CN108079766A - A kind of low concentration big flow organic exhaust gas closed loop multistage retracting device and recovery method - Google Patents
A kind of low concentration big flow organic exhaust gas closed loop multistage retracting device and recovery method Download PDFInfo
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- 238000011084 recovery Methods 0.000 title claims abstract description 48
- 238000000034 method Methods 0.000 title claims abstract description 10
- 239000007789 gas Substances 0.000 claims abstract description 122
- 238000003795 desorption Methods 0.000 claims abstract description 40
- 230000008929 regeneration Effects 0.000 claims abstract description 35
- 238000011069 regeneration method Methods 0.000 claims abstract description 35
- 239000010815 organic waste Substances 0.000 claims abstract description 26
- 239000002904 solvent Substances 0.000 claims abstract description 20
- 238000010438 heat treatment Methods 0.000 claims abstract description 18
- 238000007791 dehumidification Methods 0.000 claims abstract description 16
- 238000001179 sorption measurement Methods 0.000 claims abstract description 16
- 229910021536 Zeolite Inorganic materials 0.000 claims abstract description 5
- HNPSIPDUKPIQMN-UHFFFAOYSA-N dioxosilane;oxo(oxoalumanyloxy)alumane Chemical compound O=[Si]=O.O=[Al]O[Al]=O HNPSIPDUKPIQMN-UHFFFAOYSA-N 0.000 claims abstract description 5
- 239000010457 zeolite Substances 0.000 claims abstract description 5
- 239000012141 concentrate Substances 0.000 claims abstract description 3
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 12
- 229920006395 saturated elastomer Polymers 0.000 claims description 6
- 238000001816 cooling Methods 0.000 claims description 5
- 230000009286 beneficial effect Effects 0.000 claims description 4
- 238000009835 boiling Methods 0.000 claims description 4
- 239000000498 cooling water Substances 0.000 claims description 3
- 230000007423 decrease Effects 0.000 claims description 3
- 239000000463 material Substances 0.000 claims description 3
- 238000000746 purification Methods 0.000 claims description 3
- 230000032258 transport Effects 0.000 claims description 3
- 239000002918 waste heat Substances 0.000 claims description 3
- 238000005086 pumping Methods 0.000 claims description 2
- 239000002912 waste gas Substances 0.000 abstract description 5
- 239000012855 volatile organic compound Substances 0.000 description 63
- 238000009833 condensation Methods 0.000 description 2
- 230000005494 condensation Effects 0.000 description 2
- 238000007646 gravure printing Methods 0.000 description 2
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 2
- 239000000809 air pollutant Substances 0.000 description 1
- 231100001243 air pollutant Toxicity 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 239000000284 extract Substances 0.000 description 1
- 229930195733 hydrocarbon Natural products 0.000 description 1
- 150000002430 hydrocarbons Chemical class 0.000 description 1
- 238000004806 packaging method and process Methods 0.000 description 1
- 238000007639 printing Methods 0.000 description 1
- 230000001172 regenerating effect Effects 0.000 description 1
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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
- 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
- B01D53/06—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 with moving adsorbents, e.g. rotating beds
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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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- B01D53/26—Drying gases or vapours
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- B01D—SEPARATION
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- B01D53/34—Chemical or biological purification of waste gases
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- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
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- B01D2253/00—Adsorbents used in seperation treatment of gases and vapours
- B01D2253/10—Inorganic adsorbents
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- B01D2259/40083—Regeneration of adsorbents in processes other than pressure or temperature swing adsorption
- B01D2259/40088—Regeneration of adsorbents in processes other than pressure or temperature swing adsorption by heating
- B01D2259/4009—Regeneration of adsorbents in processes other than pressure or temperature swing adsorption by heating using hot gas
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Abstract
一种低浓度大流量有机废气闭环多级回收装置及回收方法，包括：VOC气体转轮浓缩机构、低温等离子净化器、除湿机构、回收机构、溶剂后处理器、再生风机、后置风机和加热器构成；回收机构右侧设置除湿机构，溶剂后处理器设置在回收机构上部，VOC气体转轮浓缩机构设置在回收机构下侧，低温等离子净化器设置在VOC气体转轮浓缩机构右侧；回收方法包括一级吸附器吸附，一级吸附器饱和后加热脱附以及二级吸附器饱和加热脱附。本发明通过沸石转轮浓缩将有机气体浓度浓缩数倍同时保证尾气达标排放的高效气体浓缩设备，通过浓缩转轮和采用二级吸附有机废气相结合的方法解决低浓度、大风量的废气处理问题，提高了低浓度、大排量的有机废气回收效率。
A low-concentration and large-flow organic waste gas closed-loop multi-stage recovery device and recovery method, including: VOC gas runner concentration mechanism, low-temperature plasma purifier, dehumidification mechanism, recovery mechanism, solvent post-processor, regeneration fan, rear fan and heating The dehumidification mechanism is set on the right side of the recovery mechanism, the solvent post-processor is set on the upper part of the recovery mechanism, the VOC gas runner concentration mechanism is set on the lower side of the recovery mechanism, and the low-temperature plasma purifier is set on the right side of the VOC gas wheel concentration mechanism; The method includes adsorption in the first-stage adsorber, desorption by heating after saturation of the first-stage adsorber and desorption by heating after saturation of the second-stage adsorber. The present invention concentrates the organic gas concentration several times through the concentration of the zeolite runner, and at the same time ensures that the tail gas is discharged up to the standard, and solves the problem of low-concentration and large-volume waste gas treatment through the method of combining the concentration runner and the use of secondary adsorption of organic waste gas , improving the recovery efficiency of low-concentration, large-volume organic waste gas.
Description
技术领域technical field
本发明涉及有机废气回收领域，尤其是一种低浓度大流量有机废气闭环多级回收装置及回收方法。The invention relates to the field of organic waste gas recovery, in particular to a low-concentration and large-flow organic waste gas closed-loop multi-stage recovery device and recovery method.
背景技术Background technique
目前，塑料包装印刷行业废气处理系统所针对的凹版印刷机，一台十色凹版印刷机的主排风量约30000m³/h，VOCs浓度约为1.5g/m³；地排风量约20000m³/h；VOCs浓度约为0.7g/m³；属于典型的低浓度、大风量废气排放；所需废气处理系统庞大且运行效率低下；由于大气污染物排放标准中规定非甲烷总烃的排放浓度不超过120mg/m³；北京、上海等部分地方标准中规定的排放浓度更低；但对于目前的废气回收设备来说，如果使排放尾气达到上述标准值，设备的运行效率将大幅降低，设备运行成本随之增加，因此需要一种装置来解决低浓度、大风量VOCs的废气回收效率低下的问题。At present, the gravure printing machine targeted by the waste gas treatment system in the plastic packaging and printing industry, the main exhaust air volume of a ten-color gravure printing machine is about 30,000m³/h, the VOCs concentration is about 1.5g/m³; the ground exhaust air volume is about 20,000m³/h ;The concentration of VOCs is about 0.7g/m³; it is a typical low-concentration, large-volume exhaust gas discharge; the required exhaust gas treatment system is huge and the operation efficiency is low; since the emission concentration of non-methane total hydrocarbons is stipulated in the air pollutant emission standard does not exceed 120mg /m³; the emission concentration stipulated in some local standards such as Beijing and Shanghai is lower; but for the current exhaust gas recovery equipment, if the exhaust gas emission reaches the above-mentioned standard value, the operating efficiency of the equipment will be greatly reduced, and the operating cost of the equipment will be reduced accordingly. Therefore, a device is needed to solve the problem of low efficiency of waste gas recovery of low-concentration and large-volume VOCs.
发明内容Contents of the invention
本发明提出了一种低浓度大流量有机废气闭环多级回收装置及回收方法，用于解决现有低浓度、大风量VOCs废气回收效率低下的问题。The invention proposes a low-concentration and large-flow organic waste gas closed-loop multi-stage recovery device and recovery method, which are used to solve the problem of low recovery efficiency of the existing low-concentration and high-volume VOCs waste gas.
本发明的目的采用如下技术方案来实现：The purpose of the present invention adopts following technical scheme to realize:
一种低浓度大流量有机废气闭环多级回收装置，包括VOC气体转轮浓缩机构、低温等离子净化器、除湿机构、回收机构、溶剂后处理器、再生风机、后置风机和加热器；回收机构右侧设置除湿机构，溶剂后处理器设置在回收系统上部， VOC气体转轮浓缩机构设置在回收机构下侧，低温等离子净化器设置在VOC气体转轮浓缩机构右侧，加热器设置在气体转轮浓缩机构左侧，VOC气体转轮浓缩机构左侧下部设置有机废气进气管，VOC气体转轮浓缩机构右侧下部设置有低温等离子净化器，低温等离子净化器的右侧排口设置排气管，VOC气体转轮浓缩机构上部右侧设置有再生排口与再生风机的进口设置管道，再生风机的出风口与除湿机构的进口之间设置管道，除湿机构的排口与回收机构之间设置管道，VOC气体转轮浓缩机构上部左侧设置有再生进口，回收系统吸附装置排口与后置风机的进口之间设置管道，后置风机的出风口与加热器的进口之间设置管道，加热器的出口与VOC气体转轮浓缩机构的再生进口之间设置管道；所述的VOC气体转轮浓缩机构为沸石转轮浓缩设备，内部分为处理区、冷却区和再生区，是一种将有机气体浓度浓缩数倍后进行吸附的高效气体浓缩设备。A low-concentration and large-flow organic waste gas closed-loop multi-stage recovery device, including a VOC gas runner concentration mechanism, a low-temperature plasma purifier, a dehumidification mechanism, a recovery mechanism, a solvent post-processor, a regeneration fan, a rear fan and a heater; the recovery mechanism The dehumidification mechanism is set on the right side, the solvent post-processor is set on the upper part of the recovery system, the VOC gas wheel concentration mechanism is set on the lower side of the recovery mechanism, the low-temperature plasma purifier is set on the right side of the VOC gas wheel concentration mechanism, and the heater is set on the gas wheel. On the left side of the wheel concentration mechanism, an organic waste gas intake pipe is installed on the lower left side of the VOC gas wheel concentration mechanism, and a low-temperature plasma purifier is installed on the lower right side of the VOC gas wheel concentration mechanism, and an exhaust pipe is installed on the right outlet of the low-temperature plasma purifier , the right side of the upper part of the VOC gas runner concentration mechanism is provided with a regeneration outlet and a pipeline for the inlet of the regeneration fan. There is a regeneration inlet on the left side of the upper part of the VOC gas runner concentration mechanism, a pipe is arranged between the outlet of the adsorption device of the recovery system and the inlet of the rear fan, and a pipe is arranged between the outlet of the rear fan and the inlet of the heater. A pipeline is arranged between the outlet of the VOC gas runner concentration mechanism and the regeneration inlet of the VOC gas runner concentration mechanism; the VOC gas runner concentration mechanism is a zeolite runner concentration device, and the interior is divided into a treatment area, a cooling zone and a regeneration zone. High-efficiency gas concentration equipment that absorbs after the gas concentration is concentrated several times.
所述的回收机构由一级吸附器、二级吸附器，冷凝器、脱附风机和换热器构成，所述一级吸附器的一侧设置有二级吸附器，二级吸附器的一侧分别设置冷凝器、换热器、脱附风机，一级吸附器的上口分别与冷凝器的进口之间设置管道，冷凝器的出口与脱附风机的进口之间设置管道，冷凝器的出口与二级吸附器的上口之间均设置管道，二级吸附器的上口与冷凝器的进口之间设置管道，二级吸附器的下口与脱附风机的出口之间设置管道，脱附风机的出口与换热器的进口之间设置管道，脱附风机的出口分别与每台一级吸附器的下口之间设置管道，换热器的出口分别与一级吸附器的下口、二级吸附器的下口之间设置管道。The recovery mechanism is composed of a primary adsorber, a secondary adsorber, a condenser, a desorption fan, and a heat exchanger. One side of the primary adsorber is provided with a secondary adsorber, and one side of the secondary adsorber is A condenser, a heat exchanger, and a desorption fan are respectively arranged on the side, pipes are arranged between the upper port of the first-stage adsorber and the inlet of the condenser, pipes are arranged between the outlet of the condenser and the inlet of the desorption fan, and the outlet of the condenser Pipelines are arranged between the outlet and the upper port of the secondary adsorber, pipes are provided between the upper port of the secondary adsorber and the inlet of the condenser, and pipes are provided between the lower port of the secondary adsorber and the outlet of the desorption fan. A pipeline is arranged between the outlet of the desorption fan and the inlet of the heat exchanger, and a pipeline is arranged between the outlet of the desorption fan and the lower port of each primary adsorber, and the outlet of the heat exchanger is respectively connected to the lower port of the primary adsorber. A pipeline is arranged between the outlet and the lower outlet of the secondary adsorber.
所述的一级吸附器为至少两台以活性炭作为吸附材料的吸附器并联而成。The primary adsorber is formed by parallel connection of at least two adsorbers using activated carbon as the adsorption material.
所述的再生风机、后置风机和脱附风机均为封闭式循环风机。The regeneration fan, rear fan and desorption fan are all closed circulation fans.
一种低浓度大流量有机废气闭环多级回收方法：A low-concentration and large-flow organic waste gas closed-loop multi-stage recovery method:
首先从进气口将含有VOC的有机废气经管道进入VOC气体转轮浓缩机构内被吸附， VOC气体转轮浓缩机构的内部含有VOC的有机废气处理吸附后被排出，排出的被净化气体进入低温等离子净化器内净化处理保证尾气达标后经排气管排放；加热器产生的热风通过管道对VOC气体转轮浓缩机构的再生区输入热风，吸附于浓缩转轮中的VOC，在再生区经热风处理而被脱附、浓缩，再生空气从再生排口排出，经再生风机送入除湿机构内除湿，除湿后经管道送入一级吸附器内被吸附，一级吸附器排出的洁净气体由管道输送至后置风机，后置风机将洁净气体输送至加热器，按以上步骤循环往复；First, the organic waste gas containing VOC enters the VOC gas runner concentration mechanism from the air inlet through the pipeline to be adsorbed. The organic waste gas containing VOC inside the VOC gas runner concentration mechanism is treated and adsorbed and then discharged, and the discharged purified gas enters the low temperature The internal purification treatment of the plasma purifier ensures that the tail gas is discharged through the exhaust pipe after reaching the standard; the hot air generated by the heater is input to the regeneration area of the VOC gas runner concentration mechanism through the pipeline, and the VOC adsorbed in the concentration runner is passed through the hot air in the regeneration area. After treatment, it is desorbed and concentrated, and the regeneration air is discharged from the regeneration outlet, sent to the dehumidification mechanism by the regeneration fan for dehumidification. It is sent to the rear fan, and the rear fan sends the clean gas to the heater, and the cycle is repeated according to the above steps;
一级吸附器饱和后，换热器产生的热风经管道进入一级吸附器内，使一级吸附器内温度逐渐升高，一级吸附器活性炭内吸附的VOC溶剂受热后生成VOC气体，一级吸附器内生成的高温VOC气体进入冷凝器内被冷却，有利于二级吸附器吸附回收，冷凝器冷却后的VOC气体经管道由二级吸附器的上口进入二级吸附器内被吸附，脱附风机将二级吸附器内的低浓度VOC气体从二级吸附器的下口抽出后，将低浓度VOC气体输送入换热器内加热，加热后再次进入一级吸附器内，按以上操作步骤循环往复，至一级吸附器脱附完成后停止；一级吸附器脱附结束后，换热器停止加热，冷凝器继续通入冷却水，脱附风机将冷凝器内的冷空气抽出后，通过管道不经过换热器直接输送入一级吸附器内，一级吸附器内的余热使冷空气的温度逐步升高，一级吸附器内的温度逐步降低，热空气经管道进入冷凝器内，按以上操作步骤循环往复，至一级吸附器内的温度达到标准温度后，一级吸附器重新开始吸附作业；After the primary adsorber is saturated, the hot air generated by the heat exchanger enters the primary adsorber through the pipeline, so that the temperature in the primary adsorber gradually rises, and the VOC solvent adsorbed in the activated carbon of the primary adsorber is heated to generate VOC gas. The high-temperature VOC gas generated in the first-stage adsorber enters the condenser and is cooled, which is beneficial to the adsorption and recovery of the second-stage adsorber. The VOC gas after the cooling of the condenser enters the upper port of the second-stage adsorber through the pipeline and enters the second-stage adsorber to be adsorbed. , the desorption fan pumps out the low-concentration VOC gas in the secondary adsorber from the lower port of the secondary adsorber, then transports the low-concentration VOC gas into the heat exchanger for heating, and then enters the primary adsorber again after heating, press The above operation steps are repeated until the desorption of the first-stage adsorber is completed; after the desorption of the first-stage adsorber is completed, the heat exchanger stops heating, the condenser continues to feed cooling water, and the desorption fan blows the cold air in the condenser After pumping out, it is directly transported into the first-stage adsorber through the pipeline without passing through the heat exchanger. The waste heat in the first-stage adsorber makes the temperature of the cold air gradually increase, and the temperature in the first-stage adsorber gradually decreases, and the hot air enters through the pipe. In the condenser, follow the above operation steps in a cycle, until the temperature in the first-stage adsorber reaches the standard temperature, the first-stage adsorber restarts the adsorption operation;
二级吸附器饱和后，换热器产生的热风经管道输送入二级吸附器内，使二级吸附器内温度逐渐升高，二级吸附器内吸附的VOC溶剂受热后生成高浓度VOC气体，二级吸附器内生成的高浓度VOC气体进入冷凝器内被冷凝，冷凝器能够冷凝大部分VOC气体成为VOC溶剂，冷凝后产生的VOC溶剂经管道流入溶剂后处理器内处理成轻沸成品和高沸成品，冷凝器内剩余未被冷凝的VOC气体经脱附风机送入换热器内加热，加热后进入二级吸附器，按以上操作步骤循环往复，至二级吸附器脱附完成后停止。After the secondary adsorber is saturated, the hot air generated by the heat exchanger is transported into the secondary adsorber through the pipeline, so that the temperature in the secondary adsorber gradually rises, and the VOC solvent adsorbed in the secondary adsorber is heated to generate high-concentration VOC gas , the high-concentration VOC gas generated in the secondary adsorber enters the condenser and is condensed. The condenser can condense most of the VOC gas into a VOC solvent. And high-boiling finished products, the remaining uncondensed VOC gas in the condenser is sent to the heat exchanger for heating through the desorption fan, and then enters the secondary adsorber after heating, and repeats the above operation steps until the desorption of the secondary adsorber is completed stop after.
本发明提出的技术方案，达到了有益效果是：本发明通过沸石转轮浓缩将有机气体浓度浓缩数倍同时保证尾气达标排放的高效气体浓缩设备，通过浓缩转轮和采用二级吸附有机废气相结合的方法解决低浓度、大风量的废气处理问题，提高了低浓度、大排量的有机废气回收效率，降低企业投资负担。The technical solution proposed by the present invention achieves beneficial effects as follows: the present invention uses a zeolite runner to concentrate the organic gas concentration several times while ensuring that the tail gas is discharged up to the standard. The combined method solves the problem of low-concentration and large-volume waste gas treatment, improves the recovery efficiency of low-concentration and large-volume organic waste gas, and reduces the investment burden of enterprises.
附图说明Description of drawings
图1为本发明总装结构示意图。Fig. 1 is a schematic diagram of the assembly structure of the present invention.
图中：1、进气管， 2、VOC气体转轮浓缩机构，3、低温等离子净化器，4、除湿机构，5、回收机构，5-1、一级吸附器，5-2、二级吸附器，5-3、冷凝器，5-4、脱附风机，5-5、换热器，6、溶剂后处理器，7、再生风机，8、后置风机，9、加热器，10、排气管,11、阀门。In the figure: 1. Intake pipe, 2. VOC gas runner concentration mechanism, 3. Low temperature plasma purifier, 4. Dehumidification mechanism, 5. Recovery mechanism, 5-1, primary adsorber, 5-2, secondary adsorption Device, 5-3, condenser, 5-4, desorption fan, 5-5, heat exchanger, 6, solvent post-processor, 7, regeneration fan, 8, rear fan, 9, heater, 10, Exhaust pipe, 11, valve.
具体实施方式Detailed ways
结合附图和具体实施方式对本发明做进一步说明：The present invention will be further described in conjunction with accompanying drawing and specific embodiment:
如附图1所示一种低浓度大流量有机废气闭环多级回收系统，是由：VOC气体转轮浓缩机构2、低温等离子净化器3、除湿机构4、回收机构5、溶剂后处理器6、再生风机7、后置风机8和加热器9构成；回收机构5右侧设置除湿机构4，溶剂后处理器6设置在回收机构5上部，VOC气体转轮浓缩机构2设置在回收机构5下侧，低温等离子净化器3设置在VOC气体转轮浓缩机构2右侧，加热器9和有机废气的进气管1设置在气体转轮浓缩机构2左侧，有机废气进气管1与VOC气体转轮浓缩机构2左侧下部的吸附进口连接，VOC气体转轮浓缩机构2右侧下部的吸附排气口与低温等离子净化器3的进口之间设置管道，低温等离子净化器3的右侧排口设置排气管10，VOC气体转轮浓缩机构2上部右侧设置有再生排口与再生风机的进口设置管道，再生风机7的出风口与除湿机构4的进口之间设置管道，除湿机构4的排口与回收机构5之间设置管道，VOC气体转轮浓缩机构2左侧上部，回收系统5与后置风机8的进口之间设置管道，后置风机8的出风口与加热器9的进口之间设置管道，加热器9的出口与VOC气体转轮浓缩机构2的再生进口之间设置管道；所述的VOC气体转轮浓缩机构2为沸石转轮浓缩设备，内部分为处理区、冷却区和再生区，是一种将有机气体浓度浓缩数倍后进行吸附的高效气体浓缩设备；所述的回收机构5的由一级吸附器5-1、二级吸附器5-2，冷凝器5-3、脱附风机5-4和换热器5-5构成，所述一级吸附器5-1的一侧设置有二级吸附器5-2，二级吸附器5-2的一侧分别设置冷凝器5-3、换热器5-5、脱附风机5-4，一级吸附器5-1的上口分别与冷凝器5-3的进口之间设置管道，冷凝器5-3的出口与脱附风机5-4的进口之间设置管道，冷凝器5-3的出口与二级吸附器3-2的上口之间均设置管道，二级吸附器5-2的上口与冷凝器5-3的进口之间设置管道，二级吸附器5-3的下口与脱附风机5-4的出口之间设置管道，脱附风机5-4的出口与换热器5-5的进口之间设置管道，脱附风机5-4的出口分别与每台一级吸附器5-1的下口之间设置管道，换热器5-5的出口分别与一级吸附器5-1的下口、二级吸附器5-2的下口之间设置管道，所述的连接管道上均设置有阀门11； 所述的一级吸附器5-1为至少两台以活性炭作为吸附材料的吸附器并联而成；所述的再生风机7、后置风机8和脱附风机5-4均为封闭式循环风机。As shown in Figure 1, a low-concentration and large-flow organic waste gas closed-loop multi-stage recovery system is composed of: VOC gas runner concentration mechanism 2, low-temperature plasma purifier 3, dehumidification mechanism 4, recovery mechanism 5, and solvent post-processor 6 , a regenerative fan 7, a rear fan 8 and a heater 9; a dehumidification mechanism 4 is set on the right side of the recovery mechanism 5, a solvent post-processor 6 is set on the upper part of the recovery mechanism 5, and a VOC gas runner concentration mechanism 2 is set under the recovery mechanism 5 side, the low-temperature plasma purifier 3 is arranged on the right side of the VOC gas runner enrichment mechanism 2, the heater 9 and the inlet pipe 1 of the organic waste gas are arranged on the left side of the gas runner enrichment mechanism 2, and the organic waste gas inlet pipe 1 and the VOC gas runner The adsorption inlet on the lower left side of the concentration mechanism 2 is connected, and a pipeline is set between the adsorption exhaust port on the lower right side of the VOC gas runner concentration mechanism 2 and the inlet of the low-temperature plasma purifier 3, and the right outlet of the low-temperature plasma purifier 3 is set Exhaust pipe 10, the right side of the upper part of the VOC gas runner concentration mechanism 2 is provided with a regeneration exhaust port and the inlet of the regeneration fan. A pipeline is set between the mouth and the recovery mechanism 5, the upper left side of the VOC gas runner concentration mechanism 2, a pipeline is set between the recovery system 5 and the inlet of the rear fan 8, and the air outlet of the rear fan 8 is connected to the inlet of the heater 9. A pipeline is arranged between the outlet of the heater 9 and the regeneration inlet of the VOC gas runner enrichment mechanism 2; the VOC gas runner enrichment mechanism 2 is a zeolite runner enrichment device, and the interior is divided into a treatment area and a cooling area and regeneration area, is a kind of high-efficiency gas concentration equipment that absorbs after the organic gas concentration is concentrated several times; the recovery mechanism 5 is composed of a primary adsorber 5-1, a secondary adsorber 5-2, and a condenser 5 -3. The desorption blower 5-4 and the heat exchanger 5-5 are composed, one side of the primary adsorber 5-1 is provided with a secondary adsorber 5-2, and one side of the secondary adsorber 5-2 is Condenser 5-3, heat exchanger 5-5, desorption blower 5-4 are arranged respectively, pipes are arranged between the inlet of primary adsorber 5-1 and the inlet of condenser 5-3, condenser 5- Pipelines are arranged between the outlet of 3 and the inlet of desorption fan 5-4, pipelines are arranged between the outlet of condenser 5-3 and the upper port of secondary adsorber 3-2, and the upper port of secondary adsorber 5-2 A pipeline is set between the mouth and the inlet of the condenser 5-3, a pipeline is set between the lower mouth of the secondary adsorber 5-3 and the outlet of the desorption fan 5-4, and the outlet of the desorption fan 5-4 is connected to the heat exchanger Pipelines are arranged between the inlets of 5-5, pipes are arranged between the outlets of desorption fan 5-4 and the lower ports of each primary adsorber 5-1, and the outlets of heat exchangers 5-5 are respectively connected to the first-stage adsorption Pipelines are arranged between the lower port of the device 5-1 and the lower port of the secondary adsorber 5-2, and valves 11 are arranged on the connecting pipes; the primary adsorber 5-1 is at least two or more Activated carbon is used as the adsorber of the adsorption material in parallel connection; the regeneration fan 7, the rear fan 8 and the desorption fan 5-4 are all closed circulation fans.
在进行VOC的有机废气处理时，首先从进气口1将含有VOC的有机废气经管道进入VOC气体转轮浓缩机构2内被吸附， VOC气体转轮浓缩机构2的内部含有VOC的有机废气处理吸附后被排出，排出的被净化气体进入低温等离子净化器3内净化处理保证尾气达标后经排气管10排放；加热器9产生的热风通过管道对VOC气体转轮浓缩机构2的再生区输入热风，吸附于浓缩转轮中的VOC，在再生区经热风处理而被脱附、浓缩，再生空气从再生排口排出，经再生风机7送入除湿机构4内除湿，除湿后经管道送入一级吸附器5-1内被吸附，一级吸附器5-1排出的洁净气体由管道输送至后置风机8，后置风机8将洁净气体输送至加热器9，按以上步骤循环往复；When processing the organic waste gas of VOC, the organic waste gas containing VOC is first introduced into the VOC gas runner enrichment mechanism 2 from the air inlet 1 to be adsorbed, and the organic waste gas containing VOC is treated inside the VOC gas runner concentration mechanism 2. After being adsorbed, it is discharged, and the discharged purified gas enters the low-temperature plasma purifier 3 for purification and treatment to ensure that the exhaust gas reaches the standard and then is discharged through the exhaust pipe 10; the hot air generated by the heater 9 is input to the regeneration area of the VOC gas runner concentration mechanism 2 through the pipeline Hot air, the VOC adsorbed in the concentration runner, is desorbed and concentrated by hot air treatment in the regeneration area, and the regeneration air is discharged from the regeneration outlet, sent to the dehumidification mechanism 4 by the regeneration fan 7 for dehumidification, and then sent into the dehumidification through the pipeline The primary adsorber 5-1 is adsorbed, and the clean gas discharged from the primary adsorber 5-1 is transported to the rear fan 8 through the pipeline, and the rear fan 8 transports the clean gas to the heater 9, and the above steps are repeated;
一级吸附器5-1饱和后，换热器5-5产生的热风经管道进入一级吸附器5-1内，使一级吸附器5-1内温度逐渐升高，一级吸附器5-1活性炭内吸附的VOC溶剂受热后生成VOC气体，一级吸附器5-1内生成的高温VOC气体进入冷凝器5-3内被冷却，有利于二级吸附器5-2吸附回收，冷凝器5-3冷却后的VOC气体经管道由二级吸附器5-2的上口进入二级吸附器5-2内被吸附，脱附风机5-4将二级吸附器5-2内的低浓度VOC气体从二级吸附器5-2的下口抽出后，将低浓度VOC气体输送入换热器5-5内加热，加热后再次进入一级吸附器5-1内，按以上操作步骤循环往复，至一级吸附器5-1脱附完成后停止；一级吸附器5-1脱附结束后，换热器5-5停止加热，冷凝器5-3继续通入冷却水，脱附风机5-4将冷凝器5-3内的冷空气抽出后，通过管道不经过换热器5-5直接输送入一级吸附器5-1内，一级吸附器5-1内的余热使冷空气的温度逐步升高，一级吸附器5-1内的温度逐步降低，热空气经管道进入冷凝器5-3内，按以上操作步骤循环往复，至一级吸附器5-1内的温度达到标准温度后，一级吸附器5-1重新开始吸附作业；After the primary adsorber 5-1 is saturated, the hot air generated by the heat exchanger 5-5 enters the primary adsorber 5-1 through the pipeline, so that the temperature in the primary adsorber 5-1 gradually rises, and the primary adsorber 5 -1 The VOC solvent adsorbed in the activated carbon is heated to generate VOC gas, and the high-temperature VOC gas generated in the primary adsorber 5-1 enters the condenser 5-3 to be cooled, which is beneficial to the secondary adsorber 5-2 for adsorption recovery and condensation The VOC gas cooled by the device 5-3 enters the secondary adsorber 5-2 from the upper port of the secondary adsorber 5-2 to be adsorbed through the pipeline, and the desorption fan 5-4 removes the VOC gas in the secondary adsorber 5-2. After the low-concentration VOC gas is extracted from the lower port of the secondary adsorber 5-2, the low-concentration VOC gas is transported into the heat exchanger 5-5 for heating, and then enters the primary adsorber 5-1 again after heating, and operates as above The steps are repeated until the primary adsorber 5-1 desorbs and stops; after the primary adsorber 5-1 desorbs, the heat exchanger 5-5 stops heating, and the condenser 5-3 continues to feed cooling water. After the desorption fan 5-4 extracts the cold air in the condenser 5-3, it is directly transported into the first-stage adsorber 5-1 through the pipeline without passing through the heat exchanger 5-5, and the air in the first-stage adsorber 5-1 The waste heat makes the temperature of the cold air rise gradually, and the temperature in the first-stage adsorber 5-1 gradually decreases, and the hot air enters the condenser 5-3 through the pipeline, and repeats the above operation steps until it reaches the first-stage adsorber 5-1. After the temperature inside reaches the standard temperature, the primary adsorber 5-1 restarts the adsorption operation;
二级吸附器5-2饱和后，换热器5-5产生的热风经管道输送入二级吸附器5-2内，使二级吸附器5-2内温度逐渐升高，二级吸附器5-2内吸附的VOC溶剂受热后生成高浓度VOC气体，二级吸附器5-2内生成的高浓度VOC气体进入冷凝器5-3内被冷凝，冷凝器5-3能够冷凝大部分VOC气体成为VOC溶剂，冷凝后产生的VOC溶剂经管道流入溶剂后处理器6内处理成轻沸成品和高沸成品，冷凝器5-3内剩余未被冷凝的VOC气体经脱附风机5-4送入换热器5-5内加热，加热后进入二级吸附器5-2，按以上操作步骤循环往复，至二级吸附器5-2脱附完成后停止。After the secondary adsorber 5-2 is saturated, the hot air generated by the heat exchanger 5-5 is transported into the secondary adsorber 5-2 through pipelines, so that the temperature in the secondary adsorber 5-2 gradually rises, and the secondary adsorber 5-2 The VOC solvent adsorbed in 5-2 generates high-concentration VOC gas after being heated, and the high-concentration VOC gas generated in the secondary adsorber 5-2 enters the condenser 5-3 to be condensed, and the condenser 5-3 can condense most of the VOC The gas becomes a VOC solvent, and the VOC solvent produced after condensation flows into the solvent post-processor 6 through the pipeline and is processed into a light boiling product and a high boiling product, and the remaining uncondensed VOC gas in the condenser 5-3 passes through the desorption fan 5-4 Send it into the heat exchanger 5-5 for heating, and then enter the secondary adsorber 5-2 after heating, repeat the above operation steps, and stop after the desorption of the secondary adsorber 5-2 is completed.
本发明未详述部分为现有技术。The unspecified parts of the present invention are prior art.
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| CN112546808B (en) * | 2020-12-25 | 2025-07-25 | 青岛华世洁新材料科技集团股份有限公司 | Dichloromethane waste gas treatment system and method |
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Application publication date: 20180529 |