CN114887443A - Oil gas condensation recovery combined RTO petrochemical tank area waste gas treatment system and process - Google Patents
Oil gas condensation recovery combined RTO petrochemical tank area waste gas treatment system and process Download PDFInfo
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- 239000007789 gas Substances 0.000 title claims abstract description 165
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- 238000001179 sorption measurement Methods 0.000 claims abstract description 39
- 238000006477 desulfuration reaction Methods 0.000 claims abstract description 36
- 230000023556 desulfurization Effects 0.000 claims abstract description 36
- 230000003647 oxidation Effects 0.000 claims abstract description 24
- 238000007254 oxidation reaction Methods 0.000 claims abstract description 24
- 238000003795 desorption Methods 0.000 claims abstract description 10
- 238000006864 oxidative decomposition reaction Methods 0.000 claims abstract description 9
- 238000005406 washing Methods 0.000 claims description 15
- 239000007791 liquid phase Substances 0.000 claims description 7
- 238000002485 combustion reaction Methods 0.000 claims description 6
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Abstract
本发明公开了一种油气冷凝回收结合RTO的石化罐区废气处理系统和工艺，该系统包括依次管道连通的油气脱硫单元、双通道油气冷凝回收单元、活性炭吸附单元和RTO高温热氧化处理单元，具体包括脱硫洗涤塔、冷冻组机、冷箱机组、活性炭罐、真空泵、RTO焚烧炉、阻火器和风机等，石化罐区废气依次通过油气脱硫处理、油气双通道冷凝回收、废气活性炭吸附和真空脱附以及RTO高温热氧化分解，废气的VOCs排放浓度小于60mg/m3时达标排放。本发明采用“冷凝法油气回收+RTO”组合工艺处理石化罐区废气的效率在99％以上，降低系统的运行成本，环保稳定达标的同时最大限度提高系统的使用寿命。
The invention discloses a petrochemical tank farm waste gas treatment system and process combining oil and gas condensation and recovery with RTO. The system comprises an oil and gas desulfurization unit, a dual-channel oil and gas condensation recovery unit, an activated carbon adsorption unit, and an RTO high-temperature thermal oxidation treatment unit connected in sequence. Specifically, it includes desulfurization scrubber, refrigeration unit, cold box unit, activated carbon tank, vacuum pump, RTO incinerator, flame arrester and fan, etc. The petrochemical tank area waste gas is sequentially processed by oil and gas desulfurization, oil and gas dual-channel condensation recovery, waste gas activated carbon adsorption and vacuum Desorption and high temperature thermal oxidative decomposition of RTO, when the VOCs emission concentration of the exhaust gas is less than 60mg/ m3 , the emission standard is reached. The invention adopts the "condensation method oil and gas recovery + RTO" combined process to treat the waste gas of petrochemical tank farm with an efficiency of over 99%, reduces the operating cost of the system, and maximizes the service life of the system while meeting the environmental protection and stability standards.
Description
技术领域technical field
本发明属于石油化工领域，具体涉及一种油气冷凝回收结合RTO的石化罐区废气处理系统和工艺。The invention belongs to the field of petrochemical industry, and particularly relates to a petrochemical tank farm waste gas treatment system and process combining oil and gas condensation and recovery with RTO.
背景技术Background technique
在实际工程应用中，石化油品储罐区排气VOCs浓度高且排放不连续，对于石化油品储罐区排气的废气治理，主要有活性炭吸附法、吸收法、冷凝法、膜分离法和TO(直燃式)炉等废气治理技术，已成功应用到石化油品储罐区排气VOCs治理中。但随着国家对大气排放要求的提高，国家标准对油气回收排放由25g/m3逐步提高到60mg/m3，“活性炭吸附”、“吸收法”、“冷凝法”和膜分离法对有机物的去除效率较低，达不到国家规范要求的排放标准，TO炉虽然能达标，但投资成本和运行成本高，并不适合罐区排气的废气处理，具体如下：In practical engineering applications, the concentration of VOCs in the exhaust gas of the petrochemical oil storage tank area is high and the emission is discontinuous. For the exhaust gas treatment of the exhaust gas of the petrochemical oil storage tank area, there are mainly activated carbon adsorption method, absorption method, condensation method and membrane separation method. and TO (direct-fired) furnace and other waste gas treatment technologies have been successfully applied to the treatment of exhaust VOCs in petrochemical oil storage tank areas. However, with the improvement of the country's air emission requirements, the national standard for oil and gas recovery emissions has gradually increased from 25g/m 3 to 60mg/m 3 . "Activated carbon adsorption", "absorption method", "condensation method" and membrane separation The removal efficiency is low and cannot meet the emission standards required by national regulations. Although TO furnaces can meet the standards, their investment costs and operating costs are high, and they are not suitable for waste gas treatment of tank farm exhaust. The details are as follows:
(1)单独采用油气回收系统：处理罐区尾气的排放浓度为25g/m3，不能满足国家标准要求VOCs排放浓度小于60mg/m3的环保要求；(1) The oil and gas recovery system is used alone: the emission concentration of the tail gas from the tank farm is 25g/m 3 , which cannot meet the environmental protection requirements of the national standard that the VOCs emission concentration is less than 60mg/m 3 ;
(2)TO炉焚烧：只针对连续稳定的高浓度排放废气，石化罐区排放废气是间隙排气，浓度波动比较大，TO炉运行不稳定且当废气中VOCs浓度低时，需要消耗大量的燃料；(2) TO furnace incineration: only for continuous and stable high-concentration exhaust gas. The exhaust gas discharged from the petrochemical tank area is gap exhaust gas, and the concentration fluctuation is relatively large. The TO furnace is unstable in operation and when the concentration of VOCs in the exhaust gas is low, it needs to consume a large amount of fuel;
(3)RTO炉焚烧：只针对连续稳定的低浓度排放废气，石化罐区排放废气是间隙排气，浓度波动比较大，RTO炉运行不稳定且当废气中VOCs浓度高时，RTO炉容易超温且有爆炸风险，浓度波动导致系统运行不稳定；(3) RTO furnace incineration: only for continuous and stable low-concentration exhaust gas. The exhaust gas discharged from the petrochemical tank area is gap exhaust gas, and the concentration fluctuation is relatively large. The operation of the RTO furnace is unstable and when the concentration of VOCs in the exhaust gas is high, the RTO furnace is prone to overheating. Warm and there is a risk of explosion, and fluctuations in concentration lead to unstable system operation;
(4)RCO/CO炉系统：只针对连续稳定的低浓度排放废气，催化剂对废气成分、废气浓度有比较高的要求，但石化罐区排放废气是间隙排气，浓度波动比较大，RCO/CO炉容易超温而导致催化剂失效，处理后废气排放不达标，浓度波动导致系统运行不稳定；(4) RCO/CO furnace system: only for continuous and stable low-concentration exhaust gas, the catalyst has relatively high requirements on exhaust gas composition and exhaust gas concentration, but the exhaust gas discharged from the petrochemical tank area is gap exhaust, and the concentration fluctuation is relatively large. The CO furnace is easily overheated, which leads to the failure of the catalyst, the exhaust gas emission after treatment does not meet the standard, and the concentration fluctuation leads to the unstable operation of the system;
(5)活性炭吸附脱附系统：因罐区排放的废气含有C2、C3等低沸点物质，活性炭吸附效果差，废气不能稳定达标排放；(5) Activated carbon adsorption and desorption system: Because the waste gas discharged from the tank area contains C2, C3 and other low-boiling substances, the activated carbon adsorption effect is poor, and the waste gas cannot be discharged stably up to the standard;
(6)光和氧等离子工艺：只适合低浓度、含臭气的废气，对除臭有一定的效果，而石化罐区排放废气是间隙排气，浓度波动比较大，处理过程中有安全风险，目前已被限制使用。(6) Light and oxygen plasma process: it is only suitable for low-concentration, odor-containing waste gas, and has a certain effect on deodorization, while the waste gas discharged from petrochemical tank farms is gap exhaust, and the concentration fluctuation is relatively large, and there are safety risks in the treatment process. , which is currently restricted.
发明内容SUMMARY OF THE INVENTION
针对现有技术中石化油品储罐区废气采用油气回收处理高浓度且间歇排放的VOCs污染物时普遍存在处理效率低、运行成本高和排放不达标的情况，以及采用TO炉直接焚烧处理的热回收效率低(50％左右)而导致运行能耗大、成本高的问题，本发明的主要目的是提供一种油气冷凝回收结合RTO的石化罐区废气处理系统，采用“冷凝法油气回收+RTO”组合结构用于石化罐区废气处理，VOCs排放浓度小于60mg/m3)排放。Aiming at the low treatment efficiency, high operating cost and substandard discharge when using oil and gas recovery to treat high-concentration and intermittently discharged VOCs pollutants in the waste gas of petrochemical oil storage tank farms in the prior art, and the use of TO furnace for direct incineration treatment of heat The recovery efficiency is low (about 50%), which leads to the problems of high energy consumption and high cost. The main purpose of the present invention is to provide a petrochemical tank waste gas treatment system that combines oil and gas condensation and recovery with RTO. "The combined structure is used for waste gas treatment in petrochemical tank farms, and the VOCs emission concentration is less than 60mg/m 3 ).
本发明的另一目的是提供一种油气冷凝回收结合RTO的石化罐区废气处理工艺，通过油气脱硫+双通道冷凝回收+RTO处理相结合，先对上述罐区排放的废气进行冷凝吸附油气回收，再对油气回收后的废气采用RTO焚烧炉进行氧化分解去除，处理效率可以达到99％以上。Another object of the present invention is to provide a petrochemical tank farm waste gas treatment process combining oil and gas condensation and recovery with RTO. Through the combination of oil and gas desulfurization + dual-channel condensation recovery + RTO treatment, the waste gas discharged from the above-mentioned tank farm is first condensed and adsorbed to recover oil and gas. , and then use the RTO incinerator for oxidative decomposition and removal of the waste gas after oil and gas recovery, and the treatment efficiency can reach more than 99%.
为实现上述目的，本发明采用的技术方案是：For achieving the above object, the technical scheme adopted in the present invention is:
本发明提供的一种油气冷凝回收结合RTO的石化罐区废气处理系统，包括依次管道连通的油气脱硫单元、双通道油气冷凝回收单元、活性炭吸附单元和RTO高温热氧化处理单元；其中：The invention provides a petrochemical tank farm waste gas treatment system with oil and gas condensation recovery combined with RTO, comprising an oil and gas desulfurization unit, a dual-channel oil and gas condensation recovery unit, an activated carbon adsorption unit and an RTO high-temperature thermal oxidation treatment unit connected in sequence by pipelines; wherein:
所述油气脱硫单元包括依次管道连通的第一阻火器、油气风机和脱硫洗涤塔，所述油气风机经过管道通入所述脱硫洗涤塔的底部，石化罐区废气通过所述油气风机进入所述脱硫洗涤塔内进行脱硫处理；The oil and gas desulfurization unit includes a first flame arrester, an oil and gas fan, and a desulfurization washing tower connected in sequence by pipelines. Desulfurization treatment is carried out in the desulfurization washing tower;
所述双通道油气冷凝回收单元包括第一冷箱机组、第二冷箱机组、冷冻机组和收油罐，所述第一冷箱机组和第二冷箱机组并联连接且采用“一备一用”交替工作模式，其入口均与所述脱硫洗涤塔顶部连接、出油口分别与收油罐连通；所述第一冷箱机组和第二冷箱机组通过冷冻机组相互连通形成油气冷凝循环回路，脱硫处理后的废气转换为液相的油可流入所述收油罐内，未冷凝的低浓度废气流入所述活性炭吸附单元内；The dual-channel oil and gas condensation recovery unit includes a first cold box unit, a second cold box unit, a refrigeration unit and an oil collecting tank. "Alternate working mode, its inlet is connected with the top of the desulfurization washing tower, and the oil outlet is connected with the oil collecting tank respectively; the first cold box unit and the second cold box unit are connected to each other through the refrigeration unit to form an oil and gas condensation cycle. , the desulfurized waste gas converted into liquid-phase oil can flow into the oil collecting tank, and the uncondensed low-concentration waste gas flows into the activated carbon adsorption unit;
所述活性炭吸附单元包括两并联的第一活性炭罐和第二活性炭罐以及真空泵，其底部入口分别与所述第一冷箱机组和第二冷箱机组的出口经管道连通，其顶部出口设有两通路，一条通过所述真空泵分别与所述第一冷箱机组和第二冷箱机组的入口连通，一条与所述RTO高温热氧化处理单元连通；The activated carbon adsorption unit includes two paralleled first activated carbon canisters and second activated carbon canisters and a vacuum pump, the bottom inlets of which are respectively connected with the outlets of the first cold box unit and the second cold box unit through pipes, and the top outlet is provided with Two passages, one is communicated with the inlets of the first cold box unit and the second cold box unit respectively through the vacuum pump, and the other is communicated with the RTO high temperature thermal oxidation treatment unit;
所述RTO高温热氧化处理单元包括依次连通的RTO入口风机、第二阻火器和RTO焚烧炉，所述RTO入口风机分别与所述第一活性炭罐和第二活性炭罐的出口连通，低浓度废气通过其流入所述RTO焚烧炉内,所述RTO焚烧炉包括RTO蓄热室和燃烧室,且所述RTO蓄热室内设有蓄热陶瓷进行热回收。The RTO high temperature thermal oxidation treatment unit comprises an RTO inlet fan, a second flame arrester and an RTO incinerator that are communicated in sequence, and the RTO inlet fan is respectively communicated with the outlets of the first activated carbon canister and the second activated carbon canister. It flows into the RTO incinerator through it, and the RTO incinerator includes an RTO regenerator and a combustion chamber, and the RTO regenerator is provided with a regenerative ceramic for heat recovery.
作为优选，所述RTO焚烧炉设有若干个并列的入气口，经管道分别与所述RTO入口风机连接。Preferably, the RTO incinerator is provided with several parallel air inlets, which are respectively connected with the RTO inlet fans through pipes.
作为优选，还包括排气筒，与所述RTO焚烧炉的出气口连通。Preferably, an exhaust pipe is also included, which is communicated with the gas outlet of the RTO incinerator.
作为优选，所述第一冷箱机组和第二冷箱机组内设有不低于三个冷箱串联连接。Preferably, there are no less than three cold boxes connected in series in the first cold box unit and the second cold box unit.
本发明还提供一种油气冷凝回收结合RTO的石化罐区废气处理工艺，通过上述油气冷凝回收结合RTO的石化罐区废气处理系统进行石化罐区废气处理，包括以下步骤：The present invention also provides a petrochemical tank farm waste gas treatment process combining oil and gas condensation and recovery with RTO. The petrochemical tank farm waste gas treatment is performed by the above-mentioned oil and gas condensation recovery combined with RTO petrochemical tank farm waste gas treatment system, including the following steps:
步骤1、油气脱硫处理：罐区废气通过所述油气风机进入所述脱硫洗涤塔内进行脱硫(如H2S)处理；Step 1, oil and gas desulfurization treatment: the waste gas from the tank farm enters the desulfurization washing tower through the oil and gas fan for desulfurization (such as H 2 S) treatment;
步骤2、油气双通道冷凝回收：脱硫处理后的废气通过所述双通道油气冷凝回收单元，油气由气相转换为液相后流入所述收油罐内回收储存，冷凝后的低浓度废气流入所述活性炭吸附单元内；
步骤3、废气活性炭吸附和真空脱附：冷凝后的低浓度废气进入所述活性炭吸附单元内进行活性炭吸附和真空脱附，真空脱附的高浓度废气回流入所述双通道油气冷凝回收单元重复冷凝回收，直至废气浓度小于10g/m3流入所述RTO高温热氧化处理单元内；
步骤4、废气RTO焚烧炉高温热氧化分解：浓度小于10g/m3的废气流入所述RTO高温热氧化处理单元内进行高温热氧化分解为CO2和H2O，热氧化分解后的高温废气通过所述RTO蓄热室进行热回收，废气的VOCs排放浓度小于60mg/m3达标排放。Step 4. High-temperature thermal oxidative decomposition of waste gas RTO incinerator: waste gas with a concentration of less than 10 g/m 3 flows into the RTO high-temperature thermal oxidation treatment unit for high-temperature thermal oxidative decomposition into CO 2 and H 2 O, and the high-temperature waste gas after thermal oxidative decomposition The heat recovery is carried out through the RTO regenerator, and the VOCs emission concentration of the exhaust gas is less than 60mg/ m3 , and the emission standard is reached.
作为优选，步骤2中，所述双通道油气冷凝回收单元对脱硫处理后的废气中油气采用三级低温冷凝，依次通过0～5℃、-20～-30℃和-65～-70℃三个阶段的低温冷凝回收。Preferably, in
作为优选，步骤4中，所述RTO高温热氧化处理单元内，所述RTO焚烧炉的高温热氧化分解温度不低于760℃。Preferably, in step 4, in the RTO high temperature thermal oxidation treatment unit, the high temperature thermal oxidation decomposition temperature of the RTO incinerator is not lower than 760°C.
本发明的上述油气冷凝回收结合RTO的石化罐区废气处理系统和工艺中，石化罐区废气先在油气脱硫单元进行硫化物的去除，去除硫化物后的油气继续进入双通道油气冷凝回收单元中将油气逐级从常温冷却至-65～-70℃(此处温度场可根据实际需要变更设定)，混合气体中的大部分油气直接液化回收，剩余极少量油气在吸附单元中通过吸附工艺和空气进行吸附分离，系统通过以上过程不断循环达到油气连续冷却分凝回收，同时直至终端被处理的油气达标排放，其中涉及的工艺原理如下：In the above-mentioned oil and gas condensation recovery combined with RTO in the petrochemical tank farm waste gas treatment system and process of the present invention, the petrochemical tank farm waste gas first removes sulfides in the oil and gas desulfurization unit, and the oil and gas after removing the sulfide continues to enter the dual-channel oil and gas condensation recovery unit. Cool the oil and gas from normal temperature to -65～-70℃ step by step (the temperature field here can be changed according to actual needs), most of the oil and gas in the mixed gas is directly liquefied and recovered, and the remaining very small amount of oil and gas is passed through the adsorption process in the adsorption unit Adsorption and separation are carried out with air, and the system continuously circulates through the above process to achieve continuous cooling, segregation and recovery of oil and gas, and at the same time, until the oil and gas treated at the terminal reach the standard discharge, the process principles involved are as follows:
吸收原理：根据酸碱中和反应，废气中的H2S与脱硫洗涤塔NaOH溶液反应生产Na2S，将H2S捕集下来，不溶于水的油气流入双通道油气冷凝回收单元。Absorption principle: According to the acid-base neutralization reaction, the H 2 S in the exhaust gas reacts with the NaOH solution of the desulfurization scrubber to produce Na 2 S, the H 2 S is captured, and the water-insoluble oil and gas flows into the dual-channel oil and gas condensation and recovery unit.
制冷原理：双通道油气冷凝回收单元工作时，由压缩机排出的高温高压制冷剂气体进入冷凝器被冷凝成高压过冷液体，经膨胀阀节流降压变成低温低压的气液两相混合物进入蒸发器(换热器)，制冷剂在其内吸收通过蒸发器的油气的热量进行自身气化，制冷剂充分气化后再被压缩机吸入压缩室进入下一轮循环，整机系统通过以上过程不断循环，从而达到油气连续降温回收的目的，通过降温使油气达到过饱和状态冷凝成液态直接回收，极小部分气体进入后级的活性炭吸附单元吸附处理。Refrigeration principle: When the dual-channel oil and gas condensation recovery unit is working, the high-temperature and high-pressure refrigerant gas discharged from the compressor enters the condenser and is condensed into a high-pressure subcooled liquid, which is throttled and depressurized by an expansion valve to become a low-temperature and low-pressure gas-liquid two-phase mixture. Entering the evaporator (heat exchanger), the refrigerant absorbs the heat of the oil and gas passing through the evaporator and gasifies itself. After the refrigerant is fully gasified, it is sucked into the compression chamber by the compressor and enters the next cycle. The above process is continuously circulated, so as to achieve the purpose of continuous cooling and recovery of oil and gas. Through cooling, the oil and gas can reach a supersaturated state and condense into a liquid state for direct recovery. A very small part of the gas enters the activated carbon adsorption unit in the latter stage for adsorption treatment.
变压吸附原理：变压吸附工艺是利用吸附剂对吸附质的选择性，即油气-空气混合气中各组分与吸附剂之间结合力强弱的差别，使难吸附的空气组分与易吸附的油气组分分离。同时利用吸附剂对吸附质的吸附容量随压力变化而有差异的特性，真空下脱附这些油气而使吸附剂获得再生，整个操作过程均在环境温度下进行,包括吸附和再生两个基本操作。The principle of pressure swing adsorption: The pressure swing adsorption process uses the selectivity of the adsorbent to the adsorbate, that is, the difference in the binding force between the components in the oil-air-air mixture and the adsorbent, so that the air components that are difficult to adsorb can be separated from the adsorbent. Separation of easily adsorbed oil and gas components. At the same time, using the characteristic that the adsorption capacity of the adsorbent to the adsorbate varies with the pressure, the adsorbent can be regenerated by desorbing these oil and gas under vacuum. The entire operation process is carried out at ambient temperature, including the two basic operations of adsorption and regeneration. .
RTO原理：废气从油气回收系统通过引风机输送到RTO炉,在RTO炉内经过760℃以上的高温与氧气进行热氧化分解为CO2和H2O。由于废气已在蓄热室内预热，燃料耗量大为减少。燃烧室有两个作用：一是保证废气能达到设定的氧化温度，二是保证有足够的停留时间使废气中的VOC充分氧化，废气在燃烧室中焚烧，成为净化的高温气体后离开燃烧室，进入蓄热室(在前面的循环中已被冷却)，放热降温后排出，而蓄热室吸收大量热量后升温(用于下一个循环加热废气)，净化后的废气经烟囱排入大气。RTO principle: The exhaust gas is transported from the oil and gas recovery system to the RTO furnace through the induced draft fan, and is thermally oxidized and decomposed into CO 2 and H 2 O through the high temperature of 760 ℃ and oxygen in the RTO furnace. Since the exhaust gas is already preheated in the regenerator, the fuel consumption is greatly reduced. The combustion chamber has two functions: one is to ensure that the exhaust gas can reach the set oxidation temperature, and the other is to ensure that there is enough residence time to fully oxidize the VOC in the exhaust gas. The exhaust gas is incinerated in the combustion chamber and becomes a purified high-temperature gas before leaving the combustion The regenerative chamber enters the regenerator (which has been cooled in the previous cycle), releases heat after cooling down, and the regenerator absorbs a large amount of heat and then heats up (for heating the exhaust gas in the next cycle), and the purified exhaust gas is discharged through the chimney. atmosphere.
本发明采用“冷凝法油气回收+RTO”组合工艺治理石化行业罐区废气，先将储罐区高浓度油气通过冷凝油气回收系统，废气中的油气由气相转换成液相进行收集回收，起到很好的油气回用经济效益。同时油气回收后的废气浓度小于10g/m3，再经过RTO焚烧炉760℃以上高温热氧化分解为CO2和H2O，热氧化后的高温废气通过RTO的蓄热陶瓷进行热回收，使罐区废气进行回收利用(95％的回收效率)和RTO热氧化处理(98％以上的处理效率和95％以上的热回收效率)，确保系统持续稳定达标(VOCs排放浓度小于60mg/m3)排放，与现有技术相比，具有如下有益效果：The invention adopts the "condensation method oil and gas recovery + RTO" combined process to treat the waste gas in the tank area of the petrochemical industry. First, the high-concentration oil and gas in the storage tank area is passed through the condensed oil and gas recovery system, and the oil and gas in the waste gas is converted from gas phase to liquid phase for collection and recovery. Good economic benefits of oil and gas reuse. At the same time, the concentration of exhaust gas after oil and gas recovery is less than 10g/m 3 , and then it is decomposed into CO 2 and H 2 O through high temperature thermal oxidation of RTO incinerator above 760℃. The waste gas from the tank farm is recycled (95% recovery efficiency) and RTO thermal oxidation treatment (more than 98% treatment efficiency and more than 95% heat recovery efficiency) to ensure that the system continues to meet the standard (VOCs emission concentration less than 60mg/m 3 ) Emissions, compared with the prior art, have the following beneficial effects:
(1)采用双通道三级冷凝+活性炭吸附和真空脱附油气回收工艺，废气温度冷凝到-70℃以下，解决低温下因换热器堵塞而影响油气系统连续稳定运行的问题。(1) Using dual-channel three-stage condensation + activated carbon adsorption and vacuum desorption oil and gas recovery process, the temperature of the exhaust gas is condensed below -70 °C to solve the problem that the continuous and stable operation of the oil and gas system is affected by the blockage of the heat exchanger at low temperature.
(2)油气回收效率达到95％以上，出口废气浓度小于10g/m3。(2) The recovery efficiency of oil and gas reaches more than 95%, and the concentration of exhaust gas at the outlet is less than 10g/m 3 .
(3)“冷凝法油气回收+RTO”处理效率在99％以上，排放TVOC小于60mg/m3，可达到降低系统运行成本、提高去除效率、环保稳定达标同时最大限度的提高系统使用寿命的效果。(3) The treatment efficiency of "condensation method oil and gas recovery + RTO" is above 99%, and the emission of TVOC is less than 60mg/m 3 , which can reduce the operating cost of the system, improve the removal efficiency, meet the environmental protection and stability standards, and maximize the service life of the system. .
附图说明Description of drawings
图1是实施例中油气冷凝回收结合RTO的石化罐区废气处理系统的结构示意图；Fig. 1 is the structural representation of the petrochemical tank farm waste gas treatment system of oil and gas condensation recovery combined with RTO in the embodiment;
附图标记如下：1第一阻火器，2油气风机，3脱硫洗涤塔，4第一冷箱机组，5第二冷箱机组，6冷冻机组，7第一活性炭罐，8第二活性炭罐，9真空泵，10收油罐，11RTO入口风机，12第二阻火器，13RTO焚烧炉，14排风筒。Reference numerals are as follows: 1 first flame arrester, 2 oil and gas fan, 3 desulfurization washing tower, 4 first cold box unit, 5 second cold box unit, 6 refrigeration unit, 7 first activated carbon tank, 8 second activated carbon tank, 9 vacuum pumps, 10 oil collection tanks, 11RTO inlet fans, 12 second flame arresters, 13RTO incinerators, 14 exhaust ducts.
具体实施方式Detailed ways
为使本发明实施例的目的、技术方案和优点更加清楚，下面将结合本发明实施例的附图对本发明实施例的技术方案进行清楚、完整地描述。显然，所描述的实施例是本发明的一部分实施例，而不是全部的实施例。基于所描述的本发明的实施例，本领域普通技术人员在无需创造性劳动的前提下所获得的所有其它实施例，都属于本发明保护的范围。In order to make the purpose, technical solutions and advantages of the embodiments of the present invention clearer, the technical solutions of the embodiments of the present invention will be clearly and completely described below with reference to the accompanying drawings of the embodiments of the present invention. Obviously, the described embodiments are some, but not all, embodiments of the present invention. Based on the described embodiments of the present invention, all other embodiments obtained by those of ordinary skill in the art without creative work fall within the protection scope of the present invention.
图1示例性地描述了一种油气冷凝回收结合RTO的石化罐区废气处理系统，包括依次管道连通的油气脱硫单元、双通道油气冷凝回收单元、活性炭吸附单元和RTO高温热氧化处理单元；其中：Fig. 1 exemplarily depicts a petrochemical tank farm waste gas treatment system combining oil and gas condensation and recovery with RTO, including an oil and gas desulfurization unit, a dual-channel oil and gas condensation recovery unit, an activated carbon adsorption unit, and an RTO high-temperature thermal oxidation treatment unit connected in sequence; wherein :
油气脱硫单元包括依次管道连通的第一阻火器1、油气风机2和脱硫洗涤塔3，油气风机1经过管道通入脱硫洗涤塔3的底部，石化罐区废气通过油气风机1进入脱硫洗涤塔3内进行脱硫处理；The oil and gas desulfurization unit includes a first flame arrester 1, an oil and
双通道油气冷凝回收单元包括第一冷箱机组4、第二冷箱机组5、冷冻机组6和收油罐10，第一冷箱机组4和第二冷箱机组5并联连接且采用“一备一用”交替工作模式，其入口均与脱硫洗涤塔3顶部连接、出油口分别与收油罐10连通；第一冷箱机组4和第二冷箱机组5通过冷冻机组6相互连通形成油气冷凝循环回路，脱硫处理后的废气转换为液相的油可流入收油罐内，未冷凝的低浓度废气流入活性炭吸附单元内；其中第一冷箱机组4和第二冷箱机组5内设有三个串联连接的冷箱；The dual-channel oil and gas condensation recovery unit includes a first cold box unit 4, a second
活性炭吸附单元包括两并联的第一活性炭罐7和第二活性炭罐8以及真空泵9，其底部入口与第一冷箱机组4和第二冷箱机组5的出气口经管道连通，其顶部出口设有两通路，一条通过真空泵9与第一冷箱机组4和第二冷箱机组5的入口连通，一条与RTO高温热氧化处理单元连通；The activated carbon adsorption unit includes two paralleled first activated
RTO高温热氧化处理单元包括依次连通的RTO入口风机11、第二阻火器12和RTO焚烧炉13，RTO入口风机11分别与第一活性炭罐7和第二活性炭罐8的出口连通，低浓度废气通过其流入RTO焚烧炉13内，RTO焚烧炉13设有若干个并列的入气口，经管道分别与RTO入口风机11连接，RTO焚烧炉13内设有RTO蓄热室和燃烧室，且RTO蓄热室内设有蓄热陶瓷进行热回收；还包括排气筒14，与RTO焚烧炉13的出气口连通。The RTO high temperature thermal oxidation treatment unit includes an
采用上述油气冷凝回收结合RTO的石化罐区废气处理系统进行石化罐区废气处理时，具体工艺步骤如下：When using the above-mentioned oil and gas condensation recovery combined with RTO petrochemical tank farm waste gas treatment system for petrochemical tank farm waste gas treatment, the specific process steps are as follows:
步骤1、油气脱硫处理：罐区废气通过油气风机进入脱硫洗涤塔内进行脱硫(如H2S)处理；Step 1. Oil and gas desulfurization treatment: the waste gas from the tank area enters the desulfurization washing tower through the oil and gas fan for desulfurization (such as H 2 S) treatment;
步骤2、油气双通道冷凝回收：脱硫处理后的废气通过双通道油气冷凝回收单元，油气由气相转换为液相后流入收油罐内回收储存，冷凝后的低浓度废气流入活性炭吸附单元内，双通道油气冷凝回收单元对脱硫处理后的废气中油气采用三级低温冷凝，依次通过0～5℃、-20～-30℃和-65～-70℃三个阶段的低温冷凝回收；
步骤3、废气活性炭吸附和真空脱附：冷凝后的低浓度废气进入活性炭吸附单元内进行活性炭吸附和真空脱附，真空脱附的高浓度废气回流入双通道油气冷凝回收单元重复冷凝回收，直至废气浓度小于10g/m3流入RTO高温热氧化处理单元内；
步骤4、废气RTO焚烧炉高温热氧化分解：浓度小于10g/m3的废气流入RTO高温热氧化处理单元内不低于760℃进行高温热氧化分解为CO2和H2O，热氧化分解后的高温废气再通过RTO蓄热室进行热回收，废气的VOCs排放浓度小于60mg/m3时达标排放。Step 4. High-temperature thermal oxidative decomposition of waste gas RTO incinerator: waste gas with a concentration of less than 10g/m 3 flows into the RTO high-temperature thermal oxidation treatment unit and is not lower than 760 ° C for high-temperature thermal oxidative decomposition into CO 2 and H 2 O. After thermal oxidative decomposition The high-temperature exhaust gas is then passed through the RTO regenerator for heat recovery. When the VOCs emission concentration of the exhaust gas is less than 60mg/ m3 , the emission standard is reached.
综上可知，本发明的上述系统采用“冷凝法油气回收+RTO”组合工艺处理石化行业罐区废气油气处理效率在99％以上，TVOC排放小于60mg/m3，环保稳定达标的同时可以最大限度提高系统的使用寿命。To sum up, the above system of the present invention adopts the "condensation method oil and gas recovery + RTO" combined process to treat the oil and gas treatment efficiency of the petrochemical industry tank farm waste gas above 99%, the TVOC emission is less than 60mg/m 3 , and the environmental protection and stability can meet the standard at the same time. Increase the service life of the system.
以上所述仅为本发明的较佳实施例而已，并不用以限制本发明，凡在本发明的精神和原则之内，所作的任何修改、等同替换、改进等，均应包含在本发明的保护范围之内。The above descriptions are only preferred embodiments of the present invention, and are not intended to limit the present invention. Any modification, equivalent replacement, improvement, etc. made within the spirit and principle of the present invention shall be included in the scope of the present invention. within the scope of protection.
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN115888305A (en) * | 2022-11-14 | 2023-04-04 | 江苏嘉盛环境设备制造有限公司 | Vacuum pump tail gas treatment System (VOCs) process for lithium battery industry |
| CN117089363A (en) * | 2023-10-19 | 2023-11-21 | 新乡市华音再生能源设备有限公司 | Oil gas condensation recovery device applied to junked tire oil refining system |
| CN119186178A (en) * | 2024-11-22 | 2024-12-27 | 山东潍坊双星农药有限公司 | Waste gas absorption method and device for difenoconazole intermediate |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN205461670U (en) * | 2016-01-11 | 2016-08-17 | 中国石油化工股份有限公司 | Storage tank discharged waste gas's deep purification recovery unit |
| CN109289504A (en) * | 2018-08-31 | 2019-02-01 | 江苏新久扬环保设备科技有限公司 | A kind of sulfur-containing oil-gas recyclable device and technique |
| CN217410252U (en) * | 2022-05-25 | 2022-09-13 | 上海兰宝环保科技有限公司 | Oil gas condensation recycling combines RTO's petrochemical industry jar district exhaust treatment system |
-
2022
- 2022-05-25 CN CN202210573057.5A patent/CN114887443A/en active Pending
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN205461670U (en) * | 2016-01-11 | 2016-08-17 | 中国石油化工股份有限公司 | Storage tank discharged waste gas's deep purification recovery unit |
| CN109289504A (en) * | 2018-08-31 | 2019-02-01 | 江苏新久扬环保设备科技有限公司 | A kind of sulfur-containing oil-gas recyclable device and technique |
| CN217410252U (en) * | 2022-05-25 | 2022-09-13 | 上海兰宝环保科技有限公司 | Oil gas condensation recycling combines RTO's petrochemical industry jar district exhaust treatment system |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN115888305A (en) * | 2022-11-14 | 2023-04-04 | 江苏嘉盛环境设备制造有限公司 | Vacuum pump tail gas treatment System (VOCs) process for lithium battery industry |
| CN117089363A (en) * | 2023-10-19 | 2023-11-21 | 新乡市华音再生能源设备有限公司 | Oil gas condensation recovery device applied to junked tire oil refining system |
| CN119186178A (en) * | 2024-11-22 | 2024-12-27 | 山东潍坊双星农药有限公司 | Waste gas absorption method and device for difenoconazole intermediate |
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