WO2020191915A1 - 一种水泥窑烟气脱硝脱汞脱硫系统及方法 - Google Patents

一种水泥窑烟气脱硝脱汞脱硫系统及方法 Download PDF

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WO2020191915A1
WO2020191915A1 PCT/CN2019/088673 CN2019088673W WO2020191915A1 WO 2020191915 A1 WO2020191915 A1 WO 2020191915A1 CN 2019088673 W CN2019088673 W CN 2019088673W WO 2020191915 A1 WO2020191915 A1 WO 2020191915A1
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flue gas
denitration
mercury removal
mercury
cement kiln
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PCT/CN2019/088673
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English (en)
French (fr)
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刘猛
桑圣欢
康宇
李安平
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南京凯盛国际工程有限公司
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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D46/00—Filters or filtering processes specially modified for separating dispersed particles from gases or vapours
    • B01D46/02—Particle separators, e.g. dust precipitators, having hollow filters made of flexible material
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D46/00—Filters or filtering processes specially modified for separating dispersed particles from gases or vapours
    • B01D46/42—Auxiliary equipment or operation thereof
    • B01D46/44—Auxiliary equipment or operation thereof controlling filtration
    • B01D46/442—Auxiliary equipment or operation thereof controlling filtration by measuring the concentration of particles
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/02—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography
    • B01D53/06—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography with moving adsorbents, e.g. rotating beds
    • B01D53/10—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography with moving adsorbents, e.g. rotating beds with dispersed adsorbents
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
    • B01D53/77—Liquid phase processes
    • B01D53/78—Liquid phase processes with gas-liquid contact
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
    • B01D53/86—Catalytic processes
    • B01D53/8621—Removing nitrogen compounds
    • B01D53/8625—Nitrogen oxides
    • B01D53/8628—Processes characterised by a specific catalyst
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
    • B01D53/86—Catalytic processes
    • B01D53/8665—Removing heavy metals or compounds thereof, e.g. mercury
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES 
    • F23J15/00—Arrangements of devices for treating smoke or fumes
    • F23J15/02—Arrangements of devices for treating smoke or fumes of purifiers, e.g. for removing noxious material
    • F23J15/022—Arrangements of devices for treating smoke or fumes of purifiers, e.g. for removing noxious material for removing solid particulate material from the gasflow
    • F23J15/025—Arrangements of devices for treating smoke or fumes of purifiers, e.g. for removing noxious material for removing solid particulate material from the gasflow using filters
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES 
    • F23J15/00—Arrangements of devices for treating smoke or fumes
    • F23J15/02—Arrangements of devices for treating smoke or fumes of purifiers, e.g. for removing noxious material
    • F23J15/04—Arrangements of devices for treating smoke or fumes of purifiers, e.g. for removing noxious material using washing fluids
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES 
    • F23J15/00—Arrangements of devices for treating smoke or fumes
    • F23J15/08—Arrangements of devices for treating smoke or fumes of heaters
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2251/00—Reactants
    • B01D2251/20—Reductants
    • B01D2251/206—Ammonium compounds
    • B01D2251/2062—Ammonia
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2257/00—Components to be removed
    • B01D2257/30—Sulfur compounds
    • B01D2257/302—Sulfur oxides
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2257/00—Components to be removed
    • B01D2257/60—Heavy metals or heavy metal compounds
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2258/00—Sources of waste gases
    • B01D2258/02—Other waste gases
    • B01D2258/0283—Flue gases

Definitions

  • the invention relates to the technical field of cement kiln flue gas treatment, in particular to a cement kiln flue gas denitration and mercury desulfurization system and method.
  • the "Cement Industry Development Plan” proposes to strengthen technological innovation, implement innovation drive, and encourage the research and development of flue gas deep desulfurization, denitrification and integrated collaborative control technology and equipment.
  • the "Cement Industry Air Pollutant Emission Standard” stipulates that the emission standard of NOx in key areas is 320mg/Nm 3 , the emission standard of SO 2 is 100mg/Nm 3 , and the emission standard of Hg and its compounds is 50 ⁇ g/Nm 3 .
  • Jiangsu Republic has made it clear that on the basis of achieving up-to-standard emissions from non-electric industries, it will vigorously promote the deep reduction of nitrogen oxides in coking, steel, cement, glass and other industries, and the NOx emission concentration of cement kiln flue gas will not exceed 100mg/Nm 3 ; Henan province encourages Cement enterprises carry out ultra-low emission transformation, and after the transformation, the emission concentration of sulfur dioxide and nitrogen oxide should not be higher than 50mg/Nm 3 and 100mg/Nm 3 respectively .
  • the sulfur dioxide in the flue gas of the cement industry mainly comes from the sulfide, sulfate in the raw materials and the sulfur in the fuel. Because the calcium oxide in the raw meal can remove most of the sulfur dioxide, the SO 2 concentration in the tail flue gas is low, and it is generally emitted. The concentration is 30-100mg/Nm 3 .
  • the use of low-cost and secondary pollution-free desulfurization technology has become an indispensable method for deep emission reduction of flue gas in the cement industry.
  • Cement kilns can use the following measures to control mercury emissions: reduce the temperature of cement kiln flue gas, but currently cement kiln tail gas is widely used for waste heat power generation and raw meal drying, and kiln tail gas temperature cannot be greatly reduced; activated carbon/activated coke adsorption The cost of this method is high, and the adsorbed activated carbon/activated coke is difficult to reuse; wet desulfurization has both mercury removal functions, but wet desulfurization has secondary pollution problems.
  • the present invention provides a cement kiln flue gas denitrification and mercury removal desulfurization system and method that is easy to operate and efficient in operation, and realizes ultra-low emission of NOx, SO 2 and Hg in cement kiln flue gas.
  • the present invention first provides a cement kiln flue gas denitration and mercury removal desulfurization system, which includes a kiln tail preheater, a high temperature fan, a denitration and mercury removal device containing a denitration and mercury removal catalyst, a raw material mill, a dust collector, A tail exhaust fan and a chimney; the connecting air pipe between the high temperature fan and the denitration and mercury removal device is provided with an ammonia application device, and the connection between the denitration and mercury removal device and the raw material mill is provided with a desulfurization agent injection device.
  • the desulfurizer injection device is connected with the desulfurizer powder bin.
  • a waste heat boiler is provided between the kiln tail preheater and the high temperature fan.
  • the denitration and mercury removal device is provided with an ash removal device for purging ash on the surface of the catalyst.
  • the present invention also provides a cement kiln flue gas denitration and mercury desulfurization method based on the above system, which includes the following steps:
  • Step 1 The flue gas from the kiln tail preheater passes through the waste heat boiler and the high-temperature fan in sequence, and then enters the denitration and mercury removal device containing the denitration and mercury removal catalyst. At the same time, ammonia water is sprayed into the inlet air pipe of the denitration and mercury removal device. Make the flue gas denitrify and oxidize mercury in the denitrification and mercury removal device;
  • Step 2 The flue gas treated by the desulfurization and denitrification device enters the raw material mill through the connecting air pipe, and at the same time, a desulfurizing agent is sprayed into the connecting air pipe to reduce sulfur dioxide in the flue gas and perform mercury adsorption;
  • Step 3 The flue gas entering the raw material mill is used to dry the cement raw materials.
  • the flue gas at the outlet of the raw material mill enters the bag filter to remove the dust and desulfurizer in the flue gas.
  • the clean flue gas after dust removal passes through the tail exhaust.
  • the fan is discharged after entering the chimney.
  • the outlet flue gas temperature of the kiln tail preheater is 280-350°C, and the dust concentration is 80-100 g/Nm 3 .
  • the outlet flue gas temperature of the high-temperature fan in step 1 is 150-250°C, and the dust concentration is 60-80 g/Nm 3 .
  • the mass concentration of the ammonia water sprayed in step 1 is 10-30%, and the flow rate is 0.1-1 m 3 /h.
  • the particle size of the desulfurizing agent in the desulfurizing agent powder bin is ⁇ 50 ⁇ m.
  • the present invention is convenient to operate, has high removal efficiency of NOx, Hg and SO 2 in the kiln tail flue gas, and the system has a small footprint and low equipment investment cost. Effective means for ultra-low SO 2 and Hg emissions.
  • Fig. 1 is a schematic structural diagram of a cement kiln flue gas denitration and mercury removal desulfurization system according to an embodiment of the present invention.
  • a preferred embodiment of the present invention provides a cement kiln flue gas denitration and mercury removal desulfurization system, including a kiln tail preheater system 1, a high temperature fan 3, and a denitration and mercury removal catalyst containing denitration and mercury removal catalysts connected in sequence Device 5, raw material mill 9, dust collector 10, tail exhaust fan 11 and chimney 12; the connecting air pipe between the high temperature fan 3 and the denitration and mercury removal device 5 (near the denitration and mercury removal device 5) is provided Ammonia water application device 4, the connecting air pipe 8 between the denitrification and mercury removal device 5 and the raw material mill 9 is provided with a desulfurizing agent injection device 7 which is connected to the desulfurizing agent powder bin 6.
  • a waste heat boiler 2 is provided between the kiln tail preheater 1 and the high-temperature fan 3, and the main function of the waste heat boiler 2 is to recover the high temperature flue gas from the kiln tail preheater to a certain extent. Increase the utilization rate of flue gas heat energy.
  • the denitrification and mercury removal device is equipped with an ash removal device, which is used for purging the ash accumulation on the catalyst surface (the catalyst is porous, and the surface includes the inner surface and the outer surface) to prevent dust from clogging the catalyst.
  • the ash removal device may be a compressed air type ash removal device.
  • This embodiment 2 provides a cement kiln flue gas denitration and mercury removal method based on the system described in embodiment 1, including the following steps:
  • Step 1 The flue gas from the kiln tail preheater (the flue gas temperature is 280 ⁇ 350°C, the dust concentration is 80 ⁇ 100g/Nm 3 ) is passed through the waste heat boiler, and the flue gas after heat recovery and utilization through the waste heat boiler is passed through the high temperature fan Then enter the denitration and mercury removal device containing the denitration and mercury removal catalyst (the temperature of the flue gas at the outlet of the high-temperature fan is 150-250°C, and the dust concentration is 60-80g/Nm 3 ), and spray at the inlet duct of the denitration and mercury removal device.
  • the denitration and mercury removal device the temperature of the flue gas at the outlet of the high-temperature fan is 150-250°C, and the dust concentration is 60-80g/Nm 3
  • ammonia water (the mass concentration of the injected ammonia water is 10-30%, the flow rate is 0.1-1m 3 /h), so that the flue gas is denitrified and mercury oxidized in the denitrification and mercury removal device, that is, nitrogen oxides are converted into nitrogen and water , Convert elemental mercury into compounds, reduce the content of nitrogen oxides and elemental mercury in the flue gas (specifically, NOx in the flue gas and the injected NH 3 .H 2 O undergo a catalytic oxidation reduction reaction under the action of a denitration and mercury removal catalyst to generate N 2 and H 2 O, while Hg in the flue gas is oxidized to Hg 2+ );
  • Step 2 The flue gas processed by the desulfurization and denitrification device enters the raw material mill through the connecting air pipe, and at the same time, the desulfurizing agent (fine powder) is sprayed into the connecting air pipe (near the desulfurization and mercury removal device) to reduce the flue gas Sulfur dioxide and mercury adsorption (the desulfurization agent reacts with the SO 2 and Hg 2+ in the flue gas to undergo acid-base reaction and adsorption reaction respectively, so as to realize the deep denitration, desulfurization and mercury removal of the flue gas);
  • the desulfurizing agent fine powder
  • the connecting air pipe near the desulfurization and mercury removal device
  • Step 3 The flue gas entering the raw material mill is used to dry the cement raw materials.
  • the flue gas at the outlet of the raw material mill enters the bag filter to remove the dust and desulfurizer in the flue gas.
  • the clean flue gas after dust removal passes through the tail exhaust.
  • the fan is discharged after entering the chimney.
  • the denitration and mercury removal catalyst and the desulfurizing agent are both catalysts in the prior art, and the particle size of the desulfurizing agent in the desulfurizing agent powder bin is ⁇ 50 ⁇ m.
  • the present invention uses denitrification and mercury removal catalyst to provide catalytic active sites for the NOx reaction of cement kiln flue gas, and can oxidize Hg; utilizes the alkalinity of the desulfurizer to react with SO 2 to generate sulfate, and the desulfurizer has an effect on Hg 2+ Very strong adsorption, remove Hg 2+ by adsorption.
  • Example 1 The system described in Example 1 was used to carry out denitrification and mercury desulfurization treatment on the kiln tail gas of a cement production enterprise.
  • the heavy NOx content of the kiln tail gas of the enterprise was 175.74-400 mg/Nm 3 , and the average concentration was 287.84 mg/Nm 3 ; SO 2 an amount of 75.60 ⁇ 100mg / Nm 3, an average concentration of 87.80mg / Nm 3; Hg content of 27.51 ⁇ 50 ⁇ g / Nm 3, an average concentration of 38.75 ⁇ g / Nm 3.
  • the temperature of the flue gas at the outlet of the high-temperature fan is 150 ⁇ 250°C, the dust concentration is 60 ⁇ 80g/Nm 3 , the NOx in the flue gas and the injected NH 3.
  • H 2 O undergoes catalytic oxidation reduction reaction under the action of the denitrification and mercury removal catalyst to produce N 2 and H 2 O, while the Hg in the flue gas is oxidized to Hg 2+ ; in the outlet flue of the denitrification and mercury removal device (in the connecting duct between the denitrification and mercury removal device and the raw material mill), evenly spray high-activity desulfurizer fine powder ,
  • the desulfurizer and the SO 2 and Hg 2+ in the flue gas undergo acid-base and adsorption reactions respectively; the flue gas after the reaction is sequentially discharged to the chimney through the raw material mill, dust collector and exhaust fan, and enters the atmosphere.
  • the NOx concentration in the flue gas of the kiln tail is detected at the chimney to be 24.64mg/Nm 3 , and the removal rate is 91.44%; the SO 2 concentration is 1.43 mg/Nm 3 , and the removal rate is 98.37%; Hg concentration It is 5 ⁇ g/Nm 3 , and the removal rate is 87.1%.
  • the emission concentrations of NOx, SO 2 and Hg in the flue gas at the chimney outlet all meet the ultra-low emission requirements of the cement industry.

Abstract

一种水泥窑烟气脱硝脱汞脱硫系统及方法，包括按顺序依次相连的窑尾预热器（1）、高温风机（3）、内含脱硝脱汞催化剂的脱硝脱汞装置（5）、原料磨（9）、收尘器（10）、尾排风机（11）及烟囱（12）；高温风机（3）与脱硝脱汞装置（5）间的连接风管（8）上设有氨水施加装置（4），脱硝脱汞装置（5）与原料磨（9）间的连接风管（8）上设有脱硫剂喷射装置（7），脱硫剂喷射装置（7）与脱硫剂粉仓（6）相连。

Description

一种水泥窑烟气脱硝脱汞脱硫系统及方法 技术领域
本发明涉及水泥窑烟气处理技术领域，特别是一种水泥窑烟气脱硝脱汞脱硫系统及方法。
背景技术
《水泥工业发展规划》提出加强技术创新，实施创新驱动，鼓励研发烟气深度脱硫、脱硝及其集成协同控制技术装备。
《水泥工业大气污染物排放标准》规定重点地区NOx排放标准为320mg/Nm 3，SO 2排放标准为100mg/Nm 3，Hg及其化合物排放标准为50μg/Nm 3。江苏省明确将在非电行业实现达标排放基础上，大力推进焦化、钢铁、水泥、玻璃等行业氮氧化物深度减排，水泥窑烟气NOx排放浓度不高于100mg/Nm 3；河南省鼓励水泥企业进行超低排放改造，改造后二氧化硫、氮氧化物排放浓度要分别不高于50mg/Nm 3、100mg/Nm 3。
然而，传统的分级燃烧和SNCR技术已无法满足水泥窑烟气NOx深度减排要求，对水泥生产企业来说，必须要对脱硝工艺路线进行全新升级，由SNCR脱硝技术全面转向SCR脱硝技术。
水泥工业烟气中二氧化硫主要来自于原料中的硫化物、硫酸盐及燃料中的硫，由于生料中的氧化钙能够脱除大多数二氧化硫，使得尾部烟气中SO 2浓度较低，一般排放浓度为30-100mg/Nm 3。采用低成本无二次污染的脱硫技术已成为水泥工业烟气深度减排不可缺少的手段。
我国针对燃煤烟气中汞的排放已经出台多个国家和地方标准，但未来随着环保要求的提高，汞排放标准将趋严，水泥工业烟气中 汞污染控制技术将成为热点。水泥窑脱汞国内目前鲜有实施的案例，国外烟气脱汞以活性炭/活性焦吸附为主。水泥窑控制汞排放可采用以下措施：降低水泥窑排烟温度，但目前水泥窑尾烟气广泛用于余热发电及烘干生料，窑尾烟气温度并不能大幅降低；活性炭/活性焦吸附，此方法成本高，吸附后的活性炭/活性焦难以二次利用；湿法脱硫兼有脱汞功能，但湿法脱硫存在二次污染问题。
发明内容
为了克服现有技术的不足，本发明提供了一种操作简便、运行高效的水泥窑烟气脱硝脱汞脱硫系统及方法，实现了水泥窑烟气NOx、SO 2和Hg的超低排放。
本发明解决其技术问题所采用的技术方案是：
本发明首先提供一种水泥窑烟气脱硝脱汞脱硫系统，包括按顺序依次相连的窑尾预热器、高温风机、内含脱硝脱汞催化剂的脱硝脱汞装置、原料磨、收尘器、尾排风机及烟囱；所述高温风机与脱硝脱汞装置间的连接风管上设有氨水施加装置，所述脱硝脱汞装置与原料磨间的连接风管上设有脱硫剂喷射装置，该脱硫剂喷射装置与脱硫剂粉仓相连。
优选地，所述窑尾预热器与高温风机间设有余热锅炉。
优选的，所述脱硝脱汞装置内设有用于吹扫催化剂表面积灰的清灰装置。
本发明还提供一种基于上述系统的水泥窑烟气脱硝脱汞脱硫方法，包括如下步骤：
步骤一、将来自窑尾预热器的烟气依次通过余热锅炉、高温风机后进入内含有脱硝脱汞催化剂的脱硝脱汞装置，同时在脱硝脱汞装置的进口风管处喷入氨水，以使得烟气在脱硝脱汞装置内进行脱硝和汞氧化；
步骤二、经过脱硫脱硝装置处理后的烟气通过连接风管进入到原 料磨内，同时在此连接风管内喷入脱硫剂，以降低烟气中的二氧化硫和进行汞吸附；
步骤三、进入到原料磨内的烟气对水泥原料进行烘干，原料磨出口烟气进入袋收尘器对烟气中的粉尘和脱硫剂进行脱除，除尘后的洁净烟气通过尾排风机进入烟囱后排出。
优选地，所述窑尾预热器的出口烟气温度为280～350℃，粉尘浓度为80～100g/Nm 3。
优选地，步骤一中所述高温风机的出口烟气温度为150～250℃，粉尘浓度为60～80g/Nm 3。
优选地，步骤一中所喷入的氨水的质量浓度10～30％，流量为0.1～1m 3/h。
优选地，所述脱硫剂粉仓内脱硫剂的粒径≤50μm。
本发明的积极效果：本发明操作方便，对窑尾烟气中的NOx、Hg和SO 2脱除效率高，且系统占地面积小，设备投资成本低，是目前实现水泥窑烟气NOx、SO 2和Hg超低排放的有效手段。
附图说明
图1是本发明实施例所述水泥窑烟气脱硝脱汞脱硫系统的结构示意图。
图中：1、窑尾预热器系统；2、余热锅炉；3、高温风机；4、氨水施加装置；5、脱硝脱汞装置；6、脱硫剂粉仓；7、脱硫剂喷射装置；8、连接风管；9、原料磨；10、收尘器；11、尾排风机；12、烟囱。
具体实施方式
下面结合附图对本发明的优选实施例进行详细说明。
实施例1
参照图1，本发明优选实施例提供一种水泥窑烟气脱硝脱汞脱硫系统，包括按顺序依次相连的窑尾预热器系统1、高温风机3、内含 脱硝脱汞催化剂的脱硝脱汞装置5、原料磨9、收尘器10、尾排风机11及烟囱12；所述高温风机3与脱硝脱汞装置5间的连接风管上(靠近脱硝脱汞装置5的位置处)设有氨水施加装置4，所述脱硝脱汞装置5与原料磨9间的连接风管8上设有脱硫剂喷射装置7，该脱硫剂喷射装置7与脱硫剂粉仓6相连。
进一步地，所述窑尾预热器1与高温风机3间设有余热锅炉2，该余热锅炉2的主要作用是对窑尾预热器中出来的高温烟气进行一定程度的热回收，以增加烟气热能利用率。
其中，所述脱硝脱汞装置内设有清灰装置，该清灰装置用于吹扫催化剂表面(催化剂为多孔型，其表面包括内表面及外表面)的积灰，以防止粉尘堵塞催化剂。所述清灰装置可以为压缩空气式清灰装置。
实施例2
本实施例2提供一种基于实施例1所述系统的水泥窑烟气脱硝脱汞脱硫方法，包括如下步骤：
步骤一、将来自窑尾预热器的烟气(烟气温度为280～350℃，粉尘浓度为80～100g/Nm 3)通过余热锅炉，经余热锅炉热回收利用后的烟气经高温风机后进入内含有脱硝脱汞催化剂的脱硝脱汞装置(高温风机的出口烟气温度为150～250℃，粉尘浓度为60～80g/Nm 3)，同时在脱硝脱汞装置的进口风管处喷入氨水(喷入的氨水的质量浓度10～30％，流量为0.1～1m 3/h)，以使得烟气在脱硝脱汞装置内进行脱硝和汞氧化，即将氮氧化物转化为氮气和水，将单质汞转化为化合物，降低烟气中氮氧化物与单质汞含量(具体为烟气中NOx与喷入的NH 3.H 2O在脱硝脱汞催化剂作用下进行催化氧化还原反应生成N 2和H 2O，同时烟气中的Hg被氧化成Hg 2+)；
步骤二、经过脱硫脱硝装置处理后的烟气通过连接风管进入到原料磨内，同时向此连接风管内(靠近脱硫脱汞装置)喷入脱硫剂(细粉)，以降低烟气中的二氧化硫和进行汞吸附(脱硫剂与烟气中的SO 2 和Hg 2+分别发生酸碱反应和吸附反应，从而实现烟气的深度脱硝脱硫脱汞)；
步骤三、进入到原料磨内的烟气对水泥原料进行烘干，原料磨出口烟气进入袋收尘器对烟气中的粉尘和脱硫剂进行脱除，除尘后的洁净烟气通过尾排风机进入烟囱后排出。
其中，所述脱硝拖汞催化剂及脱硫剂均为现有技术中的催化剂，所述脱硫剂粉仓内脱硫剂的粒径≤50μm。
本发明利用脱硝脱汞催化剂为水泥窑烟气NOx反应提供催化活性位，并能氧化Hg；利用脱硫剂的碱性与SO 2发生酸碱反应，生成硫酸盐，同时脱硫剂对Hg 2+有很强的吸附性，将Hg 2+吸附脱除。
实施例3
利用实施例1所述系统对某水泥生产企业窑尾烟气进行脱硝拖汞脱硫处理，其中企业窑尾烟气重NOx含量为175.74～400mg/Nm 3，平均浓度为287.84mg/Nm 3；SO 2含量为75.60～100mg/Nm 3，平均浓度为87.80mg/Nm 3；Hg含量为27.51～50μg/Nm 3，平均浓度为38.75μg/Nm 3。高温风机出口烟气温度为150～250℃，粉尘浓度为60～80g/Nm 3，烟气中NOx与喷入的NH 3.H 2O在脱硝脱汞催化剂作用下进行催化氧化还原反应生成N 2和H 2O，同时烟气中的Hg被氧化成Hg 2+；在脱硝脱汞装置出口烟道中(脱硝脱汞装置与原料磨之间的连接风管内)均匀喷射高活性脱硫剂细粉，脱硫剂与烟气中的SO 2和Hg 2+分别发生酸碱和吸附反应；反应后的烟气依次经过原料磨、收尘器和尾排风机排至烟囱，进入大气环境。脱硝脱硫脱汞完成后，在烟囱处检测窑尾烟气中的NOx浓度为24.64mg/Nm 3，去除率达91.44％；SO 2浓度为1.43mg/Nm 3，去除率达98.37％；Hg浓度为5μg/Nm 3，去除率达87.1％。烟囱出口烟气NOx、SO 2和Hg的排放浓度均满足水泥行业的超低排放要求。
以上所述的仅为本发明的优选实施例，所应理解的是，以上实施 例的说明只是用于帮助理解本发明的方法及其核心思想，并不用于限定本发明的保护范围，凡在本发明的思想和原则之内所做的任何修改、等同替换等等，均应包含在本发明的保护范围之内。

Claims (8)

  1. 一种水泥窑烟气脱硝脱汞脱硫系统，其特征在于：包括按顺序依次相连的窑尾预热器、高温风机、内含脱硝脱汞催化剂的脱硝脱汞装置、原料磨、收尘器、尾排风机及烟囱；所述高温风机与脱硝脱汞装置间的连接风管上设有氨水施加装置，所述脱硝脱汞装置与原料磨间的连接风管上设有脱硫剂喷射装置，该脱硫剂喷射装置与脱硫剂粉仓相连。
  2. 根据权利要求1所述的一种水泥窑烟气脱硝脱汞脱硫系统，其特征在于：所述窑尾预热器与高温风机间设有余热锅炉。
  3. 根据权利要求1或2所述的一种水泥窑烟气脱硝脱汞脱硫系统，其特征在于：所述脱硝脱汞装置内设有用于吹扫催化剂表面积灰的清灰装置。
  4. 一种基于权利要求1所述系统的水泥窑烟气脱硝脱汞脱硫方法，其特征在于：包括如下步骤：
    步骤一、将来自窑尾预热器的烟气依次通过余热锅炉、高温风机后进入内含有脱硝脱汞催化剂的脱硝脱汞装置，同时在脱硝脱汞装置的进口风管处喷入氨水，以使得烟气在脱硝脱汞装置内进行脱硝和汞氧化；
    步骤二、经过脱硫脱硝装置处理后的烟气通过连接风管进入到原料磨内，同时在此连接风管内喷入脱硫剂，以降低烟气中的二氧化硫和进行汞吸附；
    步骤三、进入到原料磨内的烟气对水泥原料进行烘干，原料磨出口烟气进入袋收尘器对烟气中的粉尘和脱硫剂进行脱除，除尘后的洁净烟气通过尾排风机进入烟囱后排出。
  5. 根据权利要求4所述的一种水泥窑烟气脱硝脱汞脱硫方法，其特征在于：所述窑尾预热器的出口烟气温度为280～350℃，粉尘 浓度为80～100g/Nm 3。
  6. 根据权利要求5所述的一种水泥窑烟气脱硝脱汞脱硫方法，其特征在于：步骤一中所述高温风机的出口烟气温度为150～250℃，粉尘浓度为60～80g/Nm 3。
  7. 根据权利要求4所述的一种水泥窑烟气脱硝脱汞脱硫方法，其特征在于：步骤一中所喷入的氨水的质量浓度10～30％，流量为0.1～1m 3/h。
  8. 根据权利要求4所述的一种水泥窑烟气脱硝脱汞脱硫方法，其特征在于：所述脱硫剂粉仓内脱硫剂的粒径≤50μm。
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