WO2020258940A1 - 一种含氨尾气吸收系统 - Google Patents

一种含氨尾气吸收系统 Download PDF

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Publication number
WO2020258940A1
WO2020258940A1 PCT/CN2020/080714 CN2020080714W WO2020258940A1 WO 2020258940 A1 WO2020258940 A1 WO 2020258940A1 CN 2020080714 W CN2020080714 W CN 2020080714W WO 2020258940 A1 WO2020258940 A1 WO 2020258940A1
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Prior art keywords
absorption
ammonia
tail gas
containing tail
absorption device
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PCT/CN2020/080714
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English (en)
French (fr)
Inventor
魏会
吴成
李玉博
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佳化化学科技发展（上海）有限公司
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Application filed by 佳化化学科技发展（上海）有限公司 filed Critical 佳化化学科技发展（上海）有限公司
Priority to US17/617,265 priority Critical patent/US20220226773A1/en
Priority to EP20830879.1A priority patent/EP3967387A4/en
Publication of WO2020258940A1 publication Critical patent/WO2020258940A1/zh

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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/14—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 absorption
    • B01D53/18—Absorbing units; Liquid distributors therefor
    • B01D53/185—Liquid distributors
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/14—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 absorption
    • B01D53/1406—Multiple stage absorption
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/46—Removing components of defined structure
    • B01D53/54—Nitrogen compounds
    • B01D53/58—Ammonia
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
    • B01D53/75—Multi-step processes
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
    • B01D53/77—Liquid phase processes
    • B01D53/78—Liquid phase processes with gas-liquid contact
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01C—AMMONIA; CYANOGEN; COMPOUNDS THEREOF
    • C01C1/00—Ammonia; Compounds thereof
    • C01C1/02—Preparation, purification or separation of ammonia
    • C01C1/12—Separation of ammonia from gases and vapours
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2251/00—Reactants
    • B01D2251/50—Inorganic acids
    • B01D2251/506—Sulfuric acid
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2251/00—Reactants
    • B01D2251/50—Inorganic acids
    • B01D2251/512—Phosphoric acid
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2252/00—Absorbents, i.e. solvents and liquid materials for gas absorption
    • B01D2252/10—Inorganic absorbents
    • B01D2252/103—Water
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2257/00—Components to be removed
    • B01D2257/40—Nitrogen compounds
    • B01D2257/406—Ammonia

Definitions

  • the application relates to the field of exhaust gas treatment equipment, and in particular to an ammonia-containing exhaust gas absorption system.
  • the reaction tail gas produced during the industrial production of ethanolamine contains a large amount of ammonia. If the ammonia gas is directly discharged, it will pollute the atmosphere and cause waste of production raw materials. Therefore, the general industrial production of ethanolamine needs to be produced.
  • the ammonia-containing tail gas is processed to recover the ammonia therein.
  • the difficulty of ammonia absorption treatment is also different.
  • the commonly used reactors in the ethanolamine production process are the tank reactor and the tubular reactor.
  • the tubular reactor adopts a high-pressure process, the reaction pressure is above 7 MPa, and the discharged ammonia-containing tail gas is above 1 MPa.
  • the volume of the tail gas is small.
  • the ammonia gas is relatively easy to be absorbed and treated.
  • Single-stage absorption can be used to treat the ammonia-containing tail gas. Due to the limitation of the equipment structure, the tank reactor requires low reaction pressure and high molar feed ratio of ammonia to ethylene oxide.
  • the produced tail gas contains high ammonia content, low tail gas pressure and large tail gas volume, and multi-stage absorption is required.
  • the ammonia in the ammonia-containing tail gas can be recovered by treatment.
  • the molar feed ratio of ammonia and ethylene oxide needs to be adjusted.
  • the volume of the reaction tail gas and the concentration of ammonia gas are also Corresponding changes will occur depending on the process.
  • the existing ammonia-containing tail gas absorption system usually has several fixed absorption towers, and the connection relationship between the absorption towers is also certain, which makes the ammonia-containing tail gas absorption system unable to adapt to different reaction systems and reaction processes. Different ammonia-containing tail gas processing requirements.
  • the technical problem to be solved by this application is to overcome the fixed arrangement of the ammonia-containing tail gas absorption system in the prior art, which makes the ammonia-containing tail gas absorption tower unable to adapt to different ammonia-containing tail gas for absorption, thereby providing an ammonia-containing tail gas absorption system.
  • An ammonia-containing tail gas absorption system comprising at least two sets of absorption devices, in which at least two delivery pipelines are provided at the inlets of some of the absorption devices, and the delivery pipelines are used to connect the absorption device and the reactor ammonia-containing tail gas outlet Or other absorption devices are connected, and the delivery pipeline is provided with a valve, and the valve is used to control the on and off of the delivery pipeline to switch the series-parallel relationship between the groups of absorption devices.
  • the absorption device includes:
  • the absorption tower is equipped with a spray head for reverse spraying the absorption liquid to the ammonia-containing tail gas to recover the ammonia;
  • the absorption tank is connected with the absorption tower and is used for collecting and storing the ammonia-containing absorption liquid discharged from the absorption tower.
  • the absorption tower is also provided with a packing for increasing the contact area between the ammonia-containing tail gas and the absorption liquid.
  • the absorption device further includes a circulation pump, one end of the circulation pump is connected with the absorption tank, and the other end is connected with the spray head, and is used to transport the ammonia-containing absorption liquid stored in the absorption tank to the spray head.
  • the absorption device further includes a cooler, which is used for cooling the ammonia-containing absorption liquid delivered by the circulating pump.
  • the cooler is at least one of a shell and tube heat exchanger, a plate heat exchanger or a double tube heat exchanger.
  • the absorption tank is a horizontal storage tank or a vertical storage tank.
  • the ammonia-containing tail gas absorption system provided by this application, multiple sets of absorption devices are provided, and some of the absorption devices are provided with multiple delivery pipelines, and the delivery pipelines are equipped with valves, which can control the communication of the delivery pipelines. Therefore, the series-parallel relationship between the absorption devices can be adjusted.
  • the connection relationship between the absorption devices can be set to series, so as Ammonia can be treated by single-stage or multi-stage absorption.
  • the connection relationship between the absorption devices can be switched to parallel, so that the ammonia-containing tail gas enters
  • the exhaust gas absorption system can enter multiple absorption devices at the same time, thereby reducing the flow rate of the ammonia-containing tail gas in a single absorption device, prolonging the contact time between the ammonia-containing tail gas and the processing equipment, thereby improving the absorption effect.
  • the ammonia-containing tail gas provided by the present invention can switch the treatment mode of the ammonia-containing tail gas absorption system according to different reaction systems and reaction processes, so that the ammonia-containing tail gas absorption system can adapt to different reaction systems and reaction processes, and the operation is simple and convenient.
  • the fillers can increase the contact area between the ammonia-containing tail gas and the absorption liquid, so that the absorption liquid can absorb as much ammonia in the ammonia-containing tail gas as possible
  • the number of absorption towers that need to be installed can be reduced as much as possible to achieve the purpose of reducing processing costs.
  • a circulation pump is provided in the absorption device, and the circulation pump is used to transport the absorption liquid that has absorbed ammonia to the spray head for use again, that is, the setting of the circulation pump can realize multiple repetitions of the absorption liquid By using, the absorption liquid can be replaced until the ammonia content in the absorption liquid reaches the maximum solubility, which maximizes the utilization rate of the absorption liquid, thereby saving the consumption of the absorption liquid and reducing the processing cost.
  • the ammonia-containing absorption liquid delivered by the circulating pump can be cooled by the cooler, so that when the ammonia-containing absorption liquid is re-transmitted to the nozzle, The temperature difference between the ammonia-containing absorption liquid and the ammonia-containing tail gas is relatively large, so that the ammonia-containing absorption liquid can absorb as much ammonia in the tail gas as possible.
  • Fig. 1 is a schematic structural diagram of an ammonia-containing tail gas absorption system of Example 1 of the present application.
  • the ammonia-containing tail gas absorption system includes a first absorption device 1, a second absorption device 2, a third absorption device 3, and a fourth absorption device 4.
  • a first delivery pipeline is provided at the entrance of the first absorption device 1, and the first delivery pipeline connects the inlet of the first absorption device 1 with the ammonia-containing tail gas outlet of the reactor, and a valve 101 is provided on the first delivery pipeline. .
  • the inlet of the second absorption device 2 is provided with a second delivery pipeline and a third delivery pipeline, wherein the second delivery pipeline is used to connect the inlet of the second absorption device 2 with the ammonia-containing tail gas outlet of the reactor,
  • the second delivery pipeline is provided with a No. 2 valve 102
  • the third delivery pipeline is used to connect the inlet of the second absorption device 2 with the outlet of the first absorption device 1
  • the third delivery pipeline is provided with a third valve 103.
  • a fourth delivery pipeline and a fifth delivery pipeline are provided at the entrance of the third absorption device 3.
  • the fourth delivery pipeline is used to connect the entrance of the third absorption device 3 with the outlet of the first absorption device 1.
  • the fourth delivery pipeline is provided with a fourth valve 104
  • the fifth delivery pipeline is used to connect the inlet of the third absorption device 3 with the outlet of the second absorption device 2
  • the fifth delivery pipeline is provided with a fifth valve 105.
  • a sixth conveying pipe, a seventh conveying pipe, and an eighth conveying pipe are provided at the entrance of the fourth absorbing device 4, wherein the sixth conveying pipe is used to connect the inlet of the fourth absorbing device 4 with the air outlet of the first absorbing device 1.
  • No. 6 valve 106 is provided on the fifth delivery pipeline
  • the seventh delivery pipeline is used to connect the inlet of the fourth absorption device 4 with the outlet of the second absorption device 2
  • the seventh delivery pipeline is provided with No. 7 Valve 107
  • the eighth conveying pipe is used to connect the inlet of the fourth absorption device 4 with the air outlet of the third absorption device 3
  • the eighth valve 108 is provided on the eighth conveying pipe.
  • the first absorption device 1, the second absorption device 2, the third absorption device 3 and the fourth absorption device 4 all include: an absorption tower 5 and an absorption tank 6.
  • the absorption tower 5 is provided with a nozzle 51, and the absorption tower 5 is used for The ammonia tail gas is sprayed back to the absorption liquid to recover ammonia.
  • the inlet of the absorption tower 5 is the entrance of the absorption device.
  • the absorption tank 6 is connected with the absorption tower 5, and the absorption tank 6 is used to perform the ammonia-containing absorption liquid discharged from the absorption tower 5. Collect and store, the staff can process the ammonia-containing absorption liquid stored in the absorption tank 6 to recover and reuse ammonia.
  • the ammonia-containing absorption liquid in each absorption tank 6 can be collected together for processing, or directly absorbed individually Slot 6 is treated separately.
  • the absorbing liquid can be water, phosphoric acid aqueous solution or sulfuric acid aqueous solution, etc.
  • the type of absorbing liquid is not limited, as long as it can absorb ammonia, and the concentration of phosphoric acid aqueous solution and sulfuric acid aqueous solution is also not limited.
  • the concentration of ammonia is set.
  • the concentration of the more commonly used phosphoric acid aqueous solution is 10%-20%
  • the concentration of the sulfuric acid aqueous solution is 10%-20%. More preferably, the concentration of the phosphoric acid aqueous solution is 15%-18.5%.
  • the concentration is 15%-18.5%.
  • the absorption tank 6 can be either a horizontal storage tank or a vertical storage tank.
  • a packing is also arranged in the absorption tower 5.
  • the arrangement of the packing can further extend the contact time between the ammonia-containing tail gas and the absorption liquid, so that the ammonia in the ammonia-containing tail gas can be treated
  • the packing can be made of plastic Pall ring, ceramic Pall ring, stainless steel Pall ring, etc., and it is not limited to this.
  • a circulation pump is installed in the first absorption device 1, the second absorption device 2, the third absorption device 3, and the fourth absorption device 4.
  • One end of the circulation pump is connected to The absorption tank 6 is connected, and the other end is connected with the nozzle 51 in the absorption tower 5.
  • the circulating pump is used to transport the ammonia-containing absorption liquid stored in the absorption tank 6 to the nozzle 51, so that the absorption liquid can be reused many times , You only need to replace the absorption solution when the ammonia content in the absorption solution reaches the maximum solubility.
  • the absorption solution when the pH value of the phosphoric acid aqueous solution or sulfuric acid aqueous solution in the absorption tank 6 reaches 6-8, the absorption solution
  • the more preferred replacement time is when the pH value of the phosphoric acid aqueous solution or the sulfuric acid aqueous solution reaches 7-7.5.
  • This setting can make the absorption liquid absorb as much ammonia as possible, thereby saving the amount of absorption liquid and reducing the processing cost.
  • the absorption devices are connected in series, the lower the position of the absorption device is, the less ammonia can be recovered, that is, the ammonia concentration of the ammonia-containing absorption liquid in the absorption tank at this time will always be low.
  • the ammonia-containing absorption solution with a lower ammonia concentration in the absorption device located at a later position can be used to replace the ammonia-containing absorption solution with a higher ammonia concentration in the absorption device located at the front, thereby further improving Save the role of absorbent.
  • the absorption liquid in the fourth absorption device 4 is preferably an acid solution, so that under special circumstances, the fourth absorption device 4 can absorb unreacted ethylene oxide in the reaction tail gas, thereby Prevent the emission of VOC.
  • the absorption tanks in the two absorption devices can be connected to ensure that the concentration of the ammonia-containing absorption liquid in the two absorption devices is consistent.
  • the first absorption device 1, the second absorption device 2 and the third absorption device 3 A cooler 7 is also provided inside, and the cooler 7 is used to cool the ammonia-containing absorption liquid delivered by the circulating pump.
  • the cooler 7 can be a shell-and-tube heat exchanger, a plate heat exchanger or a double-pipe heat exchanger.
  • the number of coolers 7 can be set to one or more. When the number of coolers 7 is more than one, the communication relationship between the coolers 7 can be parallel or series.
  • the specific settings of the coolers 7 can be based on The specific size of the exhaust gas absorption is determined. When the exhaust gas absorption is small, the cooler 7 may not be provided.
  • the ammonia-containing tail gas When the ammonia-containing tail gas enters the absorption device, it first enters the absorption tower 5 through the inlet of the absorption tower 5. At this time, the nozzle 51 reversely sprays the absorption liquid on the ammonia-containing tail gas, and the absorption liquid contacts with the ammonia-containing tail gas to form an ammonia-containing absorption liquid
  • the ammonia-containing tail gas after spray treatment is only discharged from the outlet of the absorption tower 5 to the next process, while the ammonia-containing absorption liquid is only sent to the cooler 7 by the circulating pump for cooling, and then sent to the nozzle 51 to form mist
  • the liquid is in contact with the newly delivered ammonia-containing tail gas to absorb the ammonia.
  • multiple sets of absorption devices are set, and some of the absorption devices are provided with multiple delivery pipelines, and the delivery pipelines are provided with valves.
  • the valves can be used to control the on and off of the delivery pipelines so as to adjust the communication between the absorption devices.
  • the series-parallel relationship enables the ammonia-containing tail gas absorption system to adapt to different types of ammonia-containing tail gas for use.
  • the reactor is a tubular reactor
  • the molar ratio of ammonia to ethylene oxide is high, the tail gas volume is small but the ammonia content is high, valve No. 101, valve No. 103, valve No. 104, No. 8
  • the valve 108 is in the open state, and the other valves are in the closed state.
  • the ammonia-containing tail gas first enters the first absorption device 1 to be processed.
  • the filler in the first absorption device 1 is a stainless steel Pall ring, the absorption liquid is water, and the cooler 7 is a column In the tubular heat exchanger, after treatment by the first absorption device 1, most of the ammonia in the tail gas is absorbed, and the tail gas containing trace ammonia after being treated by the first absorption device 1 is transported to the second absorption through the third transfer pipeline
  • the filler in the second absorption device 2 is a stainless steel Pall ring
  • the absorption liquid is water
  • the cooler 7 is a tubular heat exchanger.
  • the tail gas containing a very small amount of ammonia after the second absorption device 2 is processed It is transported to the third absorption device 3 through the fourth delivery pipeline.
  • the filler in the third absorption device 3 is stainless steel Pall ring, the absorption liquid is water, and the cooler 7 is a tube heat exchanger.
  • the ammonia-containing tail gas treated by the device 3 is finally transported to the fourth absorption device 4.
  • the filler in the fourth absorption device 4 is a stainless steel Pall ring, and the absorption liquid is an 18.5% phosphoric acid aqueous solution.
  • the fourth absorption device 4 is not installed Cooler 7, the exhaust gas after being treated by the fourth absorption device 4 can meet the discharge standard. Among them, when the pH of the phosphoric acid aqueous solution in the absorption tank 6 is 7.2, the absorption liquid is replaced to maintain the phosphoric acid aqueous solution to absorb ammonia Ability.
  • the reactor is a kettle-type reactor
  • the tail gas volume is large, the molar feed ratio of ammonia and ethylene oxide is relatively high, and the ammonia content is high
  • the eighth valve 108 is in the open state, and the other valves are in the closed state.
  • the first absorption device 1 and the second absorption device 2 are in parallel state, and the ammonia-containing tail gas output from the reactor enters the first absorption device 1 and The second absorption device 2 performs treatment, thereby reducing the flow rate of ammonia-containing tail gas in a single absorption device and prolonging the processing time of ammonia-containing tail gas.
  • the volume of ammonia-containing tail gas after the first absorption device 1 and the second absorption device 2 are processed simultaneously Significantly reduced.
  • the tail gas containing trace ammonia is sent to the third device and the fourth absorption device 4 for treatment in turn, and the tail gas after being processed by the fourth absorption device 4 can reach the emission standard.
  • the fillers in the first absorption device 1, the second absorption device 2, the third absorption device 3, and the fourth absorption device 4 are all stainless steel Pall rings.
  • the first absorption device 1, the second absorption device 2, and the third absorption device The absorption liquid in the device 3 is water, the absorption liquid in the fourth absorption device 4 is a 15% sulfuric acid aqueous solution, the coolers 7 in the first absorption device 1 and the second absorption device 2 are in-line heat exchangers, The cooler 7 in the three absorption device 3 is a double-pipe heat exchanger.
  • the reactor is a tank reactor
  • the molar feed ratio of ammonia to ethylene oxide is small
  • the tail gas volume is large
  • the ammonia content is low
  • the opening and closing states of the valves of the absorption system are the same as those of B, and only the fourth
  • the absorbing liquid in the absorbing device 4 can be replaced with water.
  • the reactor is a tubular reactor
  • the molar feed ratio of ammonia to ethylene oxide is small
  • the tail gas volume is small
  • the ammonia content is low
  • the first valve 101 and the sixth valve 106 are open
  • the other valves are closed
  • the tail gas output from the reactor is first input into the first absorption device 1 for processing.
  • the filler in the first absorption device 1 is stainless steel Pall ring
  • the absorption liquid is water
  • the cooler 7 is a tubular heat exchanger.
  • the exhaust gas treated by the first absorption device 1 is transported to the fourth absorption device 4 for processing.
  • the exhaust gas after the fourth absorption device 4 can meet the emission standard.
  • the filler in the fourth absorption device 4 is stainless steel Pall ring, the absorption liquid is water.
  • the ammonia-containing tail gas absorption system provided in this embodiment can switch the treatment mode of the ammonia-containing tail gas absorption system according to different reaction systems and reaction processes, so that the ammonia-containing tail gas absorption system can adapt to different reaction systems and reaction processes, and operate easy and convenient.

Abstract

一种含氨尾气吸收系统，包括至少两组吸收装置，其中部分吸收装置的入口处设置有至少两条输送管路，输送管路用于将吸收装置与反应器含氨尾气出口或其他吸收装置进行连通，输送管路上设置有阀门，阀门用于控制输送管路的通断以切换各组吸收装置之间的串并联关系。

Description

一种含氨尾气吸收系统 技术领域
本申请涉及尾气处理设备领域，具体涉及一种含氨尾气吸收系统。
背景技术
工业生产乙醇胺时产生的反应尾气中含有大量的氨气，若将氨气直接进行排放会对大气环境造成污染，同时也会造成生产原材料的浪费，故一般工业生产乙醇胺时都需要对其产生的含氨尾气进行处理以回收其中的氨。
一般的，根据生产尾气中氨气含量的不同以及尾气压力、尾气体积的不同，氨气吸收处理的难度也不同，如乙醇胺生产工艺中常用的反应器是釜式反应器和管式反应器，其中，管式反应器采用高压工艺，反应压力在7MPa以上，排放的含氨尾气在1MPa以上，尾气体积小，氨气相对容易被吸收处理，可以采用单级吸收对含氨尾气进行处理，而釜式反应器由于设备结构限制，要求反应压力低，氨与环氧乙烷的摩尔投料比高，因此生产的尾气中氨气含量高，而且尾气压力低，尾气体积大，需要采用多级吸收处理才能对含氨尾气中的氨进行回收，另外，在乙醇胺生产的过程中为了得到不同产品，需要调节氨与环氧乙烷的摩尔投料比，此时反应尾气的体积和氨气的浓度也会根据工艺的不同发生相应的变化。但是现有的含氨尾气吸收系统通常都是固定设置的几个吸收塔，吸收塔之间的连接关系也是一定的，从而使得含氨尾气吸收系统无法适应不同 的反应体系及反应工艺所产生的不同含氨尾气的处理需求。
申请内容
因此，本申请要解决的技术问题在于克服现有技术中的含氨尾气吸收系统固定设置，使得含氨尾气吸收塔无法适应不同的含氨尾气进行吸收的缺陷，从而提供一种含氨尾气吸收系统。
为解决上述技术问题，本申请采用的技术方案为：
一种含氨尾气吸收系统，包括至少两组吸收装置，其中部分所述吸收装置的入口处设置有至少两条输送管路，所述输送管路用于将吸收装置与反应器含氨尾气出口或其他吸收装置进行连通，所述输送管路上设置有阀门，所述阀门用于控制输送管路的通断以切换各组吸收装置之间的串并联关系。
进一步的，所述吸收装置包括：
吸收塔，设置有喷头，用于对含氨尾气逆向喷淋吸收液以对氨进行回收；
吸收槽，与所述吸收塔连通，用于对吸收塔排放出的含氨吸收液进行收集存储。
进一步的，所述吸收塔内还设置有用于增大含氨尾气与吸收液的接触面积的填料。
进一步的，所述吸收装置还包括循环泵，所述循环泵一端与所述吸收槽连 通，另一端与所述喷头连通，用于将所述吸收槽内存储的含氨吸收液输送至喷头。
进一步的，所述吸收装置还包括冷却器，所述冷却器用于对所述循环泵输送的含氨吸收液进行冷却。
进一步的，所述冷却器为管壳式换热器、板式换热器或套管式换热器中的至少一种。
进一步的，所述吸收槽为卧式储罐或立式储罐。
本申请技术方案，具有如下优点：
1.本申请提供的含氨尾气吸收系统，通过设置多组吸收装置，并在其中部分吸收装置上设置多条输送管路，且输送管路上设置有阀门，通过阀门可以控制输送管路的通断从而可以调整吸收装置之间的串并联关系，当要处理的含氨尾气的尾气压力高、尾气体积小时，可以将各吸收装置之间的连接关系设置为串联，从而对含氨尾气中的氨气进行单级或多级吸收处理即可，当要处理的含氨尾气的尾气压力低、尾气体积大时，则可将吸收装置之间的连接关系切换为并联，使得含氨尾气在进入尾气吸收系统内时可以同时进入多个吸收装置，从而降低含氨尾气在单个吸收装置内的流速，延长了含氨尾气与处理设备的接触时间，进而提高吸收效果，本发明提供的含氨尾气吸收系统，可以根据不同的反应体系与反应工艺对含氨尾气吸收系统的处理模式进行切换，从而使得含氨 尾气吸收系统可以适应不同的反应体系与反应工艺，且操作简单方便。
2.本申请提供的吸收装置，通过在吸收塔内设置填料，填料可以增大含氨尾气与吸收液的接触面积，从而可以使得吸收液能够尽可能多的将含氨尾气中的氨进行吸收，进而可以尽可能地减少吸收塔需要设置的个数，达到降低处理成本的目的。
3.本申请提供的吸收装置，通过在吸收装置内设置循环泵，循环泵用于将吸收有氨的吸收液再次输送至喷头中进行使用，即循环泵的设置可实现吸收液的多次重复利用，直至吸收液中的氨含量达到溶解度的最大值时再对吸收液进行更换即可，实现了吸收液的利用率最大化，从而可以起到节约吸收液用量的作用，降低了处理成本。
4.本申请提供的吸收装置，通过在吸收装置内设置冷却器，通过冷却器可以对循环泵输送的含氨吸收液进行降温冷却，从而可以使得当含氨吸收液被重新输送至喷头时，含氨吸收液与含氨尾气之间的温差较大，从而可以使得含氨吸收液能够对尾气中的氨尽可能多的进行吸收。
附图说明
为了更清楚地说明本申请具体实施方式或现有技术中的技术方案，下面将对具体实施方式或现有技术描述中所需要使用的附图作简单地介绍，显而易见地，下面描述中的附图是本申请的一些实施方式，对于本领域普通技术人员来 讲，在不付出创造性劳动的前提下，还可以根据这些附图获得其他的附图。
图1是本申请实施例1的含氨尾气吸收系统的结构示意图。
附图标记：
1、第一吸收装置；2、第二吸收装置；3、第三吸收装置；4、第四吸收装置；5、吸收塔；51、喷头；6、吸收槽；7、冷却器；101、一号阀门；102、二号阀门；103、三号阀门；104、四号阀门；105、五号阀门；106、六号阀门；107、七号阀门；108、八号阀门。
具体实施方式
提供下述实施例是为了更好地进一步理解本申请，并不局限于所述最佳实施方式，不对本申请的内容和保护范围构成限制，任何人在本申请的启示下或是将本申请与其他现有技术的特征进行组合而得出的任何与本申请相同或相近似的产品，均落在本申请的保护范围之内。
实施例中未注明具体实验步骤或条件者，按照本领域内的文献所描述的常规实验步骤的操作或条件即可进行。所用试剂或仪器未注明生产厂商者，均为可以通过市购获得的常规试剂产品。
实施例1
本实施例涉及一种含氨尾气吸收系统，含氨尾气吸收系统包括第一吸收装 置1、第二吸收装置2、第三吸收装置3以及第四吸收装置4。
第一吸收装置1的入口处设置有第一输送管路，第一输送管路将第一吸收装置1的入口与反应器的含氨尾气出口接通，第一输送管路上设置有一号阀门101。
第二吸收装置2的入口处设置有第二输送管路以及第三输送管路，其中，第二输送管路用于将第二吸收装置2的入口与反应器的含氨尾气出口接通，第二输送管路上设置有二号阀门102，第三输送管路用于将第二吸收装置2的入口与第一吸收装置1的出气口接通，第三输送管路上设置有三号阀门103。
第三吸收装置3的入口处设置有第四输送管路以及第五输送管路，第四输送管路用于将第三吸收装置3的入口与第一吸收装置1的出气口接通，第四输送管路上设置有四号阀门104，第五输送管路用于将第三吸收装置3的入口与第二吸收装置2的出气口接通，第五输送管路上设置有五号阀门105。
第四吸收装置4的入口处设置有第六输送管道、第七输送管道以及第八输送管道，其中，第六输送管道用于将第四吸收装置4的入口与第一吸收装置1的出气口接通，第五输送管道上设置有六号阀门106，第七输送管道用于将第四吸收装置4的入口与第二吸收装置2的出气口接通，第七输送管道上设置有七号阀门107，第八输送管道用于将第四吸收装置4的入口与第三吸收装置3的出气口接通，第八输送管道上设置有八号阀门108。
第一吸收装置1、第二吸收装置2、第三吸收装置3以及第四吸收装置4均包括：吸收塔5以及吸收槽6，吸收塔5内设置有喷头51，吸收塔5用于对含氨尾气逆向喷淋吸收液从而回收氨，吸收塔5的入口即为吸收装置的入口，吸收槽6与吸收塔5接通，吸收槽6用于对吸收塔5排放出的含氨吸收液进行收集存储，工作人员可对吸收槽6内存储的含氨吸收液进行处理从而对氨进行回收再利用，各个吸收槽6内的含氨吸收液可以被集中到一起再进行处理，或直接各个吸收槽6分开处理。
其中，吸收液可以为水、磷酸水溶液或硫酸水溶液等，吸收液的种类不受限制，只需满足可以吸收氨即可，磷酸水溶液及硫酸水溶液的浓度也不受限制，可以根据含氨尾气中氨的浓度进行设置，如较为常用的磷酸水溶液的浓度为10％-20％，硫酸水溶液的浓度为10％-20％，更为优选的，磷酸水溶液的浓度为15％-18.5％，硫酸水溶液的浓度为15％-18.5％。吸收槽6选用卧式储罐或立式储罐皆可。
为增大含氨尾气与吸收液的接触面积，在吸收塔5内还设置有填料，填料的设置可以进一步延长含氨尾气与吸收液的接触时间，从而使得含氨尾气中的氨能被处理得更完全，填料可以选用塑料鲍尔环、陶瓷鲍尔环以及不锈钢鲍尔环等，且不仅限于此。
为提高吸收液的利用率，在本实施例中，在第一吸收装置1、第二吸收装 置2、第三吸收装置3以及第四吸收装置4内均设置有循环泵，循环泵的一端与吸收槽6接通，另一端与吸收塔5中的喷头51接通，循环泵用于将吸收槽6中存储的含氨吸收液输送至喷头51中，从而使得吸收液可以得到重复多次利用，只需在吸收液中的氨含量达到溶解度的最大值时再对吸收液进行更换即可，如吸收槽6中的磷酸水溶液或硫酸水溶液的pH值达到6-8时即需对吸收液进行更换，更优选的更换时机是磷酸水溶液或硫酸水溶液的pH值达到7-7.5时，这样设置，可以使得吸收液能够尽可能多的吸收氨，从而可以节约吸收液的用量，降低了处理成本，另外，当各吸收装置形成串联状态时，位置越靠后的吸收装置内能够回收的氨含量越少，即此时的吸收槽中的含氨吸收液的氨浓度会一直处于较低的状态，此时，可用位置较为靠后的吸收装置中的含氨浓度较低的含氨吸收液对位置较为靠前的吸收装置中的含氨浓度较高的含氨吸收液进行更换，从而进一步起到节约吸收液的作用。另外，需要说明的是，第四吸收装置4中的吸收液优选为酸溶液，这样可以使得在特殊情况下，第四吸收装置4可以对反应尾气中未反应的环氧乙烷进行吸收，从而防止VOC的排放。当两吸收装置形成并联关系时，可以将这两吸收装置内的吸收槽连通，从而保证两吸收装置内的含氨吸收液的浓度一致。
由于氨气吸收过程是放热过程，故为增大含氨吸收液在与含氨尾气接触时二者之间的温差，在第一吸收装置1、第二吸收装置2以及第三吸收装置3内还设置有冷却器7，冷却器7用于对循环泵输送的含氨吸收液进行冷却降温， 冷却器7可选用管壳式换热器、板式换热器或套管式换热器，冷却器7的个数可以设置为一个或多个，当冷却器7的个数为多个时，各冷却器7之间的连通关系可以为并联或串联，冷却器7的具体设定可以根据尾气吸收量的具体大小决定，当尾气吸收量较小时，冷却器7也可以不设置。
含氨尾气进入吸收装置时，首先经由吸收塔5的入口进入吸收塔5内，此时由喷头51对含氨尾气进行逆向喷淋吸收液，吸收液与含氨尾气接触后形成含氨吸收液，经喷淋处理后的含氨尾气仅有吸收塔5的出口排出至下一工序，而含氨吸收液则仅由循环泵送至冷却器7进行冷却，再重新被输送至喷头51形成雾状液体再与新输送进来的含氨尾气进行接触吸收其中的氨。
本实施例通过设置多组吸收装置，并在其中部分吸收装置上设置多条输送管路，且输送管路上设置有阀门，通过阀门可以控制输送管路的通断从而可以调整吸收装置之间的串并联关系，进而使得含氨尾气吸收系统可以适应不同性质的含氨尾气进行使用。如：
A.当反应器为管式反应器，氨与环氧乙烷的摩尔比投料比高，尾气体积小但是氨含量高时，一号阀门101、三号阀门103、四号阀门104、八号阀门108为开启状态，其余阀门为关闭状态，含氨尾气首先进入第一吸收装置1内被处理，第一吸收装置1内的填料为不锈钢鲍尔环，吸收液为水，冷却器7为列管式换热器，经过第一吸收装置1处理后，尾气中的大部分氨被吸收，经第一吸 收装置1处理后的含有微量氨的尾气通过第三输送管路被输送至第二吸收装置2内，第二吸收装置2内的填料为不锈钢鲍尔环，吸收液为水，冷却器7为列管式换热器，经第二吸收装置2处理后的含有很微量氨的尾气再通过第四输送管路被输送至第三吸收装置3内，第三吸收装置3内的填料为不锈钢鲍尔环，吸收液为水，冷却器7为套管式换热器，经第三吸收装置3处理后的含氨尾气最终被输送至第四吸收装置4内，第四吸收装置4内的填料为不锈钢鲍尔环，吸收液为18.5％浓度的磷酸水溶液，第四吸收装置4未设置冷却器7，经第四吸收装置4处理后的尾气即可达到达标排放的标准，其中，吸收槽6内的磷酸水溶液的pH值为7.2时对吸收液进行更换，从而保持磷酸水溶液的吸收氨的能力。
B.当反应器为釜式反应器，尾气体积大，氨与环氧乙烷的摩尔投料比较高，氨含量高时，一号阀门101、二号阀门102、四号阀门104、五号阀门105、八号阀门108为开启状态，其余阀门为关闭状态，此时，第一吸收装置1与第二吸收装置2为并联状态，由反应器输出的含氨尾气同时进入第一吸收装置1以及第二吸收装置2进行处理，从而降低含氨尾气在单个吸收装置内的流速，延长含氨尾气的处理时间，在经过第一吸收装置1及第二吸收装置2同时处理后的含氨尾气体积大幅减小，此时含有微量氨气的尾气再被依次输送至第三装置以及第四吸收装置4内进行处理，再经由第四吸收装置4处理后的尾气即可达倒达标排放的标准，其中，第一吸收装置1、第二吸收装置2、第三吸收装 置3、第四吸收装置4内的填料均为不锈钢鲍尔环，第一吸收装置1、第二吸收装置2、第三吸收装置3内的吸收液均为水，第四吸收装置4内的吸收液为15％的硫酸水溶液，第一吸收装置1、第二吸收装置2内的冷却器7为列式换热器，第三吸收装置3内的冷却器7为套管式换热器。
C.当反应器为釜式反应器，氨与环氧乙烷的摩尔投料比小，尾气体积大，氨含量低时，吸收系统的各阀门开启关闭状态与B相同，仅需将其中第四吸收装置4内的吸收液更换为水即可。
D.当反应器为管式反应器，氨与环氧乙烷的摩尔投料比小，尾气体积小，氨含量低时，一号阀门101、六号阀门106为开启状态，其余阀门为关闭状态，经反应器输出的尾气首先输入至第一吸收装置1内进行处理，第一吸收装置1内的填料为不锈钢鲍尔环，吸收液为水，冷却器7为列管式换热器，经第一吸收装置1处理后的尾气再被输送至第四吸收装置4内进行处理，经第四吸收装置4处理后的尾气即可达到达标排放的标准，第四吸收装置4内的填料为不锈钢鲍尔环，吸收液为水。
本实施例提供的含氨尾气吸收系统可以根据不同的反应体系与反应工艺对含氨尾气吸收系统的处理模式进行切换，从而使得含氨尾气吸收系统可以适应不同的反应体系与反应工艺，且操作简单方便。
显然，上述实施例仅仅是为清楚地说明所作的举例，而并非对实施方式的 限定。对于所属领域的普通技术人员来说，在上述说明的基础上还可以做出其它不同形式的变化或变动。这里无需也无法对所有的实施方式予以穷举。而由此所引伸出的显而易见的变化或变动仍处于本申请创造的保护范围之中。

Claims (7)

  1. 一种含氨尾气吸收系统，其特征在于，包括至少两组吸收装置，其中部分所述吸收装置的入口处设置有至少两条输送管路，所述输送管路用于将吸收装置与反应器含氨尾气出口或其他吸收装置进行连通，所述输送管路上设置有阀门，所述阀门用于控制输送管路的通断以切换各组吸收装置之间的串并联关系。
  2. 根据权利要求1所述的含氨尾气吸收系统，其特征在于，所述吸收装置包括：
    吸收塔(5)，设置有喷头(51)，用于对含氨尾气逆向喷淋吸收液以对氨进行回收；
    吸收槽(6)，与所述吸收塔(5)连通，用于对吸收塔(5)排放出的含氨吸收液进行收集存储。
  3. 根据权利要求2所述的含氨尾气吸收系统，其特征在于，所述吸收塔(5)内还设置有用于增大含氨尾气与吸收液的接触面积的填料。
  4. 根据权利要求2所述的含氨尾气吸收系统，其特征在于，所述吸收装置还包括循环泵，所述循环泵一端与所述吸收槽(6)连通，另一端与所述喷头(51)连通，用于将所述吸收槽(6)内存储的含氨吸收液输送至喷头(51)。
  5. 根据权利要求4所述的含氨尾气吸收系统，其特征在于，所述吸收装置还包括冷却器(7)，所述冷却器(7)用于对所述循环泵输送的含氨吸收液进行冷却。
  6. 根据权利要求5所述的含氨尾气吸收系统，其特征在于，所述冷却器(7)为管壳式换热器、板式换热器或套管式换热器中的至少一种。
  7. 根据权利要求2所述的含氨尾气吸收系统，其特征在于，所述吸收槽(6)为卧式储罐或立式储罐。
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