CN104524935B - Single tower type double-cycle spray composite absorption device and method - Google Patents
Single tower type double-cycle spray composite absorption device and method Download PDFInfo
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- 238000000034 method Methods 0.000 title claims description 62
- 238000006477 desulfuration reaction Methods 0.000 claims abstract description 187
- 230000023556 desulfurization Effects 0.000 claims abstract description 187
- 239000002002 slurry Substances 0.000 claims abstract description 107
- 230000004087 circulation Effects 0.000 claims abstract description 98
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Abstract
Description
技术领域technical field
本发明涉及一种燃煤锅炉的烟气治理反应器，具体地说是一种单塔式双循环喷淋复合吸收装置及工艺系统。The invention relates to a flue gas treatment reactor of a coal-fired boiler, in particular to a single-tower double-circulation spray composite absorption device and a process system.
背景技术Background technique
氮氧化物(NOx)是大气主要污染源之一，也是目前大气污染治理的一大难题。通常所说的氮氧化物(NOx)包括N2O、NO、NO2、N2O3等，其中污染大气的主要是NO和NO2。Nitrogen oxide (NOx) is one of the main sources of air pollution, and it is also a major problem in air pollution control. Nitrogen oxides (NOx) commonly referred to include N 2 O, NO, NO 2 , N 2 O 3 , etc., among which NO and NO 2 are mainly polluting the atmosphere.
人类活动排放的NOx虽然仅是天然形成的NOx的1/10左右，但由于排放浓度高，地点集中，危害很大。NOx的排放给自然环境和人类生产生活带来的危害主要包括：NOx对人体有致毒作用；对植物的损害作用：NOx是形成酸雨、酸雾的主要原因；NOx与碳氢化合物形成化学烟雾，造成二次污染。所以，各国相继制定了含NOx废气排放指标，对NOx的排放量和排放浓度进行了限制。随着人类对环保要求的提高，对NOx的排放要求会越来越严格。自20世纪70年代起，欧、美、日等发达国家相继对燃煤电站锅炉NOx的排放作了限制,，并且随技术与经济的发展，限制日趋严格。我国是以燃煤为主的发展中国家，随着经济的快速发展，燃煤造成的环境污染日趋严重，特别是燃煤烟气中的NOx，对大气的污染已成为一个不容忽视的问题。我国火电厂燃煤锅炉NOx年排放量从2003年的597.3万吨增加到2007年的840万吨，增加了近40.6％。根据美国宇航局资助的CH INA-MAP项目，通过PAINS-ASIA模式检测了中国29个地区的污染物排放情况，结果表明，如果不加以控制，预计到2020年NOx的排放将增加到2660～2970万吨。鉴于此，我国于2011年对燃煤电站锅炉的NOx排放作了进一步的限制。现在，我国《火电厂大气污染物排放标准》对火电厂烟气中的NOx排放质量浓度最高限制为100mg/m3。为此，十二五以来我国对于NOx的控制处于蓬勃发展阶段。Although the NOx emitted by human activities is only about 1/10 of the naturally formed NOx, it is very harmful due to the high emission concentration and concentrated locations. The harms of NOx emissions to the natural environment and human production and life mainly include: NOx is toxic to the human body; damage to plants: NOx is the main cause of acid rain and acid fog; NOx and hydrocarbons form chemical smog, cause secondary pollution. Therefore, various countries have formulated NOx-containing exhaust gas emission indicators one after another, limiting the amount and concentration of NOx emissions. With the improvement of human requirements for environmental protection, the requirements for NOx emissions will become more and more stringent. Since the 1970s, developed countries such as Europe, the United States, and Japan have successively restricted the NOx emissions of coal-fired power plant boilers, and with the development of technology and economy, the restrictions have become increasingly strict. my country is a developing country dominated by coal combustion. With the rapid development of economy, the environmental pollution caused by coal combustion is becoming more and more serious, especially the NOx in coal combustion flue gas, which has become a problem that cannot be ignored. The annual NOx emissions of coal-fired boilers in thermal power plants in my country increased from 5.973 million tons in 2003 to 8.4 million tons in 2007, an increase of nearly 40.6%. According to the CHINA-MAP project funded by NASA, the pollutant emissions of 29 regions in China have been detected through the PAINS-ASIA model. The results show that if no control is carried out, the NOx emissions are expected to increase to 2660-2970 by 2020. tons. In view of this, my country imposed further restrictions on NOx emissions from coal-fired power plant boilers in 2011. Now, China's "Emission Standards for Air Pollutants from Thermal Power Plants" sets a maximum limit of NOx emission mass concentration in the flue gas of thermal power plants to 100mg/m 3 . For this reason, since the 12th Five-Year Plan, my country's control of NOx has been in a stage of vigorous development.
烟气同时脱硫脱硝技术典型的工艺有干法和湿法两类。目前我国通常采用SNCR、SCR脱硝技术，但SCR法以NH3为还原气，存在运输困难、投资及运行费用高、催化剂易失活、排放N2O和NH3等二次污染物、操作温度范围窄、工艺复杂等缺陷；SNCR法存在脱硝效率低，操作温度高，以及氨泄漏等缺点，而且投资运行成本高。因此，出现了新的干法同时脱硫脱硝工艺，包括：活性炭吸收法、高能电子活化氧化法等。The typical processes of flue gas simultaneous desulfurization and denitrification technology include dry method and wet method. At present, SNCR and SCR denitrification technologies are usually used in China, but the SCR method uses NH3 as the reducing gas, which has difficulties in transportation, high investment and operating costs, easy deactivation of catalysts, emission of secondary pollutants such as N2O and NH3 , and operating temperature Narrow range, complex process and other defects; SNCR method has disadvantages such as low denitrification efficiency, high operating temperature, and ammonia leakage, and high investment and operation costs. Therefore, a new dry simultaneous desulfurization and denitrification process has emerged, including: activated carbon absorption method, high-energy electron activation oxidation method, etc.
目前，湿法脱硫装置具有较高的脱硫效率，但是脱硝效率几乎可以忽略。这主要是因为烟气中95％以上为NO，难溶于水，很难被吸收剂所吸收。所以，发展经济可行的烟气脱硝技术势在必行。研发高效经济的脱硫脱硝一体化技术已成为国内外诸多研究机构的关注热点。At present, the wet desulfurization device has a high desulfurization efficiency, but the denitrification efficiency is almost negligible. This is mainly because more than 95% of the flue gas is NO, which is difficult to dissolve in water and is difficult to be absorbed by absorbents. Therefore, it is imperative to develop economically feasible flue gas denitrification technology. The research and development of efficient and economical desulfurization and denitrification integrated technology has become the focus of many research institutions at home and abroad.
但是如果能将NO氧化成NO2等容易被吸收的高价态NOx，那么就有可能实现脱硝，达到工艺设备简单、降低能耗、处理费用低、节省空间等效果。However, if NO can be oxidized into high-valence NOx that is easily absorbed such as NO 2 , then it is possible to achieve denitrification, and achieve the effects of simple process equipment, reduced energy consumption, low processing costs, and space saving.
目前的NO氧化技术主要有臭氧氧化、等离子体氧化、化学添加剂氧化等。The current NO oxidation technologies mainly include ozone oxidation, plasma oxidation, and chemical additive oxidation.
化学添加剂氧化吸收工艺相对更加简单成熟。The oxidation absorption process of chemical additives is relatively simple and mature.
采用钠碱法联合脱硫脱硝可以利用NaOH脱硫后的产物就可以成为脱硝的反应剂，可以原有脱硫装置的基础上实现脱硝，不仅经济可行，而且整体脱硫脱硝的系统大为简化。与其它工艺相比较，简单成熟，能够用于原有湿法脱硫装置的改造。因此对于很多中小型企业来说，无疑是一种理想的脱硝选择。The sodium-alkali method combined with desulfurization and denitrification can use the NaOH desulfurization product to become a denitrification reactant, and can realize denitrification on the basis of the original desulfurization device, which is not only economically feasible, but also greatly simplifies the overall desulfurization and denitrification system. Compared with other processes, it is simple and mature, and can be used in the transformation of the original wet desulfurization device. Therefore, it is undoubtedly an ideal denitration option for many small and medium-sized enterprises.
发明内容Contents of the invention
本发明要解决的技术问题是提供一种单塔式双循环喷淋脱硫脱硝复合吸收装置和工艺系统。The technical problem to be solved by the present invention is to provide a single-tower double-circulation spray desulfurization and denitrification composite absorption device and process system.
本发明给出一种单塔式双循环脱硫脱硝复合吸收装置，包括吸收塔；所述吸收塔内自下而上依次设置为脱硫段、臭氧氧化段和脱硝段；所述脱硫段包括贯穿吸收塔侧壁的烟气进口、设置在吸收塔底部的脱硫浆液循环池、设置在脱硫浆液循环池上方的脱硫喷淋吸收层、将脱硫浆液循环池和脱硫喷淋吸收层相互连接的脱硫浆液循环系统；所述脱硫喷淋吸收层正上方设置臭氧氧化段；所述脱硝段包括吸收塔顶端的烟气出口、设置在臭氧氧化段上方的脱硝浆液循环池、设置在脱硝浆液循环池上方的脱硝喷淋吸收层、设置在脱硝喷淋吸收层和烟气出口之间的除雾装置、将脱硝浆液循环池和脱硝喷淋吸收层相互连接的脱硝浆液循环系统。The present invention provides a single-tower double-cycle desulfurization and denitrification compound absorption device, which includes an absorption tower; the absorption tower is sequentially arranged as a desulfurization section, an ozone oxidation section, and a denitration section from bottom to top; the desulfurization section includes a through absorption The flue gas inlet on the side wall of the tower, the desulfurization slurry circulation pool arranged at the bottom of the absorption tower, the desulfurization spray absorption layer arranged above the desulfurization slurry circulation pool, and the desulfurization slurry circulation connecting the desulfurization slurry circulation pool and the desulfurization spray absorption layer system; an ozone oxidation section is set directly above the desulfurization spray absorption layer; the denitrification section includes a flue gas outlet at the top of the absorption tower, a denitration slurry circulation pool set above the ozone oxidation section, and a denitration slurry circulation pool set above the denitration slurry circulation pool The spray absorption layer, the mist removal device arranged between the denitration spray absorption layer and the flue gas outlet, and the denitrification slurry circulation system connecting the denitration slurry circulation pool and the denitration spray absorption layer to each other.
作为对本发明所述的单塔式双循环脱硫脱硝复合吸收装置的改进：所述臭氧氧化段包括相互连通的臭氧发生器和氧化段；所述臭氧氧化段与脱硝浆液循环池之间设置有升气装置；所述升气装置包括至少二个设置在氧化段上部的升气管；所述升气管进口贯穿吸收塔的侧壁后连通臭氧氧化段上方，升气管出口贯穿吸收塔的侧壁后连通脱硝浆液循环池上方。As an improvement to the single-tower double-cycle desulfurization and denitrification compound absorption device described in the present invention: the ozone oxidation section includes an interconnected ozone generator and an oxidation section; device; the air-rising device includes at least two air-rising pipes arranged on the upper part of the oxidation section; the inlet of the air-rising pipe passes through the side wall of the absorption tower and then connects to the top of the ozone oxidation section, and the outlet of the air-rising pipe passes through the side wall of the absorption tower and then connects to the denitrification Above the slurry circulation tank.
作为对本发明所述的单塔式双循环脱硫脱硝复合吸收装置的进一步改进：所述氧化段所在空间内以及升气管进口上分别设置有与臭氧发生器相互连通的臭氧喷嘴组Ⅰ和臭氧喷嘴组Ⅱ；所述臭氧喷嘴组Ⅰ内的臭氧喷嘴Ⅰ以0.1米的间距均匀的分布在氧化段的同一横截面上，所述臭氧喷嘴组Ⅰ的布置数量至少为一层；所述任意一个升气管进口均分布有3～5个臭氧喷嘴组Ⅱ内的臭氧喷嘴Ⅱ；所述臭氧喷嘴组Ⅱ内的臭氧喷嘴均沿气流水平方向设置。As a further improvement to the single-tower double-cycle desulfurization and denitrification compound absorption device described in the present invention: the space where the oxidation section is located and the inlet of the gas riser are respectively provided with an ozone nozzle group I and an ozone nozzle group connected to the ozone generator. II; the ozone nozzles I in the ozone nozzle group I are evenly distributed on the same cross-section of the oxidation section at a distance of 0.1 meters, and the arrangement number of the ozone nozzle group I is at least one layer; any one of the risers 3 to 5 ozone nozzles II in the ozone nozzle group II are evenly distributed at the inlet; the ozone nozzles in the ozone nozzle group II are all arranged along the horizontal direction of the airflow.
作为对本发明所述的单塔式双循环脱硫脱硝复合吸收装置的进一步改进：所述脱硫喷淋层的数量为2～3层；所述脱硫浆液循环系统包括脱硫循环泵和脱硫浆液箱；所述脱硫浆液循环池设有将浆液打入脱硫喷淋吸收层的脱硫循环泵；所述脱硫浆液箱分别与脱硫浆液循环池和/或脱硫喷淋吸收层相连通；所述脱硝喷淋吸收层的数量为1～2层；所述脱硝浆液循环系统包括脱硝循环泵；所述脱硝浆液循环池和脱硫浆液循环池均设有将浆液打入脱硝喷淋层的脱硝循环泵；所述脱硝浆液循环池的脱硝循环泵与脱硝喷淋吸收层上层相连通；所述脱硫浆液循环池的脱硝循环泵与脱硝喷淋吸收层下层相连通。As a further improvement to the single-tower double-circulation desulfurization and denitrification composite absorption device of the present invention: the number of desulfurization spray layers is 2 to 3 layers; the desulfurization slurry circulation system includes a desulfurization circulation pump and a desulfurization slurry tank; The desulfurization slurry circulation pool is provided with a desulfurization circulation pump that injects the slurry into the desulfurization spray absorption layer; the desulfurization slurry tank is respectively connected with the desulfurization slurry circulation pool and/or the desulfurization spray absorption layer; the denitration spray absorption layer The number of denitrification slurry is 1 to 2 layers; the denitrification slurry circulation system includes a denitration circulation pump; the denitration slurry circulation pool and the desulfurization slurry circulation pool are both equipped with a denitration circulation pump that injects the slurry into the denitration spray layer; the denitration slurry The denitrification circulation pump of the circulation pool is connected with the upper layer of the denitration spray absorption layer; the denitration circulation pump of the desulfurization slurry circulation pool is connected with the lower layer of the denitration spray absorption layer.
一种单塔式双循环脱硫脱硝复合吸收的脱硫脱硝方法，包括脱硫过程、NO氧化过程、脱硝过程；所述脱硫过程包括如下步骤：(1.1)将烟气进行深度除尘后通过烟气进口输入到脱硫浆液循环池和脱硫喷淋吸收层之间；(1.2)将NaOH从脱硫浆液循环池由脱硫循环泵打入脱硫喷淋层，由脱硫喷淋层喷淋NaOH吸收液；(1.3)烟气中的SO2和NaOH发生吸收反应：2NaOH+SO2＝Na2SO3+H2O，完成高效脱硫；(1.4)最终，在此步骤中产生的副产物Na2SO3回到脱硫浆液循环池，而脱硫后的烟气进入氧化段；所述NO氧化过程包括如下步骤：(2.1)将脱硫后的烟气通入臭氧氧化段；(2.2)将臭氧发生器产生的臭氧通过臭氧喷嘴注入到氧化段处的烟气内，臭氧与脱硫后烟气中NO充分接触，部分NO被氧化成NO2：NO+O3＝NO2+O2；(2.3)氧化后的烟气通过升气装置进入脱硝段，同时在升气管中继续发生氧化反应；所述脱硝过程包括如下步骤：(3.1)由脱硫过程产生的副产物Na2SO3通过脱硝循环泵从脱硫液循环池直接打入脱硝喷淋吸收层下层，并通过脱硝喷淋吸收层下层进行喷淋，此时副产物Na2SO3反应后回落到脱硝浆液循环池内，并由脱硝浆液循环池内的脱硝循环泵打入脱硝喷淋吸收层上层，继续进行喷淋；(3.2)NO和NO2在脱硝喷淋吸收层与Na2SO3充分接触，Na2SO3和NO2发生氧化还原反应：4Na2SO3+2NO2＝4Na2SO4+N2，最终完成高效脱硝；同时未完全反应的NaOH和NOx发生反应：2NaOH+NO+NO2＝2NaNO2+H2O和2NaOH+2NO2＝NaNO2+NaNO3+H2O；(3.3)脱硝后浆液池内的副产物定期排到曝气装置进一步氧化反应，完全转化为Na2SO4、NaHSO4和NaNO3后再进行废水处置；(3.4)脱硝完成后烟气经过除雾器脱除大量水分，最终由烟气出口排除，再经过系列气体成分检测，最后将达标的烟气从烟囱排出。A desulfurization and denitrification method of single-tower double-cycle desulfurization and denitrification combined absorption, comprising a desulfurization process, an NO oxidation process, and a denitrification process; the desulfurization process includes the following steps: (1.1) After the flue gas is subjected to deep dust removal, it is input through the flue gas inlet between the desulfurization slurry circulation tank and the desulfurization spray absorption layer; (1.2) inject NaOH from the desulfurization slurry circulation tank into the desulfurization spray layer by the desulfurization circulation pump, and spray the NaOH absorption liquid from the desulfurization spray layer; (1.3) smoke SO 2 and NaOH in the gas undergo an absorption reaction: 2NaOH+SO 2 =Na 2 SO 3 +H 2 O to complete efficient desulfurization; (1.4) Finally, the by-product Na 2 SO 3 produced in this step returns to the desulfurization slurry and the desulfurized flue gas enters the oxidation section; the NO oxidation process includes the following steps: (2.1) passing the desulfurized flue gas into the ozone oxidation section; (2.2) passing the ozone produced by the ozone generator through the ozone nozzle Injected into the flue gas at the oxidation section, the ozone fully contacts with the NO in the flue gas after desulfurization, and part of the NO is oxidized into NO 2 : NO+O 3 =NO 2 +O 2 ; (2.3) The oxidized flue gas passes through the The denitrification device enters the denitrification section, and at the same time, the oxidation reaction continues to occur in the gas riser; the denitrification process includes the following steps: (3.1) The by-product Na 2 SO 3 produced by the desulfurization process is directly pumped into the desulfurization liquid circulation tank through the denitration circulation pump. The lower layer of the denitrification spray absorption layer is sprayed through the lower layer of the denitrification spray absorption layer. At this time, the by-product Na 2 SO 3 reacts and falls back into the denitrification slurry circulation pool, and is pumped into the denitrification spray by the denitration circulation pump in the denitration slurry circulation pool. Spray the upper layer of the absorption layer and continue to spray; (3.2) NO and NO 2 fully contact with Na 2 SO 3 in the denitrification spray absorption layer, and redox reaction between Na 2 SO 3 and NO 2 occurs: 4Na 2 SO 3 +2NO 2 ＝4Na 2 SO 4 +N 2 , finally complete the high-efficiency denitrification; at the same time, the incompletely reacted NaOH and NOx react: 2NaOH+NO+NO 2 ＝2NaNO 2 +H 2 O and 2NaOH+2NO 2 ＝NaNO 2 +NaNO 3 + H 2 O; (3.3) After denitrification, the by-products in the slurry tank are regularly discharged to the aeration device for further oxidation reaction, and are completely converted into Na 2 SO 4 , NaHSO 4 and NaNO 3 before wastewater treatment; (3.4) After denitration is completed, the smoke The gas passes through the demister to remove a large amount of moisture, and finally is discharged from the flue gas outlet, and then passes through a series of gas composition tests, and finally the flue gas that meets the standard is discharged from the chimney.
作为对本发明所述的单塔式双循环脱硫脱硝复合吸收的脱硫脱硝方法的改进：所述步骤1.2中，NaOH和SO2的摩尔比控制在2.05:1，液气比8～10；所述步骤2.2中，臭氧浓度控制为1％～2％，以O3/NO＝1:1的比例均匀注入脱硫后烟气中；所述步骤3.2中，Na2SO3和NOx的摩尔比控制在1～2:1，液气比5～8。As an improvement to the desulfurization and denitrification method of single-tower double-cycle desulfurization and denitrification composite absorption described in the present invention: in the step 1.2, the molar ratio of NaOH and SO2 is controlled at 2.05:1, and the liquid-gas ratio is 8-10; the step In 2.2, the ozone concentration is controlled at 1% to 2%, and it is uniformly injected into the desulfurized flue gas at the ratio of O 3 /NO=1:1; in the step 3.2, the molar ratio of Na 2 SO 3 and NOx is controlled at 1 ～2:1, liquid-gas ratio 5～8.
一种对烟气脱硫脱硝的方法，包括如下步骤：一、脱硫：将深度除尘后的烟气，以NaOH喷淋，烟气中的SO2和NaOH发生吸收反应：2NaOH+SO2＝Na2SO3+H2O，完成高效脱硫；二、NO氧化：以O3/NO＝1:1的比例将臭氧注入到步骤一中脱硫后的烟气中，臭氧与步骤一处理后的烟气中的NO充分接触，部分NO被氧化成NO2：NO+O3＝NO2+O2；三、NOx的脱除：将步骤一中产生的脱硫副产物Na2SO3导入步骤二反应后的烟气中，NO和NO2与Na2SO3充分接触，此时：一方面，Na2SO3和NO2发生氧化还原反应，最终完成高效脱硝：4Na2SO3+2NO2＝4Na2SO4+N2；另一方面未完全反应的NaOH也能参与吸收反应，发生副反应：2NaOH+NO+NO2＝2NaNO2+H2O；控制Na2SO3和NOx的摩尔比为1～2:1，最终完成脱硝过程；四、废水、废气处理：将以上反应后的副产物通过曝气装置进行氧化反应，完全转化为Na2SO4、NaHSO4和NaNO3后，进行废水处置。A method for flue gas desulfurization and denitrification, comprising the following steps: 1. Desulfurization: spraying the flue gas after deep dust removal with NaOH, and the SO2 and NaOH in the flue gas undergo an absorption reaction: 2NaOH + SO2= Na2 SO 3 +H 2 O to complete high-efficiency desulfurization; 2. NO oxidation: inject ozone into the flue gas after desulfurization in step 1 at the ratio of O 3 /NO=1:1, and the ozone and the flue gas treated in step 1 Part of the NO is oxidized to NO 2 : NO+O 3 =NO 2 +O 2 ; 3. NOx removal: the desulfurization by-product Na 2 SO 3 produced in step 1 is introduced into step 2 after the reaction In the flue gas, NO and NO 2 are in full contact with Na 2 SO 3 , at this time: on the one hand, Na 2 SO 3 and NO 2 undergo redox reactions, and finally complete high-efficiency denitrification: 4Na 2 SO 3 +2NO 2 =4Na 2 SO 4 +N 2 ; on the other hand, incompletely reacted NaOH can also participate in the absorption reaction, and side reactions occur: 2NaOH+NO+NO 2 =2NaNO 2 +H 2 O; control the molar ratio of Na 2 SO 3 and NOx to 1 ~2:1, finally complete the denitrification process; 4. Wastewater and waste gas treatment: The by-products after the above reactions are oxidized through the aeration device, and after they are completely converted into Na2SO4, NaHSO4 and NaNO3, the waste water is disposed of.
作为本发明所述的对烟气脱硫脱硝的方法的改进：所述步骤一中，NaOH和SO2的摩尔比保持为2.05:1，液气比8～10；所述步骤二中，臭氧的质量浓度为1％～2％；所述步骤三中，Na2SO3和NOx的摩尔比保持为1～2:1，液气比5～8。As an improvement to the method for flue gas desulfurization and denitrification described in the present invention: in the step one, the molar ratio of NaOH and SO remains 2.05:1, and the liquid-gas ratio is 8-10; in the step two, the ozone The mass concentration is 1%-2%. In the third step, the molar ratio of Na 2 SO 3 and NOx is maintained at 1-2:1, and the liquid-gas ratio is 5-8.
本发明的单塔式双循环喷淋复合吸收塔与现有技术比较，具有如下的有益效果：Compared with the prior art, the single-tower double-circulation spray composite absorption tower of the present invention has the following beneficial effects:
(1)实现单塔高效脱硫脱硝，大大减少投资和运行成本，工艺简单可靠；(1) Realize high-efficiency desulfurization and denitrification in a single tower, greatly reducing investment and operating costs, and the process is simple and reliable;
(2)采用Na基混合液进行脱硫，然后采用反应所得的Na2SO3作为脱硝吸收剂，不仅吸收剂利用率高，且Na2SO3脱硝性能好；(2) Using Na-based mixed solution for desulfurization, and then using the Na 2 SO 3 obtained from the reaction as a denitrification absorbent, not only has a high utilization rate of the absorbent, but also has a good denitrification performance of Na 2 SO 3 ;
(3)三段式的结构，将SO2和NOx分别在净化装置脱硫喷淋段和净化脱硝喷淋段进行吸收，减少了竞争反应；( 3 ) The three-stage structure absorbs SO2 and NOx in the desulfurization spray section of the purification device and the purification denitrification spray section respectively, reducing the competition reaction;
(4)过渡段温度降低，用于臭氧对NO的氧化，减少了臭氧的分解，提高了NO氧化效率；(4) The temperature of the transition section is lowered, which is used for the oxidation of NO by ozone, which reduces the decomposition of ozone and improves the oxidation efficiency of NO;
(5)经过脱硫喷淋段后烟温下降，烟气体积大大减少，在一定的吸收液喷淋下，有助于提高脱硝效率。(5) After passing through the desulfurization spray section, the temperature of the flue gas drops, and the volume of the flue gas is greatly reduced. Under a certain amount of absorption liquid spraying, it helps to improve the denitrification efficiency.
附图说明Description of drawings
下面结合附图对本发明的具体实施方式作进一步详细说明。The specific implementation manners of the present invention will be described in further detail below in conjunction with the accompanying drawings.
图1是本发明的主要结构示意图；Fig. 1 is the main structural representation of the present invention;
图2图1的升气装置的俯视结构图；The top view structural diagram of the lift device of Fig. 2 Fig. 1;
图3图1的升气装置之臭氧喷嘴Ⅱ18的结构图；The structural diagram of the ozone nozzle II 18 of the gas-lifting device of Fig. 3 Fig. 1;
图4图1的臭氧氧化段之臭氧喷嘴Ⅰ19的布置图。The layout of the ozone nozzle I19 of the ozone oxidation section in Fig. 4 Fig. 1.
具体实施方式detailed description
实施例1、图1给出了一种单塔式双循环脱硫脱硝复合吸收装置，其主体结构为吸收塔，在吸收塔上，连接有曝气装置2、烟囱装置16等。Embodiment 1, Figure 1 shows a single-tower double-cycle desulfurization and denitrification compound absorption device, the main structure of which is an absorption tower, and an aeration device 2, a chimney device 16, etc. are connected to the absorption tower.
以上所述的吸收塔内自下而上依次设置为脱硫段5(烟气脱硫)、臭氧氧化段7(脱硫后的烟气氧化)和脱硝段10(氧化后烟气脱硝)。The absorption tower described above is sequentially set up from bottom to top as a desulfurization section 5 (flue gas desulfurization), an ozone oxidation section 7 (oxidation of flue gas after desulfurization) and a denitrification section 10 (denitration of flue gas after oxidation).
脱硫段5包括贯穿吸收塔侧壁的烟气进口、设置在吸收塔底部的脱硫浆液循环池3、设置在脱硫浆液循环池3上方的2～3层脱硫喷淋吸收层4(多层脱硫喷淋吸收层4的设置，确保反应效果)、将脱硫浆液循环池3和脱硫喷淋吸收层4相互连接的脱硫浆液循环系统；脱硫浆液循环系统包括脱硫循环泵和脱硫浆液箱1(内置NaOH吸收液)；脱硫浆液循环池3内设置脱硫循环泵，通过管道与每一层脱硫喷淋吸收层4均相连通；脱硫浆液箱1(内置NaOH吸收液)通过管道与每一层脱硫喷淋吸收层4均相连通，为了保障反应效率，在实际使用的时候，也可以将脱硫浆液箱1通过管道与脱硫浆液循环池3相互连通。NaOH吸收液对SO2的吸收速率是石灰石浆液的2～3倍，所以在NaOH吸收过程中达到一定的SO2吸收效率所需的停留时间更短，所需的喷淋层高度也就越低。在保证吸收效果的前提下，采用2～3层喷淋层将降低吸收塔整体高度，节省投资成本。The desulfurization section 5 includes the flue gas inlet that runs through the side wall of the absorption tower, the desulfurization slurry circulation pool 3 arranged at the bottom of the absorption tower, and the 2-3 layers of desulfurization spray absorption layer 4 (multi-layer desulfurization spray) above the desulfurization slurry circulation pool 3 setting of the desulfurization absorption layer 4 to ensure the reaction effect), a desulfurization slurry circulation system connecting the desulfurization slurry circulation pool 3 and the desulfurization spray absorption layer 4; the desulfurization slurry circulation system includes a desulfurization circulation pump and a desulfurization slurry tank 1 (built-in NaOH absorption liquid); the desulfurization slurry circulation pool 3 is provided with a desulfurization circulating pump, which is connected to each layer of desulfurization spray absorption layer 4 through pipelines; desulfurization slurry tank 1 (built-in NaOH absorption liquid) is connected to each layer of desulfurization spray absorption The layers 4 are all connected. In order to ensure the reaction efficiency, in actual use, the desulfurization slurry tank 1 can also be connected to the desulfurization slurry circulation tank 3 through pipelines. The absorption rate of SO2 by NaOH absorption liquid is 2 to 3 times that of limestone slurry, so the residence time required to achieve a certain SO2 absorption efficiency in the process of NaOH absorption is shorter, and the required height of the spray layer is also lower . Under the premise of ensuring the absorption effect, the use of 2 to 3 spray layers will reduce the overall height of the absorption tower and save investment costs.
脱硫喷淋吸收层4正上方设置臭氧氧化段7；臭氧氧化段7包括臭氧发生器13(产生臭氧)和氧化段(臭氧和脱硫后的烟气混合并发生氧化反应所在的空间)。The ozone oxidation section 7 is set directly above the desulfurization spray absorption layer 4; the ozone oxidation section 7 includes an ozone generator 13 (generating ozone) and an oxidation section (a space where ozone and desulfurized flue gas are mixed and oxidation reaction takes place).
脱硝段10包括贯穿吸收塔顶端的烟气出口、设置在臭氧氧化段正上方的脱硝浆液循环池15、设置在脱硝浆液循环池正上方的1～2层脱硝喷淋吸收层8(由于Na2SO3和NO2的反应速率较快，而且NO浓度在300～400mg/m3，所以只需要1～2层脱硝喷淋吸收层8)、设置在脱硝喷淋吸收层8和烟气出口之间的除雾装置9、将脱硝浆液循环池15和脱硝喷淋吸收层8相互连接的脱硝浆液循环系统；脱硝浆液循环系统为两个脱硝循环泵，两个脱硝循环泵分别设置在脱硝浆液循环池15和脱硫浆液循环池3(通过脱硫浆液循环池3补充Na2SO3吸收液)内，脱硝浆液循环池15的脱硝循环泵通过管道与上层的脱硝喷淋吸收层相连通，脱硫浆液循环池3的脱硝循环泵通过管道与下层的脱硝喷淋吸收层相连通。脱硝浆液循环池15上外置有曝气装置2，通过该曝气装置2排出反应后的最终副产物，并通过曝气处理。The denitration section 10 includes a flue gas outlet that runs through the top of the absorption tower, a denitrification slurry circulation pool 15 arranged directly above the ozone oxidation section, and 1 to 2 layers of denitration spray absorption layers 8 arranged directly above the denitration slurry circulation pool (due to Na 2 The reaction rate of SO 3 and NO 2 is fast, and the concentration of NO is 300-400mg/m 3 , so only 1-2 layers of denitrification spray absorption layer 8) are needed, which are arranged between the denitrification spray absorption layer 8 and the flue gas outlet The demisting device 9 between them, the denitrification slurry circulation system connecting the denitration slurry circulation pool 15 and the denitration spray absorption layer 8; In the pool 15 and the desulfurization slurry circulation pool 3 (the Na2SO3 absorption liquid is supplemented through the desulfurization slurry circulation pool 3 ), the denitration circulation pump of the denitration slurry circulation pool 15 is connected with the denitration spray absorption layer on the upper layer through the pipeline, and the desulfurization slurry circulates The denitrification circulating pump in pool 3 is connected with the denitrification spray absorption layer in the lower layer through pipelines. An aeration device 2 is installed externally on the denitrification slurry circulation tank 15 , and the final by-products after the reaction are discharged through the aeration device 2 and treated by aeration.
氧化段7与脱硝浆液循环池15之间设置有升气装置6；升气装置6的作用是将脱硫后的烟气引入脱硝段10。升气装置6包括至少两根设置在氧化段7上方两侧的升气管；升气管出口一端贯穿吸收塔的侧壁后，通过升气管道上升，直到相对于脱硝浆液循环池15的位置，再贯穿吸收塔的侧壁，通入到脱硝浆液循环池15上方(这种方式使脱硝和脱硫过程明确分离，防止SO2和NOx对Na2SO3发生竞争反应，从而提高了NOx的整体脱除率)。氧化段7所在空间内以及升气管口分别设置有与臭氧发生器13相互连通的臭氧喷嘴组Ⅰ和臭氧喷嘴组Ⅱ；臭氧喷嘴组Ⅰ内的臭氧喷嘴Ⅰ19在氧化段，并在氧化段横截面上以0.1米的间距均匀的分布；任意一个升气管进口均匀分布有3～5个臭氧喷嘴组Ⅱ内的臭氧喷嘴Ⅱ18；所述臭氧喷嘴组Ⅱ内的臭氧喷嘴Ⅱ18均沿气流水平方向设置。An air lift device 6 is arranged between the oxidation section 7 and the denitrification slurry circulation pool 15; the function of the air lift device 6 is to introduce the desulfurized flue gas into the denitrification section 10. The air lift device 6 includes at least two air lift pipes arranged on both sides above the oxidation section 7; after one end of the air lift pipe outlet passes through the side wall of the absorption tower, it rises through the air lift pipe until it reaches the position relative to the denitrification slurry circulation pool 15, and then It runs through the side wall of the absorption tower and leads to the top of the denitrification slurry circulation pool 15 (this way makes the denitrification and desulfurization processes clearly separated, prevents SO 2 and NOx from competing with Na 2 SO 3 , thereby improving the overall removal of NOx Rate). The space where the oxidation section 7 is located and the mouth of the air riser are respectively provided with the ozone nozzle group I and the ozone nozzle group II which communicate with the ozone generator 13; the ozone nozzle I19 in the ozone nozzle group I is in the oxidation section, and the cross section 3-5 ozone nozzles II 18 in the ozone nozzle group II are evenly distributed at the inlet of any air riser; the ozone nozzles II 18 in the ozone nozzle group II are all arranged along the horizontal direction of the airflow.
一种单塔式双循环脱硫脱硝复合吸收的脱硫脱硝方法，根据以上所述的单塔式双循环脱硫脱硝复合吸收装置实现，其步骤包括脱硫过程、NO氧化过程、脱硝过程。A single-tower double-cycle desulfurization and denitrification composite absorption method for desulfurization and denitrification is realized according to the above-mentioned single-tower double-cycle desulfurization and denitration composite absorption device, and the steps include a desulfurization process, an NO oxidation process, and a denitrification process.
一、脱硫过程包括如下步骤：1. The desulfurization process includes the following steps:
(1)从锅炉17出来的烟气Ⅰ(即未经过任何处理的烟气)先经过除尘装置进行深度除尘，然后烟气Ⅱ(即烟气Ⅰ通过除尘装置除尘后的烟气)进入本发明的烟气进口，在脱硫段5发生吸收反应(该吸收反应具体步骤如步骤2)。(1) The flue gas I (that is, the flue gas without any treatment) from the boiler 17 first passes through the dust removal device for deep dust removal, and then the flue gas II (that is, the flue gas after the flue gas I passes through the dust removal device) enters the present invention At the flue gas inlet, an absorption reaction occurs in the desulfurization section 5 (the specific steps of the absorption reaction are as in step 2).
(2)由脱硫浆液循环池3内的脱硫循环泵将脱硫浆液(NaOH/Na2SO3/NaHSO3的混合液；首先加入脱硫浆液循环池3内的为NaOH吸收液，由于不断反应后，产生Na2SO3以及副产物NaHSO3，所以该脱硫浆液循环池3内的吸收液逐渐变成了NaOH/Na2SO3/NaHSO3的混合液)从脱硫浆液循环池3打入脱硫喷淋吸收层4进行喷雾吸收，而喷淋出的NaOH液滴通过与SO2反应后，重新滴落到脱硫浆液循环池3内；于此同时，一定量的质量浓度为20～30％的新鲜NaOH从脱硫浆液箱2直接接入脱硫喷淋层4；在以上所述的反应过程中,需要将NaOH和SO2的摩尔比保持在2.05:1的最佳反应状态,而由于NaOH与SO2反应后不断生成Na2SO3和H2O以及副产物NaHSO3，所以脱硫浆液循环池3内的NaOH质量浓度不断降低，导致NaOH与SO2的摩尔比不能稳定在2.05:1的最佳反应状态，所以此时，通过脱硫浆液箱2将一定量(该新鲜NaOH吸收液的加入量根据SO2的脱除量计算出来，确保NaOH与SO2的摩尔比稳定在2.05:1)的质量浓度为20％～30％的NaOH吸收液打入脱硫喷淋吸收层4或者直接加入脱硫浆液循环池3内(脱硫浆液循环池3内直接上来的是NaOH/Na2SO3/NaHSO3的混合液，实际NaOH浓度低，为了保证吸收效果，液气比是比较大，一般控制在液气比8～10；而由于脱硫浆液箱2出来的NaOH是高浓度，所以NaOH流量是很小的。所以新鲜的NaOH可以加到管道内，直接带入喷淋层4；也可以直接加入浆液循环池3)。(2) The desulfurization slurry (NaOH/Na 2 SO 3 /NaHSO 3 mixture is mixed by the desulfurization circulating pump in the desulfurization slurry circulation pool 3; what is first added to the desulfurization slurry circulation pool 3 is the NaOH absorption liquid. After the continuous reaction, Na 2 SO 3 and by-product NaHSO 3 are produced, so the absorption liquid in the desulfurization slurry circulation tank 3 gradually becomes a mixture of NaOH/Na 2 SO 3 /NaHSO 3 ) from the desulfurization slurry circulation tank 3 into the desulfurization spray The absorption layer 4 is sprayed and absorbed, and the sprayed NaOH droplets are re-dropped into the desulfurization slurry circulation pool 3 after reacting with SO 2 ; at the same time, a certain amount of fresh NaOH with a mass concentration of 20-30% The desulfurization slurry tank 2 is directly connected to the desulfurization spray layer 4; in the above-mentioned reaction process, the molar ratio of NaOH and SO 2 needs to be kept at the optimal reaction state of 2.05:1, and due to the reaction of NaOH and SO 2 Afterwards, Na 2 SO 3 and H 2 O and the by-product NaHSO 3 are continuously generated, so the NaOH mass concentration in the desulfurization slurry circulation tank 3 continues to decrease, resulting in that the molar ratio of NaOH to SO 2 cannot be stabilized at the optimal reaction state of 2.05:1 , so at this moment, by the desulfurization slurry tank 2 , the mass concentration of a certain amount (the addition amount of this fresh NaOH absorbing liquid is calculated according to the removal amount of SO2 to ensure that the molar ratio of NaOH and SO2 is stable at 2.05:1) is 20% to 30% of the NaOH absorption liquid is injected into the desulfurization spray absorption layer 4 or directly into the desulfurization slurry circulation pool 3 (the mixture of NaOH/Na 2 SO 3 /NaHSO 3 comes directly from the desulfurization slurry circulation pool 3, The actual NaOH concentration is low. In order to ensure the absorption effect, the liquid-gas ratio is relatively large, generally controlled at a liquid-gas ratio of 8 to 10; and because the NaOH from the desulfurization slurry tank 2 is of high concentration, the NaOH flow rate is very small. Therefore, fresh NaOH can be added to the pipeline and directly brought into the spray layer 4; it can also be directly added to the slurry circulation tank 3).
(3)烟气Ⅱ中的SO2和NaOH发生吸收反应，完成高效脱硫,同时生成脱硫副产物Na2SO3。(3) The SO 2 and NaOH in the flue gas II undergo an absorption reaction to complete high-efficiency desulfurization and generate Na 2 SO 3 as a desulfurization by-product.
本次脱硫过程步骤中，主要的化学反应过程如下所示：In this desulfurization process step, the main chemical reaction process is as follows:
2NaOH+SO2＝Na2SO3+H2O(脱硫过程主要反应)；2NaOH+SO 2 ＝Na 2 SO 3 +H 2 O (the main reaction in the desulfurization process);
NaOH+SO2＝NaHSO3(脱硫过程副反应)。NaOH+SO 2 =NaHSO 3 (a side reaction in the desulfurization process).
二、所述NO氧化过程包括如下步骤：Two, the NO oxidation process comprises the following steps:
(1)将烟气Ⅲ(即将烟气Ⅱ脱硫后的烟气)通入臭氧氧化段7的氧化段(氧化段为存放烟气Ⅲ容器，即臭氧和脱硫后的烟气混合并发生氧化反应所在的空间)，将NO部分氧化成NO2(具体如步骤2)；(1) Pass the flue gas III (that is, the flue gas after desulfurization of the flue gas II) into the oxidation section of the ozone oxidation section 7 (the oxidation section is a container for storing the flue gas III, that is, the ozone and the desulfurized flue gas are mixed and the oxidation reaction occurs The space where the NO is located), the NO is partially oxidized into NO 2 (specifically as step 2);
(2)将臭氧发生器13产生的臭氧质量浓度控制为1％～2％左右；根据烟气中NO的浓度，将臭氧以O3/NO＝1:1的比例通过均匀布置的臭氧喷嘴组Ⅰ内的臭氧喷嘴Ⅰ19注入到氧化段处的烟气Ⅲ内，臭氧与烟气Ⅲ中NO充分接触，部分NO被氧化成NO2；(2) The mass concentration of ozone produced by the ozone generator 13 is controlled to be about 1% to 2%; according to the concentration of NO in the flue gas, the ozone is passed through the uniformly arranged ozone nozzle group with the ratio of O 3 /NO=1:1 The ozone nozzle I19 in I is injected into the flue gas III in the oxidation section, the ozone fully contacts with the NO in the flue gas III, and part of the NO is oxidized into NO 2 ;
(3)烟气Ⅳ(即烟气Ⅲ在上一步骤中氧化后的烟气)通过升气装置6导入脱硝段10的相应位置(即脱硝浆液循环池15上方)，同时，臭氧喷嘴组Ⅱ内的臭氧喷嘴Ⅱ18向升气管口喷射臭氧，使得烟气Ⅳ在升气管中继续发生氧化反应。(3) The flue gas IV (that is, the flue gas oxidized by the flue gas III in the previous step) is introduced into the corresponding position of the denitrification section 10 (that is, above the denitrification slurry circulation pool 15) through the gas lifter 6, and at the same time, the ozone nozzle group II The inner ozone nozzle II18 injects ozone to the riser mouth, so that the flue gas IV continues to oxidize in the riser.
(4)另外，随着烟气Ⅲ通入臭氧氧化段7的氧化段空间内，该烟气Ⅲ中蕴含的Na2SO3液滴(脱硫产生的Na2SO3液滴)在此时与NOx发生反应，所以无需在脱硫段进行除雾。(4) In addition, as the flue gas III passes into the oxidation section space of the ozonation section 7, the Na 2 SO 3 droplets (Na 2 SO 3 droplets produced by desulfurization) contained in the flue gas III are mixed with the NOx reacts, so there is no need for demisting in the desulfurization section.
本次NO氧化过程步骤中，主要的化学反应过程如下所示：In this NO oxidation process step, the main chemical reaction process is as follows:
NO+O3＝NO2+O2(氧化段主要反应)；NO+O 3 ＝NO 2 +O 2 (the main reaction in the oxidation section);
NO+H2O2＝NO2+H2O(氧化段副反应)。NO+H 2 O 2 =NO 2 +H 2 O (side reaction in the oxidation stage).
其中，所述H2O2由臭氧被水吸收而来：：O3+H2O＝H2O2+O2。Wherein, the H 2 O 2 comes from ozone absorbed by water: O 3 +H 2 O=H 2 O 2 +O 2 .
三、所述NOx的脱除过程包括如下步骤：Three, the removal process of described NOx comprises the following steps:
(1)烟气Ⅳ通过升气装置6进入脱硝段10；(1) The flue gas IV enters the denitrification section 10 through the gas-lifting device 6;
(2)通过脱硫浆液循环池3内的脱硝循环泵从脱硫浆液循环池3将浆液(Na2SO3、Na2SO4、NaNO3)直接打入脱硝喷淋层8下层(主要利用的是脱硫过程产生的副产物Na2SO3)，同时脱硝喷淋层8的上层由脱硝浆液循环池15内的脱硝循环泵从脱硝浆液循环池15将浆液(此处浆液主要是Na2SO3、Na2SO4、NaNO3，脱硝喷淋层8下层的浆液使用后进入脱硝浆液循环池15)打入；(2) The slurry (Na 2 SO 3 , Na 2 SO 4 , NaNO 3 ) is directly pumped into the lower layer of the denitrification spray layer 8 from the desulfurization slurry circulation tank 3 through the denitrification circulating pump in the desulfurization slurry circulation tank 3 (mainly using The by-product Na 2 SO 3 produced in the desulfurization process), and the upper layer of the denitrification spray layer 8 is fed the slurry (here the slurry is mainly Na 2 SO 3 , Na 2 SO 4 , NaNO 3 , the slurry in the lower layer of the denitrification spray layer 8 is injected into the denitrification slurry circulation pool 15) after use;
(3)烟气Ⅳ内的NO和NO2在脱硝喷淋层8与Na2SO3充分接触，并将Na2SO3和NOx的摩尔比控制在1～2:1，使得Na2SO3和NO2发生氧化还原反应，最终完成高效脱硝；(3) The NO and NO 2 in the flue gas IV fully contact with Na 2 SO 3 in the denitrification spray layer 8, and the molar ratio of Na 2 SO 3 and NOx is controlled at 1-2:1, so that Na 2 SO 3 Oxidation - reduction reaction with NO2, and finally complete efficient denitrification;
(4)脱硝后，脱硝浆液循环池15内的副产物定期排到曝气装置2进一步氧化反应，完全转化为Na2SO4、NaHSO4和NaNO3等后再进行废水处置；(4) After denitrification, the by-products in the denitrification slurry circulation tank 15 are regularly discharged to the aeration device 2 for further oxidation reaction, and are completely converted into Na 2 SO 4 , NaHSO 4 and NaNO 3 , etc. before wastewater treatment;
(5)脱硝完成后烟气经过除雾器9脱除大量水分，最终由烟气出口排出，再经过系列气体成分检测，最后将达标的烟气从烟囱16排出。(5) After the denitrification is completed, the flue gas passes through the demister 9 to remove a large amount of water, and finally is discharged from the flue gas outlet, and then passes through a series of gas composition tests, and finally the flue gas that meets the standard is discharged from the chimney 16 .
本次NOx的脱除过程步骤中，主要的化学反应过程如下所示：In this NOx removal process step, the main chemical reaction process is as follows:
4Na2SO3+2NO2＝4Na2SO4+N2(脱硝主要反应)；4Na 2 SO 3 +2NO 2 ＝4Na 2 SO 4 +N 2 (the main reaction of denitrification);
2NaOH+NO+NO2＝2NaNO2+H2O(脱硝副反应)；2NaOH+NO+NO 2 = 2NaNO 2 +H 2 O (denitrification side reaction);
2NaOH+2NO2＝NaNO2+NaNO3+H2O(脱硝副反应)。2NaOH+2NO 2 =NaNO 2 +NaNO 3 +H2O (denitrification side reaction).
一种对烟气脱硫脱硝的方法；包括如下步骤实现：A method for desulfurization and denitrification of flue gas; comprising the following steps:
一、脱硫：1. Desulfurization:
将烟气深度除尘后，以一定量的NaOH喷淋(NaOH的量通过SO2决定，即保持NaOH和SO2的摩尔比保持在2.05:1；)，此时，烟气中的SO2和NaOH发生吸收反应：2NaOH+SO2＝Na2SO3+H2O(脱硫过程主要反应)，完成高效脱硫；After the flue gas is dedusted deeply, it is sprayed with a certain amount of NaOH (the amount of NaOH is determined by SO 2 , that is, the molar ratio of NaOH and SO 2 is kept at 2.05:1;), at this time, the SO 2 and The absorption reaction of NaOH occurs: 2NaOH+SO 2 =Na 2 SO 3 +H 2 O (the main reaction in the desulfurization process), completing efficient desulfurization;
同时，进行副反应：NaOH+SO2＝NaHSO3(脱硫过程副反应)。At the same time, a side reaction occurs: NaOH+SO 2 =NaHSO 3 (a side reaction in the desulfurization process).
二、NO氧化：2. NO oxidation:
将浓度为1％～2％的臭氧按照O3/NO＝1:1的比例注入到步骤一中脱硫后的烟气中，臭氧与步骤一处理后烟气中的NO充分接触，部分NO被氧化成NO2：NO+O3＝NO2+O2(氧化段主要反应)。Inject ozone with a concentration of 1% to 2% into the flue gas after desulfurization in step 1 according to the ratio of O 3 /NO=1:1. The ozone fully contacts the NO in the flue gas after step 1 treatment, and part of the NO is Oxidation to NO 2 : NO+O 3 =NO 2 +O 2 (the main reaction in the oxidation stage).
同时，进行副反应：NO+H2O2＝NO2+H2O(氧化段副反应)。At the same time, a side reaction occurs: NO+H 2 O 2 =NO 2 +H 2 O (side reaction in the oxidation stage).
三、NOx的脱除：3. NOx removal:
将步骤一中产生的脱硫副产物Na2SO3导入步骤二反应后的烟气中，NO和NO2与Na2SO3充分接触，并控制Na2SO3和NOx的摩尔比为1～2:1，，液气比5～8，此时，Na2SO3和NO2发生氧化还原反应，最终完成高效脱硝：4Na2SO3+2NO2＝4Na2SO4+N2(脱硝主要反应)；The desulfurization by-product Na 2 SO 3 produced in step 1 is introduced into the flue gas after the reaction in step 2, NO and NO2 are fully contacted with Na 2 SO 3 , and the molar ratio of Na 2 SO 3 and NOx is controlled to be 1-2: 1. The liquid-to-gas ratio is 5-8. At this time, Na 2 SO 3 and NO 2 undergo oxidation-reduction reactions, and finally complete high-efficiency denitration: 4Na 2 SO 3 +2NO 2 = 4Na 2 SO 4 +N 2 (main denitrification reaction) ;
由于此时烟气中还有NO，所以还会进行如下的副反应：2NaOH+NO+NO2＝2NaNO2+H2O和2NaOH+2NO2＝NaNO2+NaNO3+H2O(脱硝副反应)；Since there is still NO in the flue gas at this time, the following side reactions will also occur: 2NaOH+NO+NO 2 =2NaNO 2 +H 2 O and 2NaOH+2NO 2 =NaNO 2 +NaNO 3 +H2O (denitrification side reaction) ;
四、废水、废气处理：4. Wastewater and waste gas treatment:
将以上反应后的副产物通过曝气装置进行氧化反应，完全转化为Na2SO4、NaHSO4和NaNO3后，进行废水处置。The by-products after the above reaction are oxidized through the aeration device, and after being completely converted into Na 2 SO 4 , NaHSO 4 and NaNO 3 , the waste water is disposed of.
实施案例：Implementation case:
有一采用单塔式双循环喷淋复合吸收装置及工艺系统的燃煤锅炉同时脱硫脱硝示范工程，烟气处理量2000Nm3/h，SO2初始浓度2400mg/Nm3，NOx初始浓度380mg/Nm3。不同工艺条件下示范工程实验的结果如下所示：There is a coal-fired boiler simultaneous desulfurization and denitrification demonstration project using a single-tower double-circulation spray composite absorption device and process system. The flue gas treatment capacity is 2000Nm 3 /h, the initial concentration of SO2 is 2400mg/Nm 3 , and the initial concentration of NOx is 380mg/Nm 3 . The results of demonstration engineering experiments under different process conditions are as follows:
最后，还需要注意的是，以上列举的仅是本发明的一个具体实施例。显然，本发明不限于以上实施例，还可以有许多变形。本领域的普通技术人员能从本发明公开的内容直接导出或联想到的所有变形，均应认为是本发明的保护范围。Finally, it should also be noted that what is listed above is only a specific embodiment of the present invention. Obviously, the present invention is not limited to the above embodiments, and many variations are possible. All deformations that can be directly derived or associated by those skilled in the art from the content disclosed in the present invention should be considered as the protection scope of the present invention.
Claims (7)
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| CN105833686A (en) * | 2016-03-23 | 2016-08-10 | 凯天环保科技股份有限公司 | Fume nitrogen and sulfur resource utilization method and device thereof |
| CN106390701A (en) * | 2016-10-31 | 2017-02-15 | 浙江富春江环保热电股份有限公司 | Multilevel plasma ultralow intensified smoke emission control system and multilevel plasma ultralow intensified smoke emission control method |
| CN106925097A (en) * | 2017-04-28 | 2017-07-07 | 陶汉中 | It is a kind of based on liquid phase oxidation to the combined column and its technique of flue gas desulfurization and denitrification |
| CN110292843A (en) * | 2018-03-21 | 2019-10-01 | 兰州凯特环境技术工程有限公司 | Multistage shell and tube, segmentation ozone denitration device and its method |
| CN108261905A (en) * | 2018-04-08 | 2018-07-10 | 北京美斯顿科技开发有限公司 | A kind of denitration integrated device and method |
| CN110550841B (en) * | 2019-09-26 | 2024-07-09 | 浙江富春江环保热电股份有限公司 | Flue gas deep denitration system and method in sludge drying-incineration system |
| CN112844013B (en) * | 2019-11-28 | 2025-01-24 | 中冶京诚工程技术有限公司 | Flue gas oxidation denitrification device and method |
| CN114682074A (en) * | 2022-05-09 | 2022-07-01 | 福建省青山纸业股份有限公司 | A production process for desulfurization and denitrification of alkali recovery furnace by utilizing NaOH and NaClO |
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| CN203507793U (en) * | 2013-11-06 | 2014-04-02 | 安徽同兴环保工程股份有限公司 | Device for simultaneously removing sulfur dioxide and nitrogen oxide from coke oven flue gas |
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