CN117190227A - Advanced treatment system for dioxin and sulfur dioxide in flue gas of waste gas liquid incinerator - Google Patents
Advanced treatment system for dioxin and sulfur dioxide in flue gas of waste gas liquid incinerator Download PDFInfo
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- CN117190227A CN117190227A CN202311464651.1A CN202311464651A CN117190227A CN 117190227 A CN117190227 A CN 117190227A CN 202311464651 A CN202311464651 A CN 202311464651A CN 117190227 A CN117190227 A CN 117190227A
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- flue gas
- heat boiler
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- dioxin
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- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 title claims abstract description 120
- 239000003546 flue gas Substances 0.000 title claims abstract description 120
- RAHZWNYVWXNFOC-UHFFFAOYSA-N Sulphur dioxide Chemical compound O=S=O RAHZWNYVWXNFOC-UHFFFAOYSA-N 0.000 title claims abstract description 64
- 239000007788 liquid Substances 0.000 title claims abstract description 34
- HGUFODBRKLSHSI-UHFFFAOYSA-N 2,3,7,8-tetrachloro-dibenzo-p-dioxin Chemical compound O1C2=CC(Cl)=C(Cl)C=C2OC2=C1C=C(Cl)C(Cl)=C2 HGUFODBRKLSHSI-UHFFFAOYSA-N 0.000 title claims abstract 13
- 239000002912 waste gas Substances 0.000 title claims description 29
- 239000002918 waste heat Substances 0.000 claims abstract description 69
- 238000006477 desulfuration reaction Methods 0.000 claims abstract description 57
- 230000023556 desulfurization Effects 0.000 claims abstract description 57
- 239000000428 dust Substances 0.000 claims abstract description 55
- 239000007789 gas Substances 0.000 claims abstract description 36
- 238000010791 quenching Methods 0.000 claims abstract description 28
- 230000000171 quenching effect Effects 0.000 claims abstract description 28
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 69
- 229910052799 carbon Inorganic materials 0.000 claims description 24
- 238000005507 spraying Methods 0.000 claims description 20
- UIIMBOGNXHQVGW-UHFFFAOYSA-M Sodium bicarbonate Chemical compound [Na+].OC([O-])=O UIIMBOGNXHQVGW-UHFFFAOYSA-M 0.000 claims description 18
- 238000000034 method Methods 0.000 claims description 12
- VHUUQVKOLVNVRT-UHFFFAOYSA-N Ammonium hydroxide Chemical compound [NH4+].[OH-] VHUUQVKOLVNVRT-UHFFFAOYSA-N 0.000 claims description 11
- 235000011114 ammonium hydroxide Nutrition 0.000 claims description 11
- 238000002347 injection Methods 0.000 claims description 10
- 239000007924 injection Substances 0.000 claims description 10
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 claims description 10
- 230000008569 process Effects 0.000 claims description 9
- 229910000030 sodium bicarbonate Inorganic materials 0.000 claims description 9
- 235000017557 sodium bicarbonate Nutrition 0.000 claims description 9
- 239000000243 solution Substances 0.000 claims description 9
- 230000003009 desulfurizing effect Effects 0.000 claims description 7
- 239000007921 spray Substances 0.000 claims description 7
- 239000003795 chemical substances by application Substances 0.000 claims description 5
- 239000003345 natural gas Substances 0.000 claims description 5
- 239000007787 solid Substances 0.000 claims description 4
- 239000003638 chemical reducing agent Substances 0.000 claims description 3
- 239000013505 freshwater Substances 0.000 claims description 3
- KVGZZAHHUNAVKZ-UHFFFAOYSA-N 1,4-Dioxin Chemical compound O1C=COC=C1 KVGZZAHHUNAVKZ-UHFFFAOYSA-N 0.000 description 52
- 239000000463 material Substances 0.000 description 6
- 239000000779 smoke Substances 0.000 description 6
- 239000002699 waste material Substances 0.000 description 6
- 239000002253 acid Substances 0.000 description 5
- 239000002245 particle Substances 0.000 description 5
- 150000003839 salts Chemical class 0.000 description 5
- 238000004062 sedimentation Methods 0.000 description 5
- 239000002893 slag Substances 0.000 description 5
- 239000011734 sodium Substances 0.000 description 5
- 238000003860 storage Methods 0.000 description 5
- 238000006243 chemical reaction Methods 0.000 description 4
- 238000004519 manufacturing process Methods 0.000 description 4
- 239000002351 wastewater Substances 0.000 description 4
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 4
- 239000003513 alkali Substances 0.000 description 3
- 230000003197 catalytic effect Effects 0.000 description 3
- 230000000052 comparative effect Effects 0.000 description 3
- 238000001816 cooling Methods 0.000 description 3
- 239000004744 fabric Substances 0.000 description 3
- 238000012544 monitoring process Methods 0.000 description 3
- 239000000126 substance Substances 0.000 description 3
- 231100000419 toxicity Toxicity 0.000 description 3
- 230000001988 toxicity Effects 0.000 description 3
- NLXLAEXVIDQMFP-UHFFFAOYSA-N Ammonium chloride Substances [NH4+].[Cl-] NLXLAEXVIDQMFP-UHFFFAOYSA-N 0.000 description 2
- ZAMOUSCENKQFHK-UHFFFAOYSA-N Chlorine atom Chemical compound [Cl] ZAMOUSCENKQFHK-UHFFFAOYSA-N 0.000 description 2
- CDBYLPFSWZWCQE-UHFFFAOYSA-L Sodium Carbonate Chemical compound [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 description 2
- PMZURENOXWZQFD-UHFFFAOYSA-L Sodium Sulfate Chemical compound [Na+].[Na+].[O-]S([O-])(=O)=O PMZURENOXWZQFD-UHFFFAOYSA-L 0.000 description 2
- 230000002378 acidificating effect Effects 0.000 description 2
- 230000009471 action Effects 0.000 description 2
- QGZKDVFQNNGYKY-UHFFFAOYSA-N ammonia Natural products N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 2
- 238000010531 catalytic reduction reaction Methods 0.000 description 2
- 239000000460 chlorine Substances 0.000 description 2
- 229910052801 chlorine Inorganic materials 0.000 description 2
- 238000004140 cleaning Methods 0.000 description 2
- 238000002485 combustion reaction Methods 0.000 description 2
- 239000003517 fume Substances 0.000 description 2
- 229910052938 sodium sulfate Inorganic materials 0.000 description 2
- 235000011152 sodium sulphate Nutrition 0.000 description 2
- 238000003786 synthesis reaction Methods 0.000 description 2
- VEXZGXHMUGYJMC-UHFFFAOYSA-M Chloride anion Chemical compound [Cl-] VEXZGXHMUGYJMC-UHFFFAOYSA-M 0.000 description 1
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 1
- 238000000889 atomisation Methods 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000007664 blowing Methods 0.000 description 1
- 230000000711 cancerogenic effect Effects 0.000 description 1
- 231100000315 carcinogenic Toxicity 0.000 description 1
- 239000003054 catalyst Substances 0.000 description 1
- 239000003153 chemical reaction reagent Substances 0.000 description 1
- 230000007797 corrosion Effects 0.000 description 1
- 238000005260 corrosion Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 239000003344 environmental pollutant Substances 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 230000002427 irreversible effect Effects 0.000 description 1
- 230000007774 longterm Effects 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 231100000219 mutagenic Toxicity 0.000 description 1
- 230000003505 mutagenic effect Effects 0.000 description 1
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- 231100000719 pollutant Toxicity 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 238000006722 reduction reaction Methods 0.000 description 1
- 238000012958 reprocessing Methods 0.000 description 1
- 229910000029 sodium carbonate Inorganic materials 0.000 description 1
- 159000000000 sodium salts Chemical class 0.000 description 1
- 239000004071 soot Substances 0.000 description 1
- 238000001179 sorption measurement Methods 0.000 description 1
- 229910052717 sulfur Inorganic materials 0.000 description 1
- 239000011593 sulfur Substances 0.000 description 1
- 231100000378 teratogenic Toxicity 0.000 description 1
- 230000003390 teratogenic effect Effects 0.000 description 1
- 230000008016 vaporization Effects 0.000 description 1
- 238000005406 washing Methods 0.000 description 1
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- Treating Waste Gases (AREA)
Abstract
The invention discloses a deep treatment system for dioxin and sulfur dioxide in flue gas of an exhaust gas liquid incinerator, which comprises an incinerator, a waste heat boiler and a tail gas treatment unit which are sequentially connected in series, wherein an SNCR denitration device is connected between the incinerator and the waste heat boiler in series, the waste heat boiler is provided with a bypass pipeline, the bypass pipeline is connected with a quenching desulfurization tower in series, and the quenching desulfurization tower is connected with the tail gas treatment unit in series. The advanced treatment system designs two working conditions of the waste heat boiler, and the two working conditions can be switched appropriately, SO that dioxin and SO in the flue gas are realized 2 And dust can reach the discharge standard at the same time.
Description
Technical Field
The invention relates to an advanced treatment system for dioxin and sulfur dioxide in flue gas of an exhaust gas liquid incinerator, and belongs to the technical field of exhaust gas treatment.
Background
When the waste gas liquid incinerator is used for incinerating waste gas liquid at high temperature, generated sulfur dioxide and dust are one of main pollutants of boiler flue gas, and secondary pollution is inevitably generated; in addition, when chloride ions are contained in the burned material, dioxin is generated when the burned material is incompletely burned, the dioxin is an organic compound with stronger biological toxicity, has irreversible teratogenic, carcinogenic and mutagenic toxicity, is regarded as one of the most dangerous chemical substances in the world, and is difficult to naturally degrade and eliminate once the burned material is permeated into the environment, so the burned material has the name of century toxicity, and the smoke cannot reach the standard.
In the prior art, most of the waste gas purifying facilities for dust removal, desulfurization, dioxin removal and the like are arranged for dust removal, desulfurization and dioxin reduction, but in the prior art, dioxin and SO are purified 2 The treatment efficiency is low, and the dioxin and sulfur dioxide in the flue gas cannot be treated systematically at the same time, SO the method provides a method for treating the dioxin and SO in the flue gas after the high-temperature incineration treatment of the gas-liquid incinerator 2 And the content reaches the advanced treatment system of the emission at the same time.
Disclosure of Invention
At least aiming at one problem existing in the prior art, the invention provides a deep treatment system for dioxin and sulfur dioxide in flue gas of an exhaust gas liquid incinerator, which can realize the dioxin and SO in the flue gas 2 And the dust content reaches the standard and is discharged.
In order to achieve the above purpose, the present invention adopts the following technical scheme: the advanced treatment system comprises an incinerator, a waste heat boiler and a tail gas treatment unit which are sequentially connected in series, wherein an SNCR denitration device is connected between the incinerator and the waste heat boiler in series, the waste heat boiler is provided with a bypass pipeline, the bypass pipeline is connected with a quenching desulfurization tower in series, and the quenching desulfurization tower is connected with the tail gas treatment unit in series.
Preferably, the tail gas treatment unit comprises a desulfurization device, a primary bag-type dust remover, an SCR denitration device and a secondary bag-type dust remover which are sequentially connected in series, wherein the desulfurization device is respectively connected with the waste heat boiler and the quenching desulfurization tower in series, an active carbon injection device is connected on a pipeline, communicated with the SCR denitration device, of the primary bag-type dust remover in series, and the secondary bag-type dust remover is connected with a chimney in series.
Preferably, the waste heat boiler comprises two working conditions of the waste heat boiler:
waste heat boiler working condition one: the high-temperature flue gas is directly cooled to 200 ℃ by a waste heat boiler and enters a tail gas treatment unit for treatment;
and the working condition of the waste heat boiler is II: the high-temperature flue gas enters a quenching desulfurization tower from a bypass pipeline, so that the high-temperature flue gas is cooled from 500 ℃ to 200 ℃ within 1s, and then enters a tail gas treatment unit for treatment;
the first working condition of the waste heat boiler and the second working condition of the waste heat boiler are timely switched through a plate flue gate valve;
and when the dioxin of the chimney flue gas does not reach the emission standard, switching to a second working condition of the waste heat boiler.
Preferably, the outlet temperature of the waste heat boiler is 200 ℃.
Preferably, the bypass pipeline is arranged at the position of the exhaust-heat boiler with the flue gas temperature of 500 ℃, and the outlet temperature of the quenching desulfurization tower is 200 ℃.
Preferably, atomized fresh water is sprayed in the quenching desulfurization tower.
Preferably, the desulfurization device adopts a dry desulfurization process, and sodium bicarbonate is used as a desulfurizing agent.
Preferably, the baking soda is solid, and the spraying amount of the baking soda is 60-90 kg/h.
Preferably, the SNCR denitration device and the SCR denitration device both use ammonia water solution as a reducing agent.
Preferably, the mass concentration of the ammonia water solution is 25%, and the spraying amount of the ammonia water solution is 20-50 kg/h.
Preferably, the activated carbon sprayed by the activated carbon spraying device is sprayed in an amount of 2-5 kg/h.
Preferably, the incinerator adopts natural gas ignition and afterburning, and the temperature in the incinerator is controlled to be more than or equal to 1100 ℃.
Preferably, a wall vibrator is arranged in the waste heat boiler.
The invention has the beneficial effects that:
1. the advanced treatment system for dioxin and sulfur dioxide in the flue gas of the waste gas liquid incinerator is characterized in that two working conditions are designed in a waste heat boiler, and the two working conditions can be properly switched, SO that the dioxin and SO in the flue gas generated by the incineration of the waste gas liquid treated by the advanced treatment system 2 And dust can reach the discharge standard at the same time.
2. According to the advanced treatment system for dioxin and sulfur dioxide in flue gas of the waste gas liquid incinerator, disclosed by the invention, the outlet temperature of the waste heat boiler is controlled to be less than 200 ℃, so that the generation of dioxin can be inhibited.
3. According to the advanced treatment system for dioxin and sulfur dioxide in the flue gas of the waste gas liquid incinerator, the bypass pipeline is started at the waste heat boiler to form the working condition II of the waste heat boiler, so that the temperature of the high-temperature flue gas can be reduced from 500 ℃ to 200 ℃ within 1s, the re-synthesis of dioxin in a low-temperature region is avoided, and the acid gas in the flue gas is also removed by taking alkali liquor as a main component.
4. The advanced treatment system for dioxin and sulfur dioxide in flue gas of the waste gas liquid incinerator provided by the invention has the advantages that the desulfurization device uses sodium bicarbonate for desulfurization, no wastewater is discharged, the generated sodium sulfate is subjected to sedimentation trapping by sedimentation ash, and meanwhile, SO in the flue gas is subjected to sedimentation trapping 2 The content reaches the standard and is discharged;
5. the advanced treatment system for dioxin and sulfur dioxide in the flue gas of the waste gas liquid incinerator disclosed by the invention uses the two-stage bag-type dust remover, so that excellent removal of dust and active carbon in the flue gas is realized, and the dust content in the flue gas reaches the standard.
6. The advanced treatment system for dioxin and sulfur dioxide in the flue gas of the waste gas liquid incinerator controls the incineration temperature of the incinerator to be not less than 1100 ℃, so that chlorine-containing materials are completely combusted, and the generation amount of dioxin is reduced.
Drawings
FIG. 1 is a process flow diagram of a deep treatment system for dioxin and sulfur dioxide in flue gas of an exhaust gas liquid incinerator.
Detailed Description
The invention will now be more clearly and more fully described by way of the following specific examples, which are not intended to be limiting.
The specific conditions are not noted in the examples and are carried out according to conventional conditions or conditions recommended by the manufacturer. The reagents or instruments, equipment or devices used are conventional products commercially available without the manufacturer's knowledge.
Waste gas and waste liquid from outside the boundary area enter the incinerator to burn through a waste gas and waste liquid supply system, and the pressure is controlled at micro negative pressureOxidizing all harmful organic matters in the waste gas liquid into SO 2 、CO 2 、H 2 O、N 2 The waste gas passes through a bag-type dust collector, an SCR and a washing tower to meet the emission requirement; the flue gas generated after incineration contains a large amount of heat, a waste heat boiler is arranged to recycle the heat in the flue gas, 2.0MPaG is generated, and the steam at 250 ℃ is merged into a pipe network; however, dioxin can be generated when the incineration is incomplete, so that the incineration flue gas can not reach the emission standard, and how to systematically treat the dioxin and sulfur dioxide in the flue gas simultaneously so as to reach the emission standard of the incineration flue gas.
Example 1
Advanced treatment system for dioxin and sulfur dioxide in flue gas of waste gas liquid incinerator is shown in fig. 1:
the advanced treatment system comprises an incinerator, a waste heat boiler and a tail gas treatment unit which are sequentially connected in series, wherein an SNCR denitration device is connected between the incinerator and the waste heat boiler in series; the tail gas treatment unit can remove dust and SO in the flue gas 2 And the flue gas desulfurization device is characterized in that a desulfurization device, a primary bag-type dust collector, an SCR denitration device and a secondary bag-type dust collector which are sequentially connected in series are arranged, an active carbon spraying device is arranged on a pipeline which is communicated with the primary bag-type dust collector and the SCR denitration device, the secondary bag-type dust collector is communicated with a chimney, a bypass pipeline is arranged for enabling the dioxin in the flue gas to reach the emission standard, the bypass pipeline is communicated with a quenching desulfurization tower, and the quenching desulfurization tower is connected with a tail gas treatment unit in series, and is also connected with the desulfurization device in series.
The incinerator is ignited by natural gas, the temperature in the incinerator reaches 1100 ℃ and is not lower than 1100 ℃, waste tar (BPA tar), waste water, waste gas and slack gas are combusted and treated, high-temperature flue gas at 1100 ℃ and high-temperature molten salt slag at 1100 ℃ are generated, the high-temperature flue gas is further treated and a large amount of heat in the flue gas is recovered, the high-temperature flue gas enters a waste heat boiler through a high-temperature expansion joint and a plate flue gate valve, the high-temperature molten salt slag flows into the bottom along the inner wall of the incinerator and then enters a jacketed water-cooling double-screw crushing conveyor for cooling and crushing, and the cooled and crushed waste salt slag is conveyed to a storage bin through a scraper conveyor; the burning temperature of the incinerator is controlled to be more than or equal to 1100 ℃, so that chlorine-containing materials are completely burnt, the production amount of dioxin can be reduced, and the influence of the burning temperature of the incinerator on the dioxin is avoided.
Specifically, the waste heat boiler sends the process water into the waste heat boiler, high-temperature flue gas with the temperature of 1100 ℃ from the incinerator is sent into the waste heat boiler, the high-temperature flue gas and the process water are subjected to heat replacement, and the process water absorbs the heat of the high-temperature flue gas to generate steam which can be used for production.
Under the existing normal condition, the working condition of the waste heat boiler is as follows: the high-temperature flue gas is cooled to 200 ℃ through a superheating section and a medium-saving section of the waste heat boiler and enters a tail gas treatment unit for treatment, wherein an activated carbon injection device injects activated carbon to adsorb dioxin.
If the dioxin in the flue gas can not reach the emission standard through the adsorption of activated carbon under the working condition of the waste heat boiler, the advanced treatment system of the invention is provided with the bypass pipeline, the bypass pipeline is communicated with the quenching desulfurization tower, the quenching desulfurization tower and the desulfurization device are arranged in series, the high-temperature flue gas is controlled to enter the quenching desulfurization tower from the bypass pipeline of the waste heat boiler, atomized alkali liquor is sprayed in the quenching desulfurization tower, the temperature of the high-temperature flue gas is reduced from 500 ℃ to 200 ℃ within 1s, the re-synthesis of the dioxin in a low-temperature interval is avoided, meanwhile, the acid gas in the flue gas is removed, and then the flue gas sequentially enters the desulfurization device and the tail gas treatment unit for reprocessing, and the flue gas reaches the emission standard.
In the embodiment of the invention, the working conditions of the waste heat boiler of the advanced treatment system comprise two types: waste heat boiler working condition one: the high-temperature flue gas is cooled to 200 ℃ through a superheating section and a medium-saving section of the waste heat boiler, and enters a tail gas treatment unit for treatment; and the working condition of the waste heat boiler is II: the high-temperature flue gas enters a quenching desulfurization tower through a bypass pipeline of the waste heat boiler, so that the high-temperature flue gas is cooled from 500 ℃ to 200 ℃ within 1s, and then enters a tail gas treatment unit for treatment; the working condition I of the waste heat boiler and the working condition II of the waste heat boiler are timely switched through the plate flue gate valve. In the advanced treatment system, the high-temperature flue gas is cooled from 500 ℃ to 200 ℃ in 1s through the second working condition of the waste heat boiler, so that the generation of dioxin is effectively inhibited.
In addition, in order to prevent the dust deposit corrosion in the waste heat boiler, a wall vibrator is arranged in the waste heat boiler, so that sodium salt is effectively prevented from adhering to a heating surface, the boiler operation parameters reach the design requirements, and the long-term operation of the waste heat boiler is ensured.
In the embodiment of the invention, the quenching desulfurization tower is used for reducing the temperature of the flue gas from 500 ℃ to 200 ℃ within 1s, preventing the resynthesis of dioxin in a low-temperature zone, and simultaneously removing the acid gas in the flue gas, so that a bypass pipeline communicated with the quenching desulfurization tower and a waste heat boiler is arranged at the position of the waste heat boiler, the flue gas temperature of the quenching desulfurization tower is 500 ℃, and the quenching desulfurization tower sprays alkali liquor with a certain concentration to reduce the temperature of the flue gas in a spray atomization mode.
Specifically, an SNCR denitration device belongs to furnace denitration, NOx is controlled by adopting an illegal catalytic method, ammonia water is used as a reducing agent, ammonia water solution is sprayed into an incinerator by a denitration spray gun of the SNCR denitration device, and NH is carried out within the temperature range of 850-1100 DEG C 3 React with NOx in the flue gas to generate N 2 And H 2 O, ensuring that the emission concentration of NOx in the flue gas reaches the standard, and simultaneously, completely vaporizing and taking away the moisture by the flue gas; the chemical reaction formula is as follows: 4NH 3 +4NO+O 2 →4N 2 +6H 2 O。
Specifically, the tail gas treatment unit is used for removing dust and SO in the flue gas 2 The dioxin is adsorbed by the activated carbon, after the heat of the waste heat boiler is recovered, the flue gas firstly enters a desulfurization device for sulfur dioxide and other acid mediums, then enters a primary bag-type dust collector for collecting and removing dust for the first time, and then enters an SCR denitration device for selective catalytic reduction of NOx in a tail flue to N 2 And H 2 O, and adopt active carbon to adsorb the treatment to the flue gas in the pipeline between one-level sack cleaner and SCR denitrification facility, this active carbon sprays the active carbon through active carbon injection device and gets into in one-level sack cleaner and the pipeline of SCR denitrification facility, further adsorbs dioxin, then gets into second grade sack cleaner and carries out the active carbon collection to adsorb dioxin and get rid of and then realize dust, SO in the flue gas 2 The dioxin is discharged up to the standard; tail gas treatment sheetThe flue gas desulfurization device comprises a desulfurization device, a primary cloth bag dust remover, an SCR denitration device and a secondary cloth bag dust remover which are sequentially connected in series, wherein an active carbon spraying device is arranged on a pipeline which is communicated with the SCR denitration device, the secondary cloth bag dust remover is communicated with a chimney, and the chimney is used for monitoring harmful substances in flue gas on line.
In an embodiment of the invention, the desulfurization device adopts a dry flue gas desulfurization process, and uses baking soda (NaHCO 3 ) Spraying baking soda into desulfurizing unit to obtain high temperature gas of 200 deg.c from afterheat boiler or quenching desulfurizing tower to spray NaHCO as desulfurizing agent 3 The activated surface forms a micropore structure, and flue gas in the desulfurization device is fully contacted with the activated desulfurizing agent to generate chemical reaction, SO in the flue gas 2 The acid medium is absorbed cleanly; the sodium sulfate is also subjected to sedimentation trapping by sedimentation ash by utilizing a dry flue gas desulfurization process; the chemical reaction formula is as follows: the main reaction:
（1）2NaHCO 3 (s)=Na 2 CO 3 (S)+H 2 O(g)+CO 2 (g)
（2）SO 2 (g)+Na 2 CO 3 (s)+1/2O 2 =Na 2 SO 4 (s)+CO 2 (g)
（3）SO 3 (g)+Na 2 CO3(s)=Na 2 SO 4 (s)+CO 2 (g)。
in addition, the desulfurization device comprises a desulfurizing agent storage and conveying system, a desulfurization ash recycling system, a flue system and a compressed air system.
In the embodiment of the invention, the SCR denitration device belongs to tail flue denitration, adopts selective catalytic reduction to control NOx under the action of a catalyst, and adds NH 3 Can convert NOx into N naturally contained in air 2 And H 2 O。
In the embodiment of the invention, the active carbon powder is injected into a pipeline of the primary bag-type dust collector and the SCR denitration device through an injection pump, the active carbon injection device comprises an active carbon storage bin, and a pressure release valve and a bin top filter are arranged at the top of the active carbon storage bin; the sprayed active carbon is conveyed by a Roots blower to be mixed with the flue gas.
In the embodiment of the invention, the primary bag-type dust remover and the secondary bag-type dust remover automatically remove and collect dust in the flue gas on line, the finally treated flue gas is discharged through a chimney, and the upper part of the chimney is provided with a flue gas on-line monitoring system for monitoring harmful substances in the flue gas on line; under the action of an induced draft fan, dust-containing flue gas enters a primary bag-type dust remover or a secondary bag-type dust remover, coarser dust particles are settled into an ash bucket under the impact of dead weight and a bag, and finer and lighter dust particles are adsorbed on the outer surface of a filter bag to gradually form a layer of filter bed, so that fine dust particles are prevented from entering the bag; the pulse soot blowing system in the primary bag-type dust remover or the secondary bag-type dust remover is automatically started along with the increase of dust attached to the outer surface of the bag, compressed air is blown outwards from the bag, so that ash particles fall off and fall into an ash bucket to be discharged through an ash discharging valve; the clean flue gas is discharged from the upper clean room of the primary bag-type dust collector or the secondary bag-type dust collector.
Example 2
Based on the example 1, waste water having a salt content of less than 3.8% was used as waste gas liquid to be treated for waste tar having a low heat value of 8660kcal/kg and waste gas having a heat value of 7432 kcal/kg.
The total amount of waste tar was 5000kg/h, and the total amount of waste gas was 1650Nm 3 Feeding the wastewater into an incinerator according to the total amount of 16000kg/h, wherein the heat value is 8500kcal/m 3 The natural gas is ignited in the incinerator to heat and the total amount of the natural gas is less than or equal to 1000m 3 Carrying out afterburning, controlling the burning temperature of an incinerator to be more than or equal to 1100 ℃, generating high-temperature flue gas at 1100 ℃ to enter a waste heat boiler, spraying ammonia water solution with the mass concentration of 25% of 20-50 kg/h into the incinerator by a denitration spray gun of an SNCR denitration device to treat NOx, sending process water into the waste heat boiler to carry out heat replacement to form steam, wherein the steam yield is 46t/h, selecting the first working condition of the waste heat boiler, directly cooling the high-temperature flue gas to 200 ℃ by the waste heat boiler to enter a desulfurization device, and spraying solid NaHCO (sodium carbonate) with the mass concentration of 60-90 kg/h into the desulfurization device 3 Treatment of SO 2 And its acidic medium for removing SO 2 The flue gas enters a primary bag-type dust collector to carry out dust on the flue gasTreatment to remove SO 2 The flue gas of dust gets into SCR denitrification facility to before the flue gas gets into SCR denitrification facility with the active carbon that active carbon injection apparatus spouted, the active carbon spouts the volume and is 2~5kg/h, the active carbon adsorbs the flue gas, adsorb dioxin, spout in SCR denitrification facility and have 20~50 kg/h's 25% aqueous ammonia solution to carry out catalytic treatment to remaining NOx, then get into one-level sack cleaner and handle the active carbon of flue gas, the flue gas after the cleaning detects through the chimney, the content emission standard of dioxin, SO2, NOx, smoke and dust in the flue gas is as shown in table 1, detect SO2, NOx, the content of smoke and dust reaches emission standard, the fume emission.
The incinerator generates high-temperature molten salt slag at 1100 ℃ and discharges the slag into a storage bin.
TABLE 1
Example 3
On the basis of the embodiment 2, the combustion of the waste gas liquid is continued, the cleaned flue gas is detected by a chimney, the content of dioxin is found to exceed the emission standard shown in the table 1, the spraying amount of the activated carbon is continuously increased, the spraying amount of the activated carbon is up to 12kg/h, the cleaned flue gas is detected by the chimney, the content of the dioxin can be discharged, and the phenomenon that the content of the dioxin exceeds the standard can occur when the waste gas liquid is not completely burnt for too long.
Example 4
The combustion of the exhaust gas liquid on the basis of example 2, the flue gas after cleaning was detected by a chimney, and it was found that the content of dioxin exceeded the emission standard described in table 1, or on the basis of example 3, even if the amount of activated carbon was greatly increased, the removal effect of dioxin could not reach the emission standard, and therefore, the exhaust-heat boiler condition one was switched to the exhaust-heat boiler condition two by using the plate flue gate valve, and the exhaust-heat boiler condition two was treated with high-temperature flue gas: the high-temperature flue gas enters a quenching desulfurization tower from a bypass pipeline of a preheating boiler, and atomized fresh water is sprayed into the quenching desulfurization tower, so that the temperature of the flue gas is reduced from 500 ℃ to 200 ℃ within 1s, and the flue gas is removed from quenchingThe flue gas from the sulfur tower enters a desulfurization device, and 60-90 kg/h of solid NaHCO is sprayed into the desulfurization device 3 Treatment of SO 2 And its acidic medium for removing SO 2 The flue gas enters a primary bag-type dust remover to treat dust of the flue gas, SO as to remove SO 2 The flue gas of dust gets into SCR denitrification facility to before the flue gas gets into SCR denitrification facility with the active carbon that active carbon injection apparatus spouted, the active carbon spouts the volume and is 1~3kg/h, the active carbon adsorbs the flue gas, adsorb dioxin, spout in SCR denitrification facility and have 20~50 kg/h's 25% aqueous ammonia solution to carry out catalytic treatment to remaining NOx, reentry one-level sack cleaner and handle the active carbon of flue gas after, the flue gas after the cleanness detects through the chimney, detect SO2, NOx, smoke and dust, the content of dioxin reaches the emission standard shown in table 1, the fume emission.
Comparative example 1
Based on example 2, the spraying amount of the activated carbon was adjusted to be 1.5kg/h, and the cleaned flue gas was detected by a chimney to detect the contents of SO2, NOx and smoke to the emission standards shown in Table 1, but the content of dioxin did not reach the emission standards shown in Table 1.
Comparative example 2
Based on example 3, only the spraying amount of the activated carbon was adjusted, the spraying amount of the activated carbon was 0.8kg/h, and the cleaned flue gas was detected by a chimney, and the contents of SO2, NOx and smoke were detected to reach the emission standards shown in Table 1, and dioxin did not reach the emission standards shown in Table 1.
Compared with comparative examples 1 and 2, in the embodiment 2 and 4, in the advanced treatment system of dioxin and sulfur dioxide in flue gas of the waste gas liquid incinerator, the spraying amount of activated carbon is 1-5 kg/h, and the content of dioxin can be discharged as standard; however, in actual production, the injection amount of the activated carbon exceeds 10kg/h, so that the cost of the activated carbon is increased, and the injection amount of the activated carbon is lower than 1kg/h, so that the emission of dioxin is not up to standard; therefore, the spraying amount of the activated carbon is proper at 1-5 kg/h, and the production cost is reduced.
The activated carbon in examples 2 to 3 has a particle size of 325 mesh and a specific surface area of more than 900m 2 /g。
Finally, it should be noted that the above-mentioned embodiments only illustrate rather than limit the technical solution of the present invention, and although the present invention has been described in detail with reference to the above-mentioned embodiments, it should be understood by those skilled in the art that the present invention may be modified or equivalently replaced without departing from the spirit and scope of the present invention, and any modification or partial replacement thereof should be included in the scope of the claims of the present invention.
Claims (9)
1. The advanced treatment system for dioxin and sulfur dioxide in the flue gas of the waste gas liquid incinerator is characterized by comprising an incinerator, a waste heat boiler and a tail gas treatment unit which are sequentially connected in series, wherein an SNCR denitration device is connected between the incinerator and the waste heat boiler in series, the waste heat boiler is provided with a bypass pipeline, the bypass pipeline is connected with a quenching desulfurization tower in series, and the quenching desulfurization tower is connected with the tail gas treatment unit in series;
the tail gas treatment unit comprises a desulfurization device, a primary bag-type dust remover, an SCR denitration device and a secondary bag-type dust remover which are sequentially connected in series, wherein the desulfurization device is respectively connected with a waste heat boiler and a quenching desulfurization tower in series, an active carbon injection device is connected on a pipeline, communicated with the SCR denitration device, of the primary bag-type dust remover in series, and the secondary bag-type dust remover is connected with a chimney in series;
the waste heat boiler comprises two working conditions of the waste heat boiler:
waste heat boiler working condition one: the high-temperature flue gas is directly cooled to 200 ℃ by a waste heat boiler and enters a tail gas treatment unit for treatment;
and the working condition of the waste heat boiler is II: the high-temperature flue gas enters a quenching desulfurization tower from a bypass pipeline, so that the high-temperature flue gas is cooled from 500 ℃ to 200 ℃ within 1s, and then enters a tail gas treatment unit for treatment;
the first working condition of the waste heat boiler and the second working condition of the waste heat boiler are timely switched through a plate flue gate valve;
and when the dioxin of the chimney flue gas does not reach the emission standard, the working condition of the waste heat boiler is switched into the working condition of the waste heat boiler.
2. The advanced treatment system for dioxin and sulfur dioxide in flue gas of an exhaust gas liquid incinerator according to claim 1, wherein the activated carbon spraying device sprays activated carbon;
waste heat boiler working condition one: the spraying amount of the activated carbon is 2-5 kg/h;
and the working condition of the waste heat boiler is II: the spraying amount of the activated carbon is 1-2 kg/h.
3. The advanced treatment system for dioxin and sulfur dioxide in flue gas of waste gas liquid incinerator according to claim 1, wherein the outlet temperature of the waste heat boiler is 200 ℃.
4. The advanced treatment system for dioxin and sulfur dioxide in flue gas of an exhaust gas liquid incinerator according to claim 1, wherein the bypass pipeline is arranged at the position where the temperature of the flue gas of a waste heat boiler is 500 ℃, and the outlet temperature of the quenching desulfurization tower is 200 ℃.
5. The advanced treatment system for dioxin and sulfur dioxide in flue gas of waste gas liquid incinerator according to claim 1, wherein atomized fresh water is sprayed in the quenching desulfurization tower.
6. The advanced treatment system for dioxin and sulfur dioxide in flue gas of an exhaust gas liquid incinerator according to claim 1, wherein the desulfurization device adopts a dry desulfurization process and takes baking soda as a desulfurizing agent; the baking soda is solid, and the spraying amount of the baking soda is 60-90 kg/h.
7. The advanced treatment system for dioxin and sulfur dioxide in flue gas of an exhaust gas liquid incinerator according to claim 1, wherein the SNCR denitration device and the SCR denitration device both use ammonia water solution as a reducing agent; the mass concentration of the ammonia water solution is 25%, and the spraying amount of the ammonia water solution is 20-50 kg/h.
8. The advanced treatment system for dioxin and sulfur dioxide in flue gas of waste gas liquid incinerator according to claim 1, wherein a wall vibrator is arranged in the waste heat boiler.
9. The advanced treatment system for dioxin and sulfur dioxide in flue gas of waste gas liquid incinerator according to claim 1, wherein the incinerator adopts natural gas ignition and afterburning, and the temperature in the incinerator is controlled to be more than or equal to 1100 ℃.
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| CN108458351A (en) * | 2018-03-30 | 2018-08-28 | 成都易态科技有限公司 | Solid waste incineration flue gas processing method and its system |
| CN111957197A (en) * | 2020-08-28 | 2020-11-20 | 浙江物华天宝能源环保有限公司 | Efficient flue gas deacidification, dioxin removal and waste heat utilization cooperative system and process |
| CN113701170A (en) * | 2021-08-23 | 2021-11-26 | 光大环境科技（中国）有限公司 | Hazardous waste incineration system and operation process thereof |
| CN114738770A (en) * | 2022-04-19 | 2022-07-12 | 湘潭锅炉有限责任公司 | Incineration treatment method and system for waste tar, waste gas and waste water |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108458351A (en) * | 2018-03-30 | 2018-08-28 | 成都易态科技有限公司 | Solid waste incineration flue gas processing method and its system |
| CN111957197A (en) * | 2020-08-28 | 2020-11-20 | 浙江物华天宝能源环保有限公司 | Efficient flue gas deacidification, dioxin removal and waste heat utilization cooperative system and process |
| CN113701170A (en) * | 2021-08-23 | 2021-11-26 | 光大环境科技（中国）有限公司 | Hazardous waste incineration system and operation process thereof |
| CN114738770A (en) * | 2022-04-19 | 2022-07-12 | 湘潭锅炉有限责任公司 | Incineration treatment method and system for waste tar, waste gas and waste water |
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