过向滤液箱14内加入适量的水，溶解少量的硫酸铵结晶，使滤液成为浓度为40％的硫酸铵溶液。该硫酸铵溶液通过滤液泵15，打入在线过滤器16，将溶液中直径大于1μm的灰尘全部过滤掉，过滤后的清夜通过清液泵17打到吸收塔填料层3作为吸收液，由于吸收液为不含灰尘的不饱和溶液，有效地解决了填料层结垢堵塞的问题。The overflow liquid of cyclone 11 and the filtrate of centrifuge 12 are brought together in filtrate box 14, by adding appropriate amount of water in filtrate box 14, dissolve a small amount of ammonium sulfate crystallization, make filtrate become the ammonium sulfate solution that concentration is 40%. This ammonium sulfate solution is pumped into the
实施例4Example 4
实施例4的流程与实施例3完全相同，所不同的是烟气是来自钢铁厂烧结机，温度为120℃，烟气流量为1.6×106标准立方米/小时，烟气中二氧化硫浓度为1300mg/Nm3，灰尘含量为100mg/Nm3。The flow process of embodiment 4 is exactly the same as that of embodiment 3, the difference is that the flue gas is from the sintering machine of the iron and steel plant, the temperature is 120 ℃, the flue gas flow rate is 1.6 × 10 6 standard cubic meters per hour, and the sulfur dioxide concentration in the flue gas is 1300mg/Nm 3 , the dust content is 100mg/Nm 3 .
通过吸收塔6脱硫后排出的洁净烟气中的二氧化硫浓度为65mg/Nm3，灰尘含量为20mg/Nm3。The sulfur dioxide concentration in the clean flue gas discharged after desulfurization by the absorption tower 6 is 65 mg/Nm 3 , and the dust content is 20 mg/Nm 3 .
实施例5Example 5
实施例5的流程与实施例3完全相同，所不同的是调节塔底浆池7中浆液PH，通过曝气管8注入的是纯的气氨，流量为1200kg/h，调节浆液的PH值为5-6，使浆液中亚硫酸氢铵、硫酸氢铵转化为亚硫酸铵、硫酸铵。The flow process of embodiment 5 is exactly the same as embodiment 3, and the difference is to adjust the slurry pH in the slurry tank 7 at the bottom of the tower, and what injects through the aeration pipe 8 is pure gas ammonia, and the flow rate is 1200kg/h to adjust the pH value of the slurry For 5-6, ammonium bisulfite and ammonium bisulfate in the slurry are converted into ammonium sulfite and ammonium sulfate.
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Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN101898082A (en) * | 2010-08-16 | 2010-12-01 | 殷茵 | Device and method for depriving sulfur dioxide in flue gas by using ammonia water |
| CN103115426A (en) * | 2013-02-27 | 2013-05-22 | 苏州大学 | Coal-fired equipment waste heat utilization and dust removal device |
| CN104548918A (en) * | 2015-01-14 | 2015-04-29 | 江苏揽山环境科技有限公司 | Process and system for reducing particle content after flue gas desulfurization |
| CN105056679A (en) * | 2015-08-11 | 2015-11-18 | 中国五环工程有限公司 | Method and device for removing PM2.5 (particulate matter) in WFGD (wet flue gas desulfurization) process |
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| CN101898082A (en) * | 2010-08-16 | 2010-12-01 | 殷茵 | Device and method for depriving sulfur dioxide in flue gas by using ammonia water |
| CN101898082B (en) * | 2010-08-16 | 2012-02-22 | 武汉兴能环保技术有限公司 | Device and method for depriving sulfur dioxide in flue gas by using ammonia water |
| CN103115426A (en) * | 2013-02-27 | 2013-05-22 | 苏州大学 | Coal-fired equipment waste heat utilization and dust removal device |
| CN103115426B (en) * | 2013-02-27 | 2015-06-17 | 苏州大学 | Coal-fired equipment waste heat utilization and dust collector |
| CN104548918A (en) * | 2015-01-14 | 2015-04-29 | 江苏揽山环境科技有限公司 | Process and system for reducing particle content after flue gas desulfurization |
| CN105056679A (en) * | 2015-08-11 | 2015-11-18 | 中国五环工程有限公司 | Method and device for removing PM2.5 (particulate matter) in WFGD (wet flue gas desulfurization) process |
| CN105056679B (en) * | 2015-08-11 | 2017-03-01 | 中国五环工程有限公司 | PM in process of wet desulphurization2.5Removal methods and its device |
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