CN104084025B - A kind of method of boiler smoke removal of nitrogen oxide - Google Patents
A kind of method of boiler smoke removal of nitrogen oxide Download PDFInfo
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- MWUXSHHQAYIFBG-UHFFFAOYSA-N Nitric oxide Chemical compound O=[N] MWUXSHHQAYIFBG-UHFFFAOYSA-N 0.000 title claims abstract description 51
- 238000000034 method Methods 0.000 title claims abstract description 42
- 239000000779 smoke Substances 0.000 title 1
- XEEYBQQBJWHFJM-UHFFFAOYSA-N iron Substances [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 claims abstract description 85
- KCXVZYZYPLLWCC-UHFFFAOYSA-N EDTA Chemical compound OC(=O)CN(CC(O)=O)CCN(CC(O)=O)CC(O)=O KCXVZYZYPLLWCC-UHFFFAOYSA-N 0.000 claims abstract description 41
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims abstract description 39
- 239000003546 flue gas Substances 0.000 claims abstract description 39
- 238000010521 absorption reaction Methods 0.000 claims abstract description 37
- 230000008929 regeneration Effects 0.000 claims abstract description 18
- 238000011069 regeneration method Methods 0.000 claims abstract description 18
- 229910052742 iron Inorganic materials 0.000 claims abstract description 15
- 238000006243 chemical reaction Methods 0.000 claims description 16
- 238000006722 reduction reaction Methods 0.000 claims description 15
- 238000010668 complexation reaction Methods 0.000 claims description 12
- 239000006096 absorbing agent Substances 0.000 claims description 9
- 239000007921 spray Substances 0.000 claims description 6
- 239000007788 liquid Substances 0.000 claims description 4
- 239000002184 metal Substances 0.000 claims description 4
- 229910052751 metal Inorganic materials 0.000 claims description 4
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 4
- CWYNVVGOOAEACU-UHFFFAOYSA-N Fe2+ Chemical compound [Fe+2] CWYNVVGOOAEACU-UHFFFAOYSA-N 0.000 claims description 3
- 125000002252 acyl group Chemical group 0.000 claims description 2
- 238000004064 recycling Methods 0.000 claims description 2
- 238000005507 spraying Methods 0.000 claims 1
- 239000007791 liquid phase Substances 0.000 abstract description 10
- 239000000047 product Substances 0.000 abstract description 4
- 239000002250 absorbent Substances 0.000 abstract description 3
- 230000002745 absorbent Effects 0.000 abstract description 3
- 150000003863 ammonium salts Chemical class 0.000 abstract description 3
- 230000000536 complexating effect Effects 0.000 abstract description 3
- YOBAEOGBNPPUQV-UHFFFAOYSA-N iron;trihydrate Chemical compound O.O.O.[Fe].[Fe] YOBAEOGBNPPUQV-UHFFFAOYSA-N 0.000 abstract description 3
- 239000002994 raw material Substances 0.000 abstract description 3
- 239000003638 chemical reducing agent Substances 0.000 abstract description 2
- 239000002244 precipitate Substances 0.000 abstract description 2
- 239000001054 red pigment Substances 0.000 abstract description 2
- 239000000126 substance Substances 0.000 abstract description 2
- MBMLMWLHJBBADN-UHFFFAOYSA-N Ferrous sulfide Chemical compound [Fe]=S MBMLMWLHJBBADN-UHFFFAOYSA-N 0.000 abstract 1
- NDLPOXTZKUMGOV-UHFFFAOYSA-N oxo(oxoferriooxy)iron hydrate Chemical compound O.O=[Fe]O[Fe]=O NDLPOXTZKUMGOV-UHFFFAOYSA-N 0.000 abstract 1
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 16
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 description 8
- 238000005516 engineering process Methods 0.000 description 8
- 239000007789 gas Substances 0.000 description 5
- 229910021529 ammonia Inorganic materials 0.000 description 4
- BFNBIHQBYMNNAN-UHFFFAOYSA-N ammonium sulfate Chemical compound N.N.OS(O)(=O)=O BFNBIHQBYMNNAN-UHFFFAOYSA-N 0.000 description 4
- 229910052921 ammonium sulfate Inorganic materials 0.000 description 4
- 235000011130 ammonium sulphate Nutrition 0.000 description 4
- 239000003054 catalyst Substances 0.000 description 3
- 238000002485 combustion reaction Methods 0.000 description 3
- 238000003756 stirring Methods 0.000 description 3
- UQSXHKLRYXJYBZ-UHFFFAOYSA-N Iron oxide Chemical compound [Fe]=O UQSXHKLRYXJYBZ-UHFFFAOYSA-N 0.000 description 2
- 239000002253 acid Substances 0.000 description 2
- 238000010531 catalytic reduction reaction Methods 0.000 description 2
- 239000000446 fuel Substances 0.000 description 2
- 229910000069 nitrogen hydride Inorganic materials 0.000 description 2
- 239000002912 waste gas Substances 0.000 description 2
- XSQUKJJJFZCRTK-UHFFFAOYSA-N Urea Chemical compound NC(N)=O XSQUKJJJFZCRTK-UHFFFAOYSA-N 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical group [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000002210 biocatalytic effect Effects 0.000 description 1
- 239000004202 carbamide Substances 0.000 description 1
- 238000006555 catalytic reaction Methods 0.000 description 1
- 239000002738 chelating agent Substances 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 239000008139 complexing agent Substances 0.000 description 1
- 150000001875 compounds Chemical class 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 239000000428 dust Substances 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 239000002440 industrial waste Substances 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 239000003595 mist Substances 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 239000002245 particle Substances 0.000 description 1
- 231100000572 poisoning Toxicity 0.000 description 1
- 230000000607 poisoning effect Effects 0.000 description 1
- 230000002829 reductive effect Effects 0.000 description 1
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Abstract
本发明公开了一种锅炉烟气氮氧化物脱除的方法。首先将烟气通入FeⅡEDTA溶液中,络合吸收NO得到亚铁亚酰络合物FeⅡ(NO)EDTA,再将FeⅡ(NO)EDTA引入再生装置,用金属铁还原FeⅡ(NO)EDTA再生FeⅡEDTA,同时NO转化为高浓度的NH3。本发明以液相络合吸收剂脱除烟气中的NO,有效解决了NO难以进入液相的技术困难;吸收和再生分开进行,提高了NH3浓度,可解决NH3吸收装置过于庞大的问题;产生的NH3可生成铵盐作为工业原料,也可作为还原剂进入其他锅炉烟气SNCR脱硝反应器内,铁形成的氧化铁水合沉淀物,可作为铁红颜料等化工产品。
The invention discloses a method for removing nitrogen oxides from boiler flue gas. Firstly, the flue gas is passed into the Fe Ⅱ EDTA solution, and NO is complexed and absorbed to obtain the ferrous sulfide complex Fe Ⅱ (NO) EDTA, and then the Fe Ⅱ (NO) EDTA is introduced into the regeneration device, and the Fe Ⅱ ( NO)EDTA regenerates Fe Ⅱ EDTA, and NO is converted into high-concentration NH 3 at the same time. The present invention removes NO in the flue gas with a liquid-phase complexing absorbent, which effectively solves the technical difficulty that NO is difficult to enter the liquid phase; the absorption and regeneration are carried out separately, which increases the NH3 concentration and can solve the problem that the NH3 absorption device is too large Problem: The NH 3 produced can generate ammonium salts as industrial raw materials, and can also be used as a reducing agent to enter other boiler flue gas SNCR denitrification reactors. The iron oxide hydrate precipitate formed by iron can be used as iron red pigments and other chemical products.
Description
技术领域technical field
本发明涉及一种烟气净化的方法,尤其涉及一种锅炉烟气氮氧化物脱除的方法。The invention relates to a method for purifying flue gas, in particular to a method for removing nitrogen oxides from boiler flue gas.
背景技术Background technique
工业废气中主要含有NO和NO2,且NO的浓度通常都远远高于NO2,特别是在燃烧烟气的NOx中,NO占95%左右,NO2占的比例较少。同时NO气-液传质阻力大,水中溶解度较低,其处理过程十分困难。我国目前NOx的排放量正在以高达10%的速度逐年增长,预计到2020年将达(2660~2970)×104t,因此开展对大气中NOx的污染控制研究已迫在眉睫。Industrial waste gas mainly contains NO and NO 2 , and the concentration of NO is usually much higher than that of NO 2 , especially in the NOx of combustion flue gas, NO accounts for about 95%, and NO 2 accounts for a small proportion. At the same time, NO gas-liquid mass transfer resistance is high, and its solubility in water is low, so its treatment process is very difficult. The NOx emission in our country is increasing year by year at a rate of up to 10%, and it is expected to reach (2660~2970)×104t by 2020. Therefore, it is imminent to carry out research on the pollution control of NOx in the atmosphere.
目前,NOx污染控制方法主要有三种:燃料脱氮技术、低NOx燃烧技术和烟气脱硝技术。但是由于多方面的原因,燃料脱氮技术和第NOx燃烧技术尚未达到全面实用阶段,烟气脱硝仍然是NOx污染控制最主要的方法。At present, there are three main methods of NOx pollution control: fuel denitrification technology, low NOx combustion technology and flue gas denitrification technology. However, due to various reasons, fuel denitrification technology and NOx combustion technology have not yet reached the stage of full practicality, and flue gas denitrification is still the most important method for NOx pollution control.
烟气脱硝技术使用最广泛的分为两类:选择性催化还原法(SCR)和选择性非催化还原法(SNCR),它们的反应机理都是以氨气为还原剂将烟气中NOx还原成无害的氮气和水,两者的主要差别在于SCR使用催化剂,反应温度较低,SNCR不使用催化剂反应温度较高。但是这两种方法都存在着一定的缺陷,SCR法对设计要求较高,制造和运行成本较高。在脱硝过程中,由于烟气中含有SO2、水雾和尘粒等,会造成催化剂“中毒”等不利于催化反应的现象。SNCR法氨耗量高,氨逃逸量较大,混合均匀的难度大,所以其脱硝率只能达到50~60%。同时这两种方法是用的尿素或氨气不完全反应后排空很容易造成二次污染。The most widely used flue gas denitrification technology is divided into two categories: selective catalytic reduction (SCR) and selective non-catalytic reduction (SNCR). Their reaction mechanism is to use ammonia as the reducing agent to reduce NOx in flue gas. The main difference between the two is that SCR uses a catalyst and the reaction temperature is lower, while SNCR does not use a catalyst and the reaction temperature is higher. However, both methods have certain defects. The SCR method has relatively high design requirements, and the manufacturing and operating costs are relatively high. During the denitrification process, because the flue gas contains SO 2 , water mist and dust particles, etc., it will cause catalyst "poisoning" and other phenomena that are not conducive to the catalytic reaction. The SNCR method consumes a lot of ammonia, has a large amount of ammonia escape, and is difficult to mix evenly, so its denitrification rate can only reach 50-60%. At the same time, the urea or ammonia used in these two methods is not completely reacted and then emptied, which is easy to cause secondary pollution.
近年来,采用液相络合吸收脱除烟气中氮氧化物的湿法脱硝技术研究广泛开展。该方法利用液相络合剂直接与烟气中难溶于水的NO反应,使NO进入液相,从而达到烟气脱硝的目的。根据国内外众多学者就对液相络合吸收法的研究,FeⅡEDTA溶液对NO的吸收有非常好的效果。但是到目前为止,液相络合法却仍然难以实现工业化,其主要原因是脱硝过程中需要的FeⅡEDTA消耗量较大,并且价格较高,会增加工艺运行成本,同时FeⅡEDTA在反应过程中容易被氧化为不能络合NO的FeⅢEDTA,从而会降低工艺的脱硝效率。后来有学者提出用生物催化还原法来再生FeⅡEDTA,但是该法实施过程复杂,投入实际应用还有很多问题需要解决。马乐凡提出用亚铁螯合剂络合吸收NO,然后通过铁粉与生成的亚铁亚硝酰络合物反应还原再生FeⅡEDTA,其工艺采用一体化架构,络合吸收与还原再生在同一个反应器内。该工艺的缺陷在于反应生成的NH3浓度较低,而所需要NH3吸收装置的容量必须与NO络合装置等同,这样所需的设备投入会大大增加,同时会增加整个工艺流程运行的难度。In recent years, research on wet denitrification technology using liquid phase complexation absorption to remove nitrogen oxides in flue gas has been widely carried out. In this method, the liquid phase complexing agent directly reacts with the insoluble NO in the flue gas, so that the NO enters the liquid phase, so as to achieve the purpose of flue gas denitrification. According to the research on the liquid phase complexation absorption method by many scholars at home and abroad, Fe Ⅱ EDTA solution has a very good effect on the absorption of NO. But so far, the liquid phase complexation method is still difficult to achieve industrialization, the main reason is that the consumption of Fe Ⅱ EDTA in the denitrification process is relatively large, and the price is high, which will increase the operating cost of the process . In the process, it is easily oxidized to Fe III EDTA which cannot complex NO, which will reduce the denitrification efficiency of the process. Later, some scholars proposed to use biocatalytic reduction method to regenerate Fe Ⅱ EDTA, but the implementation process of this method is complicated, and there are still many problems to be solved in practical application. Ma Lefan proposed to use ferrous chelating agent to complex absorb NO, and then reduce and regenerate Fe Ⅱ EDTA through the reaction of iron powder and the generated ferrous nitrosyl complex. The process adopts an integrated structure, complex absorption and reduction regeneration in the same inside the reactor. The disadvantage of this process is that the concentration of NH3 generated by the reaction is low, and the capacity of the required NH3 absorption device must be equal to that of the NO complexing device, so that the required equipment investment will be greatly increased, and the difficulty of the operation of the entire process will be increased at the same time .
发明内容Contents of the invention
为了解决上述技术问题,本发明提供一种锅炉烟气氮氧化物脱除的方法。In order to solve the above technical problems, the present invention provides a method for removing nitrogen oxides from boiler flue gas.
本发明解决上述技术问题的技术方案为:The technical scheme that the present invention solves the problems of the technologies described above is:
一种锅炉烟气氮氧化物脱除的方法,包括如下步骤:A method for removing nitrogen oxides from boiler flue gas, comprising the steps of:
(1)在吸收器内,以FeⅡEDTA溶液作为吸收液,通过络合吸收反应,吸收烟气中极难溶于水的NO,反应后生成的亚铁亚酰络合物引入还原再生装置;(1) In the absorber, Fe Ⅱ EDTA solution is used as the absorbing liquid to absorb NO which is extremely difficult to dissolve in water in the flue gas through complexation absorption reaction, and the ferrous and acyl complex formed after the reaction is introduced into the reduction regeneration device ;
(2)在还原再生装置内,金属铁与亚铁亚硝酰络合物发生还原反应,将络合物中的NO还原为高浓度的NH3,同时再生出FeⅡEDTA循环用于吸收NO。(2) In the reduction and regeneration device, metal iron and ferrous nitrosyl complex undergo a reduction reaction, reducing the NO in the complex to high-concentration NH 3 , and at the same time regenerate Fe II EDTA for recycling to absorb NO .
上述的锅炉烟气氮氧化物脱除的方法,所述的络合吸收反应温度为293K~323K,pH为5.0~6.5,FeⅡEDTA溶液的浓度为15~40mmol/L。In the above method for removing nitrogen oxides from boiler flue gas, the temperature of the complexation absorption reaction is 293K-323K, the pH is 5.0-6.5, and the concentration of Fe II EDTA solution is 15-40mmol/L.
上述的锅炉烟气氮氧化物脱除的方法,所述的还原反应温度为293K~323K,所述的亚铁亚硝酰络合物喷淋到金属铁上,喷淋密度0.2~1.0m3/(m2·h)。In the above-mentioned method for removing nitrogen oxides from boiler flue gas, the reduction reaction temperature is 293K-323K, and the ferrous nitrosyl complex is sprayed onto metallic iron with a spray density of 0.2-1.0m3 /(m 2 ·h).
上述的锅炉烟气氮氧化物脱除的方法,所述的吸收器为筛板塔、旋流板塔、喷淋塔或鼓泡塔。In the above method for removing nitrogen oxides from boiler flue gas, the absorber is a sieve tray tower, a swirl tray tower, a spray tower or a bubble tower.
上述的锅炉烟气氮氧化物脱除的方法,所述的还原再生装置为铁屑填料床或铁粉搅拌釜。In the above method for removing nitrogen oxides from boiler flue gas, the reduction and regeneration device is a packed bed of iron filings or an iron powder stirring tank.
上述的锅炉烟气氮氧化物脱除的方法,所述的金属铁为铁粉或铁屑。In the above method for removing nitrogen oxides from boiler flue gas, the metal iron is iron powder or iron filings.
具体反应过程如下:Concrete reaction process is as follows:
烟气通入吸收液中,FeⅡEDTA络合吸收烟气中的NO:The flue gas is passed into the absorption liquid, and Fe Ⅱ EDTA complexes and absorbs NO in the flue gas:
FeⅡEDTA+NO→FeⅡ(NO)EDTAFe Ⅱ EDTA+NO→Fe Ⅱ (NO)EDTA
铁粉与亚铁亚硝酰络合物反应,使NO还原为NH3,同时实现FeⅡEDTA还原再生:Iron powder reacts with ferrous nitrosyl complex to reduce NO to NH 3 , and at the same time realize Fe Ⅱ EDTA reduction regeneration:
2FeⅡ(NO)EDTA+Fe+8H+→2FeⅡEDTA+Fe(OH)2+2NH3 2Fe Ⅱ (NO)EDTA+Fe+8H+→2Fe Ⅱ EDTA+Fe(OH) 2 +2NH 3
NH3在酸液中能够生成铵盐:NH 3 can generate ammonium salt in acid solution:
NH3+H+→NH4 + NH 3 +H + →NH 4 +
当烟气中存在氧气时,能够将FeⅡEDTA氧化为FeⅢEDTA而失去络合作用,铁粉的存在则能够解决这个问题:When there is oxygen in the flue gas, it can oxidize Fe Ⅱ EDTA to Fe Ⅲ EDTA and lose the complexation. The existence of iron powder can solve this problem:
FeⅡEDTA+O2→FeⅢEDTAFe Ⅱ EDTA+O 2 →Fe Ⅲ EDTA
Fe+Fe3+→Fe2+ Fe+Fe 3+ →Fe 2+
反应后的铁粉在溶液中的会形成Fe(OH)2水合物,在一定条件下能够生成Fe2O3作为铁红原料:The iron powder after the reaction will form Fe(OH) 2 hydrate in the solution, and Fe 2 O 3 can be generated as iron red raw material under certain conditions:
Fe(OH)2→Fe2O3+H2O。Fe(OH) 2 →Fe 2 O 3 +H 2 O.
本发明的有益效果在于:The beneficial effects of the present invention are:
(1)本发明采用液相络合法,以液相络合吸收剂脱除烟气中的NO,有效解决了NO难以进入液相的技术困难。(1) The present invention adopts the liquid phase complexation method to remove NO in the flue gas with the liquid phase complexation absorbent, which effectively solves the technical difficulty that NO is difficult to enter the liquid phase.
(2)本发明的络合吸收反应和还原再生反应在不同装置内分开进行,络合吸收反应生成的亚铁亚硝酰络合物单独引入还原再生装置,能够解决NH3吸收装置过于庞大的问题。(2) The complexation absorption reaction and the reduction regeneration reaction of the present invention are carried out separately in different devices, and the ferrous nitrosyl complex compound generated by the complexation absorption reaction is separately introduced into the reduction regeneration device, which can solve the problem that the NH absorption device is too large question.
(3)本发明所用络合吸收剂可以循环再生利用,反应后的产物能够综合再次利用,不会产生二次污染,工艺操作简单,脱硝效率高,易于工业化。(3) The complex absorbent used in the present invention can be recycled and reused, and the reacted product can be comprehensively reused without secondary pollution. The process is simple in operation, high in denitrification efficiency, and easy to industrialize.
(4)本发明的过程产物有较好的利用价值,产生的NH3通入酸液中可以生成铵盐作为工业原料,也可以作为还原剂进入SNCR脱硝反应器内,反应消耗的铁在溶液中会形成氧化铁的水合沉淀物,可作为铁红颜料等其他化工产品。(4) the process product of the present invention has better utilization value, the NH that produces Passes in the acid solution and can generate ammonium salt as industrial raw material, also can enter in the SNCR denitrification reactor as reductive agent, the iron that reaction consumes is in solution A hydrated precipitate of iron oxide will be formed in it, which can be used as iron red pigment and other chemical products.
附图说明Description of drawings
图1为本发明的流程框图。Fig. 1 is a flowchart of the present invention.
图2为本发明的实验装置与流程示意图:1、进气口,2、吸收塔,3、吸收循环槽,4、再生反应器,5、脱水器,6、出气口。Fig. 2 is the experimental device of the present invention and schematic flow chart: 1, air inlet, 2, absorption tower, 3, absorption circulation tank, 4, regeneration reactor, 5, dehydrator, 6, gas outlet.
具体实施方式detailed description
下面结合具体实施例对本发明做进一步详细说明,但本发明并不限于此。The present invention will be described in further detail below in conjunction with specific examples, but the present invention is not limited thereto.
实施例1Example 1
FeⅡEDTA络合吸收模拟烟气中NO:以直径100mm、高1200mm的筛板吸收塔作为吸收器,内置2层筛板,开孔率17%。模拟NO废气流量20m3/h,含NO500×10-6,吸收液FeⅡEDTA浓度为25mmol·L-1,循环量为80L/h,反应温度323K,络合液起始pH为5.5,NO脱除率为97%。再生装置以直径200mm、高400mm的铁屑填料床反应器,喷淋密度0.2m3/(m2·h),313K时再生出的5%的氨气用硫酸吸收得到硫酸铵,再生出的FeⅡEDTA溶液循环用于吸收,脱硝效率仍在97%左右。Fe Ⅱ EDTA complex absorption of NO in simulated flue gas: a sieve plate absorption tower with a diameter of 100 mm and a height of 1200 mm is used as the absorber, with two layers of sieve plates built in, and the opening rate is 17%. The simulated NO exhaust gas flow rate is 20m 3 /h, containing NO500×10 -6 , the concentration of Fe Ⅱ EDTA in the absorption solution is 25mmol·L -1 , the circulation volume is 80L/h, the reaction temperature is 323K, the initial pH of the complex solution is 5.5, and the NO The removal rate was 97%. The regeneration device uses iron filings packed bed reactor with a diameter of 200mm and a height of 400mm, a spray density of 0.2m 3 /(m 2 h), and 5% of the ammonia gas regenerated at 313K is absorbed by sulfuric acid to obtain ammonium sulfate, and the regenerated The Fe Ⅱ EDTA solution is recycled for absorption, and the denitrification efficiency is still about 97%.
实施例2Example 2
FeⅡEDTA络合吸收模拟烟气中NO:以直径100mm、高1200mm的筛板吸收塔作为吸收器,内置2层筛板,开孔率17%。模拟NO废气流量20m3/h,含NO400×10-6,吸收液FeⅡEDTA浓度为25mmol·L-1,循环量为80L/h,反应温度323K,络合液起始pH为5.5,NO脱除率为98%。再生装置以直径200mm、高400mm的铁屑填料床反应器,喷淋密度0.4m3/(m2·h),303K时再生出的5%的氨气用硫酸吸收得到硫酸铵,再生出的FeⅡEDTA溶液循环用于吸收,脱硝效率仍在98%左右。Fe Ⅱ EDTA complex absorption of NO in simulated flue gas: a sieve plate absorption tower with a diameter of 100 mm and a height of 1200 mm is used as the absorber, with two layers of sieve plates built in, and the opening rate is 17%. The simulated NO waste gas flow rate is 20m 3 /h, containing NO400×10 -6 , the concentration of Fe Ⅱ EDTA in the absorption solution is 25mmol·L -1 , the circulation volume is 80L/h, the reaction temperature is 323K, the initial pH of the complex solution is 5.5, and the NO The removal rate was 98%. The regeneration device uses iron filings packed bed reactor with a diameter of 200mm and a height of 400mm, a spray density of 0.4m 3 /(m 2 h), and 5% of the ammonia gas regenerated at 303K is absorbed by sulfuric acid to obtain ammonium sulfate, and the regenerated The Fe Ⅱ EDTA solution is recycled for absorption, and the denitrification efficiency is still about 98%.
实施例3Example 3
FeⅡEDTA络合吸收模拟烟气中NO:以直径100mm、高1200mm的筛板吸收塔作为吸收器,内置2层筛板,开孔率17%。模拟NO废气流量20m3/h,含NO500×10-6,吸收液FeⅡEDTA浓度为30mmol·L-1,循环量为100L/h,反应温度323K,络合液起始pH为6.0,NO脱除率为97%以上。再生装置以直径200mm、高400mm的铁屑填料床反应器,喷淋密度0.6m3/(m2·h),293K时再生出的5%的氨气用硫酸吸收得到硫酸铵,再生出的FeⅡEDTA溶液循环用于吸收,脱硝效率仍在96%左右。Fe Ⅱ EDTA complex absorption of NO in simulated flue gas: a sieve plate absorption tower with a diameter of 100 mm and a height of 1200 mm is used as the absorber, with two layers of sieve plates built in, and the opening rate is 17%. The simulated NO exhaust gas flow rate is 20m 3 /h, containing NO500×10 -6 , the concentration of Fe Ⅱ EDTA in the absorption solution is 30mmol·L -1 , the circulation volume is 100L/h, the reaction temperature is 323K, the initial pH of the complexing solution is 6.0, and the NO The removal rate is above 97%. The regeneration device uses iron filings packed bed reactor with a diameter of 200mm and a height of 400mm. The spray density is 0.6m 3 /(m 2 ·h). The Fe Ⅱ EDTA solution is recycled for absorption, and the denitrification efficiency is still about 96%.
实施例4Example 4
FeⅡEDTA络合吸收模拟烟气中NO:以直径100mm、高1200mm的筛板吸收塔作为吸收器,内置2层筛板,开孔率17%。模拟NO废气流量20m3/h,含NO500×10-6,吸收液FeⅡEDTA浓度为20mmol·L-1,循环量为60L/h,反应温度313K,络合液起始pH为6.0,NO脱除率为98%。再生装置以直径200mm、高400mm的铁粉搅拌釜反应器,搅拌转速60转/分,293K时再生出的5%的氨气用硫酸吸收得到硫酸铵,再生出的FeⅡEDTA溶液循环用于吸收,脱硝效率仍在97%左右。Fe Ⅱ EDTA complex absorption of NO in simulated flue gas: a sieve plate absorption tower with a diameter of 100 mm and a height of 1200 mm is used as the absorber, with two layers of sieve plates built in, and the opening rate is 17%. The simulated NO exhaust gas flow rate is 20m 3 /h, containing NO500×10 -6 , the concentration of Fe Ⅱ EDTA in the absorption solution is 20mmol·L -1 , the circulation volume is 60L/h, the reaction temperature is 313K, the initial pH of the complex solution is 6.0, and the NO The removal rate was 98%. The regeneration device uses iron powder stirred tank reactor with a diameter of 200mm and a height of 400mm, the stirring speed is 60 rpm, and the 5% ammonia gas regenerated at 293K is absorbed by sulfuric acid to obtain ammonium sulfate, and the regenerated Fe Ⅱ EDTA solution is recycled for use in Absorption and denitrification efficiency are still around 97%.
实施例5Example 5
FeⅡEDTA络合吸收模拟烟气中NO:以直径100mm、高1200mm的筛板吸收塔作为吸收器,内置2层筛板,开孔率17%。模拟NO废气流量20m3/h,含NO500×10-6,吸收液FeⅡEDTA浓度为20mmol·L-1,循环量为60L/h,反应温度323K,络合液起始pH为5.5,NO脱除率为98%。再生装置以直径200mm、高400mm的铁粉搅拌釜反应器,搅拌转速80转/分,313K时再生出的5%的氨气用硫酸吸收得到硫酸铵,再生出的FeⅡEDTA溶液循环用于吸收,脱硝效率仍在97%左右。Fe Ⅱ EDTA complex absorption of NO in simulated flue gas: a sieve plate absorption tower with a diameter of 100 mm and a height of 1200 mm is used as the absorber, with two layers of sieve plates built in, and the opening rate is 17%. The simulated NO waste gas flow rate is 20m 3 /h, containing NO500×10 -6 , the concentration of Fe Ⅱ EDTA in the absorption solution is 20mmol·L -1 , the circulation volume is 60L/h, the reaction temperature is 323K, the initial pH of the complex solution is 5.5, and the NO The removal rate was 98%. The regeneration device uses iron powder stirred tank reactor with a diameter of 200mm and a height of 400mm, the stirring speed is 80 rpm, and the 5% ammonia gas regenerated at 313K is absorbed by sulfuric acid to obtain ammonium sulfate, and the regenerated Fe Ⅱ EDTA solution is recycled for use in Absorption and denitrification efficiency are still around 97%.
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