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WO2016011682A1 - Équipement et procédé pour la désulfuration, la dénitration, la demercuration, et l'élimination simultanées de dioxines de gaz de combustion calcinés selon un procédé demi-sec faisant intervenir un lit fluidisé circulant - Google Patents

Équipement et procédé pour la désulfuration, la dénitration, la demercuration, et l'élimination simultanées de dioxines de gaz de combustion calcinés selon un procédé demi-sec faisant intervenir un lit fluidisé circulant Download PDF

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Publication number
WO2016011682A1
WO2016011682A1 PCT/CN2014/084111 CN2014084111W WO2016011682A1 WO 2016011682 A1 WO2016011682 A1 WO 2016011682A1 CN 2014084111 W CN2014084111 W CN 2014084111W WO 2016011682 A1 WO2016011682 A1 WO 2016011682A1
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WIPO (PCT)
Prior art keywords
flue gas
fluidized bed
circulating fluidized
ozone
bed reaction
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Ceased
Application number
PCT/CN2014/084111
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English (en)
Chinese (zh)
Inventor
朱廷钰
徐文青
赵瑞壮
叶猛
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Beijing Zstc Environmenyal Engineering Co Ltd
Institute of Process Engineering of CAS
Original Assignee
Beijing Zstc Environmenyal Engineering Co Ltd
Institute of Process Engineering of CAS
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Publication date
Application filed by Beijing Zstc Environmenyal Engineering Co Ltd, Institute of Process Engineering of CAS filed Critical Beijing Zstc Environmenyal Engineering Co Ltd
Publication of WO2016011682A1 publication Critical patent/WO2016011682A1/fr
Anticipated expiration legal-status Critical
Ceased legal-status Critical Current

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Classifications

    • 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
    • B01D53/46—Removing components of defined structure
    • B01D53/60—Simultaneously removing sulfur oxides and nitrogen oxides
    • 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
    • B01D53/46—Removing components of defined structure
    • B01D53/64—Heavy metals or compounds thereof, e.g. mercury
    • 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
    • B01D53/46—Removing components of defined structure
    • B01D53/68—Halogens or halogen compounds
    • B01D53/70—Organic halogen compounds
    • 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
    • B01D53/75—Multi-step processes
    • 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
    • Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
    • 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

Definitions

  • the invention belongs to the field of flue gas purification, and particularly relates to a sintering flue gas circulating fluidized bed semi-dry method combined with desulfurization, denitrification, mercury removal and dioxin device and method in the steel industry.
  • CN 102228788A discloses a synergistic removal method for the combined removal of S0 2 and dioxins, but does not consider the combined removal of nitrogen oxides.
  • CFB semi-dry method combined with desulfurization and denitrification based on oxidation method has found that it has good efficiency for desulfurization and denitrification, but it has poor effect on removal of mercury and dioxins.
  • New industry emission standards require that we must actively develop effective removal technologies for multiple pollutants. Summary of the invention
  • the present invention realizes simultaneous desulfurization and denitrification of the sintering flue gas by increasing the ozone oxidation process, and further realizes mercury removal by adding an activated carbon adsorbent (AC adsorbent).
  • AC adsorbent activated carbon adsorbent
  • an aspect of the present invention provides a device for synergistic desulfurization, denitrification, demercuration and deoxygenation of steel sintering flue gas.
  • a sintering flue gas circulating fluidized bed semi-dry method combined with desulfurization and denitration device the device comprises an ozone generator 2, a dilution fan 1, a mixing buffer tank 3, an ozone distributor 4 and a circulating fluidized bed reaction tower 12;
  • the ozone generator 2 and the dilution fan 1 are connected to the inlet of the mixing buffer tank 3;
  • the ozone distributor 4 is installed in the flue 4', and a connection port is provided outside the flue 4' to be connected to the outlet of the mixing buffer tank 3;
  • the flue gas inlet 5 of the circulating fluidized bed reaction column 12 is connected to a flue 4' in which the ozone distributor 4 is disposed.
  • the ozone distributor 4 enables the ozone generated by the ozone generator 2 to be evenly distributed in the flue, thereby maximizing the oxidation efficiency and reducing the ozone loss.
  • the ozone distributor can be manufactured by the prior art, as disclosed in the invention of the application No. 201410059167.5 or 201410066906.3.
  • the circulating fluidized bed reaction column therein may be simply referred to as a CFB reaction column.
  • the portion where the ozone distributor 4 is disposed is between the flue gas inlet 5 of the circulating fluidized bed reaction column 9
  • the distance of the flue 4' is 15 ⁇ 30 meters.
  • the upper outlet 13 of the circulating fluidized bed reaction column 12 is connected to the cyclone separator 14, and the cyclone separating hopper 15 is connected to the circulating fluidized bed reaction column 12 return port 18 through the air chute 16.
  • the cyclone separator 14 functions to separate the reacted Ca-based absorbent and the activated carbon adsorbent from the flue gas, and then return to the circulating fluidized bed reaction column 12 through the air chute 16 to continue to participate in the reaction.
  • the upper outlet 13 of the circulating fluidized bed reaction column 12 is tangentially connected to the cyclone 14.
  • the bottom of the circulating fluidized bed reaction tower 12 is a venturi structure, and the Venturi expansion section 19 is provided with a feed port, a return port 18 and a water spray gun 17, and the spray gun 17 nozzle is smoked. Installed in the downstream direction;
  • the feed port is provided as two 6, 7, respectively, a Ca-based absorbent feed port 6 and an activated carbon adsorbent feed port 7.
  • the cyclone separator 14 is coupled to the baghouse 20, the baghouse 20 is connected to the ash bin 21, the ash bin 21 is provided with two outlets, and the first outlet 22 is fluidized by a pneumatic conveying pipe.
  • the bed reaction tower 12 is connected to the feed port 18, and the purpose of the bag filter 20 is to stabilize the bed pressure and achieve further recycling of the absorbent.
  • the second outlet 23 is connected to the ash store 24 to realize the outer row.
  • the baghouse 20 is provided with a chimney 25 to discharge flue gas after removing a plurality of contaminants.
  • the flue gas is further removed by the bag filter 20 and discharged into the atmosphere via the bacon 25.
  • Another object of the present invention is to provide a method for removing multi-contaminants by the above-mentioned circulating fluidized bed semi-dry method combined with desulfurization, denitration and mercury removal dioxin removal device, the method comprising the following steps:
  • step 1) the specific process of step 1) is: the ozone generated by the ozone generator 2 is uniformly mixed in the mixing buffer tank 3 by the dilution fan 1, and is sprayed into the flue 4' through the ozone distributor 4, and the smell is sprayed. Sufficient contact with the flue gas oxygen reaction, some or all of the flue gas NO is oxidized to NO X high state, S0 2 will also be partially oxidized to S0 3;
  • the molar ratio of the ozone injected in the step 1) to the NO in the flue gas is 0.25 to 1.2, for example, 0.26 to 1.49, 0.45-1.15, 0.55 to 1.05, etc.; and the reaction time is 0.5 to 5 s, For example, 0.6 to 4.9 s, 1.0 to 3.5 s, 1.5 to 2.5 s, 2 s, etc. may be selected;
  • Step 2) The Ca-based absorbent has a Ca/(S+N) molar ratio of 1.1 to 2.0, for example, 1.11 to 1.96. 1.3 to 1.8, 1.42-1.67, 1.53, etc., preferably a ratio of 1.2 to 1.5.
  • the reacted Ca-based absorbent and activated carbon adsorbent are separated by a cyclone separator 14 and returned to the circulating fluidized bed reaction column 12 through the air chute 16 to achieve multiple cycles, and the flue gas passes through the baghouse 20 After the dust is further removed and discharged into the atmosphere, the dust collected by the baghouse 20 is returned to the circulating fluidized bed reaction column 12 by pneumatic conveying, which can stabilize the bed pressure and achieve further circulation of the absorbent.
  • the water spray amount of the water spray gun (14) is adjusted to control the temperature of the flue gas in the circulating fluidized bed reaction tower (9) above the acid dew point, generally 75 to 80°. C, for example, 76 ° C, 79 ° C, 82 ° C, 84 ° C, etc.; by adjusting the circulating return amount of the air chute (13), controlling the pressure difference between the inlet and outlet of the circulating fluidized bed reaction column (9),
  • the particle concentration in the control tower satisfies the above Ca/(S+N) molar ratio requirement.
  • the invention adjusts the water spray amount according to the flue gas temperature of the outlet 13 of the circulating fluidized bed reaction tower 12, and ensures that the temperature in the circulating fluidized bed reaction tower tower is maintained above the flue gas dew point.
  • the added activated carbon adsorbent is added in a mass ratio of Ca-based absorbent to activated carbon adsorbent of 15:1-25:1, and the mass ratio may be selected from 15.1:1-24.9:1, 16 :1-24:1, 17.5:1-22.5:1, 19:1-21:1, 20:1.
  • the invention can control the Hg and dioxin pollutants in the flue gas after the treatment by controlling the addition amount of the Ca-based absorbent to control the concentration of sulfur oxides and nitrogen oxides in the flue gas after treatment and adjusting the addition amount of the activated carbon adsorbent. concentration.
  • the present invention has the following advantages:
  • the cyclone separator 14 and the bag filter 20 collect the material and return it to the absorption tower 12, thereby realizing the extra-column circulation of the absorber, thereby improving the utilization efficiency of the absorbent.
  • Figure 1 is a process flow diagram of the present invention
  • Sintering flue gas circulating fluidized bed semi-dry method synergistic desulfurization denitrification demercuration deoxygenation dioxin device characterized in that the device comprises ozone generator 2, mixing buffer tank 3, ozone distributor 4 and circulating fluidized bed reaction Tower 12;
  • the ozone generator 2 and the dilution fan 1 are connected to the inlet of the mixing buffer tank 3;
  • the ozone distributor 4 is installed in the flue 4', and a connection port is provided outside the flue 4' to be connected to the outlet of the mixing buffer tank 3;
  • the flue gas inlet 5 of the circulating fluidized bed reaction column is connected to the flue 4' where the ozone distributor 4 is disposed, preferably, the portion where the ozone distributor 4 is disposed and the flue gas inlet 5 of the circulating fluidized bed reaction column 12
  • the distance of the road is 15 ⁇ 30 meters;
  • the circulating fluidized bed reaction column upper outlet 13 is connected to the cyclone separator 14, and the cyclone separating hopper 15 is connected to the circulating fluidized bed reaction column 12 return port 18 through the air chute 16; preferably, The upper outlet 13 of the circulating fluidized bed reaction column 12 is tangentially connected to the cyclone separator 14;
  • the cyclone separator 14 is connected to the baghouse 20, the baghouse 20 is connected to the ash bin 21, the ash bin 21 is provided with two outlets, and the first outlet 22 is passed through the pneumatic conveying pipe and the circulating fluidized bed reaction tower 12
  • the material port 18 is connected, the second outlet 23 is connected to the ash store 24; the bag filter 20 is provided with a chimney 25 to discharge the flue gas after removing a plurality of pollutants;
  • the bottom of the circulating fluidized bed reaction tower 12 is a venturi structure, and the venturi expansion section 19 is provided with a feed port, a return port 18 and a water spray gun 17, and the nozzle of the water spray gun 17 follows the direction of the flue gas.
  • the feed port is provided as two 6, 7, one is a Ca-based absorbent feed port 6, and the other is an activated carbon sorbent feed port 7.
  • the method for desulfurization, denitrification, mercury removal and deodorization using the above-mentioned sintering flue gas simultaneous desulfurization and denitration device comprises the following steps:
  • the ozone generated by the ozone generator 2 and the dilution wind generated by the dilution fan 1 are mixed into the mixing buffer tank 3, and then injected into the flue 4' through the ozone distributor 4, and the injected ozone is in full contact with the flue gas, mainly the flue gas.
  • the NO X NO oxidation reaction, smoke and CFB oxidized fluidized Ca-based activated carbon adsorbent and absorbent valency to achieve a variety of pollutants SO x, NO x, Hg and dioxin, etc.
  • the flue gas after the reaction entrains a certain amount of solid particles, and the dust is collected twice by the cyclone separator 14 and the bag filter 20, and then the flue gas is discharged through the bacon 25, and the ash collected by the cyclone 14 is returned to the circulation.
  • the fluidized bed reaction column 12, the dust portion under the baghouse 20 is returned to the circulating fluidized bed reaction column 12.
  • the removal of the sintering flue gas synergistic desulfurization, denitrification, mercury removal and dioxin removal apparatus as described above includes the following steps:
  • the ozone generated by the ozone generator 2 and the dilution wind generated by the dilution fan 1 enter the mixing buffer tank 3 Line mixed, then distribution of ozone injected into the flue 4 4 ', ozone injected into full contact with the flue gas, primarily oxidizes NO to NO X in the flue gas valency, smoke and oxidized fluidized CFB the activated carbon adsorbent, and Ca-based sorbent reacts synergies removing more contaminants SO x, NO x, Hg and dioxin and other flue gas reaction after a certain amount of solid particles entrained by the cyclone 14 and the bag filter 20 collects the dust twice and then discharges the clean flue gas through the bacon 25, and the ash collected by the cyclone 14 is returned to the reaction tower 12, and the dust portion under the precipitator 20 is returned to the reaction tower 12.
  • the distance between the portion where the ozone distributor 4 is disposed and the flue gas inlet 5 of the CFB reaction tower is set to 30 m, and the molar ratio of ozone generated by the ozone generator 2 to NO in the flue gas is 0.6, and the reaction is 0.5.
  • control the amount of lime slurry injected Ca / (S + N) molar ratio is 1.5, the mass ratio of added Ca-based absorbent to activated carbon adsorbent is 15:1, desulfurization efficiency can reach more than 90%, denitration efficiency can be More than 50%, dioxin-like pollutant removal efficiency ⁇ 80%, heavy metal removal efficiency ⁇ 90%.
  • the removal of the sintering flue gas synergistic desulfurization, denitrification, mercury removal and dioxin removal apparatus as described above includes the following steps:
  • the ozone generated by the ozone generator 2 and the dilution wind generated by the dilution fan 1 are mixed into the mixing buffer tank 3, and then injected into the flue 4' through the ozone distributor 4, and the injected ozone is in full contact with the flue gas, mainly the flue gas.
  • the NO X NO oxidation reaction, smoke and CFB oxidized fluidized Ca-based activated carbon adsorbent and absorbent valency to achieve a variety of pollutants SO x, NO x, Hg and dioxin, etc.
  • the flue gas after the reaction entrains a certain amount of solid particles, and the dust is collected twice by the cyclone separator 14 and the bag filter 20, and then the flue gas is discharged through the bacon 25, and the ash collected by the cyclone 14 is returned to the reaction.
  • the dust portion under the dust remover 20 is returned to the reaction tower 12.
  • the distance between the portion where the ozone distributor 4 is disposed and the flue gas inlet 5 of the CFB reaction tower is set to 15 meters, and the molar ratio of ozone generated by the ozone generator 2 to NO in the flue gas is 1.0, 3s, control the amount of lime slurry injected Ca / (S + N) molar ratio is 1.2, the mass ratio of added Ca-based absorbent to activated carbon adsorbent is 25: 1, desulfurization efficiency can reach more than 90%, denitration efficiency can be More than 90%, dioxin-like pollutant removal efficiency ⁇ 80%, heavy metal removal efficiency ⁇ 90%.
  • the removal of the sintering flue gas synergistic desulfurization, denitrification, mercury removal and dioxin removal apparatus as described above includes the following steps:
  • the ozone generated by the ozone generator 2 and the dilution wind generated by the dilution fan 1 are mixed into the mixing buffer tank 3, and then injected into the flue 4' through the ozone distributor 4, and the injected ozone is in full contact with the flue gas, mainly the flue gas.
  • the NO X NO oxidation reaction, smoke and CFB oxidized fluidized Ca-based activated carbon adsorbent and absorbent valency to achieve a variety of pollutants SO x, NO x, Hg and dioxin, etc.
  • the flue gas after the reaction entrains a certain amount of solid particles, and the dust is collected twice by the cyclone separator 14 and the bag filter 20, and then the flue gas is discharged through the bacon 25, and the ash collected by the cyclone 14 is returned to the reaction.
  • the dust portion under the dust remover 20 is returned to the reaction tower 12.
  • the distance between the portion where the ozone distributor 4 is disposed and the flue gas inlet 5 of the CFB reaction tower is set to 20 meters, and the molar ratio of ozone generated by the ozone generator 2 to NO in the flue gas is 0.25, and the reaction is 5 seconds.
  • the Ca/(S+N) molar ratio of the injected lime slurry is 2.0, the mass ratio of the added Ca-based absorbent to the activated carbon adsorbent is 20:1, the desulfurization efficiency is over 90%, and the denitration efficiency is up to More than 20%, the removal efficiency of dioxin pollutants is ⁇ 80%, and the removal efficiency of heavy metals is ⁇ 90%.
  • the removal of the sintering flue gas synergistic desulfurization, denitrification, mercury removal and dioxin removal apparatus as described above includes the following steps:
  • the ozone generated by the ozone generator 2 is mixed with the dilution wind generated by the dilution fan 1 into the mixing buffer tank 3, and then injected into the flue 4' through the ozone distributor 4, and the injected ozone is in full contact with the flue gas.
  • the distance between the portion where the ozone distributor 4 is disposed and the flue gas inlet 5 of the CFB reaction tower is set to 25 m, and the molar ratio of the ozone generated by the ozone generator 2 to the NO in the flue gas is 1.5, and the reaction is 2.5.
  • control the amount of lime slurry injected Ca / (S + N) molar ratio is 1.1, the mass ratio of the added Ca-based absorbent to the activated carbon adsorbent is 22:1, the desulfurization efficiency can reach more than 90%, the denitration efficiency can be More than 90%, dioxin-like pollutant removal efficiency ⁇ 80%, heavy metal removal efficiency ⁇ 90%.
  • the present invention illustrates the detailed structural features of the present invention and the desulfurization and denitration method by the above embodiments, but the present invention is not limited to the above detailed structural features and the contaminant removal method, that is, does not mean that the present invention must rely on the above. Detailed structural features and removal methods can be implemented. It will be apparent to those skilled in the art that any modifications of the present invention, equivalent substitutions of the components selected for the present invention, and the addition of the components, the selection of the specific means, and the like, are all within the scope of the present invention.

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  • Chemical & Material Sciences (AREA)
  • Environmental & Geological Engineering (AREA)
  • Health & Medical Sciences (AREA)
  • Biomedical Technology (AREA)
  • Analytical Chemistry (AREA)
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  • Oil, Petroleum & Natural Gas (AREA)
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Abstract

L'invention concerne un équipement et un procédé pour la désulfuration, la dénitration, la demercuration, et l'élimination simultanées de dioxines de gaz de combustion calcinés selon un procédé demi-sec faisant intervenir un lit fluidisé circulant, comprenant un générateur d'ozone (2), un ventilateur de dilution (1), un réservoir tampon de mélange (3), un distributeur d'ozone (4), et une tour de réacteur à lit fluidisé circulant (12). Un gaz de combustion oxydé par de l'ozone est introduit dans la tour de réacteur à lit fluidisé circulant (12), l'élimination de SOx et de NOx est assurée par un absorbant à base de Ca sous l'action d'eau atomisée, et des contaminants de type Hg et dioxines dans les gaz de combustion sont éliminés par un adsorbant à charbon actif, ce qui permet de mettre en oeuvre une désulfuration, une dénitration, une demercuration, et une élimination simultanées des dioxines. Le système de l'invention est ainsi caractérisé par sa simplicité, sa grande efficacité, son faible encombrement, des investissements peu onéreux et en ce qu'il promet des perspectives d'application considérables dans l'industrie de l'acier.
PCT/CN2014/084111 2014-07-21 2014-08-11 Équipement et procédé pour la désulfuration, la dénitration, la demercuration, et l'élimination simultanées de dioxines de gaz de combustion calcinés selon un procédé demi-sec faisant intervenir un lit fluidisé circulant Ceased WO2016011682A1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
CN201410347320.4 2014-07-21
CN201410347320.4A CN104107627A (zh) 2014-07-21 2014-07-21 一种烧结烟气循环流化床半干法联合脱硫脱硝脱汞脱二恶英装置及方法

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WO2016011682A1 true WO2016011682A1 (fr) 2016-01-28

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CN (1) CN104107627A (fr)
WO (1) WO2016011682A1 (fr)

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CN104984656B (zh) * 2015-06-23 2017-05-24 哈尔滨工业大学 多级内循环半干法脱硫脱硝脱汞一体化装置
CN105716436A (zh) * 2016-03-24 2016-06-29 南通万达锅炉有限公司 矿热炉窑余热回收系统
CN105805715A (zh) * 2016-03-24 2016-07-27 南通万达锅炉有限公司 调温式余热锅炉
CN105771612A (zh) * 2016-05-03 2016-07-20 湖北思搏盈环保科技股份有限公司 一种高污染因子低温烟气环保综合治理系统及工艺
CN108970373A (zh) * 2017-05-31 2018-12-11 江苏康洁环境工程有限公司 用于化工行业尾气多污染物脱除装置及其脱除方法
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CN108144412B (zh) * 2018-02-05 2024-03-08 山东大学 粉末活性焦双循环联合臭氧氧化脱硫脱硝的装置及方法
CN110882616A (zh) * 2019-12-06 2020-03-17 唐山市德龙钢铁有限公司 一种烧结烟气低温一体化脱硫脱硝系统
CN112111302B (zh) * 2020-09-28 2022-07-01 山东祥桓环境科技有限公司 一种低阶物料气化燃烧协同烟气污染物控制一体化工艺及装置与应用
CN113813783A (zh) * 2021-10-20 2021-12-21 北京龙电宏泰环保科技有限公司 一种工业锅炉排放有机污染物前驱体及气溶胶和酸性气体协同脱除的方法
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