技术领域technical field
本发明属于大气污染物治理技术领域，具体地说是涉及一种燃煤烟气三氧化硫脱除装置和方法。The invention belongs to the technical field of air pollutant control, and in particular relates to a device and method for removing sulfur trioxide from coal-fired flue gas.
背景技术Background technique
SO2和NOX是燃煤电厂烟气中主要的大气污染物之一，为了减少NOX的排放，燃煤电厂大多安装了SCR脱硝装置。SCR催化剂有可能使部分SO2催化氧化成SO3，加上炉内生成的SO3，使SO3达到一定浓度，对电厂造成危害，例如使催化剂中毒、空预器堵塞、烟道腐蚀等。静电除尘器和湿法脱硫塔对SO3的脱除能力有限，SO3的排放到大气中会使雾霾加重，造成环境污染。在燃用高硫煤时，SO3引起的问题更加严重。实现SO3的深度脱除，对电厂的安全经济运行和大气环境的改善意义重大。SO2 and NOX are one of the main air pollutants in the flue gas of coal-fired power plants. In order to reduce NOX emissions, most coal-fired power plants have installed SCR denitrification devices. The SCR catalyst may catalyze and oxidize part of SO2 to SO3 , and the SO3 generated in the furnace will make SO3 reach a certain concentration, which will cause harm to the power plant, such as catalyst poisoning, air preheater blockage, flue corrosion, etc. Electrostatic precipitators and wet desulfurization towers have limited ability to remove SO3 , and the discharge of SO3 into the atmosphere will aggravate smog and cause environmental pollution.The problem caused by SO3 is even more serious when burning high-sulfur coal. Realizing the deep removal of SO3 is of great significance to the safe and economical operation of the power plant and the improvement of the atmospheric environment.
为了减少SO3给电厂运行带来的危害以及控制SO3的排放，目前多采用向烟道中喷入碱性吸收剂的方法。中国专利CN103055684A公开了一种利用天然碱脱除烟气三氧化硫的装置及工艺，从SCR反应器出口烟气经天然碱浆液喷洗吸收SO3，再进入空气预热器；中国专利CN104857841A公开了一种脱除烟气中三氧化硫的装置，包括料仓、螺旋给料机，喷射枪，脱硝反应器和扰流板等，通过喷射强碱性物质吸收脱硝反应器前的SO3；中国专利CN104474897A公开了一种脱除燃煤烟气中三氧化硫的方法，向脱硝装置进口端之前的烟道内、脱硝装置出口端与空气预热器之间的烟道内的的烟气中喷射一定量的碱性颗粒，将烟气中的三氧化硫脱除。上述方法虽然可以一定程度控制SO3的排放，但是并不能有效应对不同烟气条件下的SO3脱除，不能很好的达到SO3超低排放的要求。In order to reduce the harm of SO3 to the operation of power plants and control the emission of SO3 , the method of spraying alkaline absorbent into the flue is mostly used at present. Chinese patent CN103055684A discloses a device and process for removing sulfur trioxide from flue gas by using trona. The flue gas from the outlet of the SCR reactor is sprayed with trona slurry to absorb SO3 , and then enters the air preheater; Chinese patent CN104857841A discloses A device for removing sulfur trioxide in flue gas is proposed, including a silo, a screw feeder, a spray gun, a denitration reactor and a spoiler, etc., and absorbs SO3 in front of the denitration reactor by spraying strong alkaline substances; Chinese patent CN104474897A discloses a method for removing sulfur trioxide in coal-fired flue gas, spraying it into the flue gas in the flue before the inlet end of the denitrification device, and in the flue gas between the outlet end of the denitrification device and the air preheater A certain amount of alkaline particles can remove sulfur trioxide in flue gas. Although the above method can control the emission of SO3 to a certain extent, it cannot effectively deal with the removal of SO3 under different flue gas conditions, and cannot well meet the requirements of ultra-low emission of SO3 .
发明内容Contents of the invention
针对燃煤烟气中SO3产生的问题，本发明提出一种适用于不同烟气条件的燃煤烟气三氧化硫脱除装置和方法。针对不同的燃煤电厂烟气条件的差异，根据烟气的温度、SO3浓度、气氛等条件，在不同烟道位置喷射碱性吸收剂，高效脱除烟气中的SO3，减少SO3对电厂设备的危害，达到SO3超低排放的要求。Aiming at the problem of SO3 generation in coal- fired flue gas, the present invention proposes a coal-fired flue gas sulfur trioxide removal device and method suitable for different flue gas conditions. In view of the differences in the flue gas conditions of different coal-fired power plants, according to the flue gas temperature, SO3 concentration, atmosphere and other conditions, spray alkaline absorbents at different flue positions to efficiently remove SO3 in the flue gas and reduce SO3 Harm to power plant equipment, meet the requirements of SO3 ultra-low emission.
一种燃煤烟气三氧化硫脱除装置，包括烟道，所述装置还包括顺次相连通的粗料仓、螺杆式给料机、空气分级磨、细料仓、失重式给料器、主管道、分离器和喷枪，所述喷枪设置在烟道内，喷枪的下游烟道内布置有静态混合器；所述主管道还通过空气干燥机与送风机相连通。A device for removing sulfur trioxide from coal-fired flue gas, including a flue, and the device also includes a sequentially connected coarse material bin, a screw feeder, an air classifying mill, a fine material bin, and a weightless feeder , a main pipe, a separator and a spray gun, the spray gun is arranged in the flue, and a static mixer is arranged in the downstream flue of the spray gun; the main pipe is also communicated with the blower through an air dryer.
本发明失重式给料机下部与主管道连接，送风机的空气经空气干燥机干燥后送入主管道，采用气力输送来自失重式给料机的碱性吸收剂；主管道终端与分离器连接，分离器将主管道均匀分为多个支路，每一支路连接一支喷枪；喷枪均匀布置在烟道截面上，并在喷枪的下游烟道安装静态混合器，保证喷枪喷射的碱性吸收剂与烟气均匀混合。根据不同的烟气条件及烟道位置，选择不同种类的碱性吸收剂，通过喷枪向烟道中喷射碱性吸收剂吸收烟气中的SO3，减少SO3对电厂运行的危害，实现SO3的超低排放。The lower part of the weightless feeder of the present invention is connected with the main pipeline, the air of the blower is sent into the main pipeline after being dried by the air dryer, and the alkaline absorbent from the weightless feeder is transported by pneumatic force; the terminal of the main pipeline is connected with the separator, The separator divides the main pipe evenly into multiple branches, and each branch is connected to a spray gun; the spray guns are evenly arranged on the flue section, and a static mixer is installed in the downstream flue of the spray gun to ensure the alkaline absorption of the spray gun spray The agent is evenly mixed with the flue gas. According to different flue gas conditions and flue positions, select different types of alkaline absorbents, spray alkaline absorbents into the flue through the spray gun to absorb SO3 in the flue gas, reduce the harm of SO3 to the operation of the power plant, and achieve SO3 ultra-low emissions.
作为优选，所述主管道通过分离器与若干个管道支路相连通，每个管道支路均分别与相应喷枪相连通。Preferably, the main pipeline communicates with several pipeline branches through a separator, and each pipeline branch communicates with a corresponding spray gun respectively.
作为优选，所述细料仓为密封装置，并且内装有干燥装置，防止碱性吸收剂因吸水造成的团聚、结垢、堵塞管道等；所述管道支路的数量为四个。Preferably, the fine material bin is a sealing device, and a drying device is installed inside to prevent the alkaline absorbent from agglomerating, scaling, and blocking pipelines caused by water absorption; the number of pipeline branches is four.
作为优选，碱性吸收剂喷入的位置为下述单个或多个位置：省煤器和SCR反应器之间、SCR反应器和空预器之间、空预器和除尘器之间、除尘器和脱硫塔之间。As a preference, the position where the alkaline absorbent is injected is the following single or multiple positions: between the economizer and the SCR reactor, between the SCR reactor and the air preheater, between the air preheater and the dust collector, between the dust removal Between the device and the desulfurization tower.
一种燃煤烟气三氧化硫脱除方法，包括下述步骤：A method for removing sulfur trioxide from coal-fired flue gas, comprising the steps of:
(1)选择不同的烟道位置，以及碱性吸收剂的种类、粒径；(1) Select different flue positions, as well as the type and particle size of the alkaline absorbent;
(2)系统运行时，在粗料仓中储存选定的固体颗粒碱性吸收剂，粗料仓底部与螺杆式给料机相连，利用螺杆式给料机将吸收剂送入空气分级磨，将吸收剂磨成所需的细度，再送入细料仓中备用；(2) When the system is running, the selected solid particle alkaline absorbent is stored in the coarse material bin, the bottom of the coarse material bin is connected with the screw feeder, and the absorbent is sent into the air classification mill by the screw feeder, Grind the absorbent to the required fineness, and then send it to the fine material bin for standby;
(3)细料仓与失重式给料器连接，利用失重式给料器控制给料速率；(3) The fine material bin is connected with the weightless feeder, and the feeding rate is controlled by the weightless feeder;
(4)失重式给料器下部连接输送碱性吸收剂的主管道，采用气力输送的方式在输气管道中输送来自失重式给料器的细碱性吸收剂颗粒，送风机产生的风先经过空气干燥机干燥，以防止吸收剂颗粒吸水团聚、堵塞管道；(4) The lower part of the loss-in-weight feeder is connected to the main pipeline for transporting alkaline absorbent, and the fine alkaline absorbent particles from the loss-in-weight feeder are transported in the air pipeline by means of pneumatic conveying, and the wind generated by the blower first passes through Dry in an air dryer to prevent absorbent particles from agglomerating and clogging pipes;
(5)主管道的细吸收剂颗粒先送至分离器，利用分离器分为多个支路，每个支路均与相应喷枪相连接，喷枪均匀布置在烟道截面上，碱性吸收剂颗粒从喷枪喷出；(5) The fine absorbent particles in the main pipeline are first sent to the separator, which is divided into multiple branches by the separator, each branch is connected with the corresponding spray gun, and the spray gun is evenly arranged on the flue section, and the alkaline absorbent Particles are ejected from the spray gun;
(6)在喷枪的下游烟道内布置静态混合器，保证碱性吸收剂颗粒与烟气均匀混合；(6) Arrange a static mixer in the downstream flue of the spray gun to ensure that the alkaline absorbent particles are evenly mixed with the flue gas;
(7)SO3被碱性吸收剂颗粒吸收形成硫酸盐而被除去，反应产物和未反应的颗粒物通过下游的颗粒物脱除装置脱除。(7) SO3 is absorbed by the alkaline absorbent particles to form sulfate and removed, and the reaction products and unreacted particles are removed through the downstream particle removal device.
本发明基于烟气的特性，选择不同的烟道位置，利用该装置向烟道内喷射一定量及细度的碱性吸收剂颗粒，SO3与碱性吸收剂颗粒反应而被脱除，烟气中的颗粒通过下游的颗粒脱除设备脱除。The present invention selects different flue positions based on the characteristics of the flue gas, and uses the device to spray a certain amount and finenessof alkaline absorbent particles into the flue, so that SO3 reacts with the alkaline absorbent particles and is removed, and the flue gas Particles in are removed by downstream particle removal equipment.
作为优选，步骤(2)中，粗料仓中的固体碱性吸收剂颗粒为钙基类碱性吸收剂颗粒(CaO，Ca(OH)2，CaCO3等)、镁基类碱性吸收剂颗粒(MgO，Mg(OH)2，MgCO3镁等)、或钠基类碱性吸收剂颗粒(Na2CO3，NaHCO3，天然碱等)；所述固体碱性吸收剂颗粒与烟气中SO3的摩尔比为0.5：1～30：1之间，粗料仓中固体碱性吸收剂颗粒的粒径为1cm以下；空气分级磨将固体碱性吸收剂颗粒磨至10μm～100μm之间，进一步的，吸收剂磨至40～60μm。Preferably, in step (2), the solid alkaline absorbent particles in the coarse silo are calcium-based alkaline absorbent particles (CaO, Ca(OH)2 , CaCO3 , etc.), magnesium-based alkaline absorbent particles particles (MgO, Mg(OH)2 , MgCO3 magnesium, etc.), or sodium-based alkaline absorbent particles (Na2 CO3 , NaHCO3 , trona, etc.); the solid alkaline absorbent particles and smoke The molar ratio of SO3 in the medium is between 0.5:1 and 30:1, and the particle size of the solid alkaline absorbent particles in the coarse hopper is below 1cm; the air classification mill grinds the solid alkaline absorbent particles to between 10 μm and 100 μm In the meantime, further, the absorbent is ground to 40-60 μm.
作为优选，步骤(4)中，气力输送时，控制固气比为0.1～25：1，流速为18～30m/s，气体压力为0.5～1Mpa。Preferably, in step (4), during pneumatic conveying, the solid-gas ratio is controlled to be 0.1-25:1, the flow velocity is 18-30 m/s, and the gas pressure is 0.5-1 Mpa.
作为优选，步骤(5)中，碱性吸收剂的喷射采用一级或多级喷射，每两级喷射装置之前的距离为5～15m。As a preference, in step (5), the spraying of the alkaline absorbent adopts one or more stages of spraying, and the distance before each two-stage spraying device is 5-15 m.
作为优选，碱性吸收剂喷入的位置包括下述单个或多个位置：省煤器与SCR反应器之间的烟道、SCR反应器与空预器之间的烟道、空预器与除尘器之间的烟道、除尘器与脱硫塔之间的烟道；在不同的吸收剂喷射位置，烟气的温度在100℃～450℃之间，SO3的浓度在10ppm～100ppm之间，碱性吸收剂在烟道中的停留时间为0.01s～4s。Preferably, the position where the alkaline absorbent is injected includes the following single or multiple positions: the flue between the economizer and the SCR reactor, the flue between the SCR reactor and the air preheater, the air preheater and the air preheater The flue between the dust collector, the flue between the dust collector and the desulfurization tower; at different absorbent injection positions, the temperature of the flue gas is between 100°C and 450°C, and the concentration of SO3 is between 10ppm and 100ppm , The residence time of the alkaline absorbent in the flue is 0.01s to 4s.
在省煤器与SCR反应器之间的烟道，选择喷射钠基类吸收剂(Na2CO3，NaHCO3，天然碱等)；在SCR反应器与空预器之间的烟道，选择喷射镁基类吸收剂(MgO，Mg(OH)2，MgCO3镁等)；在空预器与除尘器之间的烟道，及除尘器与脱硫塔之间的烟道，选择喷射钙基类吸收剂(CaO，Ca(OH)2，CaCO3等)。燃用高硫煤时，在省煤器和SCR反应器之间的烟道中喷入碱性吸收剂脱除SO3，减少SO3对催化剂的危害；当SCR催化剂的SO2/SO3转化率较高时，在SCR反应器与空预器之间的烟道中喷入碱性吸收剂脱除SO3，减少硫酸氢氨的生成对空预器的危害；当主要目的是为了减少SO3的排放和对电厂设备的腐蚀时，在除尘器前后的烟道中喷入碱性吸收剂脱除SO3。In the flue between the economizer and the SCR reactor, choose to inject sodium-based absorbents (Na2 CO3 , NaHCO3 , trona, etc.); in the flue between the SCR reactor and the air preheater, choose Spray magnesium-based absorbents (MgO, Mg(OH)2 , MgCO3 magnesium, etc.); in the flue between the air preheater and the dust collector, and between the dust collector and the desulfurization tower, choose to spray calcium-based Absorbents (CaO, Ca(OH)2 , CaCO3 etc.). When burning high-sulfur coal, inject alkaline absorbent into the flue between the economizer and the SCR reactor to remove SO3 and reduce the damage of SO3 to the catalyst; when the conversion rate of SO2 /SO3 of the SCR catalyst When it is higher, spray alkaline absorbent into the flue between the SCR reactor and the air preheater to remove SO3 , and reduce the harm of the formation of ammonium bisulfate to the air preheater; when the main purpose is to reduce the SO3 When discharging and corroding power plant equipment, spray alkaline absorbent into the flue before and after the dust collector to remove SO3 .
作为优选，所述的燃煤烟气三氧化硫脱除方法，包括下述步骤：Preferably, the method for removing sulfur trioxide from coal-fired flue gas comprises the following steps:
(1)烟道位置位于省煤器和SCR反应器之间，烟气温度400℃，SO3浓度25ppm；天然碱作为吸收剂，天然碱平均粒径为2mm；(1) The flue is located between the economizer and the SCR reactor, the flue gas temperature is 400°C, and the SO3 concentration is 25ppm; trona is used as an absorbent, and the average particle size of trona is 2mm;
(2)系统运行时，在粗料仓中储存天然碱，粗料仓底部与螺杆式给料机相连，利用螺杆式给料机将粗颗粒的天然碱送入空气分级磨，将天然碱磨至平均粒径40μm，再送入细料仓中备用，细料仓为密封装置，并设有干燥装置；(2) When the system is running, trona is stored in the coarse material bin, and the bottom of the coarse material bin is connected with the screw feeder, and the trona with coarse particles is sent into the air classification mill by the screw feeder, and the trona is milled The average particle size is 40 μm, and then sent to the fine material bin for standby, the fine material bin is a sealed device and is equipped with a drying device;
(3)细料仓与失重式给料器连接，利用失重式给料器控制给料速率，达到天然碱与SO3的摩尔比为2：1；(3) The fine material bin is connected with the weightless feeder, and the feeding rate is controlled by the weightless feeder, so that the molar ratio of trona to SO is2 :1;
(4)失重式给料器下部连接输送碱性吸收剂的主管道，采用气力输送的方式在输气管道中输送来自失重式给料器的细天然碱颗粒，送风机产生的风先经过空气干燥机干燥；(4) The lower part of the weightless feeder is connected to the main pipeline for transporting alkaline absorbent, and the fine trona particles from the weightless feeder are transported in the air pipeline by means of pneumatic conveying, and the wind generated by the blower is first air-dried machine drying;
(5)主管道的细天然碱颗粒先送至分离器，利用分离器分为四个支路，每个支路均与相应喷枪相连接，喷枪均匀布置在烟道截面上，碱性吸收剂颗粒从喷枪喷出，与烟气顺向流动；(5) The fine trona particles in the main pipeline are first sent to the separator, which is divided into four branches by the separator, each branch is connected with the corresponding spray gun, and the spray gun is evenly arranged on the flue section, and the alkaline absorbent The particles are ejected from the spray gun and flow in the same direction as the flue gas;
(6)在喷枪的下游烟道内布置静态混合器；(6) Arrange a static mixer in the downstream flue of the spray gun;
(7)SO3被碱性吸收剂颗粒吸收形成硫酸盐而被除去，反应产物和未反应的颗粒物通过下游的颗粒物脱除装置脱除。(7) SO3 is absorbed by the alkaline absorbent particles to form sulfate and removed, and the reaction products and unreacted particles are removed through the downstream particle removal device.
本发明的有益效果在于：The beneficial effects of the present invention are:
(1)分离器将主管道均匀分为多个支路，每一支路连接一支喷枪；喷枪均匀布置在烟道截面上，并在喷枪的下游烟道安装静态混合器，保证喷枪喷射的碱性吸收剂与烟气均匀混合；(1) The separator divides the main pipe evenly into multiple branches, and each branch is connected to a spray gun; the spray guns are evenly arranged on the flue section, and a static mixer is installed in the downstream flue of the spray gun to ensure the spraying of the spray gun The alkaline absorbent is evenly mixed with the flue gas;
(2)根据不同的烟气条件及烟道位置，选择合适的碱性吸收剂，通过脱除特定烟道位置处的SO3，有效防止脱硝催化剂和空预器的堵塞，减少SO3对电厂运行的危害，并实现SO3的超低排放。(2) According to different flue gas conditions and flue positions, select the appropriate alkaline absorbent, by removing SO3 at specific flue positions, effectively prevent the blockage of the denitrification catalyst and air preheater, and reduce the impact of SO3 on the power plant operating hazards, and achieve ultra-low emissions of SO3 .
说明书附图Instructions attached
图1为本发明燃煤烟气三氧化硫脱除装置结构示意图；Fig. 1 is the structural representation of the device for removing sulfur trioxide from coal-fired flue gas of the present invention;
1-粗料仓、2-螺杆式给料机、3-空气分级磨、4-细料仓、5-失重式给料器、6-送风机、7-空气干燥机、8-主管道、9-分离器、10-管道支路、11-喷枪、12-静态混合器、13-烟道。1-coarse silo, 2-screw feeder, 3-air classification mill, 4-fine silo, 5-loss-in-weight feeder, 6-blower, 7-air dryer, 8-main pipe, 9 - separator, 10 - pipe branch, 11 - spray gun, 12 - static mixer, 13 - flue.
具体实施方式detailed description
下面结合附图和具体实施例对本发明作进一步说明，但本发明所要保护的范围并不限于此。The present invention will be further described below in conjunction with the accompanying drawings and specific embodiments, but the scope of protection of the present invention is not limited thereto.
实施例1Example 1
参照图1，一种燃煤烟气三氧化硫脱除装置，包括烟道13，所述装置还包括顺次相连通的粗料仓1、螺杆式给料机2、空气分级磨3、细料仓4、失重式给料器5、主管道8、分离器9和喷枪11，所述喷枪11设置在烟道13内，喷枪11的下游烟道内布置有静态混合器12；所述主管道8还通过空气干燥机7与送风机6相连通。With reference to Fig. 1, a kind of coal-fired flue gas sulfur trioxide removal device comprises flue 13, and described device also comprises the coarse stock bin 1 that is connected in sequence, screw type feeder 2, air classification mill 3, fine Stock bin 4, loss-in-weight feeder 5, main pipeline 8, separator 9 and spray gun 11, described spray gun 11 is arranged in the flue 13, and static mixer 12 is arranged in the downstream flue of spray gun 11; Said main pipeline 8 is also communicated with blower 6 through air dryer 7 .
所述主管道8通过分离器9与若干个管道支路10相连通，每个管道支路均分别与相应喷枪11相连通；所述管道支路的数量为四个。所述细料仓为密封装置，并且内装有干燥装置，防止碱性吸收剂因吸水造成的团聚、结垢、堵塞管道等。The main pipeline 8 communicates with several pipeline branches 10 through a separator 9, and each pipeline branch communicates with a corresponding spray gun 11; the number of the pipeline branches is four. The fine material bin is a sealing device, and is equipped with a drying device to prevent the alkaline absorbent from agglomerating, scaling, and blocking the pipeline due to water absorption.
碱性吸收剂喷入的位置为下述单个或多个位置：省煤器和SCR反应器之间、SCR反应器和空预器之间、空预器和除尘器之间、除尘器和脱硫塔之间。燃用高硫煤时，在省煤器和SCR反应器之间的烟道中喷入碱性吸收剂脱除SO3，减少SO3对催化剂的危害；当SCR催化剂的SO2/SO3转化率较高时，在SCR反应器与空预器之间的烟道中喷入碱性吸收剂脱除SO3，减少硫酸氢氨的生成对空预器的危害；当主要目的是为了减少SO3的排放和对电厂设备的腐蚀时，在除尘器前后的烟道中喷入碱性吸收剂脱除SO3。The location where the alkaline absorbent is injected is the following single or multiple locations: between the economizer and the SCR reactor, between the SCR reactor and the air preheater, between the air preheater and the dust collector, between the dust collector and the desulfurization between the towers. When burning high-sulfur coal, inject alkaline absorbent into the flue between the economizer and the SCR reactor to remove SO3 and reduce the damage of SO3 to the catalyst; when the conversion rate of SO2 /SO3 of the SCR catalyst When it is higher, spray alkaline absorbent into the flue between the SCR reactor and the air preheater to remove SO3 , and reduce the harm of the formation of ammonium bisulfate to the air preheater; when the main purpose is to reduce the SO3 When discharging and corroding power plant equipment, spray alkaline absorbent into the flue before and after the dust collector to remove SO3 .
实施例2Example 2
脱除SCR前烟道中的SO3，烟道位置位于省煤器和SCR反应器之间。烟气温度400℃，SO3浓度25ppm。根据该处的烟气条件，选择天然碱(Na2CO3·NaHCO3·2H2O)作为吸收剂，天然碱与SO3的摩尔比为2∶1。天然碱粗料平均粒径为2mm，细料平均粒径确定为40μm，碱性吸收剂在烟道中的停留时间为2s。To remove SO3 in the flue before SCR, the flue is located between the economizer and the SCR reactor. The flue gas temperature is 400°C, and the SO3 concentration is 25ppm. According to the flue gas conditions there, choose trona (Na2 CO3 ·NaHCO3 ·2H2 O) as the absorbent, and the molar ratio of trona to SO3 is 2:1. The average particle size of the trona coarse material is 2mm, the average particle size of the fine material is determined to be 40μm, and the residence time of the alkaline absorbent in the flue is 2s.
如图1所示，系统运行时，在粗料仓1中储存大量的天然碱粗料，平均粒径为2mm。粗料仓1底部与螺杆式给料机2相连；利用螺杆式给料机2将粗颗粒的天然碱送入空气分级磨3，将天然碱磨至平均粒径40μm，再送入细料仓4中备用，细料仓为密封装置，并设有干燥装置，防止碱性吸收剂因吸水造成的团聚、结垢、堵塞管道等；细料仓4与失重式给料器5连接，利用失重式给料器5控制给料速率，达到天然碱与SO3的摩尔比为2：1；失重式给料器5下部连接输送吸收剂的主管道8；在主管道8中采用气力输送的方式输送来自失重式给料器5的细天然碱颗粒，流速控制为22m/s，气体压力为0.8Mpa；送风机6产生的风先经过空气干燥器7干燥，以防止天然碱颗粒吸水团聚、堵塞管道；主管道8的细天然碱颗粒先送至分离器9，利用分离器9分为四个管道支路10，每个管道支路均与相应喷枪11连接；碱性吸收剂颗粒从喷枪11喷出，与烟气顺向流动；在喷枪的下游烟道内布置静态混合器12，保证碱性吸收剂和烟气均匀混合，碱性吸收剂颗粒与烟气中的SO3反应后形成硫酸盐而被脱除。As shown in Figure 1, when the system is running, a large amount of trona coarse material is stored in the coarse material bin 1, with an average particle size of 2 mm. The bottom of the coarse material bin 1 is connected with the screw feeder 2; the trona with coarse particles is sent to the air classification mill 3 by the screw feeder 2, and the trona is ground to an average particle size of 40 μm, and then sent into the fine material bin 4 The fine material bin is a sealed device and is equipped with a drying device to prevent the alkaline absorbent from agglomerating, scaling, and blocking pipes due to water absorption; the fine material bin 4 is connected to the weightless feeder 5, and the weightless The feeder 5 controls the feed rate to achieve a molar ratio of trona to SO3 of 2:1; the lower part of the weightless feeder 5 is connected to the main pipeline 8 for conveying the absorbent; the main pipeline 8 is transported by pneumatic conveying From the fine trona granule of loss-in-weight type feeder 5, flow velocity control is 22m/s, and gas pressure is 0.8Mpa; The wind that air blower 6 produces is first dried through air drier 7, to prevent the trona granule from absorbing water and agglomerating, clogging pipeline; The fine trona particles in the main pipeline 8 are first sent to the separator 9, and are divided into four pipeline branches 10 by the separator 9, and each pipeline branch is connected with a corresponding spray gun 11; the alkaline absorbent particles are sprayed from the spray gun 11 , flowing in the same direction as the flue gas; a static mixer 12 is arranged in the downstream flue of the spray gun to ensure that the alkaline absorbent and the flue gas are evenly mixed, and the alkaline absorbent particles react with SO in the flue gas to form sulfate and be remove.
在设计工况条件下，可以保证SO3的脱除效率90％，同时由于喷入的天然碱占烟气飞灰总量质量比小于0.5％，因此不会对下游的SCR催化剂产生较大影响。Under the design working conditions, the removal efficiency of SO3 can be guaranteed to be 90%. At the same time, since the injected trona accounts for less than 0.5% of the total mass ratio of flue gas fly ash, it will not have a great impact on the downstream SCR catalyst. .
实施例3Example 3
本实施例与实施例2的区别在于脱除空预器前烟道中的SO3，烟道位置位于SCR反应器和空预器之间。烟气温度250℃，SO3浓度40ppm。根据该处的烟气条件，选择Mg(OH)2作为吸收剂，Mg(OH)2与SO3摩尔比为4：1。Mg(OH)2粗料粒径为3mm，细料平均粒径确定为60μm，碱性吸收剂在烟道中的停留时间为1s。The difference between this example and Example 2 is that SO3 in the flue before the air preheater is removed, and the flue is located between the SCR reactor and the air preheater. The flue gas temperature is 250°C, and the SO3 concentration is 40ppm. According to the flue gas conditions here, Mg(OH)2 is selected as the absorbent, and the molar ratio of Mg(OH)2 to SO3 is 4:1. The particle size of Mg(OH)2 coarse material is 3mm, the average particle size of fine material is determined to be 60μm, and the residence time of alkaline absorbent in the flue is 1s.
在设计工况条件下，可以保证SO3的脱除效率84％。有效预防了空预器的堵塞和腐蚀。Under the design working conditions, the removal efficiency of SO3 can be guaranteed to be 84%. Effectively prevent the clogging and corrosion of the air preheater.
实施例4Example 4
本实施例与实施例2的区别在于脱除除尘器前烟道中的SO3，烟道位置位于SCR空预器和除尘器之间。烟气温度150℃，SO3浓度30ppm。根据该处的烟气条件，选择Ca(OH)2作为吸收剂，Ca(OH)2与SO3摩尔比为6：1。Ca(OH)2粗料平均粒径为4mm，细料平均粒径确定为50μm，碱性吸收剂在烟道中的停留时间为4s。The difference between this embodiment and embodiment 2 is that the SO3 in the flue before the dust collector is removed, and the flue is located between the SCR air preheater and the dust collector. The flue gas temperature is 150°C, and the SO3 concentration is 30ppm. According to the flue gas conditions here, Ca(OH)2 is selected as the absorbent, and the molar ratio of Ca(OH)2 to SO3 is6 :1. The average particle size of the Ca(OH)2 coarse material is 4 mm, the average particle size of the fine material is determined to be 50 μm, and the residence time of the alkaline absorbent in the flue is 4 s.
在设计工况条件下，可以保证SO3的脱除效率85％。有效预防了除尘器和下游设备的腐蚀。Under the design working conditions, the removal efficiency of SO3 can be guaranteed to be 85%. Effectively prevent the corrosion of the dust collector and downstream equipment.
实施例5Example 5
本实施例与实施例2的区别在于脱除脱硫塔前烟道中的SO3，烟道位置位于SCR除尘器和脱硫塔之间。烟气温度90℃，SO3浓度15ppm。根据该处的烟气条件，选择Ca(OH)2作为吸收剂，Ca(OH)2与SO3摩尔比为3：1。Ca(OH)2粗料平均粒径为4mm，细料平均粒径确定为40μm。The difference between this embodiment and embodiment 2 is that the SO3 in the flue before the desulfurization tower is removed, and the flue is located between the SCR dust collector and the desulfurization tower. The flue gas temperature is 90°C, and the SO3 concentration is 15ppm. According to the flue gas conditions here, Ca(OH)2 is selected as the absorbent, and the molar ratio of Ca(OH)2 to SO3 is3 :1. The average particle size of the Ca(OH)2 coarse material is 4 mm, and the average particle size of the fine material is determined to be 40 μm.
在设计工况条件下，可以保证SO3的脱除效率80％。有效预防了脱硫塔的腐蚀和可见烟羽的产生。Under the design working conditions, the removal efficiency of SO3 can be guaranteed to be 80%. Effectively prevent the corrosion of the desulfurization tower and the generation of visible plume.
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201610901106.8ACN106345244A (en) | 2016-10-17 | 2016-10-17 | Device and method for removing sulfur trioxide from coal-fired flue gas |
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201610901106.8ACN106345244A (en) | 2016-10-17 | 2016-10-17 | Device and method for removing sulfur trioxide from coal-fired flue gas |
| Publication Number | Publication Date |
|---|---|
| CN106345244Atrue CN106345244A (en) | 2017-01-25 |
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201610901106.8APendingCN106345244A (en) | 2016-10-17 | 2016-10-17 | Device and method for removing sulfur trioxide from coal-fired flue gas |
| Country | Link |
|---|---|
| CN (1) | CN106345244A (en) |
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| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| RJ01 | Rejection of invention patent application after publication | Application publication date:20170125 | |
| RJ01 | Rejection of invention patent application after publication |