CN105498446A - Method for recycling organic matter through organic waste gas adsorption, steam desorption and fractional condensation - Google Patents
Method for recycling organic matter through organic waste gas adsorption, steam desorption and fractional condensation Download PDFInfo
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- CN105498446A CN105498446A CN201610013453.7A CN201610013453A CN105498446A CN 105498446 A CN105498446 A CN 105498446A CN 201610013453 A CN201610013453 A CN 201610013453A CN 105498446 A CN105498446 A CN 105498446A
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- B01D53/02—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography
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- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
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- 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
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Abstract
本发明涉及有机废气回收领域，旨在提供一种有机废气吸附-蒸汽脱附-分级冷凝回收有机物的方法。该方法是将待处理气体经过滤棉预处理后，进入装填了吸附剂的吸附器脱除有机物，净化后的气体排放至大气；吸附剂的脱附再生则包括蒸汽脱附再生、热空气干燥和冷空气冷却的步骤，蒸汽与脱附气体经两级冷凝器实现分离。本发明利用两步分级冷凝，使得高沸点与低沸点有机物相互分离，提高了所回收有机物浓度。对于经处理后的少量不凝气体，通入进风口与进口废气混合，进行二次吸附，保证了全过程没有超标尾气排放。有机物回收纯度高，能耗低，无二次污染。
The invention relates to the field of organic waste gas recovery, and aims to provide a method for organic waste gas adsorption-steam desorption-stage condensation recovery of organic matter. In this method, the gas to be treated is pretreated by filter cotton, then enters the adsorber filled with adsorbent to remove organic matter, and the purified gas is discharged to the atmosphere; the desorption regeneration of the adsorbent includes steam desorption regeneration, hot air drying In the step of cooling with cold air, the steam and desorbed gas are separated by two-stage condensers. The invention utilizes two-step fractional condensation to separate high-boiling-point organic matter from low-boiling-point organic matter and increase the concentration of recovered organic matter. For a small amount of non-condensable gas after treatment, it is passed into the air inlet and mixed with the imported exhaust gas for secondary adsorption to ensure that there is no excessive exhaust gas emission in the whole process. The recovery of organic matter has high purity, low energy consumption and no secondary pollution.
Description
技术领域technical field
本发明涉及有机废气回收领域，尤其涉及一种有机废气吸附-蒸汽脱附-分级冷凝回收有机物的方法及装置。The invention relates to the field of organic waste gas recovery, in particular to a method and device for organic waste gas adsorption-steam desorption-gradient condensation recovery of organic matter.
背景技术Background technique
挥发性有机物(VOCs)不仅对人体健康有着严重的毒害作用，也是雾霾形成的重要原因之一。工业生产中有机溶剂的大量使用导致了有机废气的产生，不仅对环境造成污染，也是严重的资源浪费。目前，吸附-蒸汽脱附-冷凝回收技术由于其处理效果好、安全程度高、可回收有机物的优点，在有机废气的处理中广泛使用。但该技术在运行中存在冷凝液分离成本高，不凝性尾气超标排放的缺点。Volatile organic compounds (VOCs) not only have a serious toxic effect on human health, but also one of the important reasons for the formation of smog. The extensive use of organic solvents in industrial production has led to the generation of organic waste gas, which not only pollutes the environment, but is also a serious waste of resources. At present, the adsorption-steam desorption-condensation recovery technology is widely used in the treatment of organic waste gas due to its advantages of good treatment effect, high safety and recyclable organic matter. However, this technology has the disadvantages of high cost of condensate separation and excessive discharge of non-condensable tail gas during operation.
中国发明专利CN104740973A公开了一种高浓度有机废气中有机溶剂的回收装置，其中所脱附的气体经冷凝和气液分离后外排，少量不凝有机气体进入大气，造成污染。发明CN103585854A公开了一种活性炭吸附、N2脱附回收处理有机废气的工艺，其采用热氮气脱附，由于氮气为不凝性气体，所脱附有机废气冷凝回收率低，能耗高。发明专利CN104815518A公开了一种有机废气深度净化处理系统及其处理方法，该方法中对冷凝回收的有机溶剂进行蒸馏分离，能耗高。Chinese invention patent CN104740973A discloses a recovery device for organic solvents in high-concentration organic waste gas, in which the desorbed gas is discharged after condensation and gas-liquid separation, and a small amount of non-condensable organic gas enters the atmosphere, causing pollution. Invention CN103585854A discloses a process of activated carbon adsorption and N2 desorption to recover and treat organic waste gas. It uses hot nitrogen for desorption. Since nitrogen is a non-condensable gas, the desorbed organic waste gas has a low condensation recovery rate and high energy consumption. Invention patent CN104815518A discloses an organic waste gas advanced purification treatment system and its treatment method. In this method, the organic solvent recovered by condensation is distilled and separated, and the energy consumption is high.
发明内容Contents of the invention
本发明要解决的技术问题是，克服现有技术中存在的不足，提供了一种有机废气吸附-蒸汽脱附-分级冷凝回收有机物的方法及装置。The technical problem to be solved by the present invention is to overcome the deficiencies in the prior art and provide a method and device for organic waste gas adsorption-steam desorption-gradient condensation recovery of organic matter.
为解决技术问题，本发明的解决方案是：For solving technical problem, solution of the present invention is:
提供一种有机废气吸附-蒸汽脱附-分级冷凝回收有机物的方法，包括以下步骤：A method for organic waste gas adsorption-steam desorption-fractional condensation recovery of organic matter is provided, comprising the following steps:
(1)待处理气体经过滤棉预处理后，送入装填了吸附剂的吸附器脱除有机物，净化后的气体排放至大气；(1) After the gas to be treated is pretreated by filter cotton, it is sent to the adsorber filled with adsorbent to remove organic matter, and the purified gas is discharged to the atmosphere;
(2)吸附剂的脱附再生(2) Desorption regeneration of adsorbent
向吸附器内通入蒸汽，对使用后的吸附剂进行脱附再生；当被吸附有机物实现脱附达95％以上时，停止通入蒸汽，向吸附器内通入热空气，持续15～30min，以对吸附剂进行干燥处理并进一步脱附残留的有机物；然后开启风机，通入冷空气对吸附器进行冷却，持续5～15min；吸附剂的脱附再生过程完成，吸附器再次投入运行；Put steam into the adsorber to desorb and regenerate the used adsorbent; when the adsorbed organic matter achieves desorption of more than 95%, stop feeding steam, and let hot air into the adsorber for 15-30 minutes , to dry the adsorbent and further desorb the residual organic matter; then turn on the fan and let in cold air to cool the adsorber for 5-15 minutes; the desorption regeneration process of the adsorbent is completed, and the adsorber is put into operation again;
在通入蒸汽进行脱附再生的过程中，蒸汽与脱附气体排出吸附器后，一并进入初级冷凝器内进行初级冷凝；一次冷凝后的凝液送至油水分离器分离(主要成分为水、高沸点有机物和水溶性有机物)，不凝气体则送入二级冷凝器进行二次冷凝；二次冷凝后的凝液送入储罐(主要成分为低沸点有机物)，残余的不凝气体被送至废气进口，与新的待处理气体混合后进行再次进行吸附处理；During the desorption and regeneration process of introducing steam, after the steam and the desorbed gas are discharged from the adsorber, they enter the primary condenser together for primary condensation; the condensate after primary condensation is sent to the oil-water separator for separation (the main component is water , high-boiling point organic matter and water-soluble organic matter), the non-condensable gas is sent to the secondary condenser for secondary condensation; the condensate after the secondary condensation is sent to the storage tank (mainly composed of low-boiling point organic matter), and the remaining non-condensable gas It is sent to the exhaust gas inlet, mixed with new gas to be treated, and then adsorbed again;
在通入热空气进行干燥的过程中，热空气与脱附气体排出吸附器后，同样经过两级冷凝处理，残余不凝气体送回废气进口用于再次吸附处理。In the process of drying with hot air, after the hot air and desorbed gas are discharged from the adsorber, they are also subjected to two-stage condensation treatment, and the residual non-condensable gas is sent back to the waste gas inlet for re-adsorption treatment.
本发明中，所述吸附器至少包括两台且并联设置、交替使用；在使用一部分吸附器进行有机物回收处理时，对其它吸附器进行吸附剂脱附再生处理。In the present invention, at least two adsorbers are arranged in parallel and used alternately; when a part of the adsorbers are used for recovery of organic matter, other adsorbers are subjected to desorption and regeneration treatment of adsorbents.
本发明中，在吸附剂的脱附再生过程中，向吸附器内通入的水蒸汽的温度为110～200℃；干燥处理时，通入的热空气温度为60～90℃；通入冷空气冷却后，吸附罐内的温度降至室温。In the present invention, during the desorption and regeneration process of the adsorbent, the temperature of the water vapor passed into the adsorber is 110-200°C; After the air is cooled, the temperature inside the adsorption tank drops to room temperature.
本发明中，脱附气体经过初级冷凝器后，温度降至50～80℃；脱附气体经过二级冷凝器后，温度降至-50～10℃。In the present invention, after the desorbed gas passes through the primary condenser, the temperature drops to 50-80°C; after the desorbed gas passes through the secondary condenser, the temperature drops to -50-10°C.
本发明中，所述吸附剂是蜂窝状活性炭吸附剂、活性炭纤维吸附剂、沸石分子筛或吸附树脂中的任意一种。In the present invention, the adsorbent is any one of honeycomb activated carbon adsorbent, activated carbon fiber adsorbent, zeolite molecular sieve or adsorption resin.
本发明还提供了一种用于有机废气吸附-蒸汽脱附-分级冷凝回收有机物的装置，包括装有脱附剂的吸附器；所述吸附器至少包括两台且并联设置、交替使用；The present invention also provides a device for organic waste gas adsorption-steam desorption-staged condensation recovery of organic matter, which includes an adsorber equipped with a desorbent; the adsorber includes at least two and is arranged in parallel and used alternately;
废气入口分别通过管道接至每个吸附器的底部，且管道上装有过滤棉；吸附器的顶部分别设净化气排放管、蒸汽管道和热空气管道；吸附器底部还设有脱附气体排放管，脱附气体排放管依次与初级冷凝器、二级冷凝器相接，二级冷凝器的出口接至废气入口；初级冷凝器底部的凝液排放管接至油水分离器，二级冷凝器底部的凝液排放管接至凝液储罐。The exhaust gas inlet is connected to the bottom of each adsorber through pipes, and filter cotton is installed on the pipes; the top of the adsorber is respectively equipped with a purified gas discharge pipe, a steam pipe and a hot air pipe; the bottom of the adsorber is also provided with a desorption gas discharge pipe , the desorption gas discharge pipe is connected to the primary condenser and the secondary condenser in turn, and the outlet of the secondary condenser is connected to the exhaust gas inlet; the condensate discharge pipe at the bottom of the primary condenser is connected to the oil-water separator, and the bottom of the secondary condenser Connect the condensate drain pipe to the condensate storage tank.
本发明中，所述初级冷凝器是利用冷却水实现热交换，由循环水泵经冷却水管连接初级冷凝器与循环水冷却塔。In the present invention, the primary condenser utilizes cooling water to realize heat exchange, and the circulating water pump connects the primary condenser and the circulating water cooling tower through a cooling water pipe.
本发明中，在二级冷凝器出口端接有一个风机。In the present invention, a fan is connected to the outlet of the secondary condenser.
本发明中，所述二级冷凝器是蒸汽压缩式冷凝器、吸收式冷凝器、蒸汽喷射式冷凝器或半导体冷凝器中的任意一种。In the present invention, the secondary condenser is any one of vapor compression condenser, absorption condenser, steam injection condenser or semiconductor condenser.
经处理后，本发明装置的油水分离器中分离出水溶性有机物和高沸点有机物，凝液储罐中收集到低沸点有机物。After the treatment, the water-soluble organic matter and the high-boiling point organic matter are separated in the oil-water separator of the device of the present invention, and the low-boiling point organic matter is collected in the condensate storage tank.
与现有技术相比，本发明具有的优势为：Compared with the prior art, the present invention has the advantages of:
1、利用两步分级冷凝，使得高沸点与低沸点有机物相互分离，提高了所回收有机物浓度。1. Two-step fractional condensation is used to separate high-boiling-point and low-boiling-point organic matter, increasing the concentration of recovered organic matter.
2、对于经处理后的少量不凝气体，通入进风口与进口废气混合，进行二次吸附，保证了全过程没有超标尾气排放。2. For a small amount of non-condensable gas after treatment, it is passed into the air inlet and mixed with the imported exhaust gas for secondary adsorption to ensure that there is no excessive exhaust gas emission in the whole process.
3、本发明适用于加油站中汽油、柴油的油气回收和化工、涂装、合成革、橡胶塑料制品、印刷包装、纺织印染、木业、制鞋、化纤、生活服务业、储存运输、建筑装饰和电子信息等行业所排放的非甲烷总烃类、苯系物类、酯类、醇类、酮类和醛类有机物的回收处理，有机物回收纯度高，能耗低，无二次污染。3. The present invention is suitable for oil gas recovery of gasoline and diesel oil in gas stations, chemical industry, painting, synthetic leather, rubber and plastic products, printing and packaging, textile printing and dyeing, wood industry, shoemaking, chemical fiber, life service industry, storage and transportation, construction Recycling and treatment of non-methane total hydrocarbons, benzene series, esters, alcohols, ketones and aldehydes discharged from industries such as decoration and electronic information. The recovery of organic matter has high purity, low energy consumption, and no secondary pollution.
附图说明Description of drawings
图1是具有两台吸附器的有机废气吸附-蒸汽脱附-分级冷凝回收有机物装置的结构示意图。Figure 1 is a schematic structural diagram of an organic waste gas adsorption-steam desorption-stage condensation recovery organic matter device with two adsorbers.
1—废气进口；2—蒸汽进口；3—热空气进口；4、5—净化气出口；1—exhaust gas inlet; 2—steam inlet; 3—hot air inlet; 4, 5—purified gas outlet;
6—冷却气出口；7、8—过滤棉；9、10—吸附器；11—初级冷凝器；6—cooling air outlet; 7, 8—filter cotton; 9, 10—adsorber; 11—primary condenser;
12—油水分离装置；13—循环水泵；14—循环水冷却塔；12—oil-water separation device; 13—circulating water pump; 14—circulating water cooling tower;
15—二级冷凝器；16—凝液储罐；17—风机；18—27为阀门。15—secondary condenser; 16—condensate storage tank; 17—fan; 18—27 are valves.
图2是具有三台吸附器的有机废气吸附-蒸汽脱附-分级冷凝回收有机物装置的结构示意图。Fig. 2 is a schematic structural diagram of an organic waste gas adsorption-steam desorption-staged condensation recovery organic matter device with three adsorbers.
28—废气进口；29—蒸汽进口；30—热空气进口；31、32、33—净化气出口；34—冷却气出口；35、36、37—过滤棉；38、39、40—吸附器；41—初级冷凝器；42—油水分离装置；43—循环水泵；44—循环水冷却塔；28—exhaust gas inlet; 29—steam inlet; 30—hot air inlet; 31, 32, 33—purified gas outlet; 34—cooling air outlet; 35, 36, 37—filter cotton; 38, 39, 40—adsorber; 41—primary condenser; 42—oil-water separation device; 43—circulating water pump; 44—circulating water cooling tower;
45—二级冷凝器；46—凝液储罐；47—风机；48—61为阀门。45—secondary condenser; 46—condensate storage tank; 47—fan; 48—61 are valves.
具体实施方式detailed description
实施例1：Example 1:
本实施例提供具有两台吸附器的有机废气吸附-蒸汽脱附-分级冷凝回收有机物装置，结构示意图见图1。装置包括：1—废气进口；2—蒸汽进口；3—热空气进口；4、5—净化气出口；6—冷却气出口；7、8—过滤棉；9、10—吸附器；11—初级冷凝器；12—油水分离装置；13—循环水泵；14—循环水冷却塔；15—二级冷凝器；16—凝液储罐；17—风机；18—27为阀门。This embodiment provides an organic waste gas adsorption-steam desorption-staged condensation recovery organic matter device with two adsorbers. The schematic diagram of the structure is shown in FIG. 1 . The device includes: 1—exhaust gas inlet; 2—steam inlet; 3—hot air inlet; 4,5—purified gas outlet; 6—cooling air outlet; 7,8—filter cotton; 9,10—adsorber; 11—primary Condenser; 12—oil-water separation device; 13—circulating water pump; 14—circulating water cooling tower; 15—secondary condenser; 16—condensate storage tank; 17—fan; 18—27 are valves.
所述吸附器9和吸附器10内装填有蜂窝状活性炭吸附剂。The adsorber 9 and the adsorber 10 are filled with honeycomb activated carbon adsorbent.
所述初级冷凝器11中采用循环水冷却；所述二级冷凝器15中采用蒸汽压缩式制冷。The primary condenser 11 is cooled by circulating water; the secondary condenser 15 is refrigerated by vapor compression.
所述过滤棉7和过滤棉8可利用相应吸附器处于静止状态时进行更换。The filter cotton 7 and the filter cotton 8 can be replaced when the corresponding absorber is in a static state.
将该装置应用于某工厂涂装车间废气的处理中，该废气风量为4000m3/h，出口温度约30℃，主要成分为二甲苯和非甲烷总烃，总浓度约为800mg/m3。利用本实施例中的有机废气吸附-蒸汽脱附-分级冷凝回收有机物装置处理该废气，主要操作步骤如下：The device is applied to the treatment of exhaust gas in a painting workshop of a factory. The air volume of the exhaust gas is 4000m 3 /h, the outlet temperature is about 30°C, and the main components are xylene and non-methane total hydrocarbons, with a total concentration of about 800mg/m 3 . Using the organic waste gas adsorption-steam desorption-graded condensation recovery organic matter device in this example to treat the waste gas, the main operation steps are as follows:
(A1)打开阀门18、19，该车间废气从废气进口1进入处理装置，流经过滤棉7，脱除颗粒物与油性雾滴，再进入吸附器9内吸附，净化气体从净化气出口4排入大气。吸附器9进行吸附作业时，阀门22保持闭合，吸附器10不进行工作；(A1) Open the valves 18 and 19, the waste gas of the workshop enters the treatment device from the waste gas inlet 1, flows through the filter cotton 7, removes particulate matter and oily mist, and then enters the adsorber 9 for adsorption, and the purified gas is discharged from the purified gas outlet 4 into the atmosphere. When the adsorber 9 is performing the adsorption operation, the valve 22 remains closed, and the adsorber 10 does not work;
(A2)吸附7天后，打开阀门22和23，吸附器10开始进行吸附作业。关闭阀门18和19，打开阀门20、21和26，从蒸汽进口向吸附器9内通入110℃水蒸汽，对活性炭吸附剂进行脱附再生。蒸汽与脱附气体由阀门21从吸附器9内排出进入初级冷凝器11，由冷却水换热冷凝，温度降至80℃，凝液进入油水分离器12进行分离，不凝气体进入二级冷凝器15，由蒸汽压缩式制冷系统冷凝，温度降至-10℃，凝液进入凝液储罐16收集，少量不凝气体进入废气进口1，与待处理废气混合进行二次吸附；(A2) After 7 days of adsorption, the valves 22 and 23 are opened, and the adsorber 10 starts the adsorption operation. Close valves 18 and 19, open valves 20, 21 and 26, and feed 110°C water vapor into the adsorber 9 from the steam inlet to desorb and regenerate the activated carbon adsorbent. The steam and desorbed gas are discharged from the adsorber 9 through the valve 21 and enter the primary condenser 11, where they are condensed by cooling water heat exchange, and the temperature drops to 80°C. The condensate enters the oil-water separator 12 for separation, and the non-condensable gas enters the secondary condensation The device 15 is condensed by the vapor compression refrigeration system, the temperature drops to -10°C, the condensate enters the condensate storage tank 16 for collection, and a small amount of non-condensable gas enters the waste gas inlet 1, and is mixed with the waste gas to be treated for secondary adsorption;
(A3)蒸汽脱附30分钟后，停止通入蒸汽，从热空气进口3向吸附器9内通入80℃热空气，对吸附剂进行干燥处理并进一步脱附残留的有机物。出吸附器9的热空气与脱附气体经两级冷凝后，少量不凝气体进入废气进口1，与待处理废气混合进行二次吸附；(A3) After 30 minutes of steam desorption, stop feeding steam, and pass hot air at 80° C. into the adsorber 9 from the hot air inlet 3 to dry the adsorbent and further desorb the residual organic matter. After the hot air and desorbed gas exiting the adsorber 9 are condensed in two stages, a small amount of non-condensable gas enters the waste gas inlet 1, and is mixed with the waste gas to be treated for secondary adsorption;
(A4)热空气干燥15分钟后，关闭阀门20和26，打开阀门19和27，开启风机17，抽取大风量的冷空气对吸附器9进行冷却；(A4) After the hot air is dried for 15 minutes, close the valves 20 and 26, open the valves 19 and 27, open the blower fan 17, and extract the cold air with a large air volume to cool the adsorber 9;
(A5)冷却5分钟后，关闭风机17、阀门19、阀门21和阀门27，吸附器9恢复至常温，进入静置状态。吸附器10吸附7天后，打开阀门18和阀门19，吸附器9开始吸附过程。(A5) After cooling for 5 minutes, turn off the fan 17, valve 19, valve 21 and valve 27, and the adsorber 9 returns to normal temperature and enters a static state. After adsorber 10 adsorbs for 7 days, valve 18 and valve 19 are opened, and adsorber 9 starts the adsorption process.
重复A2～A5的步骤，完成对吸附器10的脱附再生，整套装置脱附完成，进入吸附阶段，如此循环、反复。Repeat the steps of A2-A5 to complete the desorption regeneration of the adsorber 10, the desorption of the whole set of equipment is completed, and enter the adsorption stage, so that the cycle is repeated.
通过该方法进行处理后，该涂装车间尾气得到净化，二甲苯、非甲烷总烃去除率均达到99％以上。脱附-冷凝过程完成后，油水分离装置12中回收到大量甲苯和二甲苯，储罐16中回收到大量非甲烷总烃，且纯度高。After being treated by the method, the tail gas of the painting workshop is purified, and the removal rates of xylene and non-methane total hydrocarbons both reach more than 99%. After the desorption-condensation process is completed, a large amount of toluene and xylene are recovered in the oil-water separation device 12, and a large amount of non-methane total hydrocarbons are recovered in the storage tank 16 with high purity.
实施例2：Example 2:
本实施例提供具有两台吸附器的有机废气吸附-蒸汽脱附-分级冷凝回收有机物装置，结构示意图见图1。装置包括：1—废气进口；2—蒸汽进口；3—热空气进口；4、5—净化气出口；6—冷却气出口；7、8—过滤棉；9、10—吸附器；11—初级冷凝器；12—油水分离装置；13—循环水泵；14—循环水冷却塔；15—二级冷凝器；16—凝液储罐；17—风机；18—26为阀门。This embodiment provides an organic waste gas adsorption-steam desorption-staged condensation recovery organic matter device with two adsorbers. The schematic diagram of the structure is shown in FIG. 1 . The device includes: 1—exhaust gas inlet; 2—steam inlet; 3—hot air inlet; 4,5—purified gas outlet; 6—cooling air outlet; 7,8—filter cotton; 9,10—adsorber; 11—primary Condenser; 12—oil-water separation device; 13—circulating water pump; 14—circulating water cooling tower; 15—secondary condenser; 16—condensate storage tank; 17—fan; 18—26 are valves.
所述吸附器9和吸附器10内装填有活性炭纤维吸附剂。The adsorber 9 and the adsorber 10 are filled with activated carbon fiber adsorbent.
所述初级冷凝器11中采用循环水冷却；所述二级冷凝器15中采用吸收式制冷。The primary condenser 11 adopts circulating water cooling; the secondary condenser 15 adopts absorption refrigeration.
所述过滤棉7和过滤棉8可利用相应吸附器处于静止状态时进行更换。The filter cotton 7 and the filter cotton 8 can be replaced when the corresponding absorber is in a static state.
将该装置应用于合成革企业干法废气的处理中，该废气风量为10000m3/h，出口温度约35℃，主要成分为DMF、2-丁酮和乙酸甲酯，总浓度约为200mg/m3。利用本实施例中的有机废气吸附-蒸汽脱附-分级冷凝回收有机物装置处理该废气，主要操作步骤如下：This device is applied to the treatment of dry waste gas from synthetic leather enterprises. The air volume of the waste gas is 10,000m 3 /h, the outlet temperature is about 35°C, and the main components are DMF, 2-butanone and methyl acetate, and the total concentration is about 200mg/h. m 3 . Using the organic waste gas adsorption-steam desorption-graded condensation recovery organic matter device in this example to treat the waste gas, the main operation steps are as follows:
(A1)打开阀门18、19，该车间废气从废气进口1进入处理装置，流经过滤棉7，脱除颗粒物与油性雾滴，再进入吸附器9内吸附，净化气体从净化气出口4排入大气。吸附器9进行吸附作业时，阀门22保持闭合，吸附器10不进行工作；(A1) Open the valves 18 and 19, the waste gas of the workshop enters the treatment device from the waste gas inlet 1, flows through the filter cotton 7, removes particulate matter and oily mist, and then enters the adsorber 9 for adsorption, and the purified gas is discharged from the purified gas outlet 4 into the atmosphere. When the adsorber 9 is performing the adsorption operation, the valve 22 remains closed, and the adsorber 10 does not work;
(A2)吸附10天后，打开阀门22、23，吸附器10开始进行吸附作业。关闭阀门18和阀门19，打开阀门20、阀门21和阀门26，从蒸汽进口向吸附器9内通入120℃水蒸汽，对活性炭吸附剂进行脱附再生。蒸汽与脱附气体由阀门21从吸附器9内排出进入初级冷凝器11，由冷却水换热冷凝，温度降至70℃，凝液进入油水分离器12进行分离，不凝气体进入二级冷凝器15，由蒸汽压缩式制冷系统冷凝，温度降至10℃，凝液进入储罐16收集，少量不凝气体进入废气进口1，与待处理废气混合进行二次吸附；(A2) After 10 days of adsorption, the valves 22 and 23 are opened, and the adsorber 10 starts the adsorption operation. Close valve 18 and valve 19, open valve 20, valve 21 and valve 26, and feed 120°C water vapor into the adsorber 9 from the steam inlet to desorb and regenerate the activated carbon adsorbent. The steam and desorbed gas are discharged from the adsorber 9 through the valve 21 and enter the primary condenser 11, where they are condensed by cooling water heat exchange, the temperature drops to 70°C, the condensate enters the oil-water separator 12 for separation, and the non-condensable gas enters the secondary condensation The device 15 is condensed by the vapor compression refrigeration system, the temperature drops to 10°C, the condensate enters the storage tank 16 for collection, and a small amount of non-condensable gas enters the waste gas inlet 1, and is mixed with the waste gas to be treated for secondary adsorption;
(A3)蒸汽脱附30分钟后，停止通入蒸汽，从热空气进口3向吸附器9内通入100℃热空气，对吸附剂进行干燥处理并进一步脱附残留的有机物。出吸附器9的热空气与脱附气体经两级冷凝后，少量不凝气体进入废气进口1，与待处理废气混合进行二次吸附；(A3) After 30 minutes of steam desorption, stop feeding steam, and feed hot air at 100° C. into the adsorber 9 from the hot air inlet 3 to dry the adsorbent and further desorb the residual organic matter. After the hot air and desorbed gas exiting the adsorber 9 are condensed in two stages, a small amount of non-condensable gas enters the waste gas inlet 1, and is mixed with the waste gas to be treated for secondary adsorption;
(A4)热空气干燥20分钟后，关闭阀门20和阀门26，打开阀门19和27，开启风机17，抽取大风量的冷空气对吸附器9进行冷却；(A4) After hot air is dried for 20 minutes, close valve 20 and valve 26, open valve 19 and 27, open blower fan 17, and extract the cold air of large air volume to cool adsorber 9;
(A5)冷却5分钟后，关闭风机17、阀门19、阀门21和阀门27，吸附器9恢复至常温，进入静置状态。吸附器10吸附7天后，打开阀门18和阀门19，吸附器9开始吸附过程。(A5) After cooling for 5 minutes, turn off the fan 17, valve 19, valve 21 and valve 27, and the adsorber 9 returns to normal temperature and enters a static state. After adsorber 10 adsorbs for 7 days, valve 18 and valve 19 are opened, and adsorber 9 starts the adsorption process.
重复A2～A5的步骤，完成对吸附器10的脱附再生，整套装置脱附完成，进入吸附阶段，如此循环、反复。Repeat the steps of A2-A5 to complete the desorption regeneration of the adsorber 10, the desorption of the whole set of equipment is completed, and enter the adsorption stage, so that the cycle is repeated.
通过该方法进行处理后，该涂装车间尾气得到净化，DMF、2-丁酮和乙酸甲酯去除率均达到99％以上。脱附-冷凝过程完成后，油水分离装置12中回收到DMF水溶液和2-丁酮，储罐16中回收到大量乙酸甲酯，且纯度高。After being treated by the method, the tail gas of the painting workshop is purified, and the removal rates of DMF, 2-butanone and methyl acetate all reach more than 99%. After the desorption-condensation process is completed, the DMF aqueous solution and 2-butanone are recovered in the oil-water separation device 12, and a large amount of methyl acetate is recovered in the storage tank 16 with high purity.
实施例3：Example 3:
本实施例提供具有三台吸附器的有机废气吸附-蒸汽脱附-分级冷凝回收有机物装置，结构示意图见图2。装置包括：28—废气进口；29—蒸汽进口；30—热空气进口；31、32、33—净化气出口；34—冷却气出口；35、36、37—过滤棉；38、39、40—吸附器；41—初级冷凝器；42—油水分离装置；43—循环水泵；44—循环水冷却塔；45—二级冷凝器；46—凝液储罐；47—风机；48—61为阀门。This embodiment provides an organic waste gas adsorption-steam desorption-staged condensation recovery organic matter device with three adsorbers. The schematic diagram of the structure is shown in FIG. 2 . The device includes: 28—exhaust gas inlet; 29—steam inlet; 30—hot air inlet; 31, 32, 33—purified gas outlet; 34—cooling air outlet; 35, 36, 37—filter cotton; 38, 39, 40— Adsorber; 41—primary condenser; 42—oil-water separation device; 43—circulating water pump; 44—circulating water cooling tower; 45—secondary condenser; 46—condensate storage tank; 47—fan; 48—61 is valve .
所述吸附器38、39、40内填装有一定量沸石分子筛。The adsorbers 38, 39, 40 are filled with a certain amount of zeolite molecular sieves.
所述初级冷凝器41中采用采用循环水冷却；所述二级冷凝器45中采用半导体制冷系统。The primary condenser 41 adopts circulating water cooling; the secondary condenser 45 adopts a semiconductor refrigeration system.
所述过滤棉35、36、37可利用相应吸附器处于静止状态时进行更换。The filter cottons 35, 36, 37 can be replaced when the corresponding absorbers are in a static state.
将该装置应用于某橡胶硫化车间废气的处理中，该废气风量为70000m3/h，出口温度约25℃，主要成分为甲苯和二硫化碳，总浓度约为50mg/m3。利用本实施例中的有机废气吸附-蒸汽脱附-分级冷凝回收有机物装置处理该废气，主要操作步骤如下：The device is applied to the treatment of exhaust gas in a rubber vulcanization workshop. The air volume of the exhaust gas is 70000m 3 /h, the outlet temperature is about 25℃, the main components are toluene and carbon disulfide, and the total concentration is about 50mg/m 3 . Using the organic waste gas adsorption-steam desorption-graded condensation recovery organic matter device in this example to treat the waste gas, the main operation steps are as follows:
(A1)打开阀门48、49、52和53，该车间废气从废气进口28进入处理装置，流经过滤棉35和36，脱除颗粒物与油性雾滴，再进入吸附器38和39内吸附，净化气体从净化气出口31和32排入大气。在该过程中，阀门56保持闭合，吸附器40不进行工作；(A1) Open the valves 48, 49, 52 and 53, the workshop waste gas enters the treatment device from the waste gas inlet 28, flows through the filter cotton 35 and 36, removes particulate matter and oily mist, and then enters the adsorbers 38 and 39 for adsorption. The purge gas is discharged into the atmosphere from purge gas outlets 31 and 32 . During this process, the valve 56 remains closed and the adsorber 40 does not work;
(A2)吸附14天后，打开阀门56和57，吸附器40开始吸附作业。关闭阀门48和阀门49，打开阀门50、51和60，从蒸汽进口29向吸附器38内通入200℃蒸汽，对沸石分子筛进行脱附再生。蒸汽与脱附气体由阀门51从吸附器38内排出进入初级冷凝器41，由冷却水换热冷凝，温度降至50℃，凝液进入油水分离器42进行分离，不凝气体进入二级冷凝器45，由半导体制冷系统冷凝，温度降至-50℃，凝液进入储罐46收集，少量不凝气体进入废气进口28，与待处理废气混合进行二次吸附；(A2) After 14 days of adsorption, the valves 56 and 57 are opened, and the adsorber 40 starts the adsorption operation. Close valve 48 and valve 49, open valves 50, 51 and 60, and introduce steam at 200°C from steam inlet 29 into adsorber 38 to desorb and regenerate the zeolite molecular sieve. The steam and desorbed gas are discharged from the adsorber 38 through the valve 51 and enter the primary condenser 41, where they are condensed by cooling water heat exchange, the temperature drops to 50°C, the condensate enters the oil-water separator 42 for separation, and the non-condensable gas enters the secondary condensation The device 45 is condensed by the semiconductor refrigeration system, the temperature drops to -50°C, the condensate enters the storage tank 46 for collection, and a small amount of non-condensable gas enters the waste gas inlet 28, and is mixed with the waste gas to be treated for secondary adsorption;
(A3)蒸汽脱附60分钟后，停止通入蒸汽，从热空气进口30向吸附器38内通入180℃热空气，对吸附剂进行干燥处理并进一步脱附残留的有机物。出吸附器38的热空气与脱附气体经两级冷凝后，少量不凝气体进入废气进口28，与待处理废气混合进行二次吸附；(A3) After 60 minutes of steam desorption, stop feeding steam, and feed hot air at 180° C. into the adsorber 38 from the hot air inlet 30 to dry the adsorbent and further desorb the residual organic matter. After the hot air and desorbed gas exiting the adsorber 38 are condensed in two stages, a small amount of non-condensable gas enters the waste gas inlet 28, and is mixed with the waste gas to be treated for secondary adsorption;
(A4)热空气干燥30分钟后，关闭阀门50和阀门60，打开阀门49和阀门61，开启风机47，抽取大风量的冷空气对吸附器38进行冷却；(A4) After hot air drying for 30 minutes, close valve 50 and valve 60, open valve 49 and valve 61, open blower fan 47, and extract the cold air of large air volume to cool adsorber 38;
(A5)冷却15分钟后，吸附器38恢复至常温，关闭阀门49、阀门51、阀门61和风机47，吸附器38进入静置状态。吸附14天后，打开阀门48和阀门49，吸附器38开始吸附过程。(A5) After cooling for 15 minutes, the adsorber 38 returns to normal temperature, and the valve 49, valve 51, valve 61 and fan 47 are closed, and the adsorber 38 enters a static state. After 14 days of adsorption, the valve 48 and the valve 49 are opened, and the adsorber 38 starts the adsorption process.
重复A2～A5的步骤，完成对吸附器39和40的脱附再生，整套装置脱附完成，进入吸附阶段，如此循环、反复。Repeat the steps of A2-A5 to complete the desorption regeneration of the adsorbers 39 and 40, the desorption of the whole set of devices is completed, and enter the adsorption stage, so that the cycle is repeated.
通过该方法进行处理后，该涂装车间尾气得到净化，甲苯和二硫化碳去除率均达到99％以上。脱附-冷凝过程完成后，油水分离装置42中回收到大量甲苯和二甲苯，储罐46中回收到大量二硫化碳，且纯度高。After being treated by the method, the tail gas of the painting workshop is purified, and the removal rates of toluene and carbon disulfide both reach more than 99%. After the desorption-condensation process is completed, a large amount of toluene and xylene are recovered in the oil-water separation device 42, and a large amount of carbon disulfide is recovered in the storage tank 46 with high purity.
实施例4：Example 4:
本实施例提供具有三台吸附器的有机废气吸附-蒸汽脱附-分级冷凝回收有机物装置，结构示意图见图2。装置包括：28—废气进口；29—蒸汽进口；30—热空气进口；31、32、33—净化气出口；34—冷却气出口；35、36、37—过滤棉；38、39、40—吸附器；41—初级冷凝器；42—油水分离装置；43—循环水泵；44—循环水冷却塔；45—二级冷凝器；46—凝液储罐；47—风机；48—61为阀门。This embodiment provides an organic waste gas adsorption-steam desorption-staged condensation recovery organic matter device with three adsorbers. The schematic diagram of the structure is shown in FIG. 2 . The device includes: 28—exhaust gas inlet; 29—steam inlet; 30—hot air inlet; 31, 32, 33—purified gas outlet; 34—cooling air outlet; 35, 36, 37—filter cotton; 38, 39, 40— Adsorber; 41—primary condenser; 42—oil-water separation device; 43—circulating water pump; 44—circulating water cooling tower; 45—secondary condenser; 46—condensate storage tank; 47—fan; 48—61 is valve .
所述吸附器38、39、40内填装有一定量吸附树脂。The adsorbers 38, 39, 40 are filled with a certain amount of adsorption resin.
所述初级冷凝器41中采用循环水冷却；所述二级冷凝器45中采用蒸汽喷射式制冷。The primary condenser 41 is cooled by circulating water; the secondary condenser 45 is cooled by steam injection.
所述过滤棉35、36、37可利用相应吸附器处于静止状态时进行更换。The filter cottons 35, 36, 37 can be replaced when the corresponding absorbers are in a static state.
将该装置应用于某化工企业废气的处理中，该废气风量为20000m3/h，出口温度约25℃，主要成分为甲苯、异丙醇和乙酸乙酯，总浓度约为300mg/m3。利用本实施例中的有机废气吸附-蒸汽脱附-分级冷凝回收有机物装置处理该废气，主要操作步骤如下：The device is applied to the treatment of waste gas in a chemical enterprise. The air volume of the waste gas is 20000m 3 /h, the outlet temperature is about 25°C, the main components are toluene, isopropanol and ethyl acetate, and the total concentration is about 300mg/m 3 . Using the organic waste gas adsorption-steam desorption-graded condensation recovery organic matter device in this example to treat the waste gas, the main operation steps are as follows:
(A1)打开阀门48、49、52和53，该车间废气从废气进口28进入处理装置，流经过滤棉35和36，脱除颗粒物与油性雾滴，再进入吸附器38和39内吸附，净化气体从净化气出口31和32排入大气。在该过程中，阀门56保持闭合，吸附器40不进行工作；(A1) Open the valves 48, 49, 52 and 53, the workshop waste gas enters the treatment device from the waste gas inlet 28, flows through the filter cotton 35 and 36, removes particulate matter and oily mist, and then enters the adsorbers 38 and 39 for adsorption. The purge gas is discharged into the atmosphere from purge gas outlets 31 and 32 . During this process, the valve 56 remains closed and the adsorber 40 does not work;
(A2)吸附14天后，打开阀门56和57，吸附器40开始吸附作业。关闭阀门48和阀门49，打开阀门50、51和60，从蒸汽进口29向吸附器38内通入100℃蒸汽，对沸石分子筛进行脱附再生。蒸汽与脱附气体由阀门51从吸附器38内排出进入初级冷凝器41，由冷却水换热冷凝，温度降至50℃，凝液进入油水分离器42进行分离，不凝气体进入二级冷凝器45，由半导体制冷系统冷凝，温度降至0℃，凝液进入储罐46收集，少量不凝气体进入废气进口28，与待处理废气混合进行二次吸附；(A2) After 14 days of adsorption, the valves 56 and 57 are opened, and the adsorber 40 starts the adsorption operation. Close valve 48 and valve 49, open valves 50, 51 and 60, and feed steam at 100°C from steam inlet 29 into adsorber 38 to desorb and regenerate the zeolite molecular sieve. The steam and desorbed gas are discharged from the adsorber 38 through the valve 51 and enter the primary condenser 41, where they are condensed by cooling water heat exchange, the temperature drops to 50°C, the condensate enters the oil-water separator 42 for separation, and the non-condensable gas enters the secondary condensation The device 45 is condensed by the semiconductor refrigeration system, the temperature drops to 0°C, the condensate enters the storage tank 46 for collection, and a small amount of non-condensable gas enters the waste gas inlet 28, and is mixed with the waste gas to be treated for secondary adsorption;
(A3)蒸汽脱附50分钟后，停止通入蒸汽，从热空气进口30向吸附器38内通入90℃热空气，对吸附剂进行干燥处理并进一步脱附残留的有机物。出吸附器38的热空气与脱附气体经两级冷凝后，少量不凝气体进入废气进口28，与待处理废气混合进行二次吸附；(A3) After 50 minutes of steam desorption, stop feeding steam, and feed hot air at 90° C. into the adsorber 38 from the hot air inlet 30 to dry the adsorbent and further desorb the residual organic matter. After the hot air and desorbed gas exiting the adsorber 38 are condensed in two stages, a small amount of non-condensable gas enters the waste gas inlet 28, and is mixed with the waste gas to be treated for secondary adsorption;
(A4)热空气干燥20分钟后，关闭阀门50和阀门60，打开阀门49和阀门61，开启风机47，抽取大风量的冷空气对吸附器38进行冷却；(A4) After hot air is dried for 20 minutes, close valve 50 and valve 60, open valve 49 and valve 61, open fan 47, and extract the cold air of large air volume to cool adsorber 38;
(A5)冷却10分钟后，吸附器38恢复至常温，关闭阀门49、阀门51、阀门61和风机47，吸附器38进入静置状态。吸附14天后，打开阀门48和阀门49，吸附器38开始吸附过程。(A5) After cooling for 10 minutes, the adsorber 38 returns to normal temperature, and the valve 49, valve 51, valve 61 and fan 47 are closed, and the adsorber 38 enters a static state. After 14 days of adsorption, the valve 48 and the valve 49 are opened, and the adsorber 38 starts the adsorption process.
重复A2～A5的步骤，完成对吸附器39和40的脱附再生，整套装置脱附完成，进入吸附阶段，如此循环、反复。Repeat the steps of A2-A5 to complete the desorption regeneration of the adsorbers 39 and 40, the desorption of the whole set of devices is completed, and enter the adsorption stage, so that the cycle is repeated.
通过该方法进行处理后，该化工尾气得到净化，甲苯、异丙醇和乙酸乙酯去除率均达到99％以上。脱附-冷凝过程完成后，油水分离装置42中回收到大量甲苯和异丙醇溶液，储罐46中回收到大量乙酸乙酯，且纯度高。After being treated by the method, the chemical tail gas is purified, and the removal rates of toluene, isopropanol and ethyl acetate all reach more than 99%. After the desorption-condensation process is completed, a large amount of toluene and isopropanol solutions are recovered in the oil-water separation device 42, and a large amount of ethyl acetate is recovered in the storage tank 46 with high purity.
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Application publication date: 20160420 |