CN111389117A - Active coke regeneration waste gas treatment device and method - Google Patents

Active coke regeneration waste gas treatment device and method Download PDF

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Publication number
CN111389117A
CN111389117A CN202010222704.9A CN202010222704A CN111389117A CN 111389117 A CN111389117 A CN 111389117A CN 202010222704 A CN202010222704 A CN 202010222704A CN 111389117 A CN111389117 A CN 111389117A
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China
Prior art keywords
flue gas
gas
pipeline
treatment
active coke
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CN202010222704.9A
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Chinese (zh)
Inventor
李云贵
王万寿
侯春晓
胡海平
艾可
熊郭飞
李国荣
朱鹏伟
司吉昆
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Hangzhou Huishui Technology Co ltd
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Hangzhou Huishui Technology Co ltd
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Priority to CN202010222704.9A priority Critical patent/CN111389117A/en
Publication of CN111389117A publication Critical patent/CN111389117A/en
Pending legal-status Critical Current

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    • BPERFORMING OPERATIONS; TRANSPORTING
    • B01PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01DSEPARATION
    • B01D46/00Filters or filtering processes specially modified for separating dispersed particles from gases or vapours
    • B01D46/02Particle separators, e.g. dust precipitators, having hollow filters made of flexible material
    • BPERFORMING OPERATIONS; TRANSPORTING
    • B01PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01DSEPARATION
    • B01D53/00Separation 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
    • B01D53/02Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography
    • B01D53/04Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography with stationary adsorbents
    • BPERFORMING OPERATIONS; TRANSPORTING
    • B01PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01DSEPARATION
    • B01D53/00Separation 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
    • B01D53/34Chemical or biological purification of waste gases
    • B01D53/46Removing components of defined structure
    • B01D53/48Sulfur compounds
    • B01D53/50Sulfur oxides
    • B01D53/507Sulfur oxides by treating the gases with other liquids
    • BPERFORMING OPERATIONS; TRANSPORTING
    • B01PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01DSEPARATION
    • B01D53/00Separation 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
    • B01D53/34Chemical or biological purification of waste gases
    • B01D53/74General processes for purification of waste gases; Apparatus or devices specially adapted therefor
    • B01D53/75Multi-step processes
    • BPERFORMING OPERATIONS; TRANSPORTING
    • B01PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01DSEPARATION
    • B01D53/00Separation 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
    • B01D53/34Chemical or biological purification of waste gases
    • B01D53/74General processes for purification of waste gases; Apparatus or devices specially adapted therefor
    • B01D53/77Liquid phase processes
    • B01D53/78Liquid phase processes with gas-liquid contact
    • BPERFORMING OPERATIONS; TRANSPORTING
    • B01PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01DSEPARATION
    • B01D53/00Separation 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
    • B01D53/34Chemical or biological purification of waste gases
    • B01D53/74General processes for purification of waste gases; Apparatus or devices specially adapted therefor
    • B01D53/86Catalytic processes
    • B01D53/8621Removing nitrogen compounds
    • B01D53/8625Nitrogen oxides
    • B01D53/8628Processes characterised by a specific catalyst
    • BPERFORMING OPERATIONS; TRANSPORTING
    • B01PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01DSEPARATION
    • B01D53/00Separation 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
    • B01D53/34Chemical or biological purification of waste gases
    • B01D53/74General processes for purification of waste gases; Apparatus or devices specially adapted therefor
    • B01D53/86Catalytic processes
    • B01D53/864Removing carbon monoxide or hydrocarbons
    • BPERFORMING OPERATIONS; TRANSPORTING
    • B01PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01DSEPARATION
    • B01D2251/00Reactants
    • B01D2251/20Reductants
    • B01D2251/206Ammonium compounds
    • B01D2251/2067Urea
    • BPERFORMING OPERATIONS; TRANSPORTING
    • B01PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01DSEPARATION
    • B01D2253/00Adsorbents used in seperation treatment of gases and vapours
    • B01D2253/10Inorganic adsorbents
    • B01D2253/102Carbon
    • BPERFORMING OPERATIONS; TRANSPORTING
    • B01PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01DSEPARATION
    • B01D2256/00Main component in the product gas stream after treatment
    • B01D2256/10Nitrogen
    • BPERFORMING OPERATIONS; TRANSPORTING
    • B01PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01DSEPARATION
    • B01D2256/00Main component in the product gas stream after treatment
    • B01D2256/22Carbon dioxide
    • BPERFORMING OPERATIONS; TRANSPORTING
    • B01PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01DSEPARATION
    • B01D2257/00Components to be removed
    • B01D2257/50Carbon oxides
    • B01D2257/502Carbon monoxide

Abstract

The invention discloses an active coke regeneration waste gas treatment device and method, which comprises a flue gas heat exchanger, wherein a first pipeline and a second pipeline which are independent of each other are arranged in the flue gas heat exchanger, and the first pipeline is connected with an air inlet pipeline and a high-temperature bag-type dust collector; the upper end of the high-temperature bag-type dust remover is connected with the bottom of the alkali washing desulfurization tower, and the lower end of the high-temperature bag-type dust remover is connected with a smoke dust particle collecting device; the top of the alkaline washing desulfurization tower is sequentially connected with a flue gas condenser and an active coke adsorption tank, the active coke adsorption tank is connected with a catalytic oxidation tank through a second pipeline inside the flue gas heat exchanger, and the catalytic oxidation tank is connected with an SCR denitration treatment device. The invention adopts a non-combustion method to treat the regenerated waste gas of the active coke, reduces the emission of smoke dust particles by more than 90 percent, reduces sulfur dioxide by more than 95 percent and nitrogen oxide by more than 80 percent on the basis of national standard, and can not see white smoke visually.

Description

Active coke regeneration waste gas treatment device and method
Technical Field
The invention relates to the field of activated coke regeneration waste gas treatment, in particular to an activated coke regeneration waste gas treatment device and method.
Background
The treatment technology of the active coke regenerated waste gas currently used adopts a three-level spraying mode to treat the regenerated waste gas so as to remove smoke dust particles, sulfur dioxide, nitrogen oxides and the like in the waste gas, and the treated waste gas can reach the emission standard. However, due to the adoption of the water spraying method, the spraying water is also heated in the process of treating the high-temperature flue gas, a large amount of steam is generated, the discharged flue gas contains a large amount of moisture, a large amount of white mist is generated at the smoke outlet, smoke dust particles contained in the flue gas present obvious black smoke under the background of the white mist, sensory illusion is brought to residents around a factory, the smoke dust particles are often mistakenly emitted in violation of regulations, and great inconvenience is brought to the management of the factory.
In addition, other substances such as carbon monoxide and non-methane total hydrocarbons contained in the smoke are occasionally sensed to have peculiar smell within a certain range of a factory area although the emission meets the national standard. As the application occasions of the active coke are municipal and other deep standard-lifting projects for sewage treatment, which are high-standard discharge projects, and the projects are often built around large and medium-sized cities, the waste gas generated by regeneration of the matched active coke is naturally expected to be higher. Although the current treatment technology can meet the regulations of national standards, the current treatment technology cannot meet the sensory requirements of people.
Disclosure of Invention
The invention aims to provide an active coke regeneration waste gas treatment device and method, which adopt a non-combustion method to treat active coke regeneration waste gas and discharge the active coke regeneration waste gas into the atmosphere with higher ultra-low emission control requirements.
Therefore, the first technical scheme of the invention is as follows: active burnt regeneration exhaust treatment device, its characterized in that: the device comprises a flue gas heat exchanger, wherein a first pipeline and a second pipeline which are independent of each other are arranged in the flue gas heat exchanger, and the first pipeline is connected with an air inlet pipeline and a high-temperature bag-type dust collector; the upper end of the high-temperature bag-type dust remover is connected with the bottom of the alkali washing desulfurization tower, and the lower end of the high-temperature bag-type dust remover is connected with a smoke dust particle collecting device; the top of the alkaline washing desulfurization tower is sequentially connected with a flue gas condenser and an active coke adsorption tank, the active coke adsorption tank is connected with a catalytic oxidation tank through a second pipeline inside the flue gas heat exchanger, and the catalytic oxidation tank is connected with an SCR denitration treatment device.
Preferably, an induced draft fan is arranged between the flue gas condenser and the active coke adsorption tank.
Preferably, the SCR denitration treatment device comprises an SCR reactor and a urea solution storage tank, the front end of the SCR reactor is connected with the catalytic oxidation box through a pipeline, and a nozzle is arranged on the pipeline and connected with the urea solution storage tank.
The second technical scheme of the invention is as follows: the active coke regeneration waste gas treatment method using the device comprises the following steps:
1) waste gas generated by the regeneration of the active coke is sent into a first channel of the flue gas heat exchanger through an air inlet pipeline, and the waste gas is cooled under the action of the flue gas heat exchanger;
2) the cooled waste gas enters a high-temperature bag-type dust collector to remove smoke dust particles in the waste gas;
3) the flue gas without the smoke dust enters an alkaline washing desulfurization tower, flows from bottom to top, and is in full gas-liquid contact with spray water in the tower from top to bottom to remove sulfur dioxide in the waste gas;
4) the flue gas from which the sulfur dioxide is removed enters a flue gas condenser to remove water mist in the flue gas, and then the flue gas enters an induced draft fan which provides power for the flue gas;
5) enabling the flue gas from the induced draft fan to enter an active coke adsorption tank, and removing organic substances VOCs in the flue gas;
6) the treated flue gas enters a second channel of the flue gas heat exchanger, and the low-temperature flue gas in the second channel and the regenerated high-temperature waste gas in the first channel exchange heat without direct contact;
7) the low-temperature flue gas is heated and then enters a catalytic oxidation box, and combustible gas which is not fully combusted in the flue gas is removed under the action of a catalyst;
8) and (3) the catalyzed flue gas enters an SCR denitration treatment device, urea solution is sprayed to the flue gas in a pipeline at the front end of the SCR reactor to remove nitrogen oxides in the flue gas, and finally the flue gas is discharged into the atmosphere through a chimney.
Preferably, in the step 3), the spray water in the alkaline washing desulfurization tower is a sodium hydroxide solution, and reacts with sulfur dioxide in the flue gas to generate sodium sulfite, so as to remove sulfur dioxide in the flue gas.
Preferably, in the step 7), the combustible gas in the flue gas is carbon monoxide and hydrogen, the carbon monoxide and oxygen react to form carbon dioxide under the action of the catalyst, and the hydrogen and oxygen react to form water.
Preferably, in the step 8), before entering the SCR reactor, the flue gas is fully mixed with the urea solution sprayed from the nozzle, and after entering the SCR reactor, the flue gas undergoes a reduction reaction under the action of a catalyst to generate nitrogen and water, so as to remove nitrogen oxides in the flue gas.
The invention adopts a non-combustion method to treat the regenerated waste gas of the active coke, reduces the emission of smoke dust particles by more than 90 percent, reduces sulfur dioxide by more than 95 percent and nitrogen oxide by more than 80 percent on the basis of national standard, and can not see white smoke visually. Carbon monoxide, other substances such as non-methane total hydrocarbon and the like are more effectively treated, and on the premise of meeting the national emission standard, the waste gas generated by activated coke regeneration is discharged into the atmosphere with higher ultralow emission control requirement, so that the ambient atmospheric environment of a factory is greatly improved, peculiar smell caused by waste gas emission is basically not perceived, and the management burden of the factory on the atmospheric emission is reduced.
Drawings
The following detailed description is made with reference to the accompanying drawings and embodiments of the present invention
FIG. 1 is a process flow diagram of the present invention.
Labeled as: the system comprises a flue gas heat exchanger 1, a high-temperature bag-type dust collector 2, an alkaline washing desulfurization tower 3, a flue gas condenser 4, an induced draft fan 5, an active coke adsorption tank 6, a catalytic oxidation tank 7, an SCR denitration treatment device 8, a chimney 9, an air inlet pipeline 10, a smoke particle collecting device 11, a drain pipe 12 and a urea solution storage tank 13.
Detailed Description
See the drawings. The active coke regeneration waste gas treatment device described in this embodiment includes a flue gas heat exchanger 1, a high temperature bag dust collector 2, an alkaline washing desulfurizing tower 3, an active coke adsorption tank 6, a catalytic oxidation tank 7 and an SCR denitration treatment device 8. The flue gas heat exchanger 1 is internally provided with a first pipeline and a second pipeline which are mutually independent, the first pipeline is connected with the air inlet pipeline 10 and the high-temperature bag-type dust collector 2, the bag-type dust collector is a dry dust filtering device, a dust hopper is arranged below the bag-type dust collector and is suitable for collecting fine, dry and non-fibrous dust, and the dust hopper can be connected with a smoke dust particle collecting device 11. The upper end of the high-temperature bag-type dust collector 2 is connected with the bottom of an alkaline washing desulfurization tower 3, a spray pipe is arranged above the side surface of the alkaline washing desulfurization tower 3, and a drain pipe 12 is connected below the side surface; the alkaline washing desulfurizing tower 3 is connected with a flue gas condenser 4, the flue gas condenser 4 is connected with an active coke adsorption tank 6 through an induced draft fan 5, and the induced draft fan provides power for flue gas. The active coke adsorption tank 6 is connected with the catalytic oxidation tank 7 through a second pipeline inside the flue gas heat exchanger, the catalytic oxidation tank 7 is connected with the SCR denitration treatment device 8, the SCR denitration treatment device comprises an SCR reactor and a urea solution storage tank 13, the front end of the SCR reactor is connected with the catalytic oxidation tank through a pipeline, a nozzle is arranged on the pipeline, and the nozzle is connected with the urea solution storage tank. The exhaust end of the SCR denitration treatment device 8 is connected with a chimney 9.
The active coke regeneration waste gas treatment process comprises the following steps:
1) the waste gas generated by the regeneration of the active coke is sent into the flue gas heat exchanger 1 through the air inlet pipeline 10, and the waste gas is cooled under the action of the flue gas heat exchanger, so that the temperature of the flue gas is reduced from 400 ℃ to below 200 ℃.
2) The flue gas after the heat exchange enters a high-temperature bag-type dust collector, the bag-type dust collector is a dry dust filtering device, after dust-containing gas enters the bag-type dust collector, dust with large particles and large specific gravity falls into an ash hopper due to the sedimentation of the gravity, and the dust is blocked when the gas containing fine dust passes through a filter material, so that the gas is purified, and smoke dust particles in the waste gas are removed.
3) The flue gas without the smoke dust enters an alkaline washing desulfurization tower 3, flows from bottom to top, and is in full gas-liquid contact with spray water from top to bottom in the tower so as to remove sulfur dioxide in the waste gas; sodium hydroxide solution is used as a desulfurizer, and the prepared sodium hydroxide solution is directly injected into a desulfurizing tower to react with SO in flue gas2Sodium sulfite is generated by reaction, thereby achieving the aim of flue gas desulfurization. The main chemical equation of the reaction is:
2NaOH+SO2=Na2SO3+H2O
during the one-step treatment, the waste gas generation amount is small, the sulfur dioxide content is low, the consumption of the needed desulfurizer is small, the amount of the desulfurization waste water generated every day is very small, the waste water mainly contains sodium sulfite, the concentration is low, and after simple neutralization, precipitation and clarification, the water quality meets the nano-tube standard of water quality standard GBT31962-2015 for discharging sewage into urban sewer and is discharged into a drainage pipeline.
4) The flue gas from which the sulfur dioxide is removed enters a flue gas condenser 4 for removing water mist in the flue gas and then enters an induced draft fan 5, wherein the induced draft fan is a power supply device for the flue gas in the whole process flow.
5) The flue gas from the induced draft fan enters an active coke adsorption tank 6 for removing organic matters such as VOCs in the flue gas; the active coke adsorption box 6 is mainly used for treating low-concentration organic waste gas, waste gas containing VOCs enters an active coke adsorption layer, and unbalanced and unsaturated molecular attraction or chemical bond force exists on the surface of the active coke, so that when the surface of the active coke is contacted with gas, gas molecules can be attracted, concentrated and kept on the surface of the active coke. The waste gas is contacted with the porous active coke with a large surface by utilizing the adsorption capacity of the surface of the active coke, and pollutants in the waste gas are adsorbed on the surface of the active coke and are separated from the gas mixture, thereby achieving the purpose of purifying the VOCs waste gas.
6) The flue gas is processed in the previous stage, the temperature of the flue gas is close to the normal temperature, then the flue gas enters the flue gas heat exchanger 1, the low-temperature flue gas processed in the previous stage and the regenerated high-temperature waste gas exchange heat without direct contact, the flue gas after heat exchange is heated to about 200 ℃, and then the flue gas enters the catalytic oxidation box 7.
7) The low-temperature flue gas enters the catalytic oxidation box 7 after being heated, and is used for removing combustible gas such as carbon monoxide, hydrogen and the like which are not fully combusted in the flue gas under the action of a catalyst. The catalytic oxidation box 7 is internally provided with a catalytic carrier which is prepared by taking cordierite honeycomb ceramics as a carrier, adopting a unique coating material and taking high-content noble metals Pd and Pt as active components and is used for removing carbon monoxide and hydrogen generated by incomplete combustion of various combustible gases. Under the action of the catalyst, carbon monoxide and oxygen react to form carbon dioxide, and hydrogen and oxygen react to form water. The main chemical reaction equation is:
2CO+O2=2CO2
2H2+O2=2H2O
8) the catalyzed flue gas enters the SCR denitration treatment device 8, a nozzle is arranged at the front end of the SCR denitration treatment device 8 through a pipeline opening, and a reducing agent is sprayed to a flue so that the reducing agent and the flue gas are mixedThe flue gas is fully mixed, and after entering the reactor, the flue gas undergoes a reduction reaction under the action of a catalyst to generate nitrogen and water, so that nitrogen oxides in the flue gas are removed. Urea solution is used as a reducing agent, the urea solution is sprayed into a flue and is fully mixed with raw flue gas, then the mixture enters an SCR (selective catalytic reduction) reactor, and under the action of a catalyst and in the presence of oxygen, ammonia gas generated by thermal decomposition of the urea solution is selectively mixed with NO in the flue gasX(mainly NO, NO)2) Chemical reaction is carried out to generate harmless nitrogen (N)2) And water (H)2O). The main reaction chemical equation is:
4NO+4NH3+O2→4N2+6H2O
6NO2+8NH3→7N2+12H2O
NO+NO2+2NH3→2N2+3H2O
after the treatment process, the pollutants adsorbed on the active coke are decomposed into carbon dioxide, nitrogen and water which are harmless to the environment through thermal cracking gasification and the process with ultralow emission in the scheme, and a sentence is drawn for the transfer of the pollutants.
Wherein the main pollutants: smoke is less than or equal to 10mg/NM ^3, sulfur dioxide is less than or equal to 35mg/NM ^3, nitrogen oxide is less than or equal to 50mg/NM ^3, carbon monoxide is less than or equal to 80mg/NM ^3, and non-methane total hydrocarbon is less than or equal to 50mg/NM ^ 3.

Claims (7)

1. Active burnt regeneration exhaust treatment device, its characterized in that: the device comprises a flue gas heat exchanger, wherein a first pipeline and a second pipeline which are independent of each other are arranged in the flue gas heat exchanger, and the first pipeline is connected with an air inlet pipeline and a high-temperature bag-type dust collector; the upper end of the high-temperature bag-type dust remover is connected with the bottom of the alkali washing desulfurization tower, and the lower end of the high-temperature bag-type dust remover is connected with a smoke dust particle collecting device; the top of the alkaline washing desulfurization tower is sequentially connected with a flue gas condenser and an active coke adsorption tank, the active coke adsorption tank is connected with a catalytic oxidation tank through a second pipeline inside the flue gas heat exchanger, and the catalytic oxidation tank is connected with an SCR denitration treatment device.
2. The activated coke regeneration exhaust gas treatment device according to claim 1, wherein: and an induced draft fan is arranged between the flue gas condenser and the active coke adsorption tank.
3. The activated coke regeneration exhaust gas treatment device according to claim 1, wherein: the SCR denitration treatment device comprises an SCR reactor and a urea solution storage tank, the front end of the SCR reactor is connected with the catalytic oxidation box through a pipeline, a nozzle is arranged on the pipeline, and the nozzle is connected with the urea solution storage tank.
4. The active coke regeneration waste gas treatment method is characterized by comprising the following steps: use of a treatment device according to any of claims 1 to 3, comprising the steps of:
1) waste gas generated by the regeneration of the active coke is sent into a first channel of the flue gas heat exchanger through an air inlet pipeline, and the waste gas is cooled under the action of the flue gas heat exchanger;
2) the cooled waste gas enters a high-temperature bag-type dust collector to remove smoke dust particles in the waste gas;
3) the flue gas without the smoke dust enters an alkaline washing desulfurization tower, flows from bottom to top, and is in full gas-liquid contact with spray water in the tower from top to bottom to remove sulfur dioxide in the waste gas;
4) the flue gas from which the sulfur dioxide is removed enters a flue gas condenser to remove water mist in the flue gas, and then the flue gas enters an induced draft fan which provides power for the flue gas;
5) the flue gas from the induced draft fan enters an active coke adsorption box, and Volatile Organic Compounds (VOCs) in the flue gas are removed;
6) the treated flue gas enters a second channel of the flue gas heat exchanger, and the low-temperature flue gas in the second channel and the regenerated high-temperature waste gas in the first channel exchange heat without direct contact;
7) the low-temperature flue gas is heated and then enters a catalytic oxidation box, and combustible gas which is not fully combusted in the flue gas is removed under the action of a catalyst;
8) and (3) the catalyzed flue gas enters an SCR denitration treatment device, urea solution is sprayed to the flue gas in a pipeline at the front end of the SCR reactor to remove nitrogen oxides in the flue gas, and finally the flue gas is discharged into the atmosphere through a chimney.
5. The activated coke regeneration off-gas treatment method according to claim 4, characterized in that: in the step 3), the spray water in the alkaline washing desulfurization tower is a sodium hydroxide solution, and reacts with sulfur dioxide in the flue gas to generate sodium sulfite so as to remove the sulfur dioxide in the flue gas.
6. The activated coke regeneration off-gas treatment method according to claim 4, characterized in that: in the step 7), the combustible gas in the flue gas is carbon monoxide and hydrogen, the carbon monoxide and oxygen react to form carbon dioxide under the action of the catalyst, and the hydrogen and oxygen react to form water.
7. The activated coke regeneration off-gas treatment method according to claim 4, characterized in that: and 8) fully mixing the flue gas with the urea solution sprayed out from the nozzle before the flue gas enters the SCR reactor, and performing a reduction reaction under the action of a catalyst after the flue gas enters the SCR reactor to generate nitrogen and water and remove nitrogen oxides in the flue gas.
CN202010222704.9A 2020-03-26 2020-03-26 Active coke regeneration waste gas treatment device and method Pending CN111389117A (en)

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Application Number Priority Date Filing Date Title
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Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN112121549A (en) * 2020-09-25 2020-12-25 李琰 VOC exhaust pollution treatment system

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN112121549A (en) * 2020-09-25 2020-12-25 李琰 VOC exhaust pollution treatment system

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