WO2022135223A1 - 一种气流中一氧化氮的去除装置和工艺 - Google Patents

一种气流中一氧化氮的去除装置和工艺 Download PDF

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WO2022135223A1
WO2022135223A1 PCT/CN2021/137805 CN2021137805W WO2022135223A1 WO 2022135223 A1 WO2022135223 A1 WO 2022135223A1 CN 2021137805 W CN2021137805 W CN 2021137805W WO 2022135223 A1 WO2022135223 A1 WO 2022135223A1
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storage tank
regeneration reactor
solenoid valve
material storage
nitric oxide
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PCT/CN2021/137805
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English (en)
French (fr)
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黄立维
黄华丽
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黄立维
黄华丽
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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
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/46—Removing components of defined structure
    • B01D53/54—Nitrogen compounds
    • B01D53/56—Nitrogen oxides
    • 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
    • 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
    • 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
    • B01D53/80—Semi-solid phase processes, i.e. by using slurries
    • 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
    • B01D53/96—Regeneration, reactivation or recycling of reactants
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2251/00—Reactants
    • B01D2251/60—Inorganic bases or salts
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
    • Y02A50/00—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE in human health protection, e.g. against extreme weather
    • Y02A50/20—Air quality improvement or preservation, e.g. vehicle emission control or emission reduction by using catalytic converters

Definitions

  • the invention relates to a device and a process for removing nitric oxide in gas flow, and belongs to the technical field of air pollution control and environmental protection.
  • Nitrogen oxides (NO x ) harmful gases produced by human activities mainly include NO and NO 2 , of which a large part is produced by fuel combustion. Nitrogen oxides are toxic to the human body, and a large amount of nitrogen oxides emissions are one of the main reasons for atmospheric photochemical fog and acid rain. Generally, the concentration of nitrogen oxides in the flue gas produced by burning fossil fuels in thermal power plants and the like is about several hundred to several thousand ppm, of which more than 95% is nitrogen monoxide.
  • the inventor of the present invention has disclosed a method (CN111167263) of using ferric chloride slurry as a denitration absorbent to remove nitric oxide in gas flow.
  • the principle is to use solid ferric chloride in slurry and nitric oxide gas in gas flow to The chemical adsorption reaction occurs under certain conditions to obtain the corresponding coordination compound, which is removed from the gas stream.
  • the present invention proposes a device and process for removing nitrogen monoxide in gas stream by using the absorbent slurry.
  • the purpose of the present invention is to design and provide a technical solution for a device and process for removing nitric oxide in a gas stream.
  • a device for removing nitric oxide in gas flow is composed of a nitric oxide absorption system, an absorbent regeneration system and auxiliary systems such as related material conveying pipelines and control, wherein the nitric oxide absorption system is mainly composed of an absorption tower, a material storage system and other auxiliary systems.
  • the absorbent regeneration system is mainly composed of a regeneration reactor, a vacuum pump, an air compressor, a dehydration pump unit and a nitric oxide recovery pump.
  • the material storage tank is connected with the nitric oxide absorption tower through the material discharge pipe of the material storage tank, the material conveying pump, and the material inlet of the absorption tower, and the material outlet of the absorption tower is connected with the material storage tank through the circulating material inlet of the material storage tank.
  • the material outlet is connected with the regeneration reactor through the material inlet of the regeneration reactor, the regeneration reactor is connected with the material storage tank through the material outlet of the regeneration reactor and the new material inlet of the material storage tank, and the regeneration reactor is also connected with the vacuum pump, air compressor,
  • the nitric oxide recovery air pump is communicated with the dehydration air extraction unit.
  • the dehydration and air extraction unit is mainly composed of a liquid storage tank, a circulating water pump, a venturi tube and a condenser, and the regeneration reactor is also provided with an auxiliary material inlet.
  • the technological process of removing nitric oxide in the gas stream by using the above-mentioned device is to introduce the gas stream containing nitric oxide to be treated into the absorption tower from the gas inlet, and the absorbent slurry in the material storage tank is discharged through the material discharge pipe of the material storage tank and the material conveying pump.
  • the material inlet of the absorption tower is transported to the absorption tower, and the absorbent slurry droplets sprayed down by the nozzle after being atomized in the tower contact the air flow, and the nitric oxide in the air flow and the solid ferric chloride in the absorbent slurry
  • the crystals undergo a chemical reaction and are absorbed, the removed gas flow is discharged from the gas outlet at the upper part of the absorption tower, and the sprayed absorbent slurry is discharged through the material outlet of the absorption tower and then returned to the material storage tank through the material storage tank circulation material inlet for recycling; after the reaction
  • the absorbent to be regenerated is introduced into the regeneration reactor through the material outlet after the reaction in the material storage tank, the solenoid valve 1 and the material inlet of the regeneration reactor.
  • the absorbent slurry is introduced into the material storage tank through the material outlet of the regeneration reactor, the solenoid valve 2 and the new material inlet of the material storage tank, and the introduction method adopts the air compressor pneumatic conveying (It can also be conveyed by a material pump, etc.), and re-participate in the absorption reaction of nitric oxide to complete the regeneration cycle of the nitric oxide absorbent material.
  • the equipment and pipelines of the whole system are insulated, and the regeneration reactor is heated by jacket during dehydration; the liquid storage tank of the dehydration and air extraction unit is cooled by jacket, and the condenser is cooled by cooling water or chilled water;
  • the nitric oxide gas can be washed with water, dried and dehydrated (including freeze-drying and adsorption drying) to prepare high-purity nitric oxide gas, or it can be directly used as the primary raw material of chemical products to enter the next process.
  • the material storage tank of the present invention is also provided with a stirring motor and a stirrer, and the position of the liquid inlet of the material discharge pipe of the material storage tank is below the liquid level of the material slurry and a certain height above the bottom of the storage tank container, generally above 50mm at the bottom.
  • the liquid inlet can be set vertically and horizontally, and the effect is equivalent.
  • the blades of the agitator are immersed in the slurry and can usually be set below the liquid inlet of the material discharge pipe.
  • the material outlet is set above the liquid inlet position of the material storage tank material discharge pipe below the slurry level, and the distance between the two should be more than 50mm, preferably 150-300mm, to ensure that the storage tank There is always a certain amount of material for the material transfer pump to run continuously.
  • the stirrer is generally an electric stirrer, and can also be replaced by air bubbling, ultrasonic and magnetic stirring, etc., with equivalent effects.
  • the rotation frequency is generally 0 to 100 rpm, preferably 20 to 50 rpm, which can be rotated forward or reversed, depending on needs, without special requirements.
  • the rotation frequency is increased by 10 rpm, the content of solid ferric chloride crystals in the conveyed slurry can be increased by about 1-15%.
  • the rotation frequency exceeds 50 rpm, the material in the material storage tank is basically stirred evenly, and it has little effect on increasing the solid content of the slurry in the discharge pipe.
  • the agitator blades can be selected from a variety of blades or impellers such as radial flow or axial flow. For specific parameters, please refer to the relevant chemical equipment manuals.
  • the absorbent slurry is a supersaturated ferric chloride solution
  • the solid ferric chloride crystals in the slurry have a large difference in specific gravity between the solid and liquid materials of the solution, and the ferric chloride crystals are easily deposited at the bottom of the container.
  • the material can be brought to the upper part of the slurry mixture, and then discharged through the material discharge pipe and then introduced into the absorption tower.
  • the content of solid materials in the absorbent slurry in the material discharge pipe can be controlled by adjusting the rotational speed of the agitator (when mechanical stirring is used), so that the removal effect of nitric oxide in the absorption tower can be controlled according to the load of nitric oxide in different gas streams. , improve the utilization efficiency of materials, and also prevent the blockage of the material discharge pipe.
  • the structure of the regeneration reactor is basically the same as that of the material storage tank, and an electric stirrer is also used.
  • the regeneration reactor can use conventional bottom discharge, and the auxiliary material inlet can be added with clear water or hydrochloric acid solution as needed.
  • the tail gas is returned to the regeneration reactor to maintain the dehydration of the material in an acidic environment to ensure that the ferric chloride is not decomposed during dehydration, and the pH of the slurry is generally kept below 2 to 3.
  • the working temperature of the nitric oxide absorption tower of the present invention for absorbing nitric oxide is generally 30°C to 130°C, preferably 65°C to 110°C.
  • the temperature of the regeneration reactor during dehydration of the slurry is generally above 65°C, preferably 100-160°C, and generally maintained at 50-65°C in other stages, so that the materials in the reactor can be kept in a flowing state.
  • the working temperature of the material storage tank should be above 50°C, preferably 60-80°C.
  • the pipeline of the material conveying system can be insulated by electric heating belt or jacket, and the temperature is generally 50-80°C; the regeneration reactor or the jacket of the storage tank can be heated and insulated.
  • the dehydration and air extraction unit adopts hydrochloric acid or salt solution or a mixed solution of the two as the air extraction medium, which can simultaneously absorb the moisture in the pumped gas and avoid absorbing hydrogen chloride gas in the air flow.
  • the salts are mainly chlorides or bromides of alkali metals or alkaline earth metals, preferably salts with good hygroscopicity and salting-out effect, such as lithium chloride, magnesium chloride, calcium chloride or lithium bromide and their mixed solutions, with a general concentration.
  • the salt solution concentration is high, and the corresponding saturated water vapor pressure is low at the same temperature, which is more conducive to material dehydration, and the salt solution can also be a saturated solution or a supersaturated solution.
  • hydrochloric acid solution as the pumping medium
  • the concentration of hydrochloric acid is generally above 5%, preferably 15-20%.
  • One of the advantages of using a mixed solution of hydrochloric acid and salt as the pumping medium is that the equilibrium concentration of hydrochloric acid in the solution is low, and it is not easy to absorb hydrogen chloride gas in the gas.
  • the liquid storage tank and the condenser are cooled by cooling water or chilled water during dehydration work.
  • the temperature is generally below 45 °C, and the condenser can be lower, preferably 0 °C to 15 °C.
  • heating or decompression
  • the heating and dehydration temperature is generally above 65°C, preferably 90°C to 110°C. Specific can be selected according to different media. When a hydrochloric acid solution is used, the concentration of hydrochloric acid after dehydration can reach 20%.
  • material storage tanks, regeneration reactors and related material conveying pipelines are equipped with slurry density sensors (vibration tuning fork type, gamma ray and ultrasonic density meters can be used) and temperature sensors to obtain relevant material density, temperature and other parameters.
  • Electromagnetic flowmeter can be used for medium slurry flow.
  • the density of the slurry material can also be obtained after manual sampling, and then related operations are carried out, and the effect is equivalent.
  • the liquid level in the material storage tank can be measured and controlled by ultrasonic or radar or float level gauge to keep the slurry level in the material storage tank within a certain range.
  • the system process can adopt PLC control system and work according to the absorption-regeneration-absorption cycle procedure, and the valves of the pipeline system are all normally closed solenoid valves.
  • the main technological processes are:
  • Start-up stage add the required amount of ferric chloride slurry to the material storage tank, start stirring to mix the materials evenly, the density (average) of the slurry material in the storage tank is generally above 2.1 (g/cm 3 , the same below) (including The amount of solid ferric chloride crystals is about 20% or more, specifically related to the temperature and the content of hydrogen chloride in the slurry, etc.), and the start-up stage is completed.
  • Absorption working stage start the material transfer pump absorption tower to work, at this stage, according to the concentration of nitric oxide in the air stream to be treated, the speed of the stirring motor of the material storage tank can be adjusted to increase or decrease the supply of effective solid components in the circulating slurry; when The density of the slurry material in the storage tank is about 1.7 or less (the solid content is about 5% or less, which can be set as needed) or when the nitric oxide concentration at the outlet of the absorption tower rises to a predetermined value, the absorption reaction is completed, and the absorbent is regenerated. stage.
  • the present invention consists of a nitric oxide absorption system, an absorbent regeneration system and auxiliary systems such as related material conveying pipeline valves and control systems.
  • the absorbent is recycled after regeneration, and the structure of the material storage tank can be controlled.
  • the material dehydration in the regeneration reactor adopts a dehydration vacuum pumping unit with hydrochloric acid or salt solution or a mixed solution of the two as the medium,
  • the tail gas containing hydrogen chloride is returned to the regeneration reactor to avoid the hydrolysis of ferric chloride, and the device and process are simple and reliable.
  • Figure 1 is a flow diagram of a device and process flow diagram for removing nitric oxide in a gas stream.
  • Figure 2 is a schematic diagram of the internal structure of a material storage tank.
  • Example 1 A device and process flow for removing nitric oxide in a gas stream is shown in FIG. 1 . It consists of auxiliary systems such as absorption tower 101, material storage tank 102, regeneration reactor 103, liquid storage tank 104 and related material conveying pipeline valves.
  • auxiliary systems such as absorption tower 101, material storage tank 102, regeneration reactor 103, liquid storage tank 104 and related material conveying pipeline valves.
  • the material storage tank 102 is communicated with the absorption tower 101 through the material storage tank material discharge pipe 7, the material conveying pump 4 and the absorption tower material inlet 3, and the absorption tower material outlet 5 is communicated with the material storage tank 102 through the material storage tank circulating material inlet 6,
  • the material outlet 8 is communicated with the regeneration reactor 103 through the solenoid valve 1 and the material inlet 12 of the regeneration reactor; the bottom of the regeneration reactor 103 is connected to the new material through the material storage tank through the material outlet 10 of the regeneration reactor and the solenoid valve 2.
  • the inlet 9 is communicated with the upper part of the material storage tank 102, and the upper part of the regeneration reactor 103 is connected with the nitric oxide recovery pump 22 through the solenoid valve 9 through the gas discharge port 13 of the regeneration reactor, and the other way through the solenoid valve 8, Venturi
  • the suction pipe 21 and the liquid storage tank gas-liquid mixture inlet 20 are communicated with the liquid storage tank 104, and the liquid storage tank liquid outlet 16 at the lower part of the liquid storage tank 104 is communicated with the venturi suction pipe 21 through the liquid circulation pump 17, and the liquid storage tank gas
  • the outlet 19 is communicated with the regeneration reactor 103 through the condenser 18 and the solenoid valve 4, and the lower end of the condenser 18 is also provided with a liquid discharge solenoid valve 7;
  • the upper part of the regeneration reactor 103 is connected to the vacuum pump 14 and
  • the air compressor 15 is connected, and the nitric oxide absorption tower 101 is also provided with a gas inlet 1 and a gas outlet 2; the
  • the absorption tower is an empty tower, made of glass fiber reinforced plastic, the tower diameter is ⁇ 300mm, the total tower height is about 3000mm, and the effective spray height is about 1500mm.
  • the internal structure of the material storage tank is shown in Figure 2.
  • the material storage tank is a glass-lined reactor with a diameter of ⁇ 450mm and an effective volume of about 120L. It is provided with a stirrer motor 23 and a stirring paddle 24.
  • the stirrer is arranged with double paddles and a single paddle.
  • the blades are about 30mm high and 60mm long and arranged symmetrically.
  • the height of the liquid inlet of the material discharge pipe 7 of the material storage tank is about 200mm from the bottom.
  • the density of the material in the storage tank is detected by a tuning fork type density meter, which is installed about 150mm below the liquid surface.
  • the structure and size of the regeneration reactor 103 is roughly the same as that of the material storage tank, and the material is discharged from the bottom, and the electric stirrer is used.
  • the pipelines of the whole system are insulated with a temperature of 55-65°C.
  • the regeneration reactor 103 is dehydrated by jacket heating and the temperature is 100-150°C.
  • the liquid medium of the dehydration and air extraction unit is a mixed solution of hydrochloric acid and lithium chloride (hydrochloric acid 15 %, lithium chloride 45%), the addition amount is about 200kg, the liquid storage tank 104 of the dehydration and air extraction unit is cooled by cooling water, the temperature is 35 ⁇ 45 °C, and the condenser 18 is cooled by 0 ⁇ 7 °C of cooling water.
  • the removal process is to introduce the gas stream containing nitric oxide to be treated into the absorption tower 101 from the gas inlet 1, and the absorbent slurry in the material storage tank 102 is discharged through the material storage tank material discharge pipe outlet 7, material delivery pump 4, absorption
  • the tower material inlet 3 is transported into the absorption tower, and the absorbent slurry droplets sprayed down after being atomized by the atomizing nozzle in the tower are fully contacted with the air flow, and the nitric oxide in the air flow and the chlorination in the absorbent slurry are fully contacted.
  • the iron is absorbed by chemical reaction, the removed air flow is discharged from the gas outlet 2 at the upper part of the absorption tower, and the reacted absorbent slurry is returned to the material storage tank 102 through the material outlet 5 of the absorption tower through the material storage tank circulating material inlet 6 and returned to the material storage tank 102 for recycling;
  • the absorbent to be regenerated later is introduced into the regeneration reactor 103 through the material outlet 8, the valve 1 and the material inlet 12 of the regeneration reactor after the reaction in the material storage tank.
  • a certain amount of hydrochloric acid solution added in the regeneration reactor 103 is fully mixed with the absorbent material and the absorbed nitrous oxide gas is released, which is pumped out through the regeneration reactor gas outlet 13 and solenoid valve 9 through the nitric oxide recovery pump 22
  • the absorbent slurry after removing the absorbed nitric oxide passes through the gas discharge port 13 of the regeneration reactor, the solenoid valve 8 passes through the Venturi suction pipe 21, the liquid storage tank 104, the liquid circulation pump 17 and the condenser
  • the dehydration and extraction unit composed of 18 reduces steam and dehydration, and the exhaust gas containing hydrogen chloride is returned to the regeneration reactor 103 through the solenoid valve 4 to maintain the content of hydrogen chloride in the absorbent.
  • the absorbent slurry is introduced into the material storage tank 102 through the material outlet 10 of the regeneration reactor, the solenoid valve 2 and the new material inlet 9 of the material storage tank to participate in the absorption reaction of nitric oxide again,
  • the nitric oxide absorbent material regeneration cycle is completed, and the introduction method adopts the form of pressure feeding by the air compressor 15 .
  • the initial absorbent is supersaturated ferric chloride slurry, the water content is about 7-8%, the hydrochloric acid is about 3%, and the temperature of the material storage tank is 65-75°C.
  • the material delivery pump adopts a tetrafluoro diaphragm pump, the diameter of the pump suction port is 40mm, the diameter of the discharge port is 32mm, and the pump circulation volume is about 350kg/h.
  • the auxiliary material inlet of the regeneration reactor is charged with a concentration of 20% hydrochloric acid solution, and the addition amount is about 5% of the material amount; the dehydration temperature of the regeneration reactor is 120-150 °C, and the gas flow temperature in the absorption tower is about 80-90 °C.
  • the flow rate of the treated gas is about 150m 3 /h
  • the NO concentration in the gas inlet gas flow is about 500ppm
  • the sulfur dioxide concentration is about 500ppm
  • the oxygen is about 8% (volume, the same below)
  • the moisture content is about 10%
  • the carbon dioxide content is about 10%. %
  • the rest is nitrogen
  • the effective residence time of the gas in the reactor is about 1-2s
  • the average removal rate of nitric oxide is about 85%.
  • Start-up stage add about 250kg of ferric chloride slurry to the material storage tank 102, wherein the water content is about 7-8%, start the stirring motor (the rotation speed is about 50-60 rpm, and remains unchanged) to make the material Mix evenly, and the measured density of the material in the material storage tank 102 is 2.2-2.3 (the solid content is about 20-30%).
  • Absorption working stage start the material conveying pump and start the absorption tower 101.
  • the density of the slurry in the material storage tank 102 or the conveying pipeline is reduced to 1.7-1.8 (solid content of about 3-5%) or the removal rate of nitric oxide is lower than 50 %, enter the absorbent regeneration stage.
  • Embodiment 2 other conditions are the same as in embodiment 1, and the change in the rotational speed of the material storage tank agitator changes the solid material content in the material storage tank discharge pipe (respectively using a tuning fork type density meter and sampling to detect and check) and the nitric oxide removal rate.
  • the effects are shown in Tables 1 and 2 below, respectively.
  • Table 1 The relationship between the speed of the agitator and the content of the solid material in the discharge pipe of the material storage tank (when there is no absorption)

Abstract

一种气流中氮氧化物的去除装置和工艺，属于大气污染控制和环境保护技术领域,所述的装置由吸收塔、物料储罐、再生反应器、脱水抽气机组和相关物料输送管路及阀门组成，其中氮氧化物吸收塔的功能是采用氯化铁吸收剂浆液吸收去除气流中的一氧化氮气体，再生反应器的功能是脱除吸收剂浆液中被吸收的一氧化氮和吸收剂浆液再生，脱水抽气机组的作用是给再生反应器吸收剂脱水，物料储罐的功能是提供吸收剂浆液给吸收塔工作。

Description

一种气流中一氧化氮的去除装置和工艺 技术领域
本发明涉及一种气流中一氧化氮的去除装置和工艺，属于大气污染控制和环境保护技术领域。
背景技术
人类活动产生的氮氧化物(NO x)有害气体，主要包括NO和NO 2，其中由燃料燃烧产生的占很大部分。氮氧化物对人体有致毒作用，大量的氮氧化物排放还是引起大气光化学雾和酸雨的主要原因之一。一般地，火力发电厂等以化石燃料燃烧产生的烟气中的氮氧化物浓度约为几百到几千ppm，其中约95％以上是一氧化氮。
本发明的发明人已公开了采用氯化铁浆液作为脱硝吸收剂去除气流中的一氧化氮的方法(CN111167263)，其原理是利用浆液中的固体氯化铁与气流中的一氧化氮气体在一定条件下发生的化学吸附反应，得到相应的配位化合物，从而从气流中得到去除。本发明在上述发明的基础上，提出了采用所述的吸收剂浆液去除气流中一氧化氮的去除装置和工艺。
发明内容
针对现有技术存在的问题，本发明的目的在于设计提供一种气流中一氧化氮的去除装置和工艺的技术发方案。
本发明具体通过以下技术方案实现：
一种气流中一氧化氮的去除装置，该装置由一氧化氮吸收系统、吸收剂再生系统和相关物料输送管路和控制等辅助系统组成，其中一氧化氮吸收系统主要由吸收塔、物料储罐和物料输送泵组成，吸收剂再生系统主要由再生反应器、真空抽气泵、空气压缩机、脱水抽气机组和一氧化氮回收抽气泵等组成。
其中物料储罐经物料储罐物料排出管、物料输送泵、吸收塔物料进口与一氧化氮吸收塔连通，吸收塔物料出口经物料储罐循环物料进口与物料储罐连通，物料储罐反应后物料出口经再生反应器物料进口与再生反应器连通，再生反应器经再生反应器物料出口和物料储罐新物料进口与物料储罐连通，再生反应器还分别与真空抽气泵、空气压缩机、一氧化氮回收抽气泵和脱水抽气机组连通。所述脱水抽气机组主要由液体储罐、循环水泵、文丘里管和冷凝器组成，所述的再生反应器还设置有辅料加入口。
利用上述装置去除气流中一氧化氮的工艺流程是把待处理的含一氧化氮的气流由气体进口导入吸收塔，物料储罐中的吸收剂浆液由经物料储罐物料排出管、物料输送泵、吸收塔物料 进口输送到吸收塔内，在塔内经喷头雾化后喷淋下来的吸收剂浆液液滴与所述的气流接触，气流中的一氧化氮与吸收剂浆液中的固体氯化铁晶体发生化学反应而被吸收，去除后的气流从吸收塔上部气体出口排出，喷淋下来的吸收剂浆液通过吸收塔物料出口排出后经物料储罐循环物料进口返回物料储罐循环使用；反应后需再生的吸收剂通过物料储罐反应后物料出口、电磁阀①和再生反应器物料进口导入再生反应器，所述导入的方式采用真空抽气泵抽料(也可采用物料泵输送等形式，效果相同)，然后通过辅料加入口向再生反应器内加入的一定量的水或盐酸溶液与吸收剂物料充分混合，使浆液稀释并释放出被吸收的一氧化氮气体，并通过再生反应器气体排出口、电磁阀⑨经一氧化氮回收抽气泵抽出后进一步回收利用；脱除被吸收的一氧化氮一氧化氮后的吸收剂浆液经再生反应器气体排出口、电磁阀⑧经由文丘里吸气管、液体储罐、液体循环泵和冷凝器组成的脱水抽气机组脱除水分，含氯化氢的尾气经电磁阀④返回再生反应器，冷凝器下端设置有放液电磁阀⑦定期排放被脱除的水分；再生反应器内的吸收剂再生完毕后，吸收剂浆液经再生反应器物料出口、电磁阀②和物料储罐新物料进口导入物料储罐，所述导入的方式采用空气压缩机气压输送(也可采用物料泵输送等形式)，从新参与一氧化氮的吸收反应，完成一氧化氮吸收剂物料的再生循环。全系统设备和管道均保温，再生反应器脱水时采用夹套加热；脱水抽气机组的液体储罐采用夹套冷却，冷凝器采用冷却水或冷冻水冷却；通过一氧化氮回收抽气泵抽出后的一氧化氮气体可通过水洗、干燥脱水(包括冷冻干燥和吸附干燥)等过程制备高纯度的一氧化氮气体，也可直接作为化工产品的初级原料进入下一道工序。
进一步，本发明的物料储罐中还设置有搅拌电机和搅拌器，物料储罐物料排出管的进液口位置在物料浆液液面以下并高出储罐容器底部一定高度，一般在底部50mm以上，进液口垂直和水平方向设置均可，效果相当。搅拌器的叶片浸没在浆液中，通常可设置在物料排出管进液口位置以下。所述物料储罐的物料储罐反应后物料出口设置在浆液液面以下物料储罐物料排出管的进液口位置的上方，两者距离应在50mm以上，优选150～300mm，以保证储罐始终存有一定量的物料供物料输送泵连续运行。
进一步，搅拌器一般为电动搅拌器，也可以由气流鼓泡、超声和磁力搅拌等替代，效果相当。采用电动搅拌器时，旋转频率一般为0～100转/分，优选20～50转/分，可正转也可反转，具体根据需要而定，无特殊要求。每提高旋转频率10转/分，可提高被输送浆液中固体氯化铁晶体含量约1～15％，随转速进一步提高，含量提高率减少。当旋转频率超过50转/分时，物料储罐内物料基本搅拌均匀，对增加排出管中浆液固体物料含量的效果不大。搅拌器叶片可选用径流或轴流式等多种叶片或叶轮，具体参数可参看相关的化工设备手册。
由于吸收剂浆液为过饱和氯化铁溶液，浆液中固体氯化铁晶体和溶液的固液物料比重差距大，氯化铁晶体容易沉积在容器底部，本发明通过采用搅拌方法使得沉积底部的固体物料能被 带到浆液混合物的上部，再通过物料排出管排出后导入吸收塔。可通过调节搅拌器的转速(采用机械搅拌时)来控制物料排出管吸收剂浆液中固体物料的含量，从而可实现针对不同气流中一氧化氮的负荷，控制吸收塔内一氧化氮的去除效果，提高物料的利用效率，同时也可以防止物料排出管堵塞。
进一步，再生反应器结构和物料储罐大体相同，也采用电动搅拌器。再生反应器可采用常规底部出料，辅料加入口视需要加入清水或盐酸溶液，加入量约为物料输送量的3％或以上，优选5～10％；再生反应器内浆液脱水时含氯化氢的尾气返回再生反应器，以维持物料在酸性环境下脱水，以保证氯化铁脱水时不分解，一般使浆液的pH保持在2～3以下。
进一步，本发明一氧化氮吸收塔的工作温度吸收一氧化氮的工作温度一般为30℃～130℃，优选65℃～110℃。再生反应器温度在浆液脱水时的温度为一般65℃以上，优选100～160℃，其他阶段一般维持在50～65℃，使反应器内物料保持流动状态即可。物料储罐工作温度应在50℃以上，优选60～80℃。物料输送系统管路可采用电热带或夹套保温，温度一般为50～80℃；再生反应器或储罐夹套加热保温。
进一步，本脱水抽气机组采用盐酸或盐溶液或两者混合液溶液作为抽气介质，可以同时起到既可吸收被抽气体中的水分，又可避免吸收气流中的氯化氢气体的作用。所述盐主要为碱金属或碱土金属的氯化物或溴化物，优选具有较好吸湿性和盐析效应的盐类，如氯化锂、氯化镁、氯化钙或溴化锂及其混合溶液，浓度一般为10％以上，优选40～60％，盐溶液浓度高，在相同温度下相应的饱和水蒸气压就低，更有利于物料脱水，所述的盐溶液也可以是饱和溶液或过饱和溶液。采用盐酸溶液作为抽气介质时，盐酸浓度一般为5％以上，优选15～20％。采用盐酸和盐的混合液溶液作为抽气介质的好处之一是溶液里盐酸的平衡浓度低，不易吸收气体中的氯化氢气体。液体储罐和冷凝器脱水工作时采用冷却水或冷冻水冷却，温度一般为45℃以下，冷凝器可低一些，优选0℃～15℃。液体储罐盐溶液吸收饱和后可采用加热(或减压)脱水再生，加热脱水温度一般为65℃以上，优选90℃～110℃。具体可根据介质不同选定。采用盐酸溶液时，脱水后盐酸浓度达到20％即可。
进一步，物料储罐、再生反应器和相关物料输送管道内均装有浆液密度传感器(可采用振动音叉式、γ射线和超声波等密度计)和温度传感器以获得相关物料密度、温度等参数，管道中浆液流量可采用电磁流量计。浆液物料的密度也可以人工取样后检测获得，再进行相关操作，效果相当。物料储罐内液面高度液可通过超声波或雷达或浮球式液位计来测量和控制进料量，以保持物料储罐内浆液液位在一定范围内。系统工艺可采用PLC控制系统，按照吸收－再生－吸收循环程序工作，管路系统阀门均采用常闭电磁阀。主要工艺过程有：
启动阶段：向物料储罐加入所需量的氯化铁浆液，启动搅拌使物料混合均匀，在储罐内的 浆液物料密度(平均)一般为2.1(g/cm 3，下同)以上(含固体氯化铁晶体量约为20％以上，具体与温度和浆液中氯化氢含量等有关)，启动阶段完成。
吸收工作阶段：启动物料输送泵吸收塔工作，在此阶段根据被处理气流中一氧化氮浓度大小，可调节物料储罐搅拌电机的转速以增加或减少循环浆液中的有效固体成分的供给；当储罐内的浆液物料密度约为1.7以下(含固量约在5％以下，具体可视需要设定)或吸收塔出口一氧化氮浓度上升到预定值时，吸收反应完毕，进入吸收剂再生阶段。
吸收剂再生阶段：
(a)真空抽气泵工作，电磁阀①⑤打开，回收物料到再生反应器。当物料储罐和再生反应器压差计为零时，真空抽气泵停，投料完毕，关闭真空泵和电磁阀①⑤。
(b)开启辅料加入口电磁阀③加入定量的水或稀盐酸溶液，加完关闭。
(c)开启再生反应器搅拌器、电磁阀⑨和一氧化氮回收抽气泵抽出一氧化氮气体，按预定时间抽气，抽气完成后关闭电磁阀⑨和一氧化氮回收抽气泵。
(d)脱水过程，开启电磁阀⑧、液体循环泵和电磁阀④，开启加热器把再生反应器从50～65℃加热到100～150℃，当安装在再生反应器内的浆液密度传感器获得的物料密度参数(或人工取样后检测)，约为2.2～2.5(含固量约25％以上，具体可视需要设定)达到预定要求时再生完毕，关闭电磁阀⑧、液体循环泵和电磁阀④，开启空气压缩机和电磁阀②把再生后的物料导入物料储罐，当物料储罐和再生反应器压差计为零时，空压机停，投料完毕，空气压缩机和电磁阀②关闭，重新进入吸收工作阶段。
脱水真空抽气机组的液体储罐内的盐溶液含水过多后可定期采用加热(或减压)脱除部分水，加热脱水温度一般为65℃以上，优选85℃～110℃，脱水量由设置在液体储罐的液位计控制。所述冷凝器下端设置有放液电磁阀⑦定期排放被脱除的水分，通过液位计控制自动排液。
实际使用时，再生反应器可多台并联交替工作。
与现有技术相比，本发明由一氧化氮吸收系统、吸收剂再生系统和相关物料输送管路阀门和控制系统等辅助系统组成，吸收剂经再生后循环利用，物料储罐的结构能控制和调节物料排出管中吸收剂浆液中有效固体物料的含量，从而提高物料的利用效率，再生反应器内物料脱水采用以盐酸或盐溶液或两者混合液溶液为介质的脱水真空抽气机组，含氯化氢的尾气返回再生反应器，避免了氯化铁的水解，装置和工艺简单可靠。
附图说明
图1是一种气流中一氧化氮的去除装置和工艺流程图。
图2是一种物料储罐内部结构示意图。
图中：101吸收塔；102物料储罐；103再生反应器；104液体储罐；1气体进口；2气体 出口；3吸收塔物料进口；4物料输送泵；5吸收塔物料出口；6物料储罐循环物料进口；7物料储罐物料排出管；8物料储罐反应后物料出口；9物料储罐新物料进口；10再生反应器物料出口；11辅料加入口；12再生反应器物料进口；13再生反应器气体排出口；14真空抽气泵；15空气压缩机；16液体储罐液体出口；17液体循环泵；18冷凝器；19液体储罐气体出口；20液体储罐气液混合物进口；21文丘里吸气管；22一氧化氮回收抽气泵；23搅拌电机；24搅拌器；①～⑨为电磁阀。
具体实施方式
以下结合附图和实施例对本发明作进一步详细描述。
实施例1：一种气流中一氧化氮的去除装置和工艺流程如图1所示。包括吸收塔101、物料储罐102、再生反应器103、液体储罐104和相关物料输送管路阀门等辅助系统组成。其中物料储罐102经物料储罐物料排出管7、物料输送泵4、吸收塔物料进口3与吸收塔101连通，吸收塔物料出口5经物料储罐循环物料进口6与物料储罐102连通，物料储罐反应后物料出口8经电磁阀①和再生反应器物料进口12与再生反应器103连通；再生反应器103的底部经再生反应器物料出口10和电磁阀②与经物料储罐新物料进口9与物料储罐102上部连通，再生反应器103的上部经再生反应器气体排出口13后，一路经电磁阀⑨与一氧化氮回收抽气泵22连通，另一路经电磁阀⑧、文丘里吸气管21和液体储罐气液混合物进口20与液体储罐104连通，液体储罐104下部的液体储罐液体出口16经液体循环泵17与文丘里吸气管21连通，液体储罐气体出口19经冷凝器18和电磁阀④与再生反应器103连通，冷凝器18下端还设置有放液电磁阀⑦；再生反应器103的上部经管道和阀门⑤和⑥分别与真空抽气泵14和空气压缩机15连通，一氧化氮吸收塔101还设置有气体进口1、气体出口2；再生反应器103还设置有辅料加入口11和辅料加入量控制电磁阀③，物料储罐和再生反应器内均设有搅拌器。所述的电磁阀为常闭，也可以是手动阀或气动阀等替代。
所述吸收塔为空塔，材质为玻璃钢，塔径为Φ300mm，塔总高度约3000mm，有效喷淋高度约1500mm。物料储罐内部结构如图2所示，物料储罐直径为Φ450mm，有效容积约为120L的搪玻璃反应釜，设置有搅拌器电机23和搅拌浆24，搅拌器为双桨布置，单个桨叶叶片高约30mm，长约60mm，对称布置。物料储罐物料排出管7的进液口位置距离底部高度约为200mm，物料储罐反应后物料出口8设置在物料储罐物料排出管7的进液口位置的上方约100mm处。储罐内物料密度采用音叉式密度计检测，安装在液面下约150mm处。再生反应器103结构尺寸与物料储罐大体相同，底部出料，电动搅拌器。全系统管道均采用保温，温度为55～65℃，再生反应器103脱水时采用夹套加热，温度为100～150℃，脱水抽气机组的液体介质采用盐酸和氯化锂混合溶液(盐酸15％，氯化锂45％)，加入量约200kg，脱水抽气机组液体储罐104采用冷却水 冷却，温度35～45℃，冷凝器18采用0～7℃冷却水冷却。
其去除工艺流程是把待处理的含一氧化氮的气流由气体进口1导入吸收塔101，物料储罐102中的吸收剂浆液由经物料储罐物料排出管出口7、物料输送泵4、吸收塔物料进口3输送到吸收塔内，在塔内经雾化喷头雾化后喷淋下来的吸收剂浆液液滴与所述的气流充分接触，气流中的一氧化氮与吸收剂浆液中的氯化铁发生化学反应而被吸收，去除后的气流从吸收塔上部气体出口2排出，反应后的吸收剂浆液通过吸收塔物料出口5经物料储罐循环物料进口6返回物料储罐102循环使用；反应后需再生的吸收剂通过物料储罐反应后物料出口8、阀门①和再生反应器物料进口12导入再生反应器103，导入的方式采用真空抽气泵14抽料形式，然后通过辅料加入口11向再生反应器103内加入的一定量的盐酸溶液与吸收剂物料充分混合并释放出被吸收的一氧化氮气体，通过再生反应器气体排出口13、电磁阀⑨经一氧化氮回收抽气泵22抽出后进一步回收处理；脱除被吸收的一氧化氮后的吸收剂浆液经再生反应器气体排出口13、电磁阀⑧经由文丘里吸气管21、液体储罐104、液体循环泵17和冷凝器18组成的脱水抽气机组减蒸脱水，含氯化氢的尾气经电磁阀④返回再生反应器103以维持吸收剂中氯化氢的含量，冷凝器18下端设置有放液电磁阀⑦定期排放被脱除的水分；再生反应器103内的吸收剂再生完毕后，吸收剂浆液经再生反应器物料出口10、电磁阀②和物料储罐新物料进口9导入物料储罐102重新参与一氧化氮的吸收反应，完成一氧化氮吸收剂物料再生循环，所述导入的方式采用空气压缩机15压力送料形式。
初始吸收剂为过饱和氯化铁浆液，含水量约7～8％，盐酸约3％，物料储罐温度为65～75℃。物料输送泵采用四氟隔膜泵，泵吸入口管道直径为40mm，排出口直径为32mm，泵循环量约350kg/h。再生反应器的辅料加入口加入浓度为20％盐酸溶液，加入量约为物料量的5％；再生反应器脱水温度为120～150℃，吸收塔内气流温度约为80～90℃。
被处理气体流量约150m 3/h，气体进口气流中NO浓度约为500ppm，二氧化硫浓度约为500ppm，氧气为约8％(体积，下同)，水分含量约为10％，二氧化碳含量约为10％，其余为氮气，气体在反应器内有效停留时间约为1～2s，一氧化氮平均去除率约为85％。具体处理工艺如下：
启动阶段：向物料储罐102加入氯化铁浆液质量约为250kg，其中含水量约为7～8％，启动搅拌电机(转速约为50～60转/min，并保持不变)，使物料混合均匀，测得物料储罐102内物料密度为2.2～2.3(含固量约20～30％)。
吸收工作阶段：启动物料输送泵启动吸收塔101工作，当物料储罐102或输送管道内的浆液密度降低到1.7～1.8(含固量约3～5％)或一氧化氮去除率低于50％时，进入吸收剂再生阶段。
吸收剂再生阶段：
(a)真空抽气泵(2.2kW)工作，电磁阀①⑤打开，回收物料到再生反应器103。当物料储罐和再生反应器压差计为零时，投料完毕，关闭真空抽气泵和电磁阀①⑤；
(b)开启辅料加入口电磁阀③加入所预定量稀盐酸溶液，加完关闭电磁阀③；
(c)开启再生反应器搅拌器(转速约为50转/min，并保持不变)、电磁阀⑨和一氧化氮回收抽气泵22(2.2kW)抽出释放的一氧化氮气体，抽气约10～15分钟后一氧化氮气体释放完毕，抽气完成，关闭电磁阀⑨和一氧化氮回收抽气泵22；
(d)脱水过程，开启电磁阀⑧、液体循环泵17和电磁阀④，开启加热器把再生反应器加热到120～150℃，当测得再生反应器内的浆液密度为2.3～2.4时再生完毕，关闭电磁阀⑧、液体循环泵17和电磁阀④，开启空气压缩机15(3kW)和电磁阀②把再生后的物料压入物料储罐102，当物料储罐和再生反应器压差计为零时投料完毕，关闭空气压缩机15和电磁阀②，重新进行吸收工作阶段。
实施例2：其他条件与实施例1相同，物料储罐搅拌器转速变化对物料储罐排出管中固体物料含量变化(分别采用音叉式密度计和取样检测校核)和一氧化氮去除率的影响分别见下表1和2表示。
表1搅拌器转速与物料储罐排出管中固体物料含量变化关系(无吸收时)
Figure PCTCN2021137805-appb-000001
表2搅拌器转速与一氧化氮去除率关系(新鲜物料1小时平均)
Figure PCTCN2021137805-appb-000002
以上实施例仅用于说明本发明的技术方案，对于本领域的技术人员来说，凡在本发明的精神和原则之内，对各实施例所记载的技术方案进行修改，或者对其中的部分技术特征进行任何等同替换、修改、变化和改进等，均应包含在本发明的保护范围之内。

Claims (10)

  1. 一种气流中一氧化氮的去除装置，其特征在于所述的装置由吸收塔(101)、物料储罐(102)、再生反应器(103)、液体储罐(104)和相关物料输送管路及阀门组成，其中物料储罐(102)经物料储罐物料排出管(7)、物料输送泵(4)、吸收塔物料进口(3)与吸收塔(101)连通，吸收塔物料出口(5)经物料储罐循环物料进口(6)与物料储罐(102)连通，物料储罐反应后物料出口(8)经电磁阀①和再生反应器物料进口(12)与再生反应器(103)连通，再生反应器(103)的底部经再生反应器物料出口(10)和电磁阀②与经物料储罐新物料进口(9)与物料储罐(102)上部连通，再生反应器(103)的上部经再生反应器气体排出口(13)后，一路经电磁阀⑨与一氧化氮回收抽气泵(22)连通，另一路经电磁阀⑧、文丘里吸气管(21)和液体储罐气液混合物进口(20)与液体储罐(104)连通，液体储罐(104)下部的液体储罐液体出口(16)经液体循环泵(17)与文丘里吸气管(21)连通，液体储罐气体出口(19)经冷凝器(18)和电磁阀④与再生反应器(103)连通，冷凝器(18)下端还设置有放液电磁阀⑦，再生反应器(103)的上部经管道和阀门⑤和⑥分别与真空抽气泵(14)和空气压缩机(15)连通，吸收塔(101)还设置有气体进口(1)和气体出口(2)，再生反应器(103)还设置有辅料加入口(11)和辅料加入量控制电磁阀③，物料储罐和再生反应器内均设有搅拌器。
  2. 根据权利要求1所述一种气流中一氧化氮的去除装置,其特征在于所述的物料储罐(102)中设置有搅拌电机(23)和搅拌器(24)，物料储罐物料排出管(7)的进液口位置在物料浆液液面以下并高出容器底部，所述的物料储罐(102)反应后物料出口设置在浆液液面以下物料储罐物料排出管(7)的进液口位置的上方。
  3. 根据权利要求2所述的物料储罐,其特征在于所述的物料储罐物料排出管(7)的进液口高度在容器高出底部50mm以上，所述的物料储罐(102)反应后物料出口(8)在物料储罐物料排出管(7)的进液口位置的上方50mm以上。
  4. 根据权利要求2所述一种物料储罐,其特征在于所述的搅拌器的旋转频率为0～100转/分。
  5. 根据权利要求1所述一种气流中一氧化氮的去除装置,其特征在于所述的再生反应器(103)、物料储罐(102)和物料储罐物料排出管(7)内均装有浆液密度传感器和温度传感器，所述的吸收塔(101)工作时物料储罐(102)内的浆液物料密度为2.1～2.5g/cm 3，固体氯化铁含量10％以上，物料储罐(102)工作温度在50℃以上，再生反应器(103)温度在浆液脱水时的温度为65℃以上。
  6. 根据权利要求1所述的一种气流中一氧化氮的去除装置,其特征在于所述的再生反应器(103)吸收剂浆液的脱水抽气机组是由液体储罐(104)、液体循环泵(17)、文丘里吸气管(21) 和冷凝器(18)组成，所述的脱水抽气机组的液体采用盐酸或盐溶液或两者混合液溶液作为抽气介质，所述的盐为碱金属或碱土金属的氯化物或溴化物，包括氯化锂、氯化镁、氯化钙或溴化锂及其混合溶液。
  7. 根据权利要求6所述的一种气流中一氧化氮的去除装置，其特征在于所述的抽气介质盐酸溶液浓度为5％及以上，盐溶液浓度为10％及以上。
  8. 一种利用权利要求1所述的装置去除气流中一氧化氮的工艺，其特征在于把待处理的含一氧化氮的气流由吸收塔(101)的气体进口(1)导入吸收塔(101)，物料储罐(102)中的吸收剂浆液由经物料储罐物料排出管(7)、物料输送泵(4)、吸收塔物料进口(3)输送到吸收塔(101)内，在塔内经喷头雾化后喷淋下来的吸收剂浆液液滴与所述的气流接触，气流中的一氧化氮与吸收剂浆液中的氯化铁发生化学反应而被吸收，去除后的气流从吸收塔(101)上部气体出口(2)排出，喷淋下来的吸收剂浆液通过吸收塔物料出口(5)排出经物料储罐循环物料进口(6)返回物料储罐(102)循环使用，反应后需再生的吸收剂通过物料储罐反应后物料出口(8)、阀门①和再生反应器物料进口(12)导入再生反应器(103)，所述的导入方式采用真空抽气泵(14)抽料，然后通过辅料加入口(11)向再生反应器(103)内定量加入水或盐酸溶液与吸收剂物料充分混合，释放出被吸收的一氧化氮气体，并通过再生反应器气体排出口(13)、电磁阀⑨经一氧化氮回收抽气泵(22)抽出后进一步回收利用，脱除被吸收的一氧化氮后的吸收剂浆液通过再生反应器气体排出口(13)、电磁阀⑧经由文丘里吸气管(21)、液体储罐(104)、液体循环泵(17)和冷凝器(18)组成的脱水抽气机组脱除水分，尾气经电磁阀④返回再生反应器(103)，冷凝器(18)下端设置有放液电磁阀⑦定期排放被脱除的水分，再生反应器(103)内的吸收剂再生完毕后，吸收剂浆液经再生反应器物料出口(10)、电磁阀②和物料储罐新物料进口(9)导入物料储罐(102)，所述的导入方式采用空气压缩机(15)气压输送，从新参与一氧化氮的吸收反应，完成一氧化氮吸收剂物料的再生循环。
  9. 根据权利要求8所述的去除气流中一氧化氮的工艺,其特征在于所述的通过脱氮反应器气体排出口排出的一氧化氮气体通过水洗、冷冻干燥或吸附干燥过程制备高纯度的一氧化氮气体。
  10. 根据权利要求1所述的装置或8所述的去除工艺,其特征在于所述的装置或工艺的处理工艺如下：
    启动阶段：向物料储罐(102)加入过饱和氯化铁浆液，启动搅拌电机，使物料储罐(102)内物料平均密度为2.1g/cm 3以上；
    吸收工作阶段：启动物料输送泵(4)启动吸收塔(101)工作，当物料储罐(102)内的浆液密度降低为1.7g/cm 3以下或一氧化氮去除率低于50％时，进入吸收剂再生阶段；
    吸收剂再生阶段：
    (a)真空抽气泵(14)工作，电磁阀①⑤打开，回收物料到再生反应器，当物料储罐(102)和再生反应器(103)压差计为零时，投料完毕，关闭真空抽气泵(14)和电磁阀①⑤；
    (b)开启辅料加入口电磁阀③加入所预定量稀盐酸溶液，加完关闭电磁阀③；
    (c)开启再生反应器搅拌器、电磁阀⑨和一氧化氮回收抽气泵(22)抽出释放的一氧化氮气体，抽气完成后，关闭电磁阀⑨和一氧化氮回收抽气泵(22)；
    (d)脱水过程，开启电磁阀⑧、液体循环泵(17)和电磁阀④，开启加热器把再生反应器(103)加热到脱水，再生反应器(103)内的浆液密度为2.1g/cm 3及以上时再生完毕，关闭电磁阀⑧、液体循环泵(17)和电磁阀④，开启空气压缩机(15)和电磁阀②把再生后的物料压入物料储罐(102)，当物料储罐(102)和再生反应器(103)压差计为零时投料完毕，关闭空气压缩机(15)和电磁阀②，重新进入吸收工作阶段。
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