CN110876886A - Waste incineration flue gas purification method and system - Google Patents
Waste incineration flue gas purification method and system Download PDFInfo
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- CN110876886A CN110876886A CN201911017830.4A CN201911017830A CN110876886A CN 110876886 A CN110876886 A CN 110876886A CN 201911017830 A CN201911017830 A CN 201911017830A CN 110876886 A CN110876886 A CN 110876886A
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- 239000003546 flue gas Substances 0.000 title claims abstract description 108
- UGFAIRIUMAVXCW-UHFFFAOYSA-N carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 title claims abstract description 103
- 238000004056 waste incineration Methods 0.000 title claims abstract description 42
- 238000000746 purification Methods 0.000 title claims abstract description 20
- 238000006243 chemical reaction Methods 0.000 claims abstract description 66
- OKTJSMMVPCPJKN-UHFFFAOYSA-N carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims abstract description 45
- 239000000428 dust Substances 0.000 claims abstract description 43
- 239000007789 gas Substances 0.000 claims abstract description 29
- 238000005406 washing Methods 0.000 claims abstract description 9
- 238000010531 catalytic reduction reaction Methods 0.000 claims abstract description 5
- 238000010438 heat treatment Methods 0.000 claims abstract description 4
- 238000002347 injection Methods 0.000 claims description 22
- 239000007924 injection Substances 0.000 claims description 22
- HEMHJVSKTPXQMS-UHFFFAOYSA-M sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 claims description 18
- 239000000843 powder Substances 0.000 claims description 17
- 238000005200 wet scrubbing Methods 0.000 claims description 17
- AXCZMVOFGPJBDE-UHFFFAOYSA-L Calcium hydroxide Chemical compound [OH-].[OH-].[Ca+2] AXCZMVOFGPJBDE-UHFFFAOYSA-L 0.000 claims description 16
- 239000000920 calcium hydroxide Substances 0.000 claims description 16
- 235000011116 calcium hydroxide Nutrition 0.000 claims description 16
- 229910001861 calcium hydroxide Inorganic materials 0.000 claims description 16
- 239000007788 liquid Substances 0.000 claims description 16
- 238000010521 absorption reaction Methods 0.000 claims description 10
- 239000007921 spray Substances 0.000 claims description 9
- 238000003303 reheating Methods 0.000 claims description 8
- 235000011114 ammonium hydroxide Nutrition 0.000 claims description 7
- VHUUQVKOLVNVRT-UHFFFAOYSA-N ammonium hydroxide Chemical compound [NH4+].[OH-] VHUUQVKOLVNVRT-UHFFFAOYSA-N 0.000 claims description 7
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 7
- 235000008733 Citrus aurantifolia Nutrition 0.000 claims description 6
- 235000015450 Tilia cordata Nutrition 0.000 claims description 6
- 235000011941 Tilia x europaea Nutrition 0.000 claims description 6
- 238000001816 cooling Methods 0.000 claims description 6
- 239000004571 lime Substances 0.000 claims description 6
- 239000002002 slurry Substances 0.000 claims description 6
- 235000011121 sodium hydroxide Nutrition 0.000 claims description 6
- 239000000243 solution Substances 0.000 claims description 6
- 239000003638 reducing agent Substances 0.000 claims description 4
- 239000003513 alkali Substances 0.000 claims description 2
- 239000010813 municipal solid waste Substances 0.000 abstract description 6
- 238000005516 engineering process Methods 0.000 abstract description 2
- 238000000034 method Methods 0.000 description 17
- 239000003344 environmental pollutant Substances 0.000 description 16
- 231100000719 pollutant Toxicity 0.000 description 16
- 239000000779 smoke Substances 0.000 description 15
- 239000002253 acid Substances 0.000 description 9
- 230000000052 comparative effect Effects 0.000 description 7
- 229910001385 heavy metal Inorganic materials 0.000 description 7
- 239000010881 fly ash Substances 0.000 description 6
- 229910002089 NOx Inorganic materials 0.000 description 5
- YLQBMQCUIZJEEH-UHFFFAOYSA-N furane Chemical compound C=1C=COC=1 YLQBMQCUIZJEEH-UHFFFAOYSA-N 0.000 description 5
- KVGZZAHHUNAVKZ-UHFFFAOYSA-N p-dioxin Chemical compound O1C=COC=C1 KVGZZAHHUNAVKZ-UHFFFAOYSA-N 0.000 description 5
- OSGAYBCDTDRGGQ-UHFFFAOYSA-L Calcium sulfate Chemical compound [Ca+2].[O-]S([O-])(=O)=O OSGAYBCDTDRGGQ-UHFFFAOYSA-L 0.000 description 4
- MWUXSHHQAYIFBG-UHFFFAOYSA-N Nitrogen oxide Substances O=[N] MWUXSHHQAYIFBG-UHFFFAOYSA-N 0.000 description 4
- 239000003054 catalyst Substances 0.000 description 4
- 239000000463 material Substances 0.000 description 4
- 239000000203 mixture Substances 0.000 description 4
- IJGRMHOSHXDMSA-UHFFFAOYSA-N nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 4
- VEXZGXHMUGYJMC-UHFFFAOYSA-N HCl Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 description 3
- 229910052799 carbon Inorganic materials 0.000 description 3
- 238000004140 cleaning Methods 0.000 description 3
- 229910000041 hydrogen chloride Inorganic materials 0.000 description 3
- 238000006386 neutralization reaction Methods 0.000 description 3
- 239000002918 waste heat Substances 0.000 description 3
- GBAOBIBJACZTNA-UHFFFAOYSA-L Calcium sulfite Chemical compound [Ca+2].[O-]S([O-])=O GBAOBIBJACZTNA-UHFFFAOYSA-L 0.000 description 2
- 239000002956 ash Substances 0.000 description 2
- 238000007664 blowing Methods 0.000 description 2
- UXVMQQNJUSDDNG-UHFFFAOYSA-L cacl2 Chemical compound [Cl-].[Cl-].[Ca+2] UXVMQQNJUSDDNG-UHFFFAOYSA-L 0.000 description 2
- 239000001110 calcium chloride Substances 0.000 description 2
- 229910001628 calcium chloride Inorganic materials 0.000 description 2
- 235000010261 calcium sulphite Nutrition 0.000 description 2
- 239000007795 chemical reaction product Substances 0.000 description 2
- 150000002013 dioxins Chemical class 0.000 description 2
- 238000001035 drying Methods 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 229910052757 nitrogen Inorganic materials 0.000 description 2
- 229910052813 nitrogen oxide Inorganic materials 0.000 description 2
- 239000002245 particle Substances 0.000 description 2
- 238000004537 pulping Methods 0.000 description 2
- 239000007790 solid phase Substances 0.000 description 2
- 238000005507 spraying Methods 0.000 description 2
- XSQUKJJJFZCRTK-UHFFFAOYSA-N urea Chemical compound NC(N)=O XSQUKJJJFZCRTK-UHFFFAOYSA-N 0.000 description 2
- 210000003660 Reticulum Anatomy 0.000 description 1
- 230000001133 acceleration Effects 0.000 description 1
- QGZKDVFQNNGYKY-UHFFFAOYSA-N ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 1
- PPBAJDRXASKAGH-UHFFFAOYSA-N azane;urea Chemical compound N.NC(N)=O PPBAJDRXASKAGH-UHFFFAOYSA-N 0.000 description 1
- 239000002585 base Substances 0.000 description 1
- 239000004202 carbamide Substances 0.000 description 1
- 239000003153 chemical reaction reagent Substances 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 239000010791 domestic waste Substances 0.000 description 1
- 238000002474 experimental method Methods 0.000 description 1
- 239000004744 fabric Substances 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 229910052815 sulfur oxide Inorganic materials 0.000 description 1
- -1 vanadium-titanium series Chemical class 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
Classifications
-
- 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
- B01D53/48—Sulfur compounds
- B01D53/50—Sulfur oxides
- B01D53/501—Sulfur oxides by treating the gases with a solution or a suspension of an alkali or earth-alkali or ammonium compound
- B01D53/504—Sulfur oxides by treating the gases with a solution or a suspension of an alkali or earth-alkali or ammonium compound characterised by a specific device
-
- 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
- B01D2258/00—Sources of waste gases
- B01D2258/02—Other waste gases
- B01D2258/0283—Flue gases
- B01D2258/0291—Flue gases from waste incineration plants
Abstract
The invention discloses a method and a system for purifying waste incineration flue gas. The waste incineration flue gas purification method comprises the following steps: (1) the waste incineration flue gas flows through an SNCR treatment system for denitration treatment; (2) the outlet flue gas of the SNCR treatment system enters a semi-dry reaction tower for deacidification treatment; (3) the outlet gas of the semidry reaction tower enters a bag type dust collector for dust removal treatment; (4) heating the outlet gas of the bag type dust collector, and then entering an SCR (selective catalytic reduction) reaction tower for further denitration treatment; (5) and the outlet gas of the SCR reaction tower is cooled and then enters a wet washing tower for further deacidification treatment, so that the waste incineration flue gas is purified. The invention adopts the processing technology of SNCR-semidry method-activated carbon adsorption-bag type dust removal-SCR-wet method, and can realize the high-efficiency purification treatment of the household garbage incineration flue gas.
Description
Technical Field
The invention relates to a waste incineration flue gas purification method and system, and belongs to the technical field of flue gas purification.
Background
The acceleration of the urbanization process makes the disposal of municipal solid waste a very troublesome problem. At present, in the process of treating household garbage, an incineration treatment mode is recommended, smoke generated after garbage incineration contains a large amount of harmful substances, and if the treatment does not reach the standard, the physical health of surrounding residents is affected, and serious pollution is brought to the environment. At present, the domestic common domestic garbage incineration flue gas treatment technology is an SNCR-semidry method-dry method-activated carbon adsorption-cloth bag dust removal process, and the process can control the flue gas emission index to reach the national standard. With the improvement of national environmental protection requirements and the difference of different areas, the requirements on flue gas emission indexes are more and more strict, and the requirements are difficult to achieve by simply adopting the process.
Disclosure of Invention
The invention aims to provide a method and a system for purifying waste incineration flue gas, wherein the method adopts a treatment process of SNCR-semidry method-activated carbon adsorption-bag type dust removal-SCR-wet method, and can realize high-efficiency purification treatment of the domestic waste incineration flue gas.
In the invention, the SNCR is selective non-catalytic reduction, which means that a reducing agent (ammonia water or urea) is sprayed into a temperature window suitable for denitration reaction under the action of no catalyst to reduce nitrogen oxides in flue gas into harmless nitrogen and water.
In the invention, SCR (selective catalytic reduction) refers to the process of spraying a reducing agent (ammonia or urea) under the action of a catalyst to reduce nitrogen oxides in tail gas into nitrogen and water; catalysts conventional in the art, such as honeycomb, vanadium-titanium series catalysts, may be employed.
The invention provides a waste incineration flue gas purification method, which comprises the following steps:
(1) the waste incineration flue gas flows through an SNCR treatment system for denitration treatment;
(2) the outlet flue gas of the SNCR treatment system enters a semi-dry reaction tower for deacidification treatment;
(3) the outlet gas of the semidry reaction tower enters a bag type dust collector for dust removal treatment;
(4) heating the outlet gas of the bag type dust collector, and then entering an SCR (selective catalytic reduction) reaction tower for further denitration treatment;
(5) and the outlet gas of the SCR reaction tower is cooled and then enters a wet washing tower for further deacidification treatment, so that the waste incineration flue gas is purified.
In the method for purifying waste incineration flue gas, in the step (1), the SNCR treatment system adopts ammonia water as a reducing agent, an ammonia water nozzle can be arranged on a first flue of a boiler at the outlet of the waste incinerator, ammonia water is sprayed into the flue by utilizing the high-temperature environment in the flue for denitration reaction, the concentration of NOx in the flue gas is reduced, and the concentration of the outlet of the waste heat boiler is controlled to be 200mg/Nm3The following;
the temperature of the outlet flue gas of the SNCR treatment system is 850-1100 ℃.
In the method for purifying the waste incineration flue gas, in the step (2), slaked lime is prepared into lime slurry through a pulping system, the lime slurry is sprayed into the semi-dry process reaction tower through a rotary atomizer, the flue gas entering the semi-dry process reaction tower is contacted with the highly atomized lime slurry, so that water is evaporated to reduce the smoke temperature, and sufficient neutralization reaction is carried out;
part of heavy metals and organic matters are adsorbed on dust particles, a small part of fly ash (solid phase) generated by reaction and unreacted slaked lime are discharged from the bottom of the semidry reaction tower, and most of fly ash and flue gas enter the bag-type dust collector together for discharge;
the temperature of outlet gas of the semidry method reaction tower is 140-155 ℃.
In the method for purifying the waste incineration flue gas, the tower top of the semidry method reaction tower is provided with a plurality of cooling spray guns, and the cooling spray guns are put into use during the shutdown and maintenance of the rotary atomizer, so that the temperature of the flue gas is reduced, and the removal rate of acid pollutants and the capture rate of heavy metals by a rear-end process unit are improved.
In the method for purifying the waste incineration flue gas, an activated carbon injection system and a dry powder injection system are sequentially arranged between the semidry reaction tower and the bag type dust collector;
the activated carbon injection system is used for injecting activated carbon and adsorbing heavy metals, dioxin, furan, TOC and the like;
the dry powder injection system is used for injecting slaked lime and is used as an emergency deacidification system during maintenance of the rotary atomizer in the semi-dry reaction tower; the sprayed dry slaked lime powder is fully mixed with the flue gas to remove the acid gas in the flue gas, and the unreacted materials continue to react with pollutants in the dust remover.
Specifically, the slaked lime and the activated carbon are quantitatively provided in a pneumatic conveying mode, and a pneumatic conveying system consists of a feeder, an injection fan and a conveying pipeline.
In the method for purifying waste incineration flue gas, in the step (3), the outlet gas of the semidry process reaction tower is separated from chemical reaction products (calcium chloride, calcium sulfite, calcium sulfate and the like), activated carbon for adsorbing pollutants and smoke dust when passing through the filter bag in the bag type dust collector. Meanwhile, unreacted slaked lime dry powder and active carbon powder which is not adsorbed and saturated are also attached to the surface of the filter bag to react with harmful pollutants in the smoke passing through the filter bag, so that the removal efficiency of the pollutants is further improved.
The ash removal of the bag type dust collector is a pulse back blowing mode, and the fly ash attached to the filter bag can be periodically cleaned on line/off line.
The temperature of outlet gas of the bag type dust collector is 140-155 ℃.
In the method for purifying waste incineration flue gas, in the step (4), the outlet gas of the bag-type dust collector is heated to 170-180 ℃ by a steam flue gas heater (SGH), and enters the SCR reaction tower to remove NO in the flue gasxAnd simultaneously, dioxin and furan (PCDD, PCDF) can be partially oxidized.
In the method for purifying the waste incineration flue gas, in the step (5), the outlet gas of the SCR reaction tower is cooled to 105-125 ℃ through a low-temperature flue gas reheating device (GGH).
In the method for purifying waste incineration flue gas, in the step (5), outlet gas of the SCR reaction tower is cooled and enters the wet scrubbing tower from the bottom of the wet scrubbing tower, is cooled to 60-65 ℃ after being sprayed with water, then enters the reaction part to react with sprayed circulating absorption liquid (acid-base neutralization reaction), is further sucked into the dehumidifying part, is sprayed with atomized dehumidifying liquid, and reduces the temperature of the flue gas while further absorbing residual acid gas in the flue gas, so that the saturation humidity of the flue gas is reduced, and excessive moisture in the flue gas is removed to avoid the phenomenon of 'white smoke';
in the method for purifying waste incineration flue gas, the circulating absorption liquid is caustic soda solution;
injecting alkali liquor into the circulating absorption liquid to adjust the pH value to 6-6.5 for absorbing HCl and SO in the flue gasXAcid gases such as HF;
the atomized dehumidifying liquid is caustic soda solution.
And the flue gas is discharged from the wet scrubbing tower through a chimney after being heated to about 135 ℃ by the low-temperature flue gas reheating device, so that the emission standard is met.
The waste incineration flue gas purification method can be carried out in the following waste incineration flue gas purification system:
the waste incineration flue gas purification system comprises an SNCR treatment system, a dry reaction tower, a bag type dust collector, an SCR reaction tower and a wet washing tower which are sequentially connected;
an outlet pipeline of the SCR reaction tower is communicated with the bottom of the wet scrubbing tower;
the top outlet pipeline of the wet scrubbing tower is communicated with a chimney;
nozzles are arranged at the bottom, the reaction part and the top of the wet washing tower;
the middle part of the wet scrubbing tower is the reaction part.
In the waste incineration flue gas purification system, a steam flue gas heater is arranged on an inlet pipeline of the SCR reaction tower;
and a low-temperature flue gas reheating device is arranged on an inlet pipeline of the wet scrubbing tower, and a top outlet pipeline of the wet scrubbing tower is communicated with the low-temperature flue gas reheating device.
In the waste incineration flue gas purification system, a plurality of cooling spray guns are arranged at the top of the semidry method reaction tower;
an activated carbon injection system and a dry powder injection system are sequentially arranged between the semidry reaction tower and the bag type dust collector;
the activated carbon injection system is used for injecting activated carbon; used for adsorbing heavy metal, dioxin, furan, TOC and the like;
the dry powder injection system is used for injecting slaked lime and is used as an emergency deacidification system during maintenance of the rotary atomizer in the semi-dry reaction tower; the sprayed dry slaked lime powder is fully mixed with the flue gas to remove the acid gas in the flue gas, and the unreacted materials continue to react with pollutants in the dust remover.
Specifically, the slaked lime and the activated carbon are quantitatively provided in a pneumatic conveying mode, and a pneumatic conveying system consists of a feeder, an injection fan and a conveying pipeline.
The bag type dust collector is a pulse reverse bag type dust collector.
The waste incineration flue gas purification method has the following beneficial effects:
1. high deacidification efficiency, SO2Can be reduced to 30mg/Nm3The following;
2. the denitration efficiency is high, and the emission concentration of NOx can reach 80mg/Nm3The following;
3. energy is saved, the temperature of the flue gas is increased from 150 ℃ to about 175 ℃, and the steam consumption is reduced;
4. the primary heat exchanger is reduced, the system pressure drop is reduced, and the power consumption of the induced draft fan can be reduced.
Drawings
FIG. 1 is a schematic flow chart of the waste incineration flue gas purification method of the present invention.
Detailed Description
The experimental procedures used in the following examples are all conventional procedures unless otherwise specified.
Materials, reagents and the like used in the following examples are commercially available unless otherwise specified.
The gas components in the waste incineration flue gas in the following examples are shown in table 1:
TABLE 1 content of pollutants in flue gas from refuse incineration
| Item | Design value (mg/Nm)3) |
| HCl | 1,200 |
| SO2 | 600 |
| NOx | 350 |
| TOC | |
| Particulate matter | 5,000 |
| Dioxins and dioxins | 5 |
Examples 1,
Fig. 1 is a schematic view of a waste incineration flue gas purification system according to the present invention, and the structure and treatment method of the system are described with reference to the drawing.
As shown in figure 1, an ammonia water nozzle of an SNCR system is arranged on a first flue of a boiler at the outlet of a garbage incinerator, ammonia water is sprayed into the first flue by utilizing the high-temperature environment in the first flue for denitration reaction, and NO in flue gas is converted into NOxxThe concentration is reduced and the concentration at the outlet of the waste heat boiler is ensured to be controlled at 200mg/Nm3The following.
The flue gas (about 195 ℃) at the outlet of the waste heat boiler enters a semi-dry reaction tower for the first step of deacidification treatment. The slaked lime is made into lime slurry by a pulping system and sprayed into the reaction tower through a rotary atomizer. The flue gas entering the reaction tower contacts with the highly atomized lime slurry to evaporate water to reduce the temperature of the flue gas, and sufficient neutralization reaction is carried out. Part of heavy metals and organic matters are adsorbed on dust particles. A small portion of the fly ash (solid phase) produced by the reaction is removed with unreacted slaked lime at the bottom of the reaction column. Most of fly ash and flue gas enter the bag-type dust collector together to be discharged. The flue gas discharged from the tower is about 155 ℃. Wherein, the top of each semi-dry reaction tower is provided with 6 cooling spray guns. During the period of shutdown and maintenance of the rotary atomizer, the spray gun is put into use, so that the temperature of the flue gas is reduced, and the removal rate of acid pollutants and the capture rate of heavy metals by the rear-end process unit are improved.
An activated carbon injection system and a dry powder injection system are respectively arranged between the semi-dry reaction tower and the bag-type dust remover, and the dry powder injection system is used as an emergency deacidification system when the atomizer of the semi-dry reaction tower is overhauled. The activated carbon is used for adsorbing heavy metals, dioxin, furan, TOC and the like. The sprayed dry slaked lime powder is fully mixed with the flue gas to remove the acid gas in the flue gas, and the unreacted materials continue to react with pollutants in the dust remover. The slaked lime and the active carbon are quantitatively provided in a pneumatic conveying mode, and a pneumatic conveying system consists of a feeder, an injection fan and a conveying pipeline.
Then the flue gas enters a bag type dust collector, and the flue gas and chemical reaction products (calcium chloride, calcium sulfite, calcium sulfate and the like), activated carbon for adsorbing pollutants and smoke dust are separated when the flue gas passes through a filter bag. Meanwhile, unreacted slaked lime dry powder and active carbon powder which is not adsorbed and saturated are also attached to the surface of the filter bag to react with harmful pollutants in the smoke passing through the filter bag, so that the removal efficiency of the pollutants is further improved. The ash removal of the bag type dust collector is a pulse back blowing mode, and the fly ash attached to the filter bag can be periodically cleaned on line/off line.
The flue gas at the outlet of the dust remover is about 155 ℃, is heated to 180 ℃ by a steam flue gas heater (SGH), and then enters an SCR reaction tower to remove NO in the flue gasxAnd simultaneously, dioxin and furan (PCDD, PCDF) can be partially oxidized.
SCR reaction tower outlet flue gasPart of heat recovered by a low-temperature flue gas reheating device (GGH) is reduced to about 105 ℃ and then enters a wet scrubbing tower. The wet washing tower is divided into three parts, the flue gas enters from the bottom of the tower and is firstly cooled to about 65 ℃ by water spraying, and then enters into the reaction part to carry out efficient gas-liquid exchange reaction with sprayed circulating absorption liquid (NaOH solution). Simultaneously, NaOH solution is injected into the circulating absorption liquid, the pH value of the circulating absorption liquid is adjusted to about 6, and the circulating absorption liquid is used for absorbing HCl and SO in the flue gasXAnd an acid gas such as HF. Finally, the smoke is sucked into the dehumidifying part. In the dehumidifying part, the spray nozzle above the dehumidifying part sprays atomized dehumidifying liquid, and the temperature of the smoke is reduced while the residual acid gas in the smoke is further absorbed, so that the saturation humidity of the smoke is reduced, and the redundant moisture in the smoke is separated to avoid the phenomenon of 'white smoke'.
And (4) heating the flue gas discharged from the wet scrubbing tower to about 135 ℃ through GGH, and then discharging the flue gas through a chimney.
The composition of the flue gas after the above treatment is shown in table 2:
TABLE 2 content of pollutants in the flue gas from refuse incineration treated in example 1
Comparative examples 1,
The process is carried out according to the scheme shown in FIG. 1, with the following differences: the treatment in the wet scrubber in the process of the invention is not included, and the other conditions are the same.
The composition of the final treated flue gas is shown in table 3:
TABLE 3 content of pollutants in the flue gas from refuse incineration treated in comparative example 1
Comparative examples 2,
The process is carried out according to the scheme shown in FIG. 1, with the following differences: the denitration treatment of the SCR reaction tower in the method is not included, and other conditions are the same.
The composition of the final treated smoke is shown in table 4:
TABLE 4 content of pollutants in the flue gas from refuse incineration treated in comparative example 2
Comparative examples 3,
The process is carried out according to the scheme shown in FIG. 1, with the following differences: the treatment in the SCR reactor and the wet scrubber in the process of the invention is excluded, and the other conditions are the same.
The composition of the final treated smoke is shown in table 5:
TABLE 5 content of pollutants in the flue gas from refuse incineration treated in comparative example 3
Comparing the data of example 1 and comparative examples 1-3, it can be seen that the cleaning method (combined process) of the present invention is used to remove SO from flue gasxAnd NOxAll have obvious effects, wherein, the wet washing tower is mainly used for removing SOxSCR reaction towers are used primarily for removing NOx。
Claims (10)
1. A waste incineration flue gas purification method comprises the following steps:
(1) the waste incineration flue gas flows through an SNCR treatment system for denitration treatment;
(2) the outlet flue gas of the SNCR treatment system enters a semi-dry reaction tower for deacidification treatment;
(3) the outlet gas of the semidry reaction tower enters a bag type dust collector for dust removal treatment;
(4) heating the outlet gas of the bag type dust collector, and then entering an SCR (selective catalytic reduction) reaction tower for further denitration treatment;
(5) and the outlet gas of the SCR reaction tower is cooled and then enters a wet washing tower for further deacidification treatment, so that the waste incineration flue gas is purified.
2. The method for purifying waste incineration flue gas according to claim 1, characterized in that: in the step (1), ammonia water is adopted as a reducing agent by the SNCR treatment system;
the temperature of the outlet flue gas of the SNCR treatment system is 850-1100 ℃.
3. The method for purifying waste incineration flue gas according to claim 1 or 2, characterized in that: in the step (2), lime slurry is sprayed into the semidry method reaction tower through a rotary atomizer;
the temperature of outlet gas of the semidry method reaction tower is 140-155 ℃.
4. The method for purifying waste incineration flue gas according to claim 3, characterized in that: the tower top of the semidry method reaction tower is provided with a plurality of cooling spray guns;
an activated carbon injection system and a dry powder injection system are sequentially arranged between the semidry reaction tower and the bag type dust collector;
the activated carbon injection system is used for injecting activated carbon;
the dry powder injection system is used for injecting slaked lime;
in the step (3), the bag type dust collector is a pulse reverse bag type dust collector;
the temperature of outlet gas of the bag type dust collector is 140-155 ℃.
5. The method for purifying waste incineration flue gas according to any one of claims 1 to 4, characterized by: in the step (4), outlet gas of the bag type dust collector is heated to 170-180 ℃ by a steam and flue gas heater;
in the step (5), the outlet gas of the SCR reaction tower is cooled to 105-125 ℃ through a low-temperature flue gas reheating device.
6. The method for purifying waste incineration flue gas according to any one of claims 1 to 5, characterized by: in the step (5), the outlet gas of the SCR reaction tower is cooled and then enters the wet scrubbing tower from the bottom of the wet scrubbing tower, is cooled to 60-65 ℃ after being sprayed with water, then enters the reaction part to react with the sprayed circulating absorption liquid, is further sucked into the dehumidifying part, and is sprayed with the atomized dehumidifying liquid.
7. The method for purifying waste incineration flue gas according to claim 8, characterized in that: the circulating absorption liquid is caustic soda solution;
injecting alkali liquor into the circulating absorption liquid to adjust the pH value to 6-6.5;
the atomized dehumidifying liquid is caustic soda solution.
8. A waste incineration flue gas purification system comprises an SNCR treatment system, a dry reaction tower, a bag type dust collector, an SCR reaction tower and a wet washing tower which are connected in sequence;
an outlet pipeline of the SCR reaction tower is communicated with the bottom of the wet scrubbing tower;
the top outlet pipeline of the wet scrubbing tower is communicated with a chimney;
nozzles are arranged at the bottom, the reaction part and the top of the wet washing tower;
the middle part of the wet scrubbing tower is the reaction part.
9. The waste incineration flue gas purification system according to claim 8, characterized in that: a steam flue gas heater is arranged on an inlet pipeline of the SCR reaction tower;
and a low-temperature flue gas reheating device is arranged on an inlet pipeline of the wet scrubbing tower, and a top outlet pipeline of the wet scrubbing tower is communicated with the low-temperature flue gas reheating device.
10. The waste incineration flue gas purification system according to claim 8 or 9, characterized in that: the tower top of the semidry method reaction tower is provided with a plurality of cooling spray guns;
an activated carbon injection system and a dry powder injection system are sequentially arranged between the semidry reaction tower and the bag type dust collector;
the activated carbon injection system is used for injecting activated carbon;
the dry powder injection system is used for injecting slaked lime;
the bag type dust collector is a pulse reverse bag type dust collector.
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN113559690A (en) * | 2021-07-23 | 2021-10-29 | 浙江大学 | Integrated purification system and method for waste incineration flue gas and fly ash |
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| WO2017059820A1 (en) * | 2015-10-09 | 2017-04-13 | 广州特种承压设备检测研究院 | Reduction and oxidation combined denitration system and denitration method therefor |
| CN106621754A (en) * | 2016-12-31 | 2017-05-10 | 上海康恒环境股份有限公司 | Garbage incineration fume ultralow emission purifying system |
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| WO2017059820A1 (en) * | 2015-10-09 | 2017-04-13 | 广州特种承压设备检测研究院 | Reduction and oxidation combined denitration system and denitration method therefor |
| CN106621754A (en) * | 2016-12-31 | 2017-05-10 | 上海康恒环境股份有限公司 | Garbage incineration fume ultralow emission purifying system |
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