WO2016011682A1 - Equipment and method for circulating fluidized bed semidry simultaneous desulfurization, denitration, demercuration, and removal of dioxins of sintering flue gas - Google Patents

Equipment and method for circulating fluidized bed semidry simultaneous desulfurization, denitration, demercuration, and removal of dioxins of sintering flue gas Download PDF

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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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flue gas
fluidized bed
circulating fluidized
ozone
bed reaction
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PCT/CN2014/084111
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French (fr)
Chinese (zh)
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朱廷钰
徐文青
赵瑞壮
叶猛
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中国科学院过程工程研究所
北京正实同创环境工程科技有限公司
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Priority to CN201410347320.4A priority Critical patent/CN104107627A/en
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Publication of WO2016011682A1 publication Critical patent/WO2016011682A1/en

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    • BPERFORMING OPERATIONS; TRANSPORTING
    • B01PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01DSEPARATION
    • B01D53/00Separation 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
    • B01D53/34Chemical or biological purification of waste gases
    • B01D53/46Removing components of defined structure
    • B01D53/60Simultaneously removing sulfur oxides and nitrogen oxides
    • BPERFORMING OPERATIONS; TRANSPORTING
    • B01PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01DSEPARATION
    • B01D53/00Separation 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
    • B01D53/34Chemical or biological purification of waste gases
    • B01D53/46Removing components of defined structure
    • B01D53/64Heavy metals or compounds thereof, e.g. mercury
    • BPERFORMING OPERATIONS; TRANSPORTING
    • B01PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01DSEPARATION
    • B01D53/00Separation 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
    • B01D53/34Chemical or biological purification of waste gases
    • B01D53/46Removing components of defined structure
    • B01D53/68Halogens or halogen compounds
    • B01D53/70Organic halogen compounds
    • BPERFORMING OPERATIONS; TRANSPORTING
    • B01PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01DSEPARATION
    • B01D53/00Separation 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
    • B01D53/34Chemical or biological purification of waste gases
    • B01D53/74General processes for purification of waste gases; Apparatus or devices specially adapted therefor
    • B01D53/75Multi-step processes
    • YGENERAL 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
    • Y02TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02ATECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
    • Y02A50/00TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE in human health protection, e.g. against extreme weather
    • Y02A50/20Air quality improvement or preservation, e.g. vehicle emission control or emission reduction by using catalytic converters

Abstract

Equipment and a method for circulating fluidized bed semidry simultaneous desulfurization, denitration, demercuration, and removal of dioxins of a sintering flue gas, comprising an ozone generator (2), a diluting blower (1), a mixing buffer tank (3), an ozone distributor (4), and a circulating fluidized bed reactor tower (12). A flue gas oxidized by ozone is introduced into the circulating fluidized bed reactor tower (12), removal of SOx and NOx is implemented by a Ca-based absorbent under the action of atomized water, and contaminants such as Hg and dioxins in the flue gas are removed by an activated carbon adsorbent, thus implementing simultaneous desulfurization, denitration, demercuration, and removal of the dioxins. This provides the characteristics of a simple system, great performance, small footprint, and inexpensive investments and provides very considerable application prospects in the steel industry.

Description

说 明 书 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 技术领域  Semi-dry method combined with desulfurization, denitrification, mercury removal and dioxin device and method for sintering flue gas circulation fluidized bed
本发明属于烟气净化领域, 具体涉及钢铁行业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。  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.
背景技术 Background technique
钢铁行业尾气排放污染物多种多样, 而且各种污染物均居行业排放前列, 据报道, 钢铁行业排放的 802和 NOx中 50%以上, 及 90%二恶英排放来自烧结 工序。 "十二五" 刚颁布的 《钢铁烧结、 球团工业大气污染物排放标准》 对各 种污染物的排放标准大幅度提高, 对烧结烟气污染治理提出了新的要求, 由原 来对粉尘、 二氧化硫(S02)两种单一污染物的治理, 变为对多种污染物的综合 治理, 因此针对烧结烟气中多种污染物的联合脱除技术与装置便有了迫切需 要。 Steel industry pollutant emissions varied, and emission of various pollutants rank the forefront of the industry, it was reported that more than 50%, 90% and 802 dioxin and NO x emissions from the steel industry in the sintering step. The "Twelfth Five-Year Plan" just issued the "Steel Sintering, Pellet Industry Air Pollutant Emission Standards" has greatly improved the discharge standards for various pollutants, and put forward new requirements for the treatment of sintering flue gas pollution, from the original dust, The treatment of two single pollutants of sulfur dioxide (S0 2 ) has become a comprehensive treatment of various pollutants. Therefore, there is an urgent need for a joint removal technology and device for various pollutants in sintering flue gas.
目前, 国内用于同时脱除多种钢铁烧结烟气中多种污染物的技术非常稀 缺, 现有技术多集中于单独脱硫、 脱硝, 或者联合脱硫脱硝, 对联合脱汞、 脱 二恶英等技术更是罕见。 如 CN 102228788A公布了一种联合脱除 S02和二恶英 的协同脱除方法, 但并未考虑氮氧化物的联合脱除。 目前针对基于氧化法的 CFB半干法联合脱硫脱硝拓展研究中发现, 对脱硫脱硝有很好的效率, 但对于 汞、 二恶英等脱除效果很差。 新的行业排放标准要求我们必须积极开发多种污 染物的有效脱除技术。 发明内容 At present, the domestic technology for simultaneously removing a variety of pollutants in various steel sintering flue gases is very scarce. The prior art is mostly focused on single desulfurization, denitrification, or combined desulfurization and denitrification, on combined mercury removal, de-dioxin, etc. Technology is even rarer. For example, 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. At present, the 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
针对以上提到的技术不足, 为突破现有烧结烟气单独或两种联合脱除技 术, 在现有循环流化床半干法脱硫性能基础上, 本发明通过增加臭氧氧化过程 实现烧结烟气的同时脱硫脱硝, 并通过添加活性炭吸附剂 (AC吸附剂 ), 进一步 实现了脱汞脱二恶英的目的, 本发明的一方面提供了一种用于钢铁烧结烟气协 同脱硫脱硝脱汞脱二恶英装置。 In view of the above-mentioned technical deficiencies, in order to break through the existing sintering flue gas alone or in combination On the basis of the existing semi-dry desulfurization performance of the circulating fluidized bed, 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). For the purpose of dedioxining, an aspect of the present invention provides a device for synergistic desulfurization, denitrification, demercuration and deoxygenation of steel sintering flue gas.
为达上述目的, 本发明采用如下技术方案:  In order to achieve the above object, the present invention adopts the following technical solutions:
一种烧结烟气循环流化床半干法联合脱硫脱硝装置, 所述装置包括臭氧发 生器 2、 稀释风机 1、 混合缓冲罐 3、 臭氧分布器 4以及循环流化床反应塔 12; 所述臭氧发生器 2和稀释风机 1与混合缓冲罐 3的入口相连;  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;
所述臭氧分布器 4安装在烟道 4' 中, 在烟道 4' 外部设置连接口, 与混合 缓冲罐 3的出口相连;  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;
所述循环流化床反应塔 12的烟气进口 5与布置有臭氧分布器 4的烟道 4' 相连。 臭氧分布器 4能够使臭氧发生器 2产生的臭氧均匀分布于烟道内, 最大 程度地提高氧化效率, 减少臭氧损失。 所述的臭氧分布器可以采用现有技术如 申请号为 201410059167.5或 201410066906.3的发明所公开的技术制造的。  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.
其中的循环流化床反应塔可简称为 CFB反应塔。  The circulating fluidized bed reaction column therein may be simply referred to as a CFB reaction column.
烧结烟气进入烟道 4' 后, 被臭氧发生器 2产生的臭氧气体所氧化, 烟气 中的部分或全部 NO被氧化为高价态的 NOx, 部分 S02同时也会被氧化为 S03, 氧化后的烟气通过循环流化床反应塔 12烟气进口 5进入循环流化床反应塔 12 内, 由 Ca基吸收剂在雾化水的作用下对烟气中的 S02、 SO P高价态 NOx进行 反应脱除。 After sintering flue gas into the flue 4 ', are oxidized by ozone gas generated by an ozone generator 2, 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 oxidized flue gas enters the circulating fluidized bed reaction tower 12 through the flue gas inlet 5 of the circulating fluidized bed reaction tower 12, and the S0 2 and SO P in the flue gas are caused by the Ca-based absorbent under the action of the atomized water. valence state the NO x removal reaction.
烟气中各种形态的 Hg和二恶英类等污染物主要与活性炭吸附剂进行反应 实现脱除的目的。  Various forms of Hg and dioxin in the flue gas react with the activated carbon adsorbent to achieve the purpose of removal.
优选地, 布置臭氧分布器 4的部位与循环流化床反应塔 9的烟气进口 5间 的烟道 4' 距离为 15〜30米。 Preferably, 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.
对于本发明的装置, 所述循环流化床反应塔 12上部出口 13与旋风分离器 14连接, 旋风分离器分离料斗 15通过空气斜槽 16与循环流化床反应塔 12回 料口 18连接。  For the apparatus of the present invention, 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.
旋风分离器 14的作用是将反应后的 Ca基吸收剂和活性炭吸附剂与烟气分 离后, 通过空气斜槽 16返回循环流化床反应塔 12内, 继续参与反应。  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.
优选地,所述循环流化床反应塔 12上部出口 13与旋风分离器 14切向连接。 对于本发明的装置,所述循环流化床反应塔 12底部为文丘里结构, 文丘里 扩张段 19设置有进料口、 回料口 18及喷水喷枪 17, 喷水喷枪 17喷嘴依烟气 顺流方向安装;  Preferably, the upper outlet 13 of the circulating fluidized bed reaction column 12 is tangentially connected to the cyclone 14. For the apparatus of the present invention, 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;
优选地, 进料口设置为两个 6、 7, 分别为 Ca基吸收剂进料口 6和活性炭 吸附剂进料口 7。  Preferably, 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.
对于本发明的装置, 所述旋风分离器 14与布袋除尘器 20连接, 布袋除尘 器 20料斗与灰仓 21相连, 灰仓 21设置两个出口, 第一出口 22通过气力输送 管道与循环流化床反应塔 12回料口 18连接, 布袋除尘器 20返料的目的是稳定 床压和实现吸收剂的进一步循环利用, 第二出口 23与灰库 24相连,实现外排。  For the apparatus of the present invention, 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.
优选地, 所述布袋除尘器 20后设有烟囱 25, 以排放脱除多种污染物后的 烟气。 所述烟气通过布袋除尘器 20进一步除尘后经烟肉 25排入大气。  Preferably, 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.
本发明的目的之二在于提供一种由上述的循环流化床半干法联合脱硫脱硝 脱汞脱二恶英装置进行多污染物脱除的方法, 所述方法包括以下步骤:  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:
1 ) 向烟道 4' 中喷入臭氧, 使臭氧与烟气反应;  1) spraying ozone into the flue 4' to react the ozone with the flue gas;
优选地, 步骤 1 ) 的具体过程为: 臭氧发生器 2产生的臭氧在稀释风机 1 的作用下在混合缓冲罐 3混合均匀, 经臭氧分布器 4喷入烟道 4' , 喷入的臭 氧与烟气充分接触反应, 烟气中的部分或全部 NO被氧化为高价态的 NOx, 部 分 S02同时也会被氧化为 S03 ; Preferably, 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;
2) 氧化后的烟气送入循环流化床反应塔 12, 烟气中的 S02、 S03、 和 NOx 在反应塔 12中主要与 Ca基吸收剂在雾化水的作用下进行反应脱除; 2) the oxidized flue gas fed to the circulating fluidized bed reaction tower 12, the flue gas S0 2, S0 3, and the Ca-based NO x absorbent is atomized under the action of the reaction of water in the reaction column 12 mainly Remove
3 ) 烟气中各种形态的 Hg和二恶英类等污染物主要与活性炭吸附剂进行反 应进行脱除。  3) Various forms of Hg and dioxins in the flue gas are mainly reacted with activated carbon adsorbents for removal.
对于本发明的方法,步骤 1 )喷入的臭氧与烟气中 NO的摩尔比为 0.25〜1.2, 例如可选择 0.26〜1.49, 0.45-1.15 , 0.55〜1.05等;反应的时间为 0.5〜5s, 例如可 选择 0.6〜4.9s, 1.0〜3.5s, 1.5〜2.5s, 2s等; 步骤 2) 所述 Ca基吸收剂按照 Ca/ ( S+N)摩尔比 1.1〜2.0, 例如为 1.11〜1.96, 1.3〜1.8, 1.42-1.67, 1.53等, 优选 1.2〜1.5的比例力口入。  For the method of the present invention, 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.
对于本发明的方法, 反应后的 Ca基吸收剂和活性炭吸附剂经旋风分离器 14分离后通过空气斜槽 16返入循环流化床反应塔 12实现多次循环, 烟气经过 布袋除尘器 20进一步除去粉尘后排入大气, 布袋除尘器 20收集的粉尘部分通 过气力输送返回循环流化床反应塔 12, 可以稳定床压和实现吸收剂的进一步循 环。  For the method of the present invention, 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.
对于本发明的方法, 步骤 2) 中通过调节喷水喷枪 (14 ) 喷水量, 以控制 循环流化床反应塔 (9) 内的烟气温度在酸露点以上, 一般可为 75〜80°C, 例如 为 76°C、 79°C、 82°C、 84°C等; 通过调节空气斜槽 (13 ) 的循环回料量, 控制 循环流化床反应塔(9 )进出口压差,而控制塔内颗粒浓度,满足上述的 Ca/( S+N) 摩尔比要求。  For the method of the present invention, in step 2), 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.
本发明根据循环流化床反应塔 12出口 13烟气温度来调节喷水量, 保证循 环流化床反应塔塔内温度保持在烟气露点以上。 优选地, 步骤 3)所述添加的活性炭吸附剂按照 Ca基吸收剂与活性炭吸附 剂的质量比为 15:1-25:1 加入, 所述质量比可选择 15.1:1-24.9:1, 16:1-24:1, 17.5:1-22.5:1, 19:1-21:1, 20:1。 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. Preferably, in step 3), 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.
本发明可以分别通过调节 Ca基吸收剂的加入量控制处理后烟气中的硫氧 化物和氮氧化物浓度和调节活性炭吸附剂的加入量控制处理后烟气中的 Hg和 二恶英污染物的浓度。 与已有技术方案相比, 本发明具有以下优点:  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. Compared with the prior art solutions, the present invention has the following advantages:
1) 系统简单、 占地面积小, 投资和运行费用较低。  1) The system is simple, the floor space is small, and the investment and operating costs are low.
2)通过增加臭氧氧化剂和活性炭吸附剂, 实现了 SOx、 NOx、 Hg和二恶英 等多种污染物的协同脱除。 2) by adding activated carbon adsorbent and an ozone oxidant, to achieve a synergistic removal of more contaminants SO x, NO x, Hg and dioxins.
3) 旋风分离器 14和布袋除尘器 20收集物料的返入吸收塔 12, 实现了吸 收剂的塔外循环, 提高了吸收剂的利用效率。  3) 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.
4) 对 S02、 NO、 Hg 和二恶英等都具有较高的脱除效率。 操作条件优良 时, 烟气循环流化床半干法技术脱硫效率可达 90%以上; 烟气中的 NO被 03 氧化速率非常快, 脱硝效率可以达 80%以上; 二恶英类污染物脱除效率 >70%; 重金属脱除效率≥90%。 附图说明 4) High removal efficiency for S0 2 , NO, Hg and dioxins. When good operating condition, the desulfurization efficiency CFB technology semidry up to 90%; NO in the flue gas 03 is oxidized very fast rate, the denitration efficiency can be more than 80%; dioxins Removal efficiency >70%; heavy metal removal efficiency ≥90%. DRAWINGS
图 1是本发明的工艺流程图;  Figure 1 is a process flow diagram of the present invention;
图中: 1-稀释风机; 2-臭氧发生器; 3-混合缓冲罐; 4-臭氧分布器; 4'-烟道; 5-循环流化床反应塔底部进口; 6-Ca基吸收剂进料口; 7-活性炭吸附剂仓; 8- 螺旋输送器; 9-Ca基吸收剂仓; 10-螺旋输送器; 11-AC基吸收剂仓; 12-循环 流化床反应塔; 13-循环流化床反应塔上部出口; 14-旋风分离器; 15-旋风分离 器料斗; 16-空气斜槽; 17-喷水喷枪; 18-回料口; 19-文丘里扩张段; 20-布袋除 尘器; 21灰仓; 22-第一出口; 23-第二出口; 24-灰库; 25-烟囱。 In the figure: 1-diluted fan; 2-ozone generator; 3-mixed buffer tank; 4-ozone distributor; 4'-flue; 5-cycle fluidized bed reactor bottom inlet; 6-Ca-based absorbent Slurry; 7-activated carbon adsorbent silo; 8-spiral conveyor; 9-Ca-based absorbent cartridge; 10-screw conveyor; 11-AC-based absorbent cartridge; 12-cycle Fluidized bed reaction column; 13-circulating fluidized bed reaction column upper outlet; 14-cyclone separator; 15- cyclone separator hopper; 16-air chute; 17-water spray gun; 18-return port; Venturi expansion section; 20-bag duster; 21 ash silo; 22-first exit; 23-second exit; 24-ash ash; 25-chimney.
下面对本发明进一步详细说明。 但下述的实例仅仅是本发明的简易例子, 并不代表或限制本发明的权利保护范围,本发明的保护范围以权利要求书为准。 具体实舫式  The invention is further described in detail below. However, the following examples are merely illustrative of the invention and are not intended to limit the scope of the invention. The scope of the invention is defined by the claims. Concrete implementation
为便于理解本发明, 本发明列举实施例如下。 本领域技术人员应该明了, 所述实施例仅仅用于帮助理解本发明, 不应视为对本发明的具体限制。 实施方式  In order to facilitate the understanding of the present invention, the present invention is exemplified by the following. It should be understood by those skilled in the art that the present invention is only to be construed as a Implementation
一种烧结烟气循环流化床半干法协同脱硫脱硝脱汞脱二恶英装置, 其特征 在于, 所述装置包括臭氧发生器 2、 混合缓冲罐 3、 臭氧分布器 4以及循环硫化 床反应塔 12;  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;
所述臭氧发生器 2和稀释风机 1与混合缓冲罐 3的入口相连;  The ozone generator 2 and the dilution fan 1 are connected to the inlet of the mixing buffer tank 3;
所述臭氧分布器 4安装在烟道 4' 中, 在烟道 4' 外部设置连接口, 与混合 缓冲罐 3的出口相连;  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;
循环流化床反应塔的烟气进口 5与布置有臭氧分布器 4的烟道 4' 相连, 优选地,布置臭氧分布器 4的部位与循环硫化床反应塔 12的烟气进口 5间 的烟道距离为 15〜30米;  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;
优选地, 所述循环流化床反应塔上部出口 13与旋风分离器 14连接, 旋风 分离器分离料斗 15通过空气斜槽 16与循环流化床反应塔 12回料口 18连接; 优选地,所述循环流化床反应塔 12上部出口 13与旋风分离器 14切向连接; 优选地,旋风分离器 14与布袋除尘器 20连接, 布袋除尘器 20料斗与灰仓 21相连, 灰仓 21设置两个出口, 第一出口 22通过气力输送管道与循环流化床 反应塔 12回料口 18连接, 第二出口 23与灰库 24相连; 布袋除尘器 20后设有 烟囱 25, 以排放脱除多种污染物后的烟气; Preferably, 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; Preferably, 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;
优选地, 所述循环流化床反应塔 12底部为文丘里结构, 文丘里扩张段 19 设置有进料口、 回料口 18及喷水喷枪 17, 喷水喷枪 17喷嘴依烟气顺流方向安 优选地,进料口设置为两个 6、 7, 一个为 Ca基吸收剂进料口 6, 另一个为 活性炭吸附剂进料口 7。  Preferably, 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. Preferably, 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.
采用上述烧结烟气同时脱硫脱硝装置进行脱硫脱硝脱汞脱二恶英的方法包 括如下步骤:  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:
臭氧发生器 2产生的臭氧与稀释风机 1发生的稀释风进入混合缓冲罐 3进 行混合, 然后经臭氧分布器 4喷入烟道 4' , 喷入的臭氧与烟气充分接触, 主 要将烟气中的 NO氧化为高价态的 NOx, 氧化后的烟气与 CFB中流化的 Ca基 吸收剂和活性炭吸附剂发生反应, 实现 SOx、 NOx、 Hg和二恶英等多种污染物 的协同脱除, 反应后的烟气夹带一定量的固体颗粒, 经旋风分离器 14 和布袋 除尘器 20两次收集粉尘后通过烟肉 25排出干净烟气, 旋风分离器 14收集的灰 全部返回循环流化床反应塔 12, 布袋除尘器 20下的粉尘部分返回循环流化床 反应塔 12。 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. Synergistic removal, 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.
实施例 1  Example 1
采用如上所述的烧结烟气协同脱硫脱硝脱汞脱二恶英装置进行脱除, 包括 如下步骤:  The removal of the sintering flue gas synergistic desulfurization, denitrification, mercury removal and dioxin removal apparatus as described above includes the following steps:
臭氧发生器 2产生的臭氧与稀释风机 1发生的稀释风进入混合缓冲罐 3进 行混合, 然后经臭氧分布器 4喷入烟道 4' , 喷入的臭氧与烟气充分接触, 主 要将烟气中的 NO氧化为高价态的 NOx, 氧化后的烟气与 CFB中流化的 Ca基 吸收剂和活性炭吸附剂发生反应, 实现 SOx、 NOx、 Hg和二恶英等多种污染物 的协同脱除, 反应后的烟气夹带一定量的固体颗粒, 经旋风分离器 14 和布袋 除尘器 20两次收集粉尘后通过烟肉 25排出干净烟气, 旋风分离器 14收集的灰 全部返回反应塔 12, 除尘器 20下的粉尘部分返回反应塔 12。 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.
烟道 4' 在布置臭氧分布器 4的部位与 CFB反应塔的烟气进口 5间的距离 设置为 30米, 臭氧发生器 2产生的臭氧与烟气中的 NO的摩尔比为 0.6, 反应 0.5s, 控制喷入的石灰浆量 Ca/ (S+N) 摩尔比为 1.5, 添加的 Ca基吸收剂与活 性炭吸附剂的质量比为 15:1, 脱硫效率可达 90%以上, 脱硝效率可达 50%以 上, 二恶英类污染物脱除效率≥80%, 重金属脱除效率≥90%。  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. s, 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%.
实施例 2  Example 2
采用如上所述的烧结烟气协同脱硫脱硝脱汞脱二恶英装置进行脱除, 包括 如下步骤:  The removal of the sintering flue gas synergistic desulfurization, denitrification, mercury removal and dioxin removal apparatus as described above includes the following steps:
臭氧发生器 2产生的臭氧与稀释风机 1发生的稀释风进入混合缓冲罐 3进 行混合, 然后经臭氧分布器 4喷入烟道 4' , 喷入的臭氧与烟气充分接触, 主 要将烟气中的 NO氧化为高价态的 NOx, 氧化后的烟气与 CFB中流化的 Ca基 吸收剂和活性炭吸附剂发生反应, 实现 SOx、 NOx、 Hg和二恶英等多种污染物 的协同脱除, 反应后的烟气夹带一定量的固体颗粒, 经旋风分离器 14 和布袋 除尘器 20两次收集粉尘后通过烟肉 25排出干净烟气, 旋风分离器 14收集的灰 全部返回反应塔 12, 除尘器 20下的粉尘部分返回反应塔 12。 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. Synergistic removal, 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. At the tower 12, the dust portion under the dust remover 20 is returned to the reaction tower 12.
烟道 4' 在布置臭氧分布器 4的部位与 CFB反应塔的烟气进口 5间的距离 设置为 15米, 臭氧发生器 2产生的臭氧与烟气中的 NO的摩尔比为 1.0, 反应 3s, 控制喷入的石灰浆量 Ca/ ( S+N)摩尔比为 1.2, 添加的 Ca基吸收剂与活性 炭吸附剂的质量比为 25: 1, 脱硫效率可达 90%以上, 脱硝效率可达 90%以上, 二恶英类污染物脱除效率≥80%, 重金属脱除效率≥90%。 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%.
实施例 3  Example 3
采用如上所述的烧结烟气协同脱硫脱硝脱汞脱二恶英装置进行脱除, 包括 如下步骤:  The removal of the sintering flue gas synergistic desulfurization, denitrification, mercury removal and dioxin removal apparatus as described above includes the following steps:
臭氧发生器 2产生的臭氧与稀释风机 1发生的稀释风进入混合缓冲罐 3进 行混合, 然后经臭氧分布器 4喷入烟道 4' , 喷入的臭氧与烟气充分接触, 主 要将烟气中的 NO氧化为高价态的 NOx, 氧化后的烟气与 CFB中流化的 Ca基 吸收剂和活性炭吸附剂发生反应, 实现 SOx、 NOx、 Hg和二恶英等多种污染物 的协同脱除, 反应后的烟气夹带一定量的固体颗粒, 经旋风分离器 14 和布袋 除尘器 20两次收集粉尘后通过烟肉 25排出干净烟气, 旋风分离器 14收集的灰 全部返回反应塔 12, 除尘器 20下的粉尘部分返回反应塔 12。 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. Synergistic removal, 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. At the tower 12, the dust portion under the dust remover 20 is returned to the reaction tower 12.
烟道 4' 在布置臭氧分布器 4的部位与 CFB反应塔的烟气进口 5间的距离 设置为 20米, 臭氧发生器 2产生的臭氧与烟气中的 NO的摩尔比为 0.25, 反应 5s, 控制喷入的石灰浆量 Ca/ ( S+N)摩尔比为 2.0, 添加的 Ca基吸收剂与活性 炭吸附剂的质量比为 20: 1, 脱硫效率可达 90%以上, 脱硝效率可达 20%以上, 二恶英类污染物脱除效率≥80%, 重金属脱除效率≥90%。  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%.
实施例 4  Example 4
采用如上所述的烧结烟气协同脱硫脱硝脱汞脱二恶英装置进行脱除, 包括 如下步骤:  The removal of the sintering flue gas synergistic desulfurization, denitrification, mercury removal and dioxin removal apparatus as described above includes the following steps:
臭氧发生器 2产生的臭氧与稀释风机 1发生的稀释风进入混合缓冲罐 3进 行混合, 然后经臭氧分布器 4喷入烟道 4' , 喷入的臭氧与烟气充分接触, 主 要将烟气中的 NO氧化为高价态的 NOx, 氧化后的烟气与 CFB中流化的 Ca基 吸收剂和活性炭吸附剂发生反应, 实现 SOx、 NOx、 Hg和二恶英等多种污染物 的协同脱除, 反应后的烟气夹带一定量的固体颗粒, 经旋风分离器 14 和布袋 除尘器 20两次收集粉尘后通过烟肉 25排出干净烟气, 旋风分离器 14收集的灰 全部返回反应塔 12, 除尘器 20下的粉尘部分返回反应塔 12。 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. To oxidize NO in the flue gas NO X is higher valence state, and CFB oxidized flue gas fluidized activated carbon adsorbent, and Ca-based sorbent reacts achieve SO x, NO x, Hg and dioxin and other The synergistic removal of the pollutants, 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 cyclone separator 14 collects the collected flue gas. The ash is all returned to the reaction column 12, and the dust portion under the dust remover 20 is returned to the reaction column 12.
烟道 4' 在布置臭氧分布器 4的部位与 CFB反应塔的烟气进口 5间的距离 设置为 25米, 臭氧发生器 2产生的臭氧与烟气中的 NO的摩尔比为 1.5, 反应 2.5s, 控制喷入的石灰浆量 Ca/ (S+N) 摩尔比为 1.1, 添加的 Ca基吸收剂与活 性炭吸附剂的质量比为 22:1, 脱硫效率可达 90%以上, 脱硝效率可达 90%以 上, 二恶英类污染物脱除效率≥80%, 重金属脱除效率≥90%。 申请人声明, 本发明通过上述实施例来说明本发明的详细结构特征以及脱 硫脱硝方法, 但本发明并不局限于上述详细结构特征以及污染物脱除方法, 即 不意味着本发明必须依赖上述详细结构特征以及脱除方法才能实施。 所属技术 领域的技术人员应该明了, 对本发明的任何改进, 对本发明所选用部件的等效 替换以及辅助部件的增加、 具体方式的选择等, 均落在本发明的保护范围和公 开范围之内。  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. s, 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 Applicant declares that 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.

Claims

权 利 要 求 书 Claim
1、一种烧结烟气循环流化床半干法联合脱硫脱硝装置, 其特征在于, 所述 装置包括臭氧发生器(2)、 稀释风机(1 )、 混合缓冲罐(3 )、 臭氧分布器(4) 以及循环流化床反应塔 (12) ;  A sintering flue gas circulating fluidized bed semi-dry combined desulfurization and denitration device, characterized in that 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 column (12);
所述臭氧发生器 (2) 和稀释风机 (1 ) 与混合缓冲罐 (3 ) 的入口相连; 所述臭氧分布器(4)安装在烟道(4' )中, 在烟道(4' )外部设置连接口, 与混合缓冲罐 (3 ) 的出口相连;  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'), in the flue (4') An external connection port is connected to the outlet of the mixing buffer tank (3);
所述循环流化床反应塔 (12) 的烟气进口 (5 ) 与布置有臭氧分布器 (4) 的烟道 (4' ) 相连。  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.
2、 根据权利要求 1所述的装置, 其特征在于, 布置臭氧分布器 (4) 的部 位与循环流化床反应塔(9)的烟气进口 (5 )间的烟道(4' )距离为 15〜30米。  2. Apparatus according to claim 1, characterized in that the distance between the portion where the ozone distributor (4) is arranged and the flue gas inlet (5) of the circulating fluidized bed reaction column (9) For 15 to 30 meters.
3、 根据权利要求 1或 2所述的装置, 其特征在于, 所述循环流化床反应塔 ( 12) 上部出口 (13 ) 与旋风分离器 (14) 连接, 旋风分离器分离料斗 (15 ) 通过空气斜槽 (16) 与循环流化床反应塔 (12) 回料口 (18 ) 连接;  3. Apparatus according to claim 1 or 2, characterized in that the upper outlet (13) of the circulating fluidized bed reaction column (12) is connected to a cyclone (14), and the cyclone separation hopper (15) Connected to the return port (18) of the circulating fluidized bed reaction column (12) through the air chute (16);
优选地, 所述循环流化床反应塔 (12) 上部出口 (13 ) 与旋风分离器(14) 切向连接。  Preferably, the upper outlet (13) of the circulating fluidized bed reaction column (12) is tangentially connected to the cyclone (14).
4、 根据权利要求 1-3任一项所述的装置, 其特征在于, 所述循环流化床反 应塔(12)底部为文丘里结构, 文丘里扩张段(19)设置有进料口、 回料口(18) 及喷水喷枪 (17) , 喷水喷枪 (17) 喷嘴依烟气顺流方向安装;  The apparatus according to any one of claims 1 to 3, wherein 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. The return port (18) and the water spray gun (17), the water spray gun (17) are installed in the direction of the flue gas;
优选地, 进料口设置为两个(6、 7), 分别为 Ca基吸收剂进料口 (6)和活 性炭吸附剂进料口 (7) 。  Preferably, 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).
5、根据权利要求 1-4任一项所述的装置,其特征在于,所述旋风分离器(14) 与布袋除尘器(20)连接, 布袋除尘器(20)料斗与灰仓(21 )相连, 灰仓(21 ) 设置两个出口, 第一出口 (22) 通过气力输送管道与循环流化床反应塔 (12) 回料口 (18) 连接, 第二出口 (23 ) 与灰库 (24) 相连; 5. Apparatus according to any one of claims 1 - 4, characterized in that the cyclone (14) is connected to a bag filter (20), a bag filter (20) hopper and an ash bin (21) Connected, ash silo (21) Two outlets are provided, the first outlet (22) is connected to the circulating fluidized bed reaction tower (12) return port (18) through a pneumatic conveying pipeline, and the second outlet (23) is connected to the ash silo (24);
优选地, 所述布袋除尘器 (20) 后设有烟肉 (25 ) 。  Preferably, the bag filter (20) is provided with bacon (25).
6、 一种利用权利要求 1-5任一项所述的装置进行多污染物脱除的方法, 包 括以下步骤:  6. A method of multi-contaminant removal using the apparatus of any of claims 1-5, comprising the steps of:
1 ) 向烟道 (4' ) 中喷入臭氧, 使臭氧与烟气反应;  1) Spray ozone into the flue (4') to react the ozone with the flue gas;
2) 氧化后的烟气送入循环流化床反应塔 (12) , 烟气中的 S02、 S03、 和 NOx在反应塔 (12) 中主要与 Ca基吸收剂在雾化水的作用下进行反应脱除;2) the oxidized flue gas fed to the circulating fluidized bed reaction column (12), the flue gas S0 2, S0 3, and NO x in the reaction column 12) (mainly Ca-based sorbent of the atomized water The reaction is removed under the action;
3 ) 烟气中各种形态的 Hg和二恶英类污染物主要与活性炭吸附剂进行反应 进行脱除。 3) Various forms of Hg and dioxin pollutants in the flue gas are mainly reacted with activated carbon adsorbents for removal.
7、 根据权利要求 6所述的方法, 其特征在于, 步骤 1 ) 的具体过程为: 臭 氧发生器(2)产生的臭氧在稀释风机 (1 ) 的作用下在混合缓冲罐(3 ) 混合均 匀, 经臭氧分布器 (4) 喷入烟道 (4' ) , 喷入的臭氧与烟气充分接触反应。  7. The method according to claim 6, wherein 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) , the ozone distributor (4) is sprayed into the flue (4'), and the injected ozone is in full contact with the flue gas.
8、 根据权利要求 6或 7所述的方法, 其特征在于, 步骤 1 ) 喷入的臭氧与 烟气中 NO的摩尔比为 0.25〜1.2; 反应的时间为 0.5〜5s; 步骤 2) 所述 Ca基吸 收剂按照 Ca/ (S+N) 摩尔比 1.1〜2.0, 优选 1.2〜1.5的比例加入;  The method according to claim 6 or 7, wherein the step 1) the molar ratio of the injected ozone to the NO in the flue gas is 0.25 to 1.2; the reaction time is 0.5 to 5 s; Ca-based absorbent is added in a ratio of Ca / (S + N) molar ratio of 1.1 to 2.0, preferably 1.2 to 1.5;
优选地, 反应后的 Ca基吸收剂和活性炭吸附剂经旋风分离器(14)分离后 通过空气斜槽 (16) 返入循环流化床反应塔 (12) 实现多次循环, 烟气经过布 袋除尘器 (20) 进一步除去粉尘后排入大气, 布袋除尘器 (20) 收集的粉尘部 分通过气力输送返回循环流化床反应塔 (12) 。  Preferably, the reacted Ca-based absorbent and the activated carbon adsorbent are separated by a cyclone (14) and then 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 bag. The dust remover (20) is further removed from the dust and discharged into the atmosphere, and the dust collected by the bag filter (20) is pneumatically transported back to the circulating fluidized bed reaction tower (12).
9、 根据权利要求 6-8任一项所述的方法, 其特征在于, 步骤 2) 中通过调 节喷水喷枪(14) 喷水量, 以控制循环流化床反应塔(9) 内的烟气温度在酸露 点以上; 通过调节空气斜槽 (13 ) 的循环回料量, 控制循环流化床反应塔 (9) 进出口压差, 而控制塔内颗粒浓度, 满足 Ca/ (S+N) 摩尔比要求。 The method according to any one of claims 6-8, wherein in step 2), the amount of water sprayed by the water spray gun (14) is adjusted to control the smoke in the circulating fluidized bed reaction tower (9) The gas temperature is above the acid dew point; the circulating fluidized bed reaction column is controlled by adjusting the circulating return amount of the air chute (13) (9) The pressure difference between the inlet and outlet, and the particle concentration in the control tower, meet the Ca/(S+N) molar ratio requirement.
10、根据权利要求 6-9任一项所述的方法, 其特征在于, 步骤 3)所述添加 的活性炭吸附剂按照 Ca基吸收剂与活性炭吸附剂的质量比为 15:1〜25:1加入。  The method according to any one of claims 6 to 9, wherein the step 3) the added activated carbon adsorbent has a mass ratio of the Ca-based absorbent to the activated carbon adsorbent of 15:1 to 25:1. Join.
PCT/CN2014/084111 2014-07-21 2014-08-11 Equipment and method for circulating fluidized bed semidry simultaneous desulfurization, denitration, demercuration, and removal of dioxins of sintering flue gas WO2016011682A1 (en)

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