WO2016058141A1 - 一种烟道气除尘脱硫方法和设备 - Google Patents

一种烟道气除尘脱硫方法和设备 Download PDF

Info

Publication number
WO2016058141A1
WO2016058141A1 PCT/CN2014/088632 CN2014088632W WO2016058141A1 WO 2016058141 A1 WO2016058141 A1 WO 2016058141A1 CN 2014088632 W CN2014088632 W CN 2014088632W WO 2016058141 A1 WO2016058141 A1 WO 2016058141A1
Authority
WO
WIPO (PCT)
Prior art keywords
gas
tower
flue gas
nozzle
liquid
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/CN2014/088632
Other languages
English (en)
French (fr)
Inventor
尹应武
翁慧超
赖永华
李大川
吴延庆
叶李艺
赵玉芬
孙开林
许列奎
孙佳奎
徐先海
冯泽民
杨兆斌
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 CHINA SCIENCE PURIFICATION ECO-TECHNOLOGIES Co Ltd
Original Assignee
BEIJING CHINA SCIENCE PURIFICATION ECO-TECHNOLOGIES Co Ltd
Priority date (The priority date 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 date listed.)
Filing date
Publication date
Application filed by BEIJING CHINA SCIENCE PURIFICATION ECO-TECHNOLOGIES Co Ltd filed Critical BEIJING CHINA SCIENCE PURIFICATION ECO-TECHNOLOGIES Co Ltd
Priority to PCT/CN2014/088632 priority Critical patent/WO2016058141A1/zh
Publication of WO2016058141A1 publication Critical patent/WO2016058141A1/zh
Anticipated expiration legal-status Critical
Ceased legal-status Critical Current

Links

Images

Classifications

    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D50/00—Combinations of methods or devices for separating particles from gases or vapours
    • 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

Definitions

  • the invention relates to an exhaust gas purification technology and device such as flue gas, and relates to the field of environmental protection.
  • PM is a solid or liquid particulate matter in the atmosphere.
  • PM2.5 and PM10 are fine respirable particulate matter in the atmosphere.
  • the particle size is small, and it can contain poisonous and harmful substances. It has a long residence time in the atmosphere and a long transport distance. Therefore, it has a great impact on human health and the quality of the atmospheric environment.
  • Mechanical dust removal, electric dust removal, filter dust removal, washing and dust removal are several common dust removal methods.
  • Mechanical dust removal relies on mechanical force to remove dust particles from the airflow.
  • the structure is simple, equipment costs and operating costs are low, but the dust removal efficiency is not high.
  • Electrostatic precipitator uses electrostatic attraction to separate dust particles from a large amount of airflow. It is characterized by low airflow resistance and dust removal efficiency of over 99%, but high investment and large equipment size.
  • the filter dust collector allows the dust-containing airflow to collect dust particles through the filter material, and the dust removal efficiency is generally 90% to 99%, but it is not suitable for the dusty gas with high temperature.
  • the above several dust removal methods need to be separately desulfurized. Water washing and dust removal and desulfurization is the most commonly used exhaust gas purification method.
  • the maximum allowable emission standard for sulfur dioxide in fuel oil and coal-fired boilers is 900mg/m 3
  • the maximum allowable emission standard for sulfur dioxide in light diesel oil and kerosene boilers is 500mg/m 3
  • the sulfur dioxide emission standard for gas-fired boilers is 100mg/m. 3.
  • the maximum allowable emission standard for nitrogen oxides in oil and gas boilers is 400 mg/m 3 .
  • the mist and dust in the flue gas often form an aerosol that is difficult to capture due to electrostatic repulsion, and the simple filtering and electrostatic dust removal effects are not good.
  • the water washing method has several advantages in eliminating static electricity, dust removal, desulfurization and waste heat utilization. Therefore, the high-efficiency water washing exhaust gas purification technology is worthy of further study.
  • the diameter of the tornado in nature is about tens of meters, and the gas velocity is from ten to two hundred meters. It is due to the volumetric contraction caused by local cold in the atmosphere and the rapid replenishment of a wide range of surrounding atmospheres. The power and lift generated by the swirl can entrain large amounts of solids and dispersed liquids, causing tremendous damage. Can the tornado be miniaturized and used in industrial production?
  • the general gas velocity of the flue gas is more than ten meters, and the temperature is between 160 °C and 180 °C. During the water washing process, the temperature can drop by more than 100 degrees Celsius, and the gas shrinks by at least 1/4, so it has the basic conditions for forming a tornado.
  • Using the principle of forming a tornado may solve the problem of exhaust gas purification such as flue gas.
  • a reasonable solution should be to rotate the hot flue gas entering the flue along the horizontal tangential direction and spiral up, while using the pump to apply kinetic energy to the circulating wash water.
  • the reaction force generated when the nozzle is ejected pushes the movable nozzle to rotate in the direction of the airflow.
  • the rotating atomizing nozzle can effectively convert the potential energy obtained by the water into the kinetic energy that drives the nozzle and the gas to rotate, and the surface energy that promotes the further dispersion of the droplet, which can be greatly increased.
  • the opportunity and time of gas-liquid contact strengthen flue gas desulfurization and dust removal reaction and mass transfer heat transfer process, small flow of rotating water mist, can achieve rapid vaporization and cooling, so that the high temperature flue gas volume suddenly drops to form a negative pressure, in a reasonable setting
  • the swirling deflector guides a rapid swirling effect similar to a tornado, allowing the flue gas to wash.
  • the spiral rise motion in the polyester tower changes from the overall upward movement direction to the spiral upward movement.
  • the dust, sulfur dioxide and nitrogen dioxide entrained in the flue gas have more opportunities and suspensions driven by the centrifugal force generated by their own power and swirl.
  • the weakly alkaline water atomized in the system is fully contacted or captured, and the humid environment and the weakly alkaline water mist can significantly eliminate the static electricity of the system and enhance the effect of capturing and sedimenting dust and harmful gases.
  • the rapid movement of the gas-liquid cyclone accelerates and promotes the concentration of dust and liquid to the wall surface, which can significantly enhance the dust removal effect.
  • the water vapor-rich flue gas produces secondary water mist during rotation and cooling, and can also assist in vacuuming and being effectively separated.
  • the multi-tower series and multi-position up-and-down rotary spray devices can further ensure the effect.
  • the specific technical scheme of the present invention is: removing the auxiliary filler such as the stone in the original water dust removing device, and adopting the original equipment to adopt the mode of the spray tower once or multiple towers in series to perform dust removal and desulfurization.
  • an arc-shaped baffle matching the curvature of the treatment tower is added to guide the flue gas into the desulfurization washing tower, and the bottom, middle and upper portions of each dedusting tower can be arranged according to specific conditions and requirements.
  • One or more rotating nozzles are installed every 3-5m), the desulfurization liquid is sprayed through the nozzle, and the nozzle automatically rotates by the recoil force generated when the water is sprayed (at a pressure of 5 kg, the flow rate is 3 m 3 /h, the rotation speed can be Up to 300r/min or more).
  • the installation of the baffle reduces the gas outlet cross-section by 20% to 80%, the negative pressure formed by the rapid cooling after the flue gas inlet increases the gas flow rate. The actual situation also proves that the proper setting of the swirling baffle will not cause the airflow to be poor. .
  • the use of initial kinetic energy and the guiding effect of the gas, while making full use of the system temperature difference, pressure, volume can form a high-efficiency swirling system with a long range of long distances, and can play a huge role in the fields of purification of exhaust gas such as flue gas and utilization of waste heat.
  • Figure 1 is a typical high efficiency purification device
  • FIG. 2 is a simplified schematic diagram of a high efficiency purification device
  • Figure 3 is a schematic view of a typical rotating nozzle
  • Figure 4 is a simple swirl generator
  • Figure 5 is a comparison result of heat transfer effect of gas swirl in a spray tower
  • Figure 6 is a comparison result of mass transfer effect of gas swirl in a spray tower
  • Figure 7 is a schematic diagram of the process of the yellow phosphorus tail gas washing phosphorus section
  • Phosphorus Tower 1 (1), Phosphorus Tower 2 (2), Phosphorus Tower 3 (3), Phosphorus Tower (4)
  • Figure 8 is a schematic diagram of the process of the yellow phosphorus tail gas purification section
  • Purification tower 1 (1), purification tower 2 (2), purification tower 3 (3)
  • Figure 9 is the temperature change data under each condition.
  • Example 1 Comparison of heat transfer effects of gas swirls in a spray tower
  • the same temperature hot water is sprayed from the top of the tower, and the temperature difference of the liquid collected by the top of the tower and the bottom of the tower can be used to determine the tendency of the surface of the atomized water droplet to vaporize into the gas phase, and the heat transfer effect is evaluated.
  • the temperature drop value of the mixed gas swirling flow is obviously larger than that of the non-swirl.
  • the hot water temperature in the non-swirl experimental system is reduced from 61 °C to 48 °C.
  • the hot water temperature of the experimental system with swirling was reduced from 62 °C to 42 °C; when both were lowered to 40 °C, the experimental system without swirling required 8 min, while the experimental system with swirling only took 6.5 min. It is proved that the gas swirl has a significant improvement effect on the gas-liquid heat transfer under convection.
  • Example 2 Comparison of mass transfer effects of gas swirls in a spray tower
  • the atomization spray is sprayed from the top of the tower with the same concentration of NaOH solution with the same initial conductance value.
  • the conductance value of the mixed gas swirling flow is obviously faster than that of the non-swirl state.
  • the conductance stability value of the non-swirl generator is 4.95, and there is a swirl generator.
  • the conductance stability value is 4.84; when the gas volume is 100m 3 /h, the conductance stability value of the non-swirl generator is 4.63, and the conductance stability value of the cyclone generator is 4.52.
  • Yellow phosphorus production includes batching section, reaction section, washing section, exhaust gas purification section and Yellow phosphorus refining section.
  • the water washing section (shown in Fig. 7) is generally connected in series by three water washing towers (1-3), the cooling water sprays cold phosphorus from the top of the tower, and the condensed yellow phosphorus directly flows into the bottom phosphorus receiving tank.
  • the temperature drops from 140-150 ° C to about 55 ° C.
  • the temperature of the third tower drops from 45 ° C to 30 ° C. about.
  • the exhaust gas purification section (shown in Figure 8) consists of three washing towers (1-3) connected in series, and the tail gas is washed again with water, but the effect is not good. Strengthening the heat transfer and mass transfer effect of the washing section can improve the recovery rate of yellow phosphorus, remove dust, and promote the hydrolysis and removal of fluorosilicone compounds. However, phosphine and hydrogen sulfide are removed chemically in the tail gas purification section.
  • the flow rate of the tower is 3200Nm 3 /h, the temperature is about 140 ° C, the tower diameter is 2 meters, the tower height is 14 meters, and the baffle is installed at the gas inlet of the bottom of the tower.
  • the opening cross-sectional area is 70% of the cross-sectional area of the gas pipeline.
  • the bottom is equipped with a rotating nozzle of 6m 3 /h flow direction, the direction is upwards; two rotating nozzles with a flow rate of 3m 3 /h are installed in the middle of the tower, one direction upwards and one downward direction; the top of the tower is equipped with one 3m 3 /h Rotate the nozzle with the direction facing down.
  • the swirling tower can significantly improve the purification and cooling effect, especially for dust, when the liquid flow rate is low or substantially constant.
  • the removal effect is remarkable, and the specific results are analyzed as follows:
  • the main components of the yellow phosphorus by-product tail gas are carbon monoxide, carbon dioxide, hydrogen sulfide, phosphine and silicon fluoride. Every 4t, 140 °C yellow phosphorus tail gas will bring out 1t yellow phosphorus steam, and also entrain a large amount of calcium oxide, silicon oxide dust.
  • the system is a complex system of gas-liquid-solid three-phase, and it is considered that the cyclone tower is more representative of its purification effect.
  • the results of continuous monitoring and on-site monitoring of PM2.5 and PM10 for 10 days show that the improved cyclone tower, especially the dedusting effect of tower 1, is remarkable, and the exhaust gas treated by tower 1 has PM10 below 1 mg/m 3 (PM2.
  • the content of 5 accounts for half of PM10, indicating that the smaller the particle size, the more difficult it is to remove.
  • the PM10 data after dedusting by other towers is reduced by about half, and the removal effect is far less than that of tower 1, which fully proves the tower with strong swirling effect.
  • the dust removal effect of 1 is obvious. Only the dust removal effect of Tower 1 is far below the national maximum dust emission permit.
  • the PM10 of the gas discharged is also only about 1 mg/m 3 , which is relatively stable.
  • environmental monitoring of PM10 environmental data is greatly affected by temperature, wind and rain, sometimes higher or sometimes lower than the measured value.
  • the device has a yellow phosphorus capacity of 1.2t per hour, and produces 4000Nm 3 yellow phosphorus tail gas.
  • the phosphorus vapor turns into liquid phosphorus in the cold water, and is flushed by water to the bottom of the tower.
  • the amount of phosphide entrained at the top of tower 1 is less than 1g/m 3 , so the amount of yellow phosphorus carried out from the top of the tower 1 is up to about 1g/m 3 , so the amount of leaching per hour is only 4kg, which is greater than 99.6% of the yellow phosphorus can be fully collected in the first cyclone.
  • the dephosphorization effect also proves the high efficiency dust removal performance of the cyclone tower from the side.
  • the yellow phosphorus tail gas with a gas temperature of 140 ° C and a flow rate of 50 Nm 3 or more per minute is sprayed in the tower 1 simultaneously or separately with a bottom, a tower or a top nozzle, and sprayed with 1/1000 to 2/1000 spray liquid.
  • the temperature at the bottom of the tower 1 can be rapidly cooled to about 55 ° C
  • the temperature at the top of the tower 1 can be reduced to about 40 ° C
  • the temperature after passing through the tower 2, the tower 3, and the tower 4 is only decreased by 10 ° C, and is reduced to about 30 ° C. .
  • the cooling and waste heat utilization is mainly in the tower 1, especially the bottom of the tower 1 where the swirling is the most intense, and the temperature can be drastically dropped by about 85 °C. To the top of the tower can be lowered by about 15 °C. Further experiments have shown that using the bottom or middle nozzle alone with a liquid volume of 6 m 3 /h has a good cooling effect, especially the effect of using the central nozzle alone. Therefore, the upper and lower swirl nozzles are installed at the appropriate position on the upper part of the flue gas inlet, and only a small amount of liquid discharge is required to be optimal, and the heat transfer effect of the large flow rate and the multi-nozzle is not the best cooling effect.
  • the temperature change data under each condition can be seen in Figure 9.
  • the magnitude of the cooling can reflect the dispersion of the liquid, the swirling flow and the sufficient mixing of the gas and liquid, which indicates that the gas swirling device guides the swirling of the gas, and the rotating nozzle generates the water mist, which can effectively cool the yellow phosphorus vapor and rapidly evaporate and cool down. , produces a cooling and negative pressure similar to the tornado eye. This result can be extended to the waste heat utilization process of chemical absorption, condensation, reaction and evaporation concentration with large volume changes.
  • the phosphate ore is mainly in the form of calcium fluorophosphate
  • fluorine is taken up in the form of silicon tetrafluoride or hydrogen fluoride with yellow phosphorus tail gas
  • the fluoride content in the exhaust gas is as high as 0.5 to 2 g/m3.
  • Silicon fluoride can be hydrolyzed, but the existing equipment fails to hydrolyze the silicon fluoride well, resulting in blockage of the entire gas supply pipeline. As a fuel gas, it will cause scaling and corrosion of the boiler, causing poisoning and surface coverage of the catalyst as a raw material gas. And inactivated.
  • the yellow phosphorus tail gas with an average fluorine content of about 1g/m 3 , the exhaust gas of about 140 ° C can be removed by the effective contact and swirling reaction of the tower 1 to remove more than 50% of fluorine, and further defluorination by the tower 2 to the tower 6
  • the content of fluorine will be reduced by about 30 mg/m 3 , and the removal rate of fluorine is more than 97%. See Figure 10 for the defluorination effect of each column.
  • the cyclone tower is also an efficient gas-liquid reactor.
  • the flue gas flow rate is 55000 Nm 3 /h, the flue gas temperature is 180 ° C, and the inlet SO 2 concentration is 2000 mg/Nm 3 .
  • the tower diameter is 1.2m, the tower height is 9m, the liquid-gas ratio is 2/1000, and the desulfurization liquid is a mixture of saturated lime water and 1% sodium hydroxide.
  • the desulfurization efficiency before transformation is 90%, the export sulfur content is 200mg/Nm 3 , the desulfurization rate after transformation is about 95%, and the export sulfur content is less than 100mg/Nm 3 . It shows that the cyclone tower can also effectively improve the desulfurization efficiency.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Health & Medical Sciences (AREA)
  • Biomedical Technology (AREA)
  • Environmental & Geological Engineering (AREA)
  • Analytical Chemistry (AREA)
  • General Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Treating Waste Gases (AREA)

Abstract

一种烟道气除尘脱硫方法和装置。在烟道气入口处增设弧形导流板，引导烟道气（1）切向进入塔体（3），根据具体情况和要求在塔体（3）底部、中部、上部安装一个或多个旋转喷嘴（2），脱硫液通过喷嘴（2）喷出，喷嘴（2）依靠喷液体时产生的反作用力自动旋转，气流在塔体（3）内快速螺旋上升，烟道气中夹带的灰尘、二氧化硫和二氧化氮等在自身动力和旋流产生的离心力的推动下可与悬浮其中的充分雾化的弱碱水接触反应或被捕获。该方法和装置可用于反应、吸收、尾气净化、烘干、再除尘、浓缩、干燥等各种化工、加工、环保领域中。

Description

[根据细则37.2由ISA制定的发明名称]　一种烟道气除尘脱硫方法和设备 技术领域
本发明涉及烟道气等废气净化技术与装置，涉及环保领域。
背景技术
PM是大气中的固体或液体颗粒状物质，PM2.5以及PM10是大气中的细微可吸入颗粒物，其粒径小，可夹带有毒、有害物质，在大气中的停留时间长、输送距离远，因而对人体健康和大气环境质量的影响很大。
各种工业过程是PM2.5与PM10的主要固定来源，尤其是煤等化石燃料燃烧时候会产生二氧化硫、氮氧化物、挥发性有机物等严重污染环境的烟道气，并夹带大量的细小颗粒，对周围环境造成严重的危害。
机械除尘、电除尘、过滤除尘、洗涤除尘等是目前几种常见的除尘方式。机械除尘依靠机械力将尘粒从气流中除去，其结构简单，设备费和运行费均较低，但除尘效率不高。电除尘利用静电吸引力从大量气流中分离尘粒，特点是气流阻力小，除尘效率可达99％以上，但投资高，设备尺寸大。过滤除尘器使含尘气流通过滤料捕集尘粒，除尘效率一般为90％～99％，但不适用于温度高的含尘气体，上述几种除尘方式需要再进行单独脱硫。水洗涤除尘脱硫是最常采用的尾气净化方式，，它是通过喷淋稀碱水的方式使尘粒、二氧化硫、氮氧化物等污染物与液滴或液膜在空间中或填料表面充分接触被俘获，除尘效率为80％～95％，可以同时脱除二氧化硫等有害气体，但存在净化效果差、成本较高的问题。由于除尘难度较大，而且情况复杂，因此国家排放标准并不高，而且差异性大(表一为不同行业的尾气颗粒物排 放标准)。尽管如此，仍有很多企业难以达到排放标准。宽松的排放标准、企业排放的不达标及对形成雾霾的PM2.5没有明确标准，已经在我国多地导致严重的、频繁的、长时间的雾霾天气，对人们的健康和日常生活造成严重影响。因此开发高效节能的烟道气脱硫除尘技术已迫在眉睫。
表一不同行业的颗粒粉尘排放国家标准
Figure PCTCN2014088632-appb-000001
*国家对燃料油和燃煤锅炉的二氧化硫最高允许排放标准为900mg/m3，对轻柴油、煤油锅炉的二氧化硫最高允许排放标准为500mg/m3，对燃气锅炉的二氧化硫排放标准为100mg/m3，对燃油锅炉和燃气锅炉的氮氧化物的最高允许排放标准为400mg/m3。
发明内容
烟道气中的雾滴和灰尘由于静电排斥，往往形成难以捕获的气溶胶，简单过滤和静电除尘效果都不佳。水洗法兼具消除静电、除尘、脱硫和余热利用几大优势，因此高效水洗尾气净化技术值得深入研究。
仔细分析烟道气和水洗除尘脱硫过程可以发现，高温烟道气由于产生量大，二氧化硫浓度低，洗涤水雾化效果差，洗涤水量受限，导致除尘和脱硫效果不理想。由于高温烟道气进入水洗塔接触循环冷却水后会迅速冷却导致体积会急剧收缩，形成负压，这种有效能并没有被很好利用，而是形成复杂湍流造成能量耗散。
自然界的龙卷风直径大约几十米，气速为十几米到两百米。它是由于大气局部的遇冷导致的体积收缩和大范围周边大气的快速补充，形成的大气旋流现象。旋流产生的动力和升力，可以夹带大量固体和分散液体，产生巨大的破坏作用。龙卷风可否小型化，应用于工业生产中？
烟道气的一般进塔气速大于十米，温度在160℃～180℃，在水洗过程中，气温可以下降100摄氏度以上，气体至少收缩1/4，因此具备形成龙卷风的基本条件。利用形成龙卷风的原理可能破解烟道气等废气净化难题，合理的方案应该是使进入烟道的热烟道气沿着水平切线方向旋转并螺旋上升，同时利用泵施加了动能的循环洗水从喷嘴喷出时产生的反作用力推动活动喷嘴顺气流方向旋转，旋转的雾化喷嘴可将水获得的势能有效转化为推动喷嘴和气体旋转的动能以及促进液滴进一步分散的表面能，可大大增加气液接触的机会和时间，强化烟道气脱硫除尘反应及传质传热过程，小流量的旋转水雾，可以实现快速汽化降温，使高温烟道气体积骤降形成负压，在合理设置的旋流导流板导引下可能产生类似龙卷风的快速旋流效果，使烟道气在洗 涤塔内产生螺旋上升运动，从整体向上运动方向改变为螺旋上升运动，烟道气中夹带的灰尘、二氧化硫和二氧化氮等在自身动力和旋流产生的离心力推动下有更多机会与悬浮在体系中雾化的弱碱水充分接触反应或被捕获，潮湿的环境和弱碱性的水雾可以显著消除体系静电，增强捕捉和沉降灰尘和有害气体效果。快速运动的气液旋流加速和促进了比重大的灰尘、液体朝着壁面富集，可显著增强除尘效果。此外，富含水蒸汽的烟道气在旋转和冷却过程中会产生二次水雾，也可以协助吸尘和被有效分离。采用多塔串联和多位置的上下方向的旋喷雾装置可以进一步确保效果。
本发明具体技术方案为：在原有的水除尘装置中取消麻石等辅助填料，利用原有的设备采取喷雾塔一次或多塔串联的模式进行除尘脱硫。在烟道气入口处增设与处理塔弧度相匹配的弧形导流板，引导烟道气切向进入脱硫洗塔，根据具体情况和要求可在每一段除尘塔底部、中部、上部(或每隔3-5m)安装一个或多个旋转喷嘴，脱硫液通过喷嘴喷出，喷嘴依靠喷水时产生的反冲力自动旋转(在压力为5公斤，流量为3m3/h的情况下，转速可达300r/min以上)。安装导流板虽然使气体出口横截面缩小20％～80％，烟道气进口后急速冷却形成的负压会增加气体流速，实际情况也证明合理设置旋流导流板不会导致气流不畅。
常见的旋风除尘、旋液分离、旋流塔等设备是完全依靠进塔流体的初始动能，因此作用的强度和距离有限，设备尺寸受限，本技术的最大不同在于：本技术是以气体旋流为诱导，主要利用了体积收缩产生的自身的有效能，促使流体更强、更快、作用范围更大的定向旋流运动，不受设备大小限制，这项组合技术不但考虑气体的进塔初始动能的利用和气体的导向作用，同时充分利用了体系温差、压力、体积 变化的自生有效能，可以形成大范围长距离的高效旋流体系，对于烟道气等废气的净化、余热的利用等领域能发挥巨大的作用。
附图说明
图1是一种典型的高效净化装置
入塔气流(1)、旋转喷嘴(2)、塔体(3)、出塔气流(4)
图2是高效净化装置简单示意图
进气管道(1)、旋流导流板(2)、旋转喷嘴(3)、塔体(4)
图3是一种典型的旋转喷嘴示意图
液体入口(1)、轴承(2)、提供力矩的小喷嘴(3)、顶部小喷(4)
图4是一种简易旋流发生器
气体进口(1)、轴承(2)、气体出口(3)
图5是喷雾塔中气体旋流的传热效果比较结果
图6是喷雾塔中气体旋流的传质效果比较结果
图7是黄磷尾气洗磷工段流程示意图
洗磷塔塔1(1)、洗磷塔塔2(2)、洗磷塔塔3(3)、受磷塔(4)
图8是黄磷尾气净化工段流程示意图
净化塔塔1(1)、净化塔塔2(2)、净化塔塔3(3)
图9是各条件下的温度变化数据
图10是各塔脱氟效果
具体实施例
一、实验效果证明
实施例1：喷雾塔中气体旋流的传热效果比较
在直径300mm，高度为1000mm的塔中用流量为200L/h、61℃的热水从塔顶部喷淋，空气从塔底部的活动导气管两端相反方向喷出，气体的反作用力导致喷气头旋转，形成气体旋流，简易旋流发生器详 见附图4。
用同样温度的热水从塔顶雾化喷淋，通过塔顶和塔底收集液体的温差变化，可以判断雾化水液滴表面汽化进入气相的趋势大小，评估传热效果。
如图5所示，混合气旋流情况下的温度下降值趋势明显大于无旋流情况，在同样5min循环喷淋情况下，无旋流的实验体系中热水温度从61℃降到48℃，有旋流的实验体系的热水温度从62℃降到42℃；当两者同时降到40℃，无旋流的实验体系需要8min，而有旋流的实验体系只需要6.5min。证明气体旋流对于对流状态下的气液传热也有明显的提升效果。
实施例2：喷雾塔中气体旋流的传质效果比较
在直径300mm，高度为1000mm的塔中用0.1％浓度，流量为200L/h的NaOH溶液从塔顶部喷淋，CO2～空气混合气从塔底部的活动导气管两端相反方向喷出，气体的反作用力导致喷气头旋转，形成气体旋流，简易旋流发生器详见附图X。
用同样浓度具有相同的初始电导值的NaOH溶液从塔顶雾化喷淋，通过测量塔底收集液的电导值变化，根据旋流和未旋流CO2～空气混合气与碱反应的电导值变化，可以判断气体旋流与否在液膜控制情况下的传质提升效果。
如图6所示，混合气旋流情况下的电导值下降趋势明显快于无旋流状态，在气量为40m3/h时，无旋流发生器的电导稳定值为4.95，有旋流发生器的电导稳定值为4.84；在气量为100m3/h时，无旋流发生器的电导稳定值为4.63，有旋流发生器的电导稳定值为4.52。
二、现场黄磷尾气净化实施效果评价
黄磷生产包括配料工段、反应工段、水洗工段、尾气净化工段和 黄磷精制工段。其中，水洗工段(附图7所示)一般由三个水洗塔(1-3)串联，冷却水从塔顶进行喷淋冷磷，冷凝的黄磷直接流入底部受磷槽中。反应炉气经过第一个水洗塔后温度从140-150℃下降到55℃左右，经过第二塔后温度从55℃下降到40℃左右，经过第三个塔温度从45℃下降到30℃左右。尾气净化工段(附图8所示)由三个串联的洗涤塔(1-3)组成，利用水对尾气进行再次洗涤，但效果不佳。强化水洗工段的传热和传质效果，可以提高黄磷回收率，脱除粉尘，促进氟硅化合物的水解与脱除。但磷化氢和硫化氢在尾气净化工段通过化学方法除去。
进塔流量为3200Nm3/h,温度约为140℃，塔径2米，塔高14米，在塔底气体入口处装有导流板，开口截面积为气体管道截面积的70％，塔底装有1个6m3/h流量的旋转喷嘴，方向朝上；塔中部装有2个3m3/h流量的旋转喷嘴，方向一个朝上，一个朝下；塔顶装有1个3m3/h旋转喷嘴，方向朝下。
通过连续10天分析塔顶的粉尘含量、磷含量、温度变化和脱硫效果评价，在液体流量较低或基本不变的情况下，旋流塔可以显著提高净化和降温效果，特别是对粉尘的脱除效果显著，具体结果分析如下：
实施例3除尘效果评价
黄磷副产尾气的主要成分为一氧化碳、二氧化碳、硫化氢、磷化氢和氟化硅等。每4t、140℃黄磷尾气会带出1t黄磷蒸汽，还夹带大量氧化钙、氧化硅粉尘。该体系是气液固三相的复杂体系，考察旋流塔对其净化效果更具代表性。10天连续跟踪和现场监测PM2.5和PM10的结果表明，改进后的旋流塔，特别是塔1的除尘效果显著，经塔1处理后的尾气，PM10在1mg/m3以下(PM2.5的含量占PM10 的一半，表明粒径越小越难脱除)，经过其他塔脱尘后的PM10数据大约再降低一半，其脱除效果远不及塔1，充分证明旋流效果强的塔1的除尘效果明显。仅塔1的除尘效果已经远低于国家最高的粉尘允许排放标准。净化后的尾气经燃气锅炉燃烧后，其排出的气体的PM10也仅在1mg/m3左右，相对稳定。同时环境监测的PM10环境数据受温度、风、雨影响很大，有时高于或有时低于测定值。
实施例4洗磷效果评价
该装置每小时黄磷产能为1.2t，产生4000Nm3黄磷尾气，磷蒸汽遇冷水变成液态的磷，被水冲洗到塔底收磷槽。塔1顶部夹带磷化物的量多次测定结果低于1g/m3，因此塔1顶部尾气带出的黄磷量最多为1g/m3左右，所以每小时带出量仅为4kg，可见大于99.6％的黄磷可在第一个旋流塔中被充分收集。脱磷效果也从侧面证明了旋流塔的高效除尘性能。
实施例5降温效果评价
气体温度为140℃、每分钟流量50Nm3以上的黄磷尾气在塔1中同时或单独用塔底、塔中或塔顶喷嘴，用1/1000～2/1000喷淋液进行旋转喷淋的情况下塔1底部的温度可以迅速被降温到55℃左右，塔1顶部温度可以被降低到40℃左右，通过塔2、塔3、塔4后的温度只下降10℃，降到30℃左右。可见，降温和余热利用主要在塔1，特别是旋流最剧烈的塔1底部，温度可骤降85℃左右。到塔顶可再降15℃左右。进一步实验表明，只用6m3/h液量的单独使用底部或中部喷嘴，就有很好的降温效果，特别是单独使用中部喷嘴的效果最佳。因此，在烟道气进口的上部适当位置安装上下旋流喷嘴，只需要很少的喷液量效果最佳，大流量和多喷嘴的换热效果不是能取得最好的降温效果。各条件下的温度变化数据可参见图9。因为降温幅度的大小 能够反应液体的分散、旋流和气液的充分混合状况，这说明了气体旋流装置引导了气体的旋流，而旋转喷嘴产生水雾可以有效冷却黄磷蒸汽并迅速蒸发降温，产生类似龙卷风眼的降温和负压作用。这一结果可以推广到有较大体积变化的化工吸收、冷凝、反应和蒸发浓缩等余热利用过程。
实施例6脱氟效果评价
由于磷矿石主要以氟磷酸钙的形式存在，在还原成黄磷的过程中，氟以四氟化硅或氟化氢的形式随黄磷尾气带出，尾气中氟化物含量高达0.5～2g/m3。氟化硅可水解，但现有设备未能很好地使氟化硅水解，导致整个送气管道堵塞，作为燃料气，会导致锅炉的结垢和腐蚀，作为原料气导致催化剂的中毒和表面覆盖而失活。因此，气体在塔内的2分钟左右停留时间内尽可能除掉氟化物是黄磷尾气资源化的另一个关键。利用氟化硅与水反应生成氟化氢，生成的氟化氢可以与溶液中的钙盐生成难溶于水的氟化钙，被水洗入受磷槽，从而除去绝大部分氟化物。旋流塔作为高效反应器可保持气液充分接触和较高反应温度，促进高温烟道气和雾化的水蒸汽在短时间内充分反应有效脱氟。10天连续跟踪和现场监测结果表明脱氟效果极佳，数据如下：
平均含氟量为1g/m3左右的黄磷尾气，140℃左右的尾气通过塔1的有效接触和旋流充分反应可以去掉50％以上的氟，通过塔2到塔6进一步脱氟后，氟的含量会降调30mg/m3左右，氟的脱除率大于97％，各塔脱氟效果参见图10。说明旋流塔也是个高效的气液反应器。
三、烟道气脱硫效果评价
为了进一步验证旋流塔的效果，我们另外进行了燃煤锅炉中二氧化硫脱除效果评价。
实施例7燃煤锅炉烟道气脱硫效果评价
在4t的燃煤锅炉中进行了双碱法脱硫实验。相关条件和结果如下：
烟道气流量55000 Nm3/h，烟气温度180℃，进口SO2浓度为2000mg/Nm3。塔径1.2m，塔高9m，液气比为2/1000，脱硫液为饱和石灰水和1％的氢氧化钠的混合液。改造前脱硫效率为90％，出口硫含量在200mg/Nm3，改造后脱硫率在95％左右，出口硫含量小于100mg/Nm3。说明旋流塔也能有效提高脱硫效率。

Claims (7)

  1. 一种烟道气除尘脱硫新技术，其特征在于：通过旋流导流板(3)使气体沿切线方向进入前置的除尘水洗塔或直接进入烟道中，促使热烟道气沿着水平切线方向旋转并螺旋上升，同时利用泵施加了动能的循环洗涤液从喷嘴喷出时产生的反作用力推动活动喷嘴顺气流方向旋转，利用雾化喷嘴或可以活动的旋转喷嘴充分雾化洗涤液，小流量的旋转水雾，可以实现快速汽化降温，使高温烟道气体积骤降形成负压，在合理设置的旋流导流板导引下可能产生类似龙卷风的快速旋流效果，使烟道气在洗涤塔内产生螺旋上升运动，从整体向上运动方向改变为螺旋上升运动，烟道气中夹带的灰尘、二氧化硫和二氧化氮等在自身动力和旋流产生的离心力推动下有更多机会与悬浮在体系中雾化的弱碱水充分接触反应或被捕获，潮湿的环境和碱弱性的水雾可以显著消除体系静电，增强捕捉和沉降灰尘和有害气体效果。快速运动的气液旋流加速和促进了比重大的灰尘、液体朝着壁面富集，可显著增强除尘效果。此外，富含水蒸汽的烟道气在旋转和冷却过程中会产生二次水雾，也可以协助吸尘和被有效分离。采用多塔串联和多位置的上下方向的旋喷雾装置可以进一步确保效果。
  2. 根据权利要求1所述，首先使进塔气体产生旋流，可在气流入塔处安装旋流导流板(3)，旋流导流板(3)可以是弧形等任意形状，优选弧形；也可以改变管道以切线方式进气形成旋流。根据具体情形，气体出口横截面可以缩小到原来的5％～95％，优选30％～70％。
  3. 根据权利要求1所述，塔内安装雾化喷头、旋转喷嘴或者其他能够产生气液旋转提高分散效果的装置，优选旋转喷嘴。可以通过控制流体压力和流量， 达到不同的净化要求。甚至在较高气速的情况下，可以不使用喷嘴或旋转喷嘴。
  4. 根据权利要求1所述的旋转喷嘴，可以是任何可以转动的喷嘴，也可以是转动喷嘴和雾化喷嘴的结合。其材质可以是不锈钢、塑料、聚四氟乙烯、玻璃、陶瓷等。
  5. 根据权利要求1所述的喷嘴，根据具体情况和要求可在水洗塔、串联水洗塔、烟道的底部、中部、上部(或每隔3-5m)安装一个或多个。旋转喷嘴，可以喷射液体或者气体。可以是扇形喷嘴、锥形喷嘴或者射流喷嘴等各种液体雾化或溅射装置。
  6. 根据权利要求1所述的烟道气，可以是燃煤锅炉尾气、燃气锅炉尾气、燃油锅炉尾气、黄磷尾气、炼铁炼钢尾气、焦炉尾气、水泥厂尾气等各种需要除尘、脱硫、脱硝、脱臭的外排尾气。
  7. 根据权利要求1所述的烟道气净化技术，可以拓展应用于反应、吸收、尾气净化、烘干、再除尘、浓缩、干燥及其它余热利用等各种化工、加工、环保领域。
PCT/CN2014/088632 2014-10-15 2014-10-15 一种烟道气除尘脱硫方法和设备 Ceased WO2016058141A1 (zh)

Priority Applications (1)

Application Number Priority Date Filing Date Title
PCT/CN2014/088632 WO2016058141A1 (zh) 2014-10-15 2014-10-15 一种烟道气除尘脱硫方法和设备

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
PCT/CN2014/088632 WO2016058141A1 (zh) 2014-10-15 2014-10-15 一种烟道气除尘脱硫方法和设备

Publications (1)

Publication Number Publication Date
WO2016058141A1 true WO2016058141A1 (zh) 2016-04-21

Family

ID=55745957

Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/CN2014/088632 Ceased WO2016058141A1 (zh) 2014-10-15 2014-10-15 一种烟道气除尘脱硫方法和设备

Country Status (1)

Country Link
WO (1) WO2016058141A1 (zh)

Cited By (27)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN108088286A (zh) * 2018-01-16 2018-05-29 苏州工业园区五九洁净工程有限公司 一种聚酯薄膜生产尾气低聚物清除和余热回用系统
CN108246038A (zh) * 2018-03-28 2018-07-06 罗力 抗堵塞长周期运行的烟气湿法脱硫气液固分离工艺及系统
CN108636065A (zh) * 2018-06-28 2018-10-12 珠海恒基达鑫国际化工仓储股份有限公司 一种废气脱硫除臭装置
CN110180483A (zh) * 2019-06-28 2019-08-30 南充西南石油大学设计研究院有限责任公司成都分公司 无轴流体反应器与含硫气体浆液法脱硫装置
CN110354670A (zh) * 2019-08-15 2019-10-22 太原黑猫炭黑有限责任公司 一种炭黑尾气锅炉烟气脱白系统和方法
CN110605013A (zh) * 2019-10-31 2019-12-24 广东佳德环保科技有限公司 烟气脱硫塔
CN112107990A (zh) * 2020-09-01 2020-12-22 邹华智 一种高效雾化喷淋脱硫塔及其脱硫工艺
CN112121613A (zh) * 2019-06-24 2020-12-25 陆丹 一种化工尾气回收循环再利用装置及其操作方法
CN112275085A (zh) * 2020-11-05 2021-01-29 北京清新环境技术股份有限公司 一种安装在脱硫吸收塔内的烟气冷凝收水装置、系统
CN112403231A (zh) * 2020-11-23 2021-02-26 浙江鸿盛新材料科技集团股份有限公司 一种模块化脱硫脱硝脱voc除尘一体系统
CN113648798A (zh) * 2021-07-29 2021-11-16 张陆军 一种烟气脱硫装置
CN114644323A (zh) * 2020-12-17 2022-06-21 中节能工业节能有限公司 一种除尘收磷系统及除尘收磷方法
CN114774174A (zh) * 2022-04-14 2022-07-22 河海大学 一种填料原位灵活更换的沼气提纯装置
CN114797418A (zh) * 2021-01-19 2022-07-29 北京紫光英力化工技术有限公司 一种烟道气深度除尘脱硫脱硝新工艺及高效节能装备系统
CN115253642A (zh) * 2022-08-16 2022-11-01 肇庆宏旺金属实业有限公司 一种不锈钢冷轧带酸洗废气处理装置
CN115318049A (zh) * 2022-08-09 2022-11-11 江苏乾峰顺驰电力设备有限公司 一种降温高效烟气脱硫除尘器
CN115671991A (zh) * 2022-09-20 2023-02-03 中国大唐集团科学技术研究总院有限公司西北电力试验研究院 一种自适应脱硫喷淋塔的气液传质装置
CN115772428A (zh) * 2022-11-18 2023-03-10 铜陵泰富特种材料有限公司 一种湿法脱硫工艺中焦炉煤气高效脱硫捕雾方法
CN116200215A (zh) * 2023-04-11 2023-06-02 上海电气集团股份有限公司 燃气净化系统和净化工艺
CN116692792A (zh) * 2023-06-08 2023-09-05 昆明理工大学 一种黄磷尾气干法脱硫耦合磷矿石品位提升的方法及装置
CN116764406A (zh) * 2023-06-15 2023-09-19 连云港石化有限公司 一种低阻力尾气协同净化装置
CN117052531A (zh) * 2023-08-18 2023-11-14 北京博威能源科技股份有限公司 一种静音型的柴油发电机组
CN117065571A (zh) * 2023-10-13 2023-11-17 汇舸(南通)环保设备有限公司 一种利用旋流提高净化效率的烟气过滤智能净化装置
CN117339324A (zh) * 2023-09-28 2024-01-05 邓宪国 一种环保多功能除尘设备
CN117643775A (zh) * 2024-01-30 2024-03-05 国家能源集团煤焦化有限责任公司 一种逆流淋喷型油水分离器
CN117797580A (zh) * 2024-01-19 2024-04-02 浙江闰土染料有限公司 喷雾干燥塔尾气无烟化循环处理系统
CN120479177A (zh) * 2025-06-11 2025-08-15 河南神马氢化学有限责任公司 一种硫回收制酸用尾气洗涤装置及洗涤方法

Citations (9)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN2230609Y (zh) * 1995-08-30 1996-07-10 戎兴汉 一种填料塔用布液器
CN2510149Y (zh) * 2001-12-06 2002-09-11 杨振坤 复螺旋叶导向除尘脱硫装置
CN2779257Y (zh) * 2004-10-25 2006-05-10 福建鑫泽环保设备工程有限公司 双旋湿法烟气净化装置
CN201329247Y (zh) * 2008-11-24 2009-10-21 徐瑞丰 一种气动旋流复合式脱硫除尘装置
CN101642670A (zh) * 2009-08-28 2010-02-10 史剑武 旋流除尘脱硫装置
CN102085450A (zh) * 2010-12-17 2011-06-08 秦皇岛双轮环保科技有限公司 中小型锅炉烟气一体化脱硫除尘方法
CN202289795U (zh) * 2011-10-26 2012-07-04 程德荣 旋流式水膜脱硫除尘器
CN202555164U (zh) * 2012-04-18 2012-11-28 哈尔滨蔚蓝环保设备制造有限公司 一种带有湿式旋流塔板的脱硫塔
CN104096434A (zh) * 2013-04-03 2014-10-15 厦门大学 一种烟道气除尘脱硫新技术和新装备

Patent Citations (9)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN2230609Y (zh) * 1995-08-30 1996-07-10 戎兴汉 一种填料塔用布液器
CN2510149Y (zh) * 2001-12-06 2002-09-11 杨振坤 复螺旋叶导向除尘脱硫装置
CN2779257Y (zh) * 2004-10-25 2006-05-10 福建鑫泽环保设备工程有限公司 双旋湿法烟气净化装置
CN201329247Y (zh) * 2008-11-24 2009-10-21 徐瑞丰 一种气动旋流复合式脱硫除尘装置
CN101642670A (zh) * 2009-08-28 2010-02-10 史剑武 旋流除尘脱硫装置
CN102085450A (zh) * 2010-12-17 2011-06-08 秦皇岛双轮环保科技有限公司 中小型锅炉烟气一体化脱硫除尘方法
CN202289795U (zh) * 2011-10-26 2012-07-04 程德荣 旋流式水膜脱硫除尘器
CN202555164U (zh) * 2012-04-18 2012-11-28 哈尔滨蔚蓝环保设备制造有限公司 一种带有湿式旋流塔板的脱硫塔
CN104096434A (zh) * 2013-04-03 2014-10-15 厦门大学 一种烟道气除尘脱硫新技术和新装备

Cited By (37)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN108088286A (zh) * 2018-01-16 2018-05-29 苏州工业园区五九洁净工程有限公司 一种聚酯薄膜生产尾气低聚物清除和余热回用系统
CN108246038A (zh) * 2018-03-28 2018-07-06 罗力 抗堵塞长周期运行的烟气湿法脱硫气液固分离工艺及系统
CN108636065A (zh) * 2018-06-28 2018-10-12 珠海恒基达鑫国际化工仓储股份有限公司 一种废气脱硫除臭装置
CN108636065B (zh) * 2018-06-28 2023-11-14 珠海恒基达鑫国际化工仓储股份有限公司 一种废气脱硫除臭装置
CN112121613A (zh) * 2019-06-24 2020-12-25 陆丹 一种化工尾气回收循环再利用装置及其操作方法
CN110180483A (zh) * 2019-06-28 2019-08-30 南充西南石油大学设计研究院有限责任公司成都分公司 无轴流体反应器与含硫气体浆液法脱硫装置
CN110180483B (zh) * 2019-06-28 2024-05-28 南充西南石油大学设计研究院有限责任公司成都分公司 无轴流体反应器与含硫气体浆液法脱硫装置
CN110354670A (zh) * 2019-08-15 2019-10-22 太原黑猫炭黑有限责任公司 一种炭黑尾气锅炉烟气脱白系统和方法
CN110605013A (zh) * 2019-10-31 2019-12-24 广东佳德环保科技有限公司 烟气脱硫塔
CN112107990A (zh) * 2020-09-01 2020-12-22 邹华智 一种高效雾化喷淋脱硫塔及其脱硫工艺
CN112275085A (zh) * 2020-11-05 2021-01-29 北京清新环境技术股份有限公司 一种安装在脱硫吸收塔内的烟气冷凝收水装置、系统
CN112403231A (zh) * 2020-11-23 2021-02-26 浙江鸿盛新材料科技集团股份有限公司 一种模块化脱硫脱硝脱voc除尘一体系统
CN114644323A (zh) * 2020-12-17 2022-06-21 中节能工业节能有限公司 一种除尘收磷系统及除尘收磷方法
CN114644323B (zh) * 2020-12-17 2023-11-28 中节能工业节能有限公司 一种除尘收磷系统及除尘收磷方法
CN114797418A (zh) * 2021-01-19 2022-07-29 北京紫光英力化工技术有限公司 一种烟道气深度除尘脱硫脱硝新工艺及高效节能装备系统
CN114797418B (zh) * 2021-01-19 2024-06-04 北京紫光英力化工技术有限公司 一种烟道气深度除尘脱硫脱硝新工艺及高效节能装备系统
CN113648798B (zh) * 2021-07-29 2023-06-27 山东瑞龙环保科技有限公司 一种烟气脱硫装置
CN113648798A (zh) * 2021-07-29 2021-11-16 张陆军 一种烟气脱硫装置
CN114774174A (zh) * 2022-04-14 2022-07-22 河海大学 一种填料原位灵活更换的沼气提纯装置
CN115318049A (zh) * 2022-08-09 2022-11-11 江苏乾峰顺驰电力设备有限公司 一种降温高效烟气脱硫除尘器
CN115253642A (zh) * 2022-08-16 2022-11-01 肇庆宏旺金属实业有限公司 一种不锈钢冷轧带酸洗废气处理装置
CN115253642B (zh) * 2022-08-16 2024-03-19 肇庆宏旺金属实业有限公司 一种不锈钢冷轧带酸洗废气处理装置
CN115671991A (zh) * 2022-09-20 2023-02-03 中国大唐集团科学技术研究总院有限公司西北电力试验研究院 一种自适应脱硫喷淋塔的气液传质装置
CN115772428A (zh) * 2022-11-18 2023-03-10 铜陵泰富特种材料有限公司 一种湿法脱硫工艺中焦炉煤气高效脱硫捕雾方法
CN116200215A (zh) * 2023-04-11 2023-06-02 上海电气集团股份有限公司 燃气净化系统和净化工艺
CN116692792A (zh) * 2023-06-08 2023-09-05 昆明理工大学 一种黄磷尾气干法脱硫耦合磷矿石品位提升的方法及装置
CN116764406B (zh) * 2023-06-15 2024-05-28 连云港石化有限公司 一种低阻力尾气协同净化装置
CN116764406A (zh) * 2023-06-15 2023-09-19 连云港石化有限公司 一种低阻力尾气协同净化装置
CN117052531B (zh) * 2023-08-18 2024-02-09 北京博威能源科技股份有限公司 一种静音型的柴油发电机组
CN117052531A (zh) * 2023-08-18 2023-11-14 北京博威能源科技股份有限公司 一种静音型的柴油发电机组
CN117339324A (zh) * 2023-09-28 2024-01-05 邓宪国 一种环保多功能除尘设备
CN117065571A (zh) * 2023-10-13 2023-11-17 汇舸(南通)环保设备有限公司 一种利用旋流提高净化效率的烟气过滤智能净化装置
CN117065571B (zh) * 2023-10-13 2024-01-23 汇舸(南通)环保设备有限公司 一种利用旋流提高净化效率的烟气过滤智能净化装置
CN117797580A (zh) * 2024-01-19 2024-04-02 浙江闰土染料有限公司 喷雾干燥塔尾气无烟化循环处理系统
CN117643775A (zh) * 2024-01-30 2024-03-05 国家能源集团煤焦化有限责任公司 一种逆流淋喷型油水分离器
CN117643775B (zh) * 2024-01-30 2024-04-02 国家能源集团煤焦化有限责任公司 一种逆流淋喷型油水分离器
CN120479177A (zh) * 2025-06-11 2025-08-15 河南神马氢化学有限责任公司 一种硫回收制酸用尾气洗涤装置及洗涤方法

Similar Documents

Publication Publication Date Title
CN104096434A (zh) 一种烟道气除尘脱硫新技术和新装备
CN105107365B (zh) 烟气复合相变除尘脱硫工艺及装置
CN205042255U (zh) 双筒多级气旋烟气净化装置及设有该装置的脱硫吸收塔
CN205019942U (zh) 烟气复合相变除尘脱硫装置
CN103868087A (zh) 一种协同增强pm2.5脱除和烟气余热深度利用的方法及装置
CN104667687B (zh) 无源板式湿式除尘除雾装置及其处理工艺
CN202860335U (zh) 一种脱硫除尘器
CN106621680A (zh) 一种湿法脱硫后的烟气深度除尘方法和系统
CN101185840A (zh) 涡轮式增压加速烟气脱硫除尘塔
CN204582953U (zh) 一种可以同时脱除多种污染物的节能脱硫装置
CN204411992U (zh) 无源板式湿式除尘除雾装置
CN204543929U (zh) 烟气净化装置
CN107158913A (zh) 一种脱硫烟气超净除尘的装置和方法
CN110898584A (zh) 低温湿式烟气除尘消白装置及其使用方法
CN205435424U (zh) 一种同步脱硫脱硝脱汞系统
CN207137534U (zh) 一种凝并增强型旋流除尘除雾装置
CN204637887U (zh) 多级多气旋除雾除尘装置
CN203469746U (zh) 设有多级加湿除雾装置的湿法脱硫系统
CN204107255U (zh) 一种组合文氏管除尘器
CN106964224A (zh) 一种除尘除雾装置及其水循环系统
CN201684533U (zh) 湿式除尘脱硫装置
CN205850571U (zh) 一种烟气so3脱除提效装置
CN201249099Y (zh) 一种具有脱硫功能的水膜除尘装置
CN205435417U (zh) 一种协同脱汞系统
CN106039911A (zh) 一种烟气处理的设备和方法

Legal Events

Date Code Title Description
121 Ep: the epo has been informed by wipo that ep was designated in this application

Ref document number: 14904003

Country of ref document: EP

Kind code of ref document: A1

NENP Non-entry into the national phase

Ref country code: DE

32PN Ep: public notification in the ep bulletin as address of the adressee cannot be established

Free format text: NOTING OF LOSS OF RIGHTS PURSUANT TO RULE 112(1) EPC (EPO FORM 1205A DATED 10.08.2017)

122 Ep: pct application non-entry in european phase

Ref document number: 14904003

Country of ref document: EP

Kind code of ref document: A1