CN104437082A - Ultra-clean discharge system and method for fluidized bed boiler - Google Patents
Ultra-clean discharge system and method for fluidized bed boiler Download PDFInfo
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- 238000000034 method Methods 0.000 title claims abstract description 14
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims abstract description 123
- 239000003546 flue gas Substances 0.000 claims abstract description 123
- 238000006477 desulfuration reaction Methods 0.000 claims abstract description 83
- 230000023556 desulfurization Effects 0.000 claims abstract description 83
- 239000000428 dust Substances 0.000 claims abstract description 47
- 239000007789 gas Substances 0.000 claims abstract description 14
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 claims description 25
- 229910021529 ammonia Inorganic materials 0.000 claims description 11
- 239000000446 fuel Substances 0.000 claims description 6
- 239000010440 gypsum Substances 0.000 claims description 4
- 229910052602 gypsum Inorganic materials 0.000 claims description 4
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 claims description 4
- 235000019738 Limestone Nutrition 0.000 claims description 3
- 239000006028 limestone Substances 0.000 claims description 3
- 239000000295 fuel oil Substances 0.000 claims description 2
- 239000003345 natural gas Substances 0.000 claims description 2
- 238000011084 recovery Methods 0.000 claims description 2
- 238000005516 engineering process Methods 0.000 abstract description 16
- 238000002485 combustion reaction Methods 0.000 abstract description 13
- 230000007613 environmental effect Effects 0.000 abstract description 3
- 238000005457 optimization Methods 0.000 abstract description 2
- 239000000809 air pollutant Substances 0.000 abstract 1
- 231100001243 air pollutant Toxicity 0.000 abstract 1
- 239000003054 catalyst Substances 0.000 description 11
- 239000003638 chemical reducing agent Substances 0.000 description 7
- 239000000779 smoke Substances 0.000 description 6
- 238000009792 diffusion process Methods 0.000 description 5
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 4
- 239000003245 coal Substances 0.000 description 4
- MWUXSHHQAYIFBG-UHFFFAOYSA-N Nitric oxide Chemical compound O=[N] MWUXSHHQAYIFBG-UHFFFAOYSA-N 0.000 description 3
- XSQUKJJJFZCRTK-UHFFFAOYSA-N Urea Chemical compound NC(N)=O XSQUKJJJFZCRTK-UHFFFAOYSA-N 0.000 description 3
- 238000003915 air pollution Methods 0.000 description 3
- 239000004202 carbamide Substances 0.000 description 3
- 238000006243 chemical reaction Methods 0.000 description 3
- 239000006227 byproduct Substances 0.000 description 2
- 238000010531 catalytic reduction reaction Methods 0.000 description 2
- 238000009434 installation Methods 0.000 description 2
- 229910052757 nitrogen Inorganic materials 0.000 description 2
- 239000002893 slag Substances 0.000 description 2
- AKEJUJNQAAGONA-UHFFFAOYSA-N sulfur trioxide Chemical compound O=S(=O)=O AKEJUJNQAAGONA-UHFFFAOYSA-N 0.000 description 2
- BIGPRXCJEDHCLP-UHFFFAOYSA-N ammonium bisulfate Chemical compound [NH4+].OS([O-])(=O)=O BIGPRXCJEDHCLP-UHFFFAOYSA-N 0.000 description 1
- BFNBIHQBYMNNAN-UHFFFAOYSA-N ammonium sulfate Chemical compound N.N.OS(O)(=O)=O BFNBIHQBYMNNAN-UHFFFAOYSA-N 0.000 description 1
- 229910052921 ammonium sulfate Inorganic materials 0.000 description 1
- 235000011130 ammonium sulphate Nutrition 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000005260 corrosion Methods 0.000 description 1
- 230000007797 corrosion Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 230000008569 process Effects 0.000 description 1
- 239000000047 product Substances 0.000 description 1
- 230000009466 transformation Effects 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
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- Y02A50/00—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE in human health protection, e.g. against extreme weather
- Y02A50/20—Air quality improvement or preservation, e.g. vehicle emission control or emission reduction by using catalytic converters
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02C—CAPTURE, STORAGE, SEQUESTRATION OR DISPOSAL OF GREENHOUSE GASES [GHG]
- Y02C20/00—Capture or disposal of greenhouse gases
- Y02C20/10—Capture or disposal of greenhouse gases of nitrous oxide (N2O)
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Abstract
一种用于流化床锅炉的超净排放方法，在流化床锅炉密相区进行炉内一次脱硫；在炉膛出口进行基于SNCR的一次脱硝；经炉内一次脱硫和一次脱硝后的烟气进行高温除尘后进行基于SCR的二次脱硝；经二次脱硝后的烟气换热至正常排烟温度进入低温除尘器进行二次除尘；经二次除尘后的烟气送入脱硫系统进行二次脱硫，本发明还提供了相应的系统，采用高、低温除尘装置进行两级除尘并结合SNCR+SCR方式联合脱硝，同时采用炉内+炉外方式脱硫，并通过燃烧优化技术+环保系统参数精确控制，使得NOx、SO2排放达到《火电厂大气污染物排放标准》GB13223-2011中重点地区燃气轮机组的排放标准，具有脱硝效率高、脱硫效率高、系统可靠性高、工况适应性强、NOx、SO2排放可控性好、运行周期长、运行费用低等优点。
An ultra-clean emission method for fluidized bed boilers, performing primary desulfurization in the dense phase area of the fluidized bed boiler; performing primary denitrification based on SNCR at the furnace outlet; flue gas after primary desulfurization and primary denitrification in the furnace After the high-temperature dedusting, the secondary denitrification based on SCR is carried out; the flue gas after the secondary denitrification is heat exchanged to the normal exhaust gas temperature and enters the low-temperature dust collector for secondary dedusting; the flue gas after the secondary dedusting is sent to the desulfurization system for secondary dedusting. The present invention also provides a corresponding system, using high and low temperature dedusting devices for two-stage dedusting combined with SNCR+SCR combined denitrification, while adopting furnace+outside desulfurization, and through combustion optimization technology+environmental protection system parameters Accurate control makes NO x and SO 2 emissions meet the emission standards of gas turbine units in key areas in the "Emission Standards of Air Pollutants for Thermal Power Plants" GB13223-2011, with high denitrification efficiency, high desulfurization efficiency, high system reliability and adaptability to working conditions Strong, NO x , SO 2 emission controllable, long operating cycle, low operating costs and other advantages.
Description
技术领域technical field
本发明属于锅炉环保技术领域，特别涉及一种用于流化床锅炉的超净排放系统及方法。The invention belongs to the technical field of boiler environmental protection, and in particular relates to an ultra-clean discharge system and method for a fluidized bed boiler.
背景技术Background technique
循环流行化床锅炉技术是近十几年来迅速发展的一项高效低污染清洁燃烧枝术，具有燃料适应性广、燃烧效率高、高效脱硫、氮氧化物(NOX)排放低、燃烧强度高、炉膛截面积小、负荷调节范围大、负荷调节快、易于实现灰渣综合利用、燃料预处理系统简单、给煤点少等优点。因此这项技术在电站锅炉、工业锅炉和废弃物处理利用等领域均得到了广泛的商业应用。Circulating popularized bed boiler technology is a high-efficiency, low-pollution and clean combustion technology that has developed rapidly in the past ten years. It has wide fuel adaptability, high combustion efficiency, high-efficiency desulfurization, low nitrogen oxide (NO X ) emissions, and high combustion intensity. , Small cross-sectional area of the furnace, large load adjustment range, fast load adjustment, easy to realize comprehensive utilization of ash and slag, simple fuel pretreatment system, few coal feeding points, etc. Therefore, this technology has been widely used commercially in the fields of power station boilers, industrial boilers and waste treatment and utilization.
运行经验表明，循环流化床锅炉的NOX排放值基本在400mg/m3以下。循环流化床锅炉NOX排放低是由于以下两个原因：一是低温燃烧，此时空气中的氮一般不会生成NOX；二是分段燃烧，抑制燃料中的氮转化为NOX，并使部分已生成的NOX得到还原。Operating experience shows that the NOx emission value of circulating fluidized bed boilers is basically below 400mg/m 3 . The low emission of NO X from circulating fluidized bed boilers is due to the following two reasons: one is low-temperature combustion, at which time the nitrogen in the air generally does not generate NO X ; And make part of the NO X that has been generated be reduced.
《火电厂大气污染排放标准》(GB13223-2003)中对SO2和NOX的排放限值分别为400mg/m3、450mg/m3。对于循环流化床锅炉，仅需进行炉内脱硫即可使SO2排放、NOX排放达标，故原有循环流化床锅炉机组基本不设置脱硝装置。《火电厂大气污染排放标准》(GB13223-2011)实施后，对SO2和NOX的排放限值均降为100mg/m3，导致现有设备条件基本无法满足环保要求。The emission limits for SO 2 and NO X in the "Emission Standards for Air Pollution from Thermal Power Plants" (GB13223-2003) are 400mg/m 3 and 450mg/m 3 , respectively. For circulating fluidized bed boilers, only desulfurization in the furnace is required to make SO2 emissions and NOx emissions meet the standards, so the original circulating fluidized bed boiler units basically do not have denitrification devices. After the implementation of the "Emission Standards for Air Pollution from Thermal Power Plants" (GB13223-2011), the emission limits for SO 2 and NO X were both reduced to 100mg/m 3 , resulting in the existing equipment conditions basically failing to meet environmental protection requirements.
目前应用于锅炉的脱硝技术主要分为燃烧控制技术和烟气脱硝技术。燃烧控制技术包括：CFB锅炉燃烧技术、空气分级燃烧、燃料分级燃烧、烟气再循环、低氮燃烧器技术、燃烧优化；烟气脱硝技术主要包括：SCR(选择性催化还原技术)、SNCR(选择性非催化还原法)、SNCR+SCR。目前应用于循环流化床锅炉的主要是燃烧控制技术。The denitrification technology currently applied to boilers is mainly divided into combustion control technology and flue gas denitrification technology. Combustion control technology includes: CFB boiler combustion technology, air staged combustion, fuel staged combustion, flue gas recirculation, low nitrogen burner technology, combustion optimization; flue gas denitration technology mainly includes: SCR (selective catalytic reduction technology), SNCR ( Selective non-catalytic reduction method), SNCR+SCR. At present, the combustion control technology is mainly used in circulating fluidized bed boilers.
SCR的优点是：脱硝效率高(70～90％)、技术成熟，国内应用多；缺点是：投资成本高(需要催化剂、造价为SNCR的3倍以上)、运行成本较高(还原剂、催化剂)、安装方式对锅炉结构改变大、尾部易沾污、腐蚀、适用于新建煤粉机组。The advantages of SCR are: high denitrification efficiency (70-90%), mature technology, and many domestic applications; the disadvantages are: high investment cost (requires catalyst, cost is more than 3 times that of SNCR), high operating cost (reductant, catalyst ), the installation method changes the boiler structure greatly, the tail is easy to be stained and corroded, and is suitable for new pulverized coal units.
SNCR的优点是：占地面积小(布置在锅炉本体上)、投资成本低(造价为SCR的1/4～1/3)、运行成本较低(0.003～0.004元/kWh)、安装及操作较易、技术成熟；适应参数、负荷、煤质变化快；有助于降低平均成本、不催化增加三氧化硫(SO3)、不造成尾部受热面、空气预热器的堵塞或腐蚀；特别适用于CFB机组及老机组脱硝改造；缺点是：脱硝效率不够高、氨逃逸量较SCR稍高。The advantages of SNCR are: small footprint (arranged on the boiler body), low investment cost (1/4-1/3 of SCR), low operating cost (0.003-0.004 yuan/kWh), installation and operation Relatively easy, mature technology; adapt to parameters, loads, and coal quality changes quickly; help reduce average cost, do not catalyze the increase of sulfur trioxide (SO 3 ), and do not cause blockage or corrosion of the rear heating surface and air preheater; especially It is suitable for the denitrification transformation of CFB units and old units; the disadvantages are: the denitrification efficiency is not high enough, and the amount of ammonia escape is slightly higher than that of SCR.
SNCR+SCR的特点：脱硝效率高(40～80％)、投资成本略低、运行成本略低(还原剂、少量催化剂)、氨逃逸量低、可大幅减少SCR的反应容积。逃逸的氨会随烟气流向下游的SCR系统，使其利用率反应率更为完全。还原剂可使用尿素代替较危险的液氨。缺点是：流化床锅炉应用经验较少，同时也存在SCR催化剂寿命短等问题。The characteristics of SNCR+SCR: high denitrification efficiency (40-80%), slightly lower investment cost, slightly lower operating cost (reductant, small amount of catalyst), low ammonia escape, and can greatly reduce the reaction volume of SCR. The escaped ammonia will flow to the downstream SCR system with the flue gas, making its utilization rate more complete. The reducing agent can use urea to replace the more dangerous liquid ammonia. The disadvantages are: less experience in the application of fluidized bed boilers, and there are also problems such as short life of SCR catalysts.
目前应用于流化床锅炉的脱硫技术主要是炉内脱硫，烟气脱硫主要应用于煤粉炉。流化床锅炉通过炉内添加脱硫剂(石灰石、电石渣等)可将SO2排放值控制到较低水平，但在新的环保标准下，现有炉内脱硫装置存在出力不够、经济性差、脱硫难以达标等问题。The desulfurization technology currently applied to fluidized bed boilers is mainly in-furnace desulfurization, and flue gas desulfurization is mainly used in pulverized coal boilers. Fluidized bed boilers can control SO 2 emissions to a low level by adding desulfurizers (limestone, carbide slag, etc.) Desulfurization is difficult to meet the standard and other issues.
发明内容Contents of the invention
为了克服上述现有技术的缺点，本发明的目的在于提供一种用于流化床锅炉的超净排放系统及方法，具有本系统具有脱硝效率高、脱硫效率高、系统可靠性高、工况适应性强、NOx、SO2排放可控性好、运行周期长、运行费用低等优点，可使现有流化床锅炉满足《火电厂大气污染排放标准》(GB13223-2011)的要求。In order to overcome the above-mentioned shortcomings of the prior art, the object of the present invention is to provide an ultra-clean exhaust system and method for fluidized bed boilers, which has the advantages of high denitrification efficiency, high desulfurization efficiency, high system reliability, and high working conditions. The advantages of strong adaptability, good controllability of NOx and SO2 emissions, long operation period and low operation cost can make the existing fluidized bed boiler meet the requirements of "Emission Standard of Air Pollution for Thermal Power Plants" (GB13223-2011).
为了实现上述目的，本发明采用的技术方案是：In order to achieve the above object, the technical scheme adopted in the present invention is:
一种用于流化床锅炉的超净排放方法，其中：A method of ultra-clean discharge for a fluidized bed boiler, wherein:
在流化床锅炉密相区进行炉内一次脱硫；In-furnace desulfurization in the dense-phase area of the fluidized bed boiler;
在炉膛出口进行基于SNCR的一次脱硝；Perform primary denitrification based on SNCR at the furnace outlet;
经炉内一次脱硫和一次脱硝后的烟气进行高温除尘后进行基于SCR的二次脱硝；The flue gas after the primary desulfurization and primary denitrification in the furnace is subjected to high-temperature dust removal, and then the secondary denitrification based on SCR is carried out;
经二次脱硝后的烟气换热至正常排烟温度并进入低温除尘器进行二次除尘；After the second denitrification, the flue gas is heat-exchanged to the normal exhaust gas temperature and enters the low-temperature dust collector for secondary dust removal;
经二次除尘后的烟气送入脱硫系统进行二次脱硫。The flue gas after secondary dedusting is sent to the desulfurization system for secondary desulfurization.
所述高温除尘的温度在360℃以上，所述正常排烟温度为130-140℃。The temperature of the high-temperature dust removal is above 360°C, and the normal exhaust gas temperature is 130-140°C.
本发明还提供了一种用于流化床锅炉的超净排放系统，包括布置于流化床锅炉密相区的炉内脱硫装置17和布置于炉膛16出口的SNCR装置15，其特征在于，所述SNCR装置15出口连接分离器14，出分离器14的烟气依次经过过热器13和省煤器12后接入高温除尘器11，高温除尘器11的烟气出口与SCR装置22连接，SCR装置22的烟气出口与空气预热器7连接，空气预热器7的烟气出口与低温除尘器6的烟气入口连接，低温除尘器6的烟气出口与脱硫系统1的烟气入口相连接且在连接管路上设置有引风机23和增压风机26，引风机23和增压风机26的连接管路上设置有烟气挡板三25，出脱硫系统1的烟气排至烟囱并在管线上设置用于提升烟气温度的洁净烟气发生器3。The present invention also provides an ultra-clean discharge system for a fluidized bed boiler, comprising an in-furnace desulfurization device 17 arranged in the dense phase area of the fluidized bed boiler and an SNCR device 15 arranged at the outlet of the furnace 16, characterized in that, The outlet of the SNCR device 15 is connected to the separator 14, and the flue gas from the separator 14 passes through the superheater 13 and the economizer 12 in turn, and then is connected to the high-temperature dust collector 11, and the flue gas outlet of the high-temperature dust collector 11 is connected to the SCR device 22, The flue gas outlet of the SCR device 22 is connected to the air preheater 7, the flue gas outlet of the air preheater 7 is connected to the flue gas inlet of the low temperature dust collector 6, and the flue gas outlet of the low temperature dust collector 6 is connected to the flue gas of the desulfurization system 1 The inlets are connected and an induced draft fan 23 and a booster fan 26 are installed on the connecting pipeline, and a flue gas baffle 3 25 is installed on the connecting pipeline between the induced fan 23 and the booster fan 26, and the flue gas exiting the desulfurization system 1 is discharged to the chimney And a clean flue gas generator 3 for raising the flue gas temperature is arranged on the pipeline.
所述SCR装置22并联设置有SCR旁路10，SCR旁路10与SCR装置22的烟气入口连接管路上有烟气挡板四21，SCR旁路10与SCR装置22的烟气出口连接管路上有烟气挡板五9，所述SCR旁路10、烟气挡板四21和烟气挡板五9用于实现SCR装置22的投退切换；所述脱硫系统1并联设置有脱硫系统旁路24，脱硫系统1设置在烟气挡板三25和烟气挡板一4之间，所述脱硫系统旁路24、烟气挡板三25和烟气挡板一4用于实现脱硫系统1的投退切换。The SCR device 22 is provided with an SCR bypass 10 in parallel, and there is a flue gas baffle 21 on the flue gas inlet connection pipeline between the SCR bypass 10 and the SCR device 22, and the flue gas outlet connection pipe between the SCR bypass 10 and the SCR device 22 There is a flue gas baffle 5 9 on the road, and the SCR bypass 10, flue gas baffle 4 21 and flue gas baffle 5 9 are used to realize the switching of the SCR device 22; the desulfurization system 1 is provided with a desulfurization system in parallel Bypass 24, the desulfurization system 1 is arranged between the flue gas baffle 3 25 and the flue gas baffle 1 4, the desulfurization system bypass 24, the flue gas baffle 3 25 and the flue gas baffle 1 4 are used to realize desulfurization System 1 switchover.
所述炉膛16底部连接有风室18，送风机8供风通过空气预热器7预热后通往风室18。The bottom of the furnace 16 is connected with an air chamber 18 , and the blower 8 supplies air to the air chamber 18 after being preheated by the air preheater 7 .
所述分离器14的下部通过返料器19回接至流化床锅炉密相区。The lower part of the separator 14 is connected back to the dense phase zone of the fluidized bed boiler through a feeder 19 .
所述SNCR装置15布置在炉膛16出口800～1050℃区域，所述炉内脱硫装置17布置在炉膛16的下部。The SNCR device 15 is arranged at the 800-1050°C area at the outlet of the furnace 16, and the furnace desulfurization device 17 is arranged at the lower part of the furnace 16.
所述高温除尘器11布置于省煤器12之后烟气温度360℃区域，除尘效率设计不低于90％，所述空气预热器7布置于SCR装置22之后，用于降低烟气温度及热量回收，所述低温除尘器6布置于空气预热器7之后正常排烟温度区域。The high-temperature dust collector 11 is arranged behind the economizer 12 in the area where the flue gas temperature is 360°C, and the design dust removal efficiency is not lower than 90%. The air preheater 7 is arranged after the SCR device 22 to reduce the flue gas temperature and For heat recovery, the low-temperature dust collector 6 is arranged in the normal exhaust gas temperature area after the air preheater 7 .
所述脱硫系统1采用氨法脱硫或者石灰石/石膏湿法脱硫。The desulfurization system 1 adopts ammonia desulfurization or limestone/gypsum wet desulfurization.
所述洁净烟气发生器3采用天然气或燃油作为燃料，用于提升脱硫系统1出口烟气温度，以保证烟气的扩散能力，洁净烟气发生器3与出脱硫系统1的烟气之间设置有烟气挡板二2。The clean flue gas generator 3 uses natural gas or fuel oil as fuel to increase the flue gas temperature at the outlet of the desulfurization system 1 to ensure the diffusion capacity of the flue gas. A smoke baffle 2 is provided.
与现有技术相比，本发明的有益效果是：Compared with prior art, the beneficial effect of the present invention is:
1)本系统采用高、低温除尘装置进行两级除尘，除尘效率更高。1) This system adopts high and low temperature dust removal device to carry out two-stage dust removal, and the dust removal efficiency is higher.
2)本系统所述SCR装置布置在高温除尘器出口区域，烟尘较少，催化剂工作环境较好，使用周期长；同时，SCR装置工作烟温仍较高，催化剂比较成熟，选择余地大。2) The SCR device described in this system is arranged in the outlet area of the high-temperature dust collector, so there is less smoke and dust, the catalyst has a better working environment, and the service life is long; at the same time, the working smoke temperature of the SCR device is still high, the catalyst is relatively mature, and the choice is large.
3)本系统设置的洁净烟气发生器可以提升脱硫系统出口烟气温度，以保证烟气有较高的扩散能力。3) The clean flue gas generator set in this system can increase the flue gas temperature at the outlet of the desulfurization system to ensure a high diffusion capacity of the flue gas.
4)本系统采用SNCR+SCR：脱硝效率高(40～80％)、投资成本略低、运行成本略低(还原剂、少量催化剂)、氨逃逸量低、可大幅减少SCR装置的反应容积。逃逸的氨会随烟气流向下游的SCR装置，使其利用率反应率更为完全，还原剂可使用尿素代替较危险的液氨；因而使得系统运行稳定性、经济性加强的同时，氨逃逸大大降低。4) The system adopts SNCR+SCR: high denitrification efficiency (40-80%), slightly lower investment cost, slightly lower operating cost (reductant, small amount of catalyst), low ammonia escape, and can greatly reduce the reaction volume of the SCR device. The escaped ammonia will flow to the downstream SCR device with the flue gas flow, making its utilization rate more complete, and the reductant can use urea instead of the more dangerous liquid ammonia; thus, the stability and economy of the system are enhanced, and the ammonia escape Greatly reduced.
5)本系统采用炉内脱硫结合炉外脱硫系统两级脱硫，同样也增加了SO2排放的可控性，炉外脱硫还可回收具有一定经济价值的副产品(硫酸铵、石膏等)，降低了脱硫系统运行成本。5) This system adopts the two-stage desulfurization of the furnace desulfurization combined with the external desulfurization system, which also increases the controllability of SO2 emissions. The external desulfurization can also recover by-products with certain economic value (ammonium sulfate, gypsum, etc.), reducing operating cost of the desulfurization system.
综上所述，本系统具有脱硝效率高、脱硫效率高、系统可靠性高、工况适应性强、NOx、SO2排放可控性好、运行周期长、运行费用低等优点。In summary, this system has the advantages of high denitrification efficiency, high desulfurization efficiency, high system reliability, strong adaptability to working conditions, good controllability of NO x and SO 2 emissions, long operation period, and low operation cost.
附图说明Description of drawings
图1是本发明用于流化床锅炉的超净排放系统的结构示意图。Fig. 1 is a structural schematic diagram of the ultra-clean discharge system used in a fluidized bed boiler according to the present invention.
具体实施方式Detailed ways
下面结合附图和实施例详细说明本发明的实施方式。The implementation of the present invention will be described in detail below in conjunction with the drawings and examples.
一种用于流化床锅炉的超净排放方法，主要通过如下工艺环节实现：An ultra-clean discharge method for a fluidized bed boiler, which is mainly realized through the following process links:
在流化床锅炉密相区进行炉内一次脱硫；In-furnace desulfurization in the dense-phase area of the fluidized bed boiler;
在炉膛出口进行基于SNCR的一次脱硝；Perform primary denitrification based on SNCR at the furnace outlet;
经炉内一次脱硫和一次脱硝后的烟气进行高温除尘后进行基于SCR的二次脱硝，高温除尘的温度在360℃以上；The flue gas after the primary desulfurization and primary denitrification in the furnace is subjected to high-temperature dedusting, and then the secondary denitrification based on SCR is carried out. The temperature of high-temperature dedusting is above 360°C;
经二次脱硝后的烟气换热至正常排烟温度(130-140℃)并进入低温除尘器进行二次除尘；After the second denitrification, the flue gas is heat-exchanged to the normal exhaust gas temperature (130-140°C) and enters the low-temperature dust collector for secondary dust removal;
经二次除尘后的烟气送入脱硫系统进行二次脱硫。The flue gas after secondary dedusting is sent to the desulfurization system for secondary desulfurization.
为了实现上述方法，并有效适应各种不同的实际工况，本发明还提供了一种用于流化床锅炉的超净排放系统，如图1所示，包括布置于流化床锅炉密相区的炉内脱硫装置17，炉内脱硫装置17位于炉膛16的下部，炉膛16底部连接有风室18，风室18与为锅炉提供配风的送风机17连通。SNCR装置15布置在炉膛16出口的800～1050℃区域。In order to realize the above method and effectively adapt to various actual working conditions, the present invention also provides an ultra-clean exhaust system for fluidized bed boilers, as shown in Figure 1, including The furnace desulfurization device 17 in the zone is located at the lower part of the furnace 16, and the bottom of the furnace 16 is connected with an air chamber 18, and the air chamber 18 communicates with the blower 17 that provides air distribution for the boiler. The SNCR device 15 is arranged in the 800-1050°C area at the outlet of the furnace 16 .
SNCR装置15出口连接分离器14，分离器14的下部通过返料器19回接至流化床锅炉密相区。出分离器14的烟气依次经过过热器13和省煤器12后接入高温除尘器11，高温除尘器11布置于省煤器12之后烟气温度360℃区域，除尘效率设计不低于90％。高温除尘器11的烟气出口与SCR装置22连接，SCR装置22的烟气出口与空气预热器7连接，空气预热器7用于降低烟气温度及热量回收，送风机8连接空气预热器7，空气预热器7通过流化风风道20连接风室18。空气预热器7的烟气出口与低温除尘器6的烟气入口连接，低温除尘器6布置于空气预热器7之后正常排烟温度区域。低温除尘器6的烟气出口与脱硫系统1的烟气入口相连接且在连接管路上设置有引风机23和增压风机26，引风机23和增压风机26的连接管路上设置有烟气挡板三25，出脱硫系统1的烟气排至烟囱；另外设置洁净烟气发生器3，并设置烟气挡板二2，用于提升脱硫系统出口烟气温度，以保证烟气的扩散能力。The outlet of the SNCR device 15 is connected to the separator 14, and the lower part of the separator 14 is connected back to the dense-phase zone of the fluidized bed boiler through the feeder 19. The flue gas exiting the separator 14 passes through the superheater 13 and the economizer 12 in sequence, and then connects to the high-temperature dust collector 11. The high-temperature dust collector 11 is arranged in the area where the flue gas temperature is 360°C after the economizer 12, and the design dust removal efficiency is not lower than 90 %. The flue gas outlet of the high-temperature dust collector 11 is connected to the SCR device 22, and the flue gas outlet of the SCR device 22 is connected to the air preheater 7. The air preheater 7 is used to reduce the temperature of the flue gas and recover heat, and the blower 8 is connected to the air preheater The air preheater 7 and the air preheater 7 are connected to the air chamber 18 through the fluidizing air duct 20 . The flue gas outlet of the air preheater 7 is connected to the flue gas inlet of the low-temperature dust collector 6 , and the low-temperature dust collector 6 is arranged behind the air preheater 7 in the normal exhaust gas temperature area. The flue gas outlet of the cryogenic dust collector 6 is connected to the flue gas inlet of the desulfurization system 1 and an induced draft fan 23 and a booster fan 26 are arranged on the connecting pipeline, and a flue gas is arranged on the connecting pipeline of the induced draft fan 23 and the booster fan 26 Baffle 3 25, the flue gas from the desulfurization system 1 is discharged to the chimney; in addition, a clean flue gas generator 3 is installed, and a flue gas baffle 2 2 is installed to increase the flue gas temperature at the outlet of the desulfurization system to ensure the diffusion of flue gas ability.
为适应不同工况，SCR装置22并联设置有SCR旁路10，SCR旁路10与SCR装置22的烟气入口连接管路上有烟气挡板四21，SCR旁路10与SCR装置22的烟气出口连接管路上有烟气挡板五9，所述SCR旁路10、烟气挡板四21和烟气挡板五9用于实现SCR装置22的投退切换；所述脱硫系统1并联设置有脱硫系统旁路24，脱硫系统旁路24设置在烟气挡板三25和烟气挡板一4之间，所述脱硫系统旁路24、烟气挡板三25和烟气挡板一4用于实现脱硫系统1的投退切换。In order to adapt to different working conditions, the SCR device 22 is provided with an SCR bypass 10 in parallel. There is a flue gas baffle 21 on the connecting pipeline between the SCR bypass 10 and the flue gas inlet of the SCR device 22, and the flue gas of the SCR bypass 10 and the SCR device 22 There is a flue gas baffle 5 9 on the gas outlet connecting pipeline, and the SCR bypass 10, flue gas baffle 4 21 and flue gas baffle 5 9 are used to realize the switch between switching on and off of the SCR device 22; the desulfurization system 1 is connected in parallel A desulfurization system bypass 24 is provided, and the desulfurization system bypass 24 is arranged between the flue gas baffle 3 25 and the flue gas baffle 1 4, the desulfurization system bypass 24, the flue gas baffle 3 25 and the flue gas baffle -4 is used to realize the switching of the desulfurization system 1 on and off.
本发明的工作原理是：The working principle of the present invention is:
燃料在循环流化床锅炉中燃烧，脱硫剂由锅炉密相区炉内脱硫装置17给入，进行炉内一次脱硫；燃烧烟气流至炉膛16出口时，由SNCR装置15进行一次脱硝，脱去大部分NOX；经过炉内脱硫和一次脱硝后烟气经过热器13、省煤器12后进入高温除尘器11进行一次除尘，除去约90％的烟尘；之后高温烟气进入SCR装置22进行二次脱硝以使排放达标，因此处烟气温度仍在360℃以上，故催化剂可使用较为成熟产品，选择余地较大；脱硝完毕的烟气随后进入空气预热器7进行换热，之后正常排烟温度的烟气进入低温除尘器6进行二次除尘以使排放达标；除尘完毕后的烟气进入脱硫系统1进行二次脱硫以使排放达标；最终超净烟气由烟囱5排至大气。The fuel is burned in the circulating fluidized bed boiler, and the desulfurizer is fed by the desulfurization device 17 in the dense phase zone of the boiler to perform primary desulfurization in the furnace; when the combustion flue gas flows to the outlet of the furnace 16, the SNCR device 15 performs primary denitrification and desulfurization. Remove most of the NOx ; after furnace desulfurization and primary denitrification, the flue gas passes through the heater 13 and the economizer 12, and then enters the high-temperature dust collector 11 for a dust removal, removing about 90% of the smoke; after that, the high-temperature flue gas enters the SCR device 22 Secondary denitrification is carried out to meet the emission standards, so the temperature of the flue gas is still above 360°C, so the catalyst can use relatively mature products, and the choice is large; the flue gas after denitrification is then entered into the air preheater 7 for heat exchange, and then The flue gas with normal exhaust temperature enters the low-temperature dust collector 6 for secondary dust removal to make the emission meet the standard; the flue gas after dust removal enters the desulfurization system 1 for secondary desulfurization to make the emission reach the standard; finally, the ultra-clean flue gas is discharged from the chimney 5 to atmosphere.
正常工况下，关闭SCR旁路挡板10、脱硫系统旁路24，打开烟气挡板五9、烟气挡板四21、烟气挡板一4、烟气挡板三25，通过烟气挡板二2调节烟囱入口烟气温度，以增加烟气扩散能力；Under normal working conditions, close the SCR bypass damper 10 and the desulfurization system bypass 24, open the flue gas damper 5 9, the flue gas damper 4 21, the flue gas damper 1 4, the flue gas damper 3 25, and pass the flue gas Gas baffle 2 2 adjusts the flue gas temperature at the chimney inlet to increase the flue gas diffusion capacity;
炉内脱硫、SNCR脱硝即可达到排放指标时，打开SCR旁路挡板10、脱硫系统旁路24，关闭烟气挡板五9、烟气挡板四21、烟气挡板一4、烟气挡板三25，通过烟气挡板二2调节烟囱入口烟气温度，以增加烟气扩散能力；When the desulfurization in the furnace and SNCR denitrification can reach the emission target, open the SCR bypass baffle 10, the desulfurization system bypass 24, close the flue gas baffle 5 9, the flue gas baffle 4 21, the flue gas baffle 1 4, the flue gas baffle Gas baffle three 25, adjust the flue gas temperature at the chimney inlet through the flue gas baffle two 2, to increase the flue gas diffusion capacity;
通过调整炉内脱硫、SNCR脱硝效率，本系统可方便调节炉内脱硫、脱硝与炉外脱硫、脱硝比例，以达到整套系统综合能效最高的最优工况。By adjusting the efficiency of desulfurization and SNCR denitrification in the furnace, this system can easily adjust the ratio of desulfurization and denitration in the furnace to that of desulfurization and denitrification outside the furnace, so as to achieve the optimal working condition with the highest comprehensive energy efficiency of the whole system.
由于本系统采用高、低温除尘装置进行两级除尘，除尘效率更高；同时SCR装置22布置在高温除尘器11出口区域，烟尘较少，催化剂工作环境较好，使用周期长；而且SCR工作烟温仍较高，催化剂比较成熟，选择余地大；采用SNCR+SCR方式脱硝效率高(40～80％)、投资成本略低、运行成本略低(还原剂、少量催化剂)、氨逃逸量低、可大幅减少SCR的反应容积；逃逸的氨会随烟气流向下游的SCR系统，使其利用率反应率更为完全，还原剂可使用尿素代替较危险的液氨；因而使得系统运行稳定性、经济性加强的同时，氨逃逸大大降低；本系统采用炉内脱硫结合炉外脱硫系统两级脱硫，增加了SO2排放的可控性，炉外脱硫还可回收具有一定经济价值的副产品(硫酸铵、石膏等)，降低了脱硫系统运行成本。Since this system uses high and low temperature dust removal devices for two-stage dust removal, the dust removal efficiency is higher; at the same time, the SCR device 22 is arranged in the outlet area of the high temperature dust collector 11, with less smoke and dust, better catalyst working environment and long service life; and SCR working smoke The temperature is still high, the catalyst is relatively mature, and the choice is large; the SNCR+SCR method has high denitrification efficiency (40-80%), slightly lower investment cost, slightly lower operating cost (reductant, a small amount of catalyst), low ammonia slip, It can greatly reduce the reaction volume of SCR; the escaped ammonia will flow to the downstream SCR system with the flue gas flow, making its utilization rate more complete, and the reductant can use urea instead of the more dangerous liquid ammonia; thus making the system stable and efficient While the economy is enhanced, the escape of ammonia is greatly reduced; this system adopts the two-stage desulfurization of the furnace desulfurization combined with the external desulfurization system, which increases the controllability of SO2 emissions, and the external desulfurization can also recover by-products with certain economic value (sulfuric acid ammonium, gypsum, etc.), which reduces the operating cost of the desulfurization system.
因而，本系统具有本系统具有脱硝效率高、脱硫效率高、系统可靠性高、工况适应性强、NOx、SO2排放可控性好、运行周期长、运行费用低等优点。Therefore, this system has the advantages of high denitrification efficiency, high desulfurization efficiency, high system reliability, strong adaptability to working conditions, good controllability of NO x and SO 2 emissions, long operation period, and low operation cost.
以上对本发明的一个实例进行了详细说明，但内容仅为本发明的较佳实施例，不能认为用于限定本发明的实施范围。凡依本发明申请范围所做出的变化与改进等，均应仍归属于本发明的保护涵盖范围之内。An example of the present invention has been described in detail above, but the content is only a preferred embodiment of the present invention, and cannot be considered as limiting the implementation scope of the present invention. All changes and improvements made according to the application scope of the present invention shall still belong to the scope of protection of the present invention.
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