CN111701427A - Process for removing NOx in waste gas generated by burning tetrachloroethylene residual liquid - Google Patents
Process for removing NOx in waste gas generated by burning tetrachloroethylene residual liquid Download PDFInfo
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- CN111701427A CN111701427A CN202010524393.1A CN202010524393A CN111701427A CN 111701427 A CN111701427 A CN 111701427A CN 202010524393 A CN202010524393 A CN 202010524393A CN 111701427 A CN111701427 A CN 111701427A
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- tetrachloroethylene
- waste gas
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- removing nox
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- 239000002912 waste gas Substances 0.000 title claims abstract description 56
- 238000000034 method Methods 0.000 title claims abstract description 54
- CYTYCFOTNPOANT-UHFFFAOYSA-N Perchloroethylene Chemical group ClC(Cl)=C(Cl)Cl CYTYCFOTNPOANT-UHFFFAOYSA-N 0.000 title claims abstract description 50
- 229950011008 tetrachloroethylene Drugs 0.000 title claims abstract description 47
- 239000007788 liquid Substances 0.000 title claims abstract description 41
- 238000005406 washing Methods 0.000 claims abstract description 32
- 239000001257 hydrogen Substances 0.000 claims abstract description 29
- 229910052739 hydrogen Inorganic materials 0.000 claims abstract description 29
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims abstract description 27
- 230000001590 oxidative effect Effects 0.000 claims abstract description 26
- ZAMOUSCENKQFHK-UHFFFAOYSA-N Chlorine atom Chemical compound [Cl] ZAMOUSCENKQFHK-UHFFFAOYSA-N 0.000 claims abstract description 24
- 239000000460 chlorine Substances 0.000 claims abstract description 24
- 229910052801 chlorine Inorganic materials 0.000 claims abstract description 24
- 239000007800 oxidant agent Substances 0.000 claims abstract description 21
- 239000011552 falling film Substances 0.000 claims abstract description 13
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 11
- 239000000446 fuel Substances 0.000 claims abstract description 10
- 238000007599 discharging Methods 0.000 claims abstract description 3
- 239000003513 alkali Substances 0.000 claims description 44
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 claims description 28
- ATUOYWHBWRKTHZ-UHFFFAOYSA-N Propane Chemical compound CCC ATUOYWHBWRKTHZ-UHFFFAOYSA-N 0.000 claims description 16
- 239000005708 Sodium hypochlorite Substances 0.000 claims description 14
- SUKJFIGYRHOWBL-UHFFFAOYSA-N sodium hypochlorite Chemical compound [Na+].Cl[O-] SUKJFIGYRHOWBL-UHFFFAOYSA-N 0.000 claims description 14
- 239000007789 gas Substances 0.000 claims description 10
- 239000000243 solution Substances 0.000 claims description 9
- 239000001294 propane Substances 0.000 claims description 8
- CDBYLPFSWZWCQE-UHFFFAOYSA-L sodium carbonate Substances [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 claims description 8
- 239000002918 waste heat Substances 0.000 claims description 8
- 238000001816 cooling Methods 0.000 claims description 5
- WQYVRQLZKVEZGA-UHFFFAOYSA-N hypochlorite Chemical group Cl[O-] WQYVRQLZKVEZGA-UHFFFAOYSA-N 0.000 claims description 4
- 229910000029 sodium carbonate Inorganic materials 0.000 claims description 4
- 238000010521 absorption reaction Methods 0.000 claims description 3
- ZKQDCIXGCQPQNV-UHFFFAOYSA-N Calcium hypochlorite Chemical compound [Ca+2].Cl[O-].Cl[O-] ZKQDCIXGCQPQNV-UHFFFAOYSA-N 0.000 claims description 2
- 239000012670 alkaline solution Substances 0.000 claims description 2
- 150000002431 hydrogen Chemical class 0.000 claims description 2
- SATVIFGJTRRDQU-UHFFFAOYSA-N potassium hypochlorite Chemical compound [K+].Cl[O-] SATVIFGJTRRDQU-UHFFFAOYSA-N 0.000 claims description 2
- 239000003507 refrigerant Substances 0.000 claims description 2
- 238000005507 spraying Methods 0.000 claims description 2
- 230000007812 deficiency Effects 0.000 abstract description 7
- 239000003546 flue gas Substances 0.000 description 36
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 30
- 239000006096 absorbing agent Substances 0.000 description 9
- XSQUKJJJFZCRTK-UHFFFAOYSA-N Urea Chemical compound NC(N)=O XSQUKJJJFZCRTK-UHFFFAOYSA-N 0.000 description 8
- MWUXSHHQAYIFBG-UHFFFAOYSA-N nitrogen oxide Inorganic materials O=[N] MWUXSHHQAYIFBG-UHFFFAOYSA-N 0.000 description 6
- 238000002485 combustion reaction Methods 0.000 description 5
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 4
- KZBUYRJDOAKODT-UHFFFAOYSA-N Chlorine Chemical compound ClCl KZBUYRJDOAKODT-UHFFFAOYSA-N 0.000 description 4
- 239000004202 carbamide Substances 0.000 description 4
- 235000013877 carbamide Nutrition 0.000 description 4
- QWPPOHNGKGFGJK-UHFFFAOYSA-N hypochlorous acid Chemical compound ClO QWPPOHNGKGFGJK-UHFFFAOYSA-N 0.000 description 4
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 2
- 229910021529 ammonia Inorganic materials 0.000 description 2
- 238000006243 chemical reaction Methods 0.000 description 2
- 239000003153 chemical reaction reagent Substances 0.000 description 2
- 238000010574 gas phase reaction Methods 0.000 description 2
- 239000000463 material Substances 0.000 description 2
- 238000002156 mixing Methods 0.000 description 2
- 239000000779 smoke Substances 0.000 description 2
- 239000007858 starting material Substances 0.000 description 2
- 230000009286 beneficial effect Effects 0.000 description 1
- 239000003638 chemical reducing agent Substances 0.000 description 1
- 238000004140 cleaning Methods 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 230000002950 deficient Effects 0.000 description 1
- 238000002474 experimental method Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 229910052757 nitrogen Inorganic materials 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 238000011160 research Methods 0.000 description 1
- 239000007921 spray Substances 0.000 description 1
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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
- B01D53/74—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
- B01D53/46—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
- B01D53/34—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
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F22—STEAM GENERATION
- F22B—METHODS OF STEAM GENERATION; STEAM BOILERS
- F22B1/00—Methods of steam generation characterised by form of heating method
- F22B1/02—Methods of steam generation characterised by form of heating method by exploitation of the heat content of hot heat carriers
- F22B1/18—Methods of steam generation characterised by form of heating method by exploitation of the heat content of hot heat carriers the heat carrier being a hot gas, e.g. waste gas such as exhaust gas of internal-combustion engines
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
- F23G5/00—Incineration of waste; Incinerator constructions; Details, accessories or control therefor
- F23G5/44—Details; Accessories
- F23G5/442—Waste feed arrangements
- F23G5/446—Waste feed arrangements for liquid waste
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
- F23G7/00—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals
- F23G7/04—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals of waste liquors, e.g. sulfite liquors
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES
- F23J15/00—Arrangements of devices for treating smoke or fumes
- F23J15/06—Arrangements of devices for treating smoke or fumes of coolers
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2251/00—Reactants
- B01D2251/10—Oxidants
- B01D2251/108—Halogens or halogen compounds
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- B01D2251/00—Reactants
- B01D2251/30—Alkali metal compounds
- B01D2251/304—Alkali metal compounds of sodium
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- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
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Abstract
The invention relates to the technical field of tetrachloroethylene raffinate treatment, in particular to a process for removing NOx in waste gas generated by burning tetrachloroethylene raffinate, which comprises the following steps: when the tetrachloroethylene residual liquid is burnt, the adding amount of the hydrogen-containing fuel is controlled, so that chlorine can be generated in the tetrachloroethylene residual liquid in the burning process; the generated waste gas is sequentially cooled, absorbed by falling film and washed by water,and then carrying out alkaline washing treatment, adding a strong oxidant into alkaline washing liquid subjected to the alkaline washing treatment, and finally discharging waste gas to finish the process of removing NOx in the waste gas generated by burning the tetrachloroethylene residual liquid. The invention keeps the burning process in a hydrogen deficiency state by controlling the introduction amount of hydrogen-containing fuel in the burning process of the tetrachloroethylene residual liquid, so that chlorine with strong oxidizing property is generated by chlorine element in the residual liquid in the hydrogen deficiency environment, namely, strong oxidizer is prepared during the burning process, and the strong oxidizer can oxidize NO in the waste gas into NO2Thereby achieving the purpose of reducing the NO content in the waste gas at the outlet of the incinerator.
Description
Technical Field
The invention relates to the technical field of tetrachloroethylene residual liquid treatment, and particularly relates to a process for removing NOx in waste gas generated by burning tetrachloroethylene residual liquid.
Background
The information in this background section is only for enhancement of understanding of the general background of the invention and is not necessarily to be construed as an admission or any form of suggestion that this information forms the prior art that is already known to a person of ordinary skill in the art.
NOx purification is the most difficult and expensive technique. This is due to the inert (chemical reaction does not occur easily) and water-insoluble nature of NO, which makes it difficult for NO to be absorbed efficiently during alkaline cleaning. NOx in the incinerator flue gas is predominantly NO, with levels as high as 95% or more. At present, the removal of NOx in the waste gas of a tetrachloroethylene raffinate incinerator mostly adopts an SNCR method (refer to the attached figure 1 in the specification), and the method is to spray reducing agent carbamide (urea) at an outlet of the incinerator and reduce the NOx into nitrogen by using the carbamide (urea) under the condition of high temperature (800-1000 ℃).
However, the inventor researches and discovers that the existing SNCR method for denitration of waste gas of a tetrachloroethylene raffinate incinerator mainly has the defects of high equipment investment of ①, low denitration efficiency of ②, difficult guarantee of sufficient mixing of gas phase reaction, high ammonia liquid consumption, strict ③ temperature requirement, low temperature, low NOx conversion rate, overhigh temperature, NH, and the like3It is easily oxidized into NOx, and NH is offset3The removal efficiency of (2).
Disclosure of Invention
Aiming at the problems, the invention provides a process for removing NOx in waste gas generated by burning tetrachloroethylene residual liquid, which not only overcomes the bottleneck problems of large equipment investment and harsh control conditions in an SNCR method, but also can more efficiently and thoroughly remove the nitrogen oxides in the waste gas. In order to achieve the purpose, the technical scheme of the invention is as follows.
A process for removing NOx in waste gas generated by burning tetrachloroethylene residual liquid comprises the following steps:
(1) when the tetrachloroethylene residual liquid is burnt, the adding amount of the hydrogen-containing fuel is controlled, so that chlorine can be generated in the tetrachloroethylene residual liquid in the burning process.
(2) And (2) sequentially cooling, falling film absorption and water washing the waste gas generated in the step (1), then performing alkali washing treatment, adding a strong oxidant into alkali washing liquid subjected to the alkali washing treatment, and finally discharging the waste gas to finish the process of removing NOx in the waste gas generated by burning the tetrachloroethylene residual liquid.
Further, in the step (1), the adding proportion of the hydrogen-containing fuel is as follows: the chlorine/hydrogen ratio was controlled at 12:21, molar ratio. The hydrogen-containing fuel feeding amount in the incinerator is controlled to ensure that the incinerator maintains the incineration environment with insufficient hydrogen element, chlorine element in residual liquid generates trace chlorine in the hydrogen-deficient environment, and the chlorine is a strong oxidant and can oxidize NO in waste gas into NO2And the NO content in the smoke of the incinerator is reduced. In addition, maintaining a trace amount of chlorine gas can help to avoid causing secondary pollution as well.
Optionally, the hydrogen-containing fuel comprises any one of hydrogen, propane, water gas, and the like.
Further, in the step (2), the cooling method includes: and (2) introducing the waste gas generated in the step (1) into heat exchange equipment to exchange heat with a refrigerant in the heat exchange equipment, and chilling, so that the temperature of the waste gas is reduced. Optionally, the heat exchange device comprises any one of a waste heat boiler, a heat exchanger and the like.
Further, in the step (2), the alkaline solution includes any one of sodium hydroxide, sodium carbonate solution and the like. Optionally, the mass concentration (%) ranges from 10% to 15%
Further, the strong oxidant is hypochlorite, including any one or more of sodium hypochlorite, potassium hypochlorite, calcium hypochlorite and the like. Optionally, the adding proportion ranges from 1% to 2%, and the mass is concentrated.
Further, in the step (2), the alkali washing treatment is carried out in an alkali washing tower, the alkali washing liquid is in countercurrent contact with the exhaust gas in a circulating spraying mode, and the NO remained in the exhaust gas is further oxidized into NO by a strong oxidant2，NO2And then absorbed and removed by alkaline washing liquid.
Further, step (2) further comprises a metering pump, and the adding amount of the strong oxidant is controlled according to the change of the NOx content in the exhaust gas.
Compared with the prior art, the invention has the following beneficial effects:
(1) the invention controls the introduction amount of hydrogen-containing fuel in the combustion process of the tetrachloroethylene residual liquid to keep the incineration process in a hydrogen deficiency state, so that chlorine with strong oxidizing property is generated by chlorine element in the residual liquid in the hydrogen deficiency environment, which is equivalent to preparing a strong oxidizer during combustion, and the strong oxidizer can oxidize NO in waste gas into NO2 under the joint participation of moisture provided in a falling film absorption process, thereby achieving the purpose of reducing the NO content in the waste gas at the outlet of the incinerator.
(2) The strong oxidant is added in the alkali washing treatment process, so that residual NO in the waste gas can be further oxidized into NO2，NO2Then absorbed by alkali liquor and removed, and then effectively reduces NO in the waste gas at the outlet of the incinerator, and finally more efficiently and thoroughly removes the nitrogen oxides in the waste gas.
Drawings
The accompanying drawings, which are incorporated in and constitute a part of this specification, are included to provide a further understanding of the invention, and are incorporated in and constitute a part of this specification, illustrate exemplary embodiments of the invention and together with the description, serve to explain the invention without unduly limiting the invention.
FIG. 1 is a flow chart of a process for removing NOx from waste gas generated by burning tetrachloroethylene raffinate in the prior art.
FIG. 2 is a flow chart of a process for removing NOx from waste gas generated by burning tetrachloroethylene raffinate in the embodiment of the present invention.
Detailed Description
The invention will be further illustrated with reference to the following specific examples. It should be understood that these examples are for illustrative purposes only and are not intended to limit the scope of the present invention. The experimental procedures, in which specific conditions are not noted in the following examples, are generally carried out according to conventional conditions or according to conditions recommended by the manufacturers.
Unless defined otherwise, all technical and scientific terms used herein have the same meaning as commonly understood by one of ordinary skill in the art. The reagents or starting materials used in the present invention can be purchased from conventional sources, and unless otherwise specified, the reagents or starting materials used in the present invention can be used in a conventional manner in the art or in accordance with the product specifications. In addition, any methods and materials similar or equivalent to those described herein can be used in the methods of the present invention. The preferred methods and materials described in this invention are exemplary only.
As described above, the conventional SNCR method for denitration c of waste gas from a tetrachloroethylene raffinate incinerator has the disadvantages of large equipment investment, low denitration efficiency, difficulty in ensuring sufficient mixing in gas phase reaction, large ammonia liquid consumption, strict requirement on temperature, and the like. Therefore, the invention provides a process for removing NOx in waste gas generated by burning tetrachloroethylene residual liquid, and the invention is further explained by combining the attached drawings and the specific embodiment of the specification.
First embodiment
A process for removing NOx in waste gas generated by burning tetrachloroethylene raffinate refers to FIG. 2, and comprises the following steps:
the tetrachloroethylene residual liquid and the propane enter the incinerator through the combustor to be combusted at about 1200 ℃ in an incineration hearth, and the tetrachloroethylene residual liquid and the propane can participate in combustion in a hydrogen deficiency environment by controlling the feeding proportion (the chlorine/hydrogen molar ratio is 12:21) to generate trace chlorine in the hearth.
Leading out high-temperature flue gas from the incinerator, then feeding the high-temperature flue gas into a waste heat boiler, cooling the high-temperature flue gas to about 550 ℃, and then exciting the high-temperature flue gasThe temperature of the cooling tower is reduced to about 60 ℃, and then the cooled gas enters the falling film absorber to be reduced to 30 ℃, trace chlorine in the flue gas reacts with water to generate hypochlorous acid in the process, and the hypochlorous acid has strong oxidizing property and can oxidize NO into NO2(NO+Cl2+H2O＝2NO2+HCl)。
NO in cooled flue gas2Continuously contacts with alkali liquor (sodium hydroxide solution with the mass concentration of about 10%) in the alkali washing tower in a reverse direction, and is absorbed and removed by the alkali liquor. Adding strong oxidant (sodium hypochlorite, the mass concentration of the added sodium hypochlorite in the alkali liquor is about 1.5%) in the alkali washing treatment process according to the content of NOx at the outlet of the chimney, and further oxidizing residual NO in the waste gas into NO2，NO2Then absorbed and removed by lye. And finally, the content of NOx in the discharged flue gas is reduced to below 50ppm by controlling the chlorine/hydrogen ratio.
Second embodiment
A process for removing NOx in waste gas generated by burning tetrachloroethylene raffinate refers to FIG. 2, and comprises the following steps:
the tetrachloroethylene residual liquid and the water gas enter the incinerator through the combustor to be combusted at about 1200 ℃ in an incineration hearth, and the tetrachloroethylene residual liquid and the water gas can participate in combustion in a hydrogen deficiency environment by controlling the feeding proportion (the chlorine/hydrogen molar ratio is 12:21) to generate trace chlorine in the hearth.
Leading high-temperature flue gas out of the incinerator, then entering a waste heat boiler, reducing the temperature of the flue gas to about 550 ℃, then reducing the temperature of the flue gas to about 60 ℃ through a chilling tower, then entering a falling film absorber, reducing the temperature of the falling film absorber to 30 ℃, and reacting trace chlorine in the flue gas with water to generate hypochlorous acid which has strong oxidizing property and can oxidize NO into NO2(NO+Cl2+H2O＝2NO2+HCl)。
NO in cooled flue gas2Continuously contacts with alkali liquor (sodium carbonate solution with the mass concentration of about 15%) in the alkali washing tower in a reverse direction, and is absorbed and removed by the alkali liquor. Adding strong oxidant (sodium hypochlorite, the mass concentration of the added sodium hypochlorite in the alkali liquor is about 2.0%) in the alkali washing treatment process according to the content of NOx at the outlet of the chimney, and further oxidizing residual NO in the waste gas into NO2，NO2Then absorbed and removed by lye. By controlling the chlorine/hydrogen ratio, the content of NOx in the discharged flue gas is finally reduced to be below 38 ppm.
Third embodiment
A process for removing NOx in waste gas generated by burning tetrachloroethylene raffinate refers to FIG. 2, and comprises the following steps:
the tetrachloroethylene residual liquid and the propane enter the incinerator through the combustor to be combusted at about 1200 ℃ in an incineration hearth, and the tetrachloroethylene residual liquid and the propane can participate in combustion in a hydrogen deficiency environment by controlling the feeding proportion (the chlorine/hydrogen molar ratio is 12:21) to generate trace chlorine in the hearth.
Leading high-temperature flue gas out of the incinerator, then entering a waste heat boiler, reducing the temperature of the flue gas to about 550 ℃, then reducing the temperature of the flue gas to about 60 ℃ through a chilling tower, then entering a falling film absorber, reducing the temperature of the falling film absorber to 30 ℃, and reacting trace chlorine in the flue gas with water to generate hypochlorous acid which has strong oxidizing property and can oxidize NO into NO2(NO+Cl2+H2O＝2NO2+HCl)。
NO in cooled flue gas2Continuously contacts with alkali liquor (sodium hydroxide solution with the mass concentration of about 13%) in the alkali washing tower in a reverse direction, and is absorbed and removed by the alkali liquor. Adding strong oxidant (sodium hypochlorite, the mass concentration of the added sodium hypochlorite in the alkali liquor is about 1.0%) in the alkali washing treatment process according to the content of NOx at the outlet of the chimney, and further oxidizing residual NO in the waste gas into NO2，NO2Then absorbed and removed by lye. And finally, the content of NOx in the discharged flue gas is reduced to be lower than 43ppm by controlling the chlorine/hydrogen ratio.
Fourth embodiment
A process for removing NOx in waste gas generated by burning tetrachloroethylene raffinate refers to FIG. 2, and comprises the following steps:
the tetrachloroethylene residual liquid and sufficient propane enter an incinerator through a burner and are combusted at about 1200 ℃ in an incineration hearth, high-temperature flue gas is led out from the incinerator and enters a waste heat boiler, the temperature of the flue gas is reduced to about 550 ℃ after being cooled, the temperature of the flue gas is reduced to about 60 ℃ through a chilling tower, and then the flue gas enters a falling film absorber and is reduced to 30 ℃.
NO in cooled flue gas2Continuously contacts with alkali liquor (sodium hydroxide solution with the mass concentration of about 10%) in the alkali washing tower in a reverse direction, and is absorbed and removed by the alkali liquor. Adding strong oxidant (sodium hypochlorite, the mass concentration of the added sodium hypochlorite in the alkali liquor is about 1.5%) in the alkali washing treatment process according to the content of NOx at the outlet of the chimney, and further oxidizing residual NO in the waste gas into NO2，NO2Then absorbed and removed by alkali liquor, and finally the NOx content in the discharged flue gas is measured to be more than 739 ppm.
Fifth embodiment
A process for removing NOx in waste gas generated by burning tetrachloroethylene raffinate refers to FIG. 2, and comprises the following steps:
the tetrachloroethylene residual liquid and water gas (enough) enter an incinerator through a burner, are combusted at about 1200 ℃ in an incineration hearth, high-temperature flue gas is led out from the incinerator and then enters a waste heat boiler, the temperature of the flue gas is reduced to about 550 ℃, then the temperature of the flue gas is reduced to about 60 ℃ through a chilling tower, and then the flue gas enters a falling film absorber and the temperature of the falling film absorber is reduced to 30 ℃.
NO in cooled flue gas2The alkaline washing tower is in reverse contact with alkali liquor (sodium carbonate solution with the mass concentration of about 15%) and is absorbed and removed by the alkali liquor. Adding strong oxidant (sodium hypochlorite, the mass concentration of the added sodium hypochlorite in the alkali liquor is about 2.0%) in the alkali washing treatment process according to the content of NOx at the outlet of the chimney, and further oxidizing residual NO in the waste gas into NO2，NO2Then absorbed and removed by lye. Finally, the content of NOx in the discharged flue gas is measured to be above 641 ppm.
Sixth embodiment
A process for removing NOx in waste gas generated by burning tetrachloroethylene raffinate refers to FIG. 2, and comprises the following steps:
the tetrachloroethylene residual liquid and sufficient propane enter an incinerator through a burner and are combusted at about 1200 ℃ in an incineration hearth, high-temperature flue gas is led out from the incinerator and enters a waste heat boiler, the temperature of the flue gas is reduced to about 550 ℃ after being cooled, the temperature of the flue gas is reduced to about 60 ℃ through a chilling tower, and then the flue gas enters a falling film absorber and is reduced to 30 ℃.
NO in cooled flue gas2Continuously contacts with alkali liquor (sodium hydroxide solution with the mass concentration of about 13%) in the alkali washing tower in a reverse direction, and is absorbed and removed by the alkali liquor. Adding strong oxidant (sodium hypochlorite, the mass concentration of the added sodium hypochlorite in the alkali liquor is about 1.0%) in the alkali washing treatment process according to the content of NOx at the outlet of the chimney, and further oxidizing residual NO in the waste gas into NO2，NO2Then absorbed and removed by lye. Finally, the content of NOx in the discharged smoke is measured to be higher than 686 ppm.
Although the present invention has been described in detail with reference to the foregoing embodiments, it will be apparent to those skilled in the art that changes may be made in the embodiments and/or equivalents thereof without departing from the spirit and scope of the invention. Any modification, equivalent replacement, or improvement made within the spirit and principle of the present invention should be included in the protection scope of the present invention.
Claims (10)
1. A process for removing NOx in waste gas generated by burning tetrachloroethylene residual liquid is characterized by comprising the following steps:
(1) when the tetrachloroethylene residual liquid is burnt, the adding amount of the hydrogen-containing fuel is controlled, so that chlorine can be generated in the tetrachloroethylene residual liquid in the burning process;
(2) and (2) sequentially cooling, falling film absorption and water washing the waste gas generated in the step (1), then performing alkali washing treatment, adding a strong oxidant into alkali washing liquid subjected to the alkali washing treatment, and finally discharging the waste gas to finish the process of removing NOx in the waste gas generated by burning the tetrachloroethylene residual liquid.
2. The process for removing NOx from waste gas from the incineration of tetrachloroethylene raffinate according to claim 1, wherein in the step (1), the hydrogen-containing fuel is added in a ratio of: the chlorine/hydrogen ratio was controlled at 12:21, molar ratio.
3. The process for removing NOx from waste gas generated by incinerating tetrachloroethylene residue according to claim 1, wherein the hydrogen-containing fuel comprises any one of hydrogen, propane and water gas.
4. The process for removing NOx from waste gas generated by burning tetrachloroethylene raffinate according to claim 1, wherein in the step (2), the temperature reduction method comprises the following steps: introducing the waste gas generated in the step (1) into heat exchange equipment to exchange heat with a refrigerant in the heat exchange equipment, and chilling; preferably, the heat exchange device comprises any one of a waste heat boiler and a heat exchanger.
5. The process for removing NOx from waste gas generated by incinerating tetrachloroethylene residue according to claim 1, wherein in the step (2), the alkaline solution comprises any one of sodium hydroxide and sodium carbonate solution.
6. The process for removing NOx from waste gas generated by burning tetrachloroethylene raffinate according to claim 5, wherein the mass concentration of the alkaline wash liquid is in the range of 10 to 15%.
7. The process for removing NOx from a tetrachloroethylene residual liquid incineration exhaust gas according to claim 1, wherein the strong oxidant is hypochlorite including any one or more of sodium hypochlorite, potassium hypochlorite and calcium hypochlorite.
8. The process for removing NOx from waste gas generated by burning tetrachloroethylene raffinate according to claim 1, wherein the addition ratio of the strong oxidant in the alkaline washing solution is in the range of 1-2% by mass concentration.
9. The process for removing NOx from waste gas from the incineration of tetrachloroethylene raffinate according to claim 1, wherein in the step (2), the alkali washing treatment is carried out in an alkali washing tower, and the alkali washing liquid is brought into counter-current contact with the waste gas by means of circulating spraying.
10. The process for removing NOx from a waste gas from the incineration of tetrachloroethylene residue according to any one of claims 1 to 9, wherein the step (2) further comprises a metering pump for controlling the amount of the strong oxidizer to be added according to the change of the NOx content in the waste gas.
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