CN110548384A - Ultra-clean emission system and method for hazardous waste incineration flue gas - Google Patents
Ultra-clean emission system and method for hazardous waste incineration flue gas Download PDFInfo
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- CN110548384A CN110548384A CN201910723277.XA CN201910723277A CN110548384A CN 110548384 A CN110548384 A CN 110548384A CN 201910723277 A CN201910723277 A CN 201910723277A CN 110548384 A CN110548384 A CN 110548384A
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- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 title claims abstract description 98
- 239000003546 flue gas Substances 0.000 title claims abstract description 93
- 238000000034 method Methods 0.000 title claims abstract description 30
- 239000002920 hazardous waste Substances 0.000 title claims abstract description 21
- 238000004056 waste incineration Methods 0.000 title claims abstract description 15
- 239000000428 dust Substances 0.000 claims abstract description 53
- 238000010791 quenching Methods 0.000 claims abstract description 19
- 239000012535 impurity Substances 0.000 claims abstract description 8
- 238000005406 washing Methods 0.000 claims description 47
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 31
- 239000007789 gas Substances 0.000 claims description 29
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical class [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 25
- 239000002918 waste heat Substances 0.000 claims description 17
- 239000000779 smoke Substances 0.000 claims description 12
- 239000000843 powder Substances 0.000 claims description 11
- 235000008733 Citrus aurantifolia Nutrition 0.000 claims description 10
- 235000011941 Tilia x europaea Nutrition 0.000 claims description 10
- 239000002253 acid Substances 0.000 claims description 10
- 238000001914 filtration Methods 0.000 claims description 10
- 239000004571 lime Substances 0.000 claims description 10
- 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 claims description 9
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 claims description 9
- XSQUKJJJFZCRTK-UHFFFAOYSA-N Urea Chemical compound NC(N)=O XSQUKJJJFZCRTK-UHFFFAOYSA-N 0.000 claims description 9
- 239000004202 carbamide Substances 0.000 claims description 9
- 239000000243 solution Substances 0.000 claims description 9
- 238000005507 spraying Methods 0.000 claims description 9
- 239000007864 aqueous solution Substances 0.000 claims description 8
- 239000003795 chemical substances by application Substances 0.000 claims description 7
- 239000003344 environmental pollutant Substances 0.000 claims description 7
- 231100000719 pollutant Toxicity 0.000 claims description 7
- 230000000171 quenching effect Effects 0.000 claims description 7
- 150000003839 salts Chemical class 0.000 claims description 7
- 239000012530 fluid Substances 0.000 claims description 6
- 239000000443 aerosol Substances 0.000 claims description 4
- AXCZMVOFGPJBDE-UHFFFAOYSA-L calcium dihydroxide Chemical compound [OH-].[OH-].[Ca+2] AXCZMVOFGPJBDE-UHFFFAOYSA-L 0.000 claims description 4
- 239000000920 calcium hydroxide Substances 0.000 claims description 4
- 235000011116 calcium hydroxide Nutrition 0.000 claims description 4
- 229910001861 calcium hydroxide Inorganic materials 0.000 claims description 4
- 238000006243 chemical reaction Methods 0.000 claims description 4
- 239000010419 fine particle Substances 0.000 claims description 4
- 229910001385 heavy metal Inorganic materials 0.000 claims description 4
- 239000007788 liquid Substances 0.000 claims description 4
- 239000003595 mist Substances 0.000 claims description 4
- 229920006395 saturated elastomer Polymers 0.000 claims description 4
- 238000010517 secondary reaction Methods 0.000 claims description 4
- CDBYLPFSWZWCQE-UHFFFAOYSA-L sodium carbonate Substances [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 claims description 4
- 238000005728 strengthening Methods 0.000 claims description 4
- 238000004140 cleaning Methods 0.000 claims description 3
- 238000001816 cooling Methods 0.000 claims description 3
- 230000007797 corrosion Effects 0.000 claims description 3
- 238000005260 corrosion Methods 0.000 claims description 3
- 230000003111 delayed effect Effects 0.000 claims description 3
- 239000004744 fabric Substances 0.000 claims description 3
- 238000003860 storage Methods 0.000 claims description 3
- 238000010531 catalytic reduction reaction Methods 0.000 claims description 2
- 238000006722 reduction reaction Methods 0.000 claims description 2
- 229910000029 sodium carbonate Inorganic materials 0.000 claims description 2
- 238000002347 injection Methods 0.000 claims 1
- 239000007924 injection Substances 0.000 claims 1
- 239000002341 toxic gas Substances 0.000 abstract description 3
- 239000002912 waste gas Substances 0.000 abstract description 2
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 description 7
- 229910000041 hydrogen chloride Inorganic materials 0.000 description 7
- IXCSERBJSXMMFS-UHFFFAOYSA-N hydrogen chloride Substances Cl.Cl IXCSERBJSXMMFS-UHFFFAOYSA-N 0.000 description 7
- 239000000463 material Substances 0.000 description 7
- 238000012856 packing Methods 0.000 description 6
- 230000002378 acidificating effect Effects 0.000 description 4
- 239000000126 substance Substances 0.000 description 4
- 230000015572 biosynthetic process Effects 0.000 description 3
- 229910002091 carbon monoxide Inorganic materials 0.000 description 3
- 238000005516 engineering process Methods 0.000 description 3
- MWUXSHHQAYIFBG-UHFFFAOYSA-N nitrogen oxide Inorganic materials O=[N] MWUXSHHQAYIFBG-UHFFFAOYSA-N 0.000 description 3
- -1 NO X Inorganic materials 0.000 description 2
- RAHZWNYVWXNFOC-UHFFFAOYSA-N Sulphur dioxide Chemical compound O=S=O RAHZWNYVWXNFOC-UHFFFAOYSA-N 0.000 description 2
- 229910052793 cadmium Inorganic materials 0.000 description 2
- 238000001514 detection method Methods 0.000 description 2
- 239000011152 fibreglass Substances 0.000 description 2
- 229910052753 mercury Inorganic materials 0.000 description 2
- 239000004810 polytetrafluoroethylene Substances 0.000 description 2
- 229920001343 polytetrafluoroethylene Polymers 0.000 description 2
- 229910000975 Carbon steel Inorganic materials 0.000 description 1
- KRHYYFGTRYWZRS-UHFFFAOYSA-N Fluorane Chemical compound F KRHYYFGTRYWZRS-UHFFFAOYSA-N 0.000 description 1
- 229910000831 Steel Inorganic materials 0.000 description 1
- YKTSYUJCYHOUJP-UHFFFAOYSA-N [O--].[Al+3].[Al+3].[O-][Si]([O-])([O-])[O-] Chemical compound [O--].[Al+3].[Al+3].[O-][Si]([O-])([O-])[O-] YKTSYUJCYHOUJP-UHFFFAOYSA-N 0.000 description 1
- 229910052787 antimony Inorganic materials 0.000 description 1
- 229910052785 arsenic Inorganic materials 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 238000007664 blowing Methods 0.000 description 1
- BDOSMKKIYDKNTQ-UHFFFAOYSA-N cadmium atom Chemical compound [Cd] BDOSMKKIYDKNTQ-UHFFFAOYSA-N 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 239000010962 carbon steel Substances 0.000 description 1
- 239000004568 cement Substances 0.000 description 1
- 229910052804 chromium Inorganic materials 0.000 description 1
- 150000001875 compounds Chemical class 0.000 description 1
- 229910052802 copper Inorganic materials 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 230000008021 deposition Effects 0.000 description 1
- 238000011038 discontinuous diafiltration by volume reduction Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 230000005684 electric field Effects 0.000 description 1
- 239000000835 fiber Substances 0.000 description 1
- 229910000040 hydrogen fluoride Inorganic materials 0.000 description 1
- 229910052745 lead Inorganic materials 0.000 description 1
- 230000007774 longterm Effects 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- QSHDDOUJBYECFT-UHFFFAOYSA-N mercury Chemical compound [Hg] QSHDDOUJBYECFT-UHFFFAOYSA-N 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 239000000178 monomer Substances 0.000 description 1
- 229910052757 nitrogen Inorganic materials 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 229910052698 phosphorus Inorganic materials 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 229910052708 sodium Inorganic materials 0.000 description 1
- 239000011734 sodium Substances 0.000 description 1
- 239000010959 steel Substances 0.000 description 1
- 229910052717 sulfur Inorganic materials 0.000 description 1
- 238000003786 synthesis reaction Methods 0.000 description 1
- 229910052718 tin Inorganic materials 0.000 description 1
- 231100000331 toxic Toxicity 0.000 description 1
- 230000002588 toxic effect Effects 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
- B01D50/00—Combinations of methods or devices for separating particles from gases or vapours
-
- 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
- B01D53/02—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography
- B01D53/04—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography with stationary adsorbents
-
- 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
- B01D53/38—Removing components of undefined structure
- B01D53/40—Acidic components
-
- 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
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
- B01D53/77—Liquid phase processes
- B01D53/78—Liquid phase processes with gas-liquid contact
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
- B01D53/81—Solid phase processes
- B01D53/83—Solid phase processes with moving reactants
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2253/00—Adsorbents used in seperation treatment of gases and vapours
- B01D2253/10—Inorganic adsorbents
- B01D2253/102—Carbon
-
- 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
Landscapes
- Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- Environmental & Geological Engineering (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Analytical Chemistry (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Health & Medical Sciences (AREA)
- Biomedical Technology (AREA)
- Treating Waste Gases (AREA)
Abstract
An ultra-clean discharge system and method for hazardous waste incineration flue gas belong to the technical field of waste gas treatment. The technical scheme adopted by the invention sequentially comprises the following devices and processes, and sequentially comprises the following steps: the system comprises an SNCR high-temperature denitration system, a quench tower, a dry type deacidification system, a low-filtering-speed bag type dust remover, a double-tower double-circulation wet type deacidification system, a honeycomb tube type wet type electric demister, a flue gas reheater, an induced air discharge system and the like; the system and the method of the invention can effectively reduce and remove the toxic gas and impurities in the incineration flue gas, and achieve the clean emission degree.
Description
Technical Field
the invention belongs to the technical field of waste gas treatment, and particularly relates to an ultra-clean discharge system and method for hazardous waste incineration flue gas.
Background
The hazardous waste is treated by the incineration method, so that the hazardous waste has the advantages of high harmless degree, good volume reduction effect, small occupied area and the like, toxic and harmful substances in the hazardous waste can be treated in a harmless and reducing manner, most harmful compounds are decomposed into simple and harmless substances (mainly CO 2 and H 2 O), and combustible substances are thoroughly oxidized to reach a stable state.
the incineration flue gas contains a certain amount of dust, toxic gases (carbon monoxide, nitrogen oxides, sulfur dioxide, hydrogen chloride, hydrogen fluoride and the like), dioxin substances, heavy metals such as mercury, cadmium, lead and the like. In order to prevent the smoke generated by incineration from causing secondary pollution to the atmospheric environment, the smoke must be purified according to relevant regulations in hazardous waste incineration pollution control standards.
in recent years, emission control standards are becoming more strict, so that hazardous waste incineration operation enterprises must select a technology capable of stably maintaining ultra-clean flue gas emission for a long time, and the improvement of treatment processes is becoming more urgent.
(1) Dust removing equipment
The traditional bag-type dust collector is generally designed to have a filtering air speed of 0.8-1 m/min. Although the whole cost is reduced by the higher design flow velocity, the phenomena of difficult cloth bag ash removal, unclean ash removal, excessive dust discharge and the like are easily caused. Meanwhile, dust is easy to escape due to high filtering wind speed.
According to the invention, the low-filtering-speed bag type dust collector is adopted, the filtering air speed is controlled to be below 0.5m/min, the filtering efficiency is improved, and meanwhile, a stable secondary reaction filtering layer is formed on the surface of the filtering bag by the dry deacidification agent and the activated carbon, so that the reaction efficiency of the dry deacidification agent and the activated carbon is improved.
(2) Tail gas equipment
In the traditional process, flue gas is deacidified by a wet method and then directly enters a flue gas reheater to be heated and is discharged by a draught fan. As the wet deacidification flue gas contains more water and is easy to form acid mist and aerosol with impurities such as insoluble salt, the particulate matters in the tail gas emission exceed the standard.
According to the invention, a set of honeycomb tube type wet electric demister is arranged behind the wet deacidification system, and fine particles and fog drops are removed by an external high-voltage electric field, so that the corrosion of wet flue gas to a chimney is delayed, and simultaneously, the content of pollution components in tail gas emission can be reduced.
(3) Deacidification equipment
The domestic built treatment of hazardous waste incineration smoke, the main stream deacidification process is dry method + wet method single tower deacidification, and the condition that the short-time acidic pollutants exceed the standard is easy to occur under the condition of material fluctuation.
In order to reduce the influence of materials on emission indexes, the invention adopts a dry method and wet method double-tower double-circulation deacidification technology, and is suitable for projects with high acidic components, large fluctuation and high deacidification efficiency. The wet double-tower double-circulation deacidification system mainly comprises a precooler and a washing tower, wherein the precooler adopts a hollow tower structure to reduce the system resistance. Due to the adoption of the hollow tower structure, the TDS of the circulating water can be controlled to be more than 150000 mg/L. The salt discharge concentration is improved, and simultaneously, the blockage in the tower is avoided. The washing tower adopts a flow-through sieve plate tower, and a porous sieve plate is adopted as a tower internal part, so that compared with the conventional structured packing, the problems of salt deposition blockage, packing collapse and the like can be effectively avoided, and the running stability of the whole device is improved. After the dry method and double-tower double-circulation technology is adopted, the emission index of acidic pollutants is more stable and controllable, and the overall deacidification efficiency reaches more than 99%.
Disclosure of Invention
The invention aims to provide an ultra-clean emission process system for hazardous waste incineration flue gas, aiming at the defects of the existing incineration flue gas treatment system in application and the increasingly strict tail gas emission control standard. Aiming at the characteristics of incineration flue gas, the system selects and combines a plurality of purification monomer devices suitable for actual production. The incineration flue gas is discharged after being treated, and can meet the requirements on flue gas emission indexes in the latest edition hazardous waste incineration pollution control standard and European Union industry emission instruction.
in order to achieve the purpose, the technical scheme adopted by the invention comprises the following steps: the system comprises an SNCR high-temperature denitration system, a quench tower, a dry type deacidification system, a low-filtering-speed bag type dust remover, a double-tower double-circulation wet type deacidification system, a honeycomb tube type wet type electric demister, a flue gas reheater, an induced air discharge system and the like;
the flue for feeding high-temperature flue gas (1) is communicated with a waste heat boiler (2), an SNCR high-temperature denitration system (4) is arranged in the waste heat boiler (2), the inlet pipe of a urea solution (3) is connected with the SNCR high-temperature denitration system (4) to enable the high-temperature flue gas and urea to be mixed and react in the first return stroke of the waste heat boiler (2), the gas outlet of the waste heat boiler (2) is connected with the side surface of the upper part of a quench tower (6) through a pipeline, a double-fluid spraying system (7) is arranged on the upper top surface inside the quench tower (6), the ash outlet at the lower part of the quench tower (6) is connected with an ash conveying device (8), the gas outlet of the quench tower (6) is connected with a dry deacidification tower (9) through a pipeline, the dry deacidification tower (9) is respectively connected with the inlet pipe of lime powder (10) and the inlet pipe of activated carbon powder (11), the gas outlet of the dry deacidification tower (9) is connected with the gas inlet of a bag type dust remover, an ash bucket (13) is arranged at the lower part of the bag-type dust collector (12), an air outlet of the bag-type dust collector (12) is connected with an air inlet of a precooler (14), the precooler (14) is washed and cooled by alkaline aqueous solution, a primary washing water (15) is formed at a liquid outlet at the lower end of the precooler (14), and the primary washing water (15) is stored in a primary washing water tank and is recycled as the alkaline aqueous solution of the precooler (14); the air outlet of the precooler (14) is connected with the air inlet of the washing tower (18), the washing tower (18) adopts alkaline aqueous solution for washing, a liquid outlet at the lower end of the washing tower (18) forms secondary washing water (17), and the secondary washing water (17) is stored in a secondary washing water tank and is recycled as the alkaline aqueous solution of the washing tower (18); a gas outlet of the washing tower (18) is connected with a honeycomb tube type wet electric demister (19), a gas outlet of the honeycomb tube type wet electric demister (19) is connected with a gas inlet of a tube side of a flue gas reheater (20), the gas outlet of the tube side of the flue gas reheater (20) is connected with a chimney (22) through a draught fan (5), and the discharged flue gas (23) of the chimney (22) can be monitored on line and is discharged into the atmosphere after reaching the standard; the shell side air inlet of the flue gas reheater (20) is connected with the saturated low-pressure steam (21) outlet of the waste heat boiler (2) through a pipeline and a valve, and the shell side air outlet (16) of the flue gas reheater (20) is connected with a chimney (22).
The bag-type dust collector (12) adopts a multistage parallel series structure, and an ash bucket (13) is arranged below each bag-type dust collector.
The bag type dust collector (12) is a low-filtering-speed bag type dust collector.
The lime powder and the activated carbon powder are stored in respective storage bins, are proportioned by a disc feeder and are added from the middle upper part of the dry deacidification tower through a Roots blower.
The precooler adopts a hollow structure design, the washing tower adopts a multilayer flow-through sieve plate tower, compared with the conventional structured packing, the problems of salt formation blockage, packing collapse and the like can be effectively avoided, the operation stability of the whole device is improved, the discharge index of acidic pollutants is more stable and controllable, more than 95 percent of SO 2 and more than 99 percent of HCl are removed, the pH value of the secondary washing water in the washing tower is not lower than that of the primary washing water in the precooler, the preferred pH value of the secondary washing water is 8-9, and the pH value of the primary washing water is 7-8.
The method for carrying out ultra-clean emission of the flue gas generated by burning the hazardous waste by adopting the system is characterized in that the high-temperature flue gas passes through an SNCR high-temperature denitration system in a first return stroke of the waste heat boiler, and urea solution is fully mixed with the flue gas by a spraying device, and the NO x component and the urea are subjected to a reduction reaction at the high temperature of 950-1000 ℃;
After passing through the waste heat boiler, the flue gas enters a quenching tower from the upper part through a flue in order to prevent the dioxin from being synthesized again in the cooling process; a double-fluid spraying system arranged at the upper part of the quenching tower generates atomized water drops to rapidly cool the flue gas;
The cooled flue gas enters a dry type deacidification system, slaked lime powder and activated carbon powder are added at the dry type deacidification system, and the flue gas enters a dry type deacidification strengthening section, so that part of acid gas is removed in the dry type deacidification system, and pollutants such as dioxin, heavy metals and the like are effectively adsorbed;
The flue gas carries slaked lime powder and activated carbon powder added in the dry deacidification system to enter a bag type dust collector together, and in the dust collector, lime and activated carbon form a stable secondary reaction filter layer on the surface of a filter bag by controlling a lower filtering air speed, so that the reaction efficiency of a dry deacidification agent and the activated carbon is improved; when the running resistance of the bag-type dust collector is increased, compressed air is used for cleaning dust, and the dust is blown out from the back of the filter bag, so that the smoke dust falls off to a lower dust hopper;
After cloth bag dust removal, the flue gas enters a double-tower double-circulation wet type deacidification system, namely a precooler and a washing tower, and acid gas in the flue gas is deeply removed by spraying sodium hydroxide or sodium carbonate solution as a deacidification agent. The water passes through a precooler and a washing tower in sequence, the precooler adopts a hollow tower structure to reduce system resistance, the TDS of the circulating water can be controlled at 150000mg/L, the salt discharge concentration is improved, and meanwhile, the blockage in the tower is avoided. The washing tower adopts a flow-through sieve plate tower, compared with the conventional structured packing, the problems of salt formation blockage, packing collapse and the like can be effectively avoided, the operation stability of the whole device is improved, the acid pollutant discharge index is more stable and controllable, and the whole deacidification efficiency reaches more than 99%.
The flue gas deacidified by the wet method firstly enters a honeycomb tube type wet electric demister to remove impurities such as fine particles, acid mist, aerosol and the like, the corrosion of the wet flue gas to a chimney is delayed, simultaneously, the impurity content in tail gas emission can be reduced, then the residual moisture is gasified by a flue gas reheater, and finally the residual moisture enters the atmosphere through an induced air exhaust system, and a flue gas online detection device is arranged on the flue gas at the outlet of the chimney and is used for detecting smoke dust, HF, SO 2, CO, NO X, HCl, CO 2 and the like in the exhaust flue gas.
The system and the method of the invention can effectively reduce and remove the toxic gas and impurities in the incineration flue gas, and achieve the clean emission degree.
Drawings
FIG. 1 is a flow chart of the process steps of the present invention.
the system comprises high-temperature flue gas 1, a waste heat boiler 2, a urea solution 3, an SNCR (selective non catalytic reduction) high-temperature denitration system 4, a draught fan 5, a quench tower 6, a two-fluid spraying system 7, an ash conveying device 8, a dry deacidification tower 9, lime powder 10, activated carbon powder 11, a bag type dust collector 12, an ash hopper 13, a precooler 14, primary washing water 15, a flue gas reheater shell pass gas outlet 16, secondary washing water 17, a washing tower 18, a honeycomb tube type wet electric demister 19, a flue gas reheater 20, saturated low-pressure steam 21, a chimney 22, exhaust flue gas 23 and a dry deacidification strengthening section 24.
Detailed Description
the present invention will be further illustrated with reference to the following examples, but the present invention is not limited to the following examples.
Example 1
xIn order to prolong the service life of each device in the process and ensure that the smoke is discharged after reaching the standard, the content of each element of dangerous waste entering the rotary kiln is controlled, wherein Cl is less than 3%, F is less than 0.4%, S is less than 2%, P is less than 0.5%, and N is less than 2%.
After passing through the waste heat boiler, the temperature of the flue gas is reduced to 500-600 ℃, and in order to avoid the secondary synthesis of dioxin in the cooling process, the flue gas enters the quenching tower 6 from the upper part through the flue. The material of the quenching tower 6 comprises a steel plate with the thickness of 10mm, an aluminum silicate fiber felt with the thickness of 100mm and a wear-resistant castable with the thickness of 80mm, a double-fluid spraying system 7 is arranged at the top of the quenching tower, and atomized water drops are generated to rapidly cool the flue gas to below 200 ℃ within 0.8 s.
The cooled flue gas enters a dry type deacidification system, a deacidification tower is made of carbon steel and lined with KPI acid-resistant cement, lime powder 10 and activated carbon powder 11 are added from the middle upper part of a dry type deacidification tower 9 through a Roots blower according to the proportion of a disc feeder from respective storage bins, and are fully mixed with the flue gas after passing through a dry type deacidification strengthening section 24, SO that more than 75% of SO 2 and more than 80% of HCl are removed, dioxin and heavy metal pollutants are effectively adsorbed, the flow rate of the gas in the system is not more than 3m/s, and the pressure drop is not more than 300 Pa.
The method comprises the steps of mixing flue gas, lime powder and activated carbon powder in a dry deacidification system 9, feeding the mixture into a low-filtering-speed bag type dust collector 12, controlling the filtering air speed in the dust collector to be below 0.5m/min, forming a stable secondary reaction filtering layer on the surface of a PTFE + PTFE coated filter bag by the lime and the activated carbon, and improving the reaction efficiency of a dry deacidification agent and the activated carbon, when the operation resistance of the bag type dust collector exceeds 1500Pa, cleaning the dust by using compressed air, blowing the dust out from the back of the filter bag to a lower dust hopper 13, wherein in order to ensure the stable operation of the low-filtering-speed bag type dust collector 12, the inlet temperature of the flue gas of the dust collector needs to be controlled to be within 220 ℃ of 180 DEG, the inlet flue gas content is less than or equal to 30%, the dust content concentration is less than or equal to 10g/Nm 3, the maximum long-term working temperature is less than or equal to 260 ℃, the instantaneous (less than 5min/h) temperature is less than or equal.
The dedusted flue gas enters a double-tower double-circulation wet-type deacidification system, and passes through a precooler 14 and a washing tower 18 in sequence, 30% NaOH solution or 30% Na 2 CO 3 solution is sprayed on the top of the tower, the precooler 14 is made of glass fiber reinforced plastic, the flue gas is cooled to 75 ℃ from 160-.
The flue gas after wet deacidification enters a honeycomb tube type wet electric demister 19 to remove impurities such as fine particles, acid mist, aerosol and the like. The inlet and outlet smoke box is made of FRP material, the cathode line is made of 2205 material, the anode tube is made of conductive glass fiber reinforced plastic material, the flow rate of smoke is less than 1m/s, and the pressure drop is less than 300 Pa.
The demisted flue gas enters a flue gas reheater 20, 1.0MPa saturated low-pressure steam 21 generated in a waste heat boiler is used as a heat source, the flue gas is heated to 135 ℃, and tail gas plume is eliminated.
the flue gas finally enters the atmosphere through an induced air discharge system, an induced draft fan 5 is made of 316L material, the operation noise is less than or equal to 80dB, a chimney 22 is 50 meters in height, the diameter of an outlet is 1.3 meters, a flue gas online detection device is arranged at the position of the outlet and used for detecting smoke dust, HF, SO 2, CO, NO X, HCl, O 2, CO 2 and the like in the discharged flue gas 23, and the discharged flue gas 23 can reach the following discharge standards that the smoke dust is less than or equal to 10mg/m 3, the SO 2 is less than or equal to 80mg/m 3, the NO X is less than or equal to 250mg/m 3, the HCl is less than or equal to 50mg/m 3, the HF is less than or equal to 2mg/m 3, the Hg is less than or equal to 0.05mg/m 3, the Cd is less than or equal to 0.05mg/m 3, the As + Ni is less than or equal to 0.05mg/m 3, the Pb is less than or equal to 0..
The flue gas after being treated by the flue gas treatment process is measured in 2018, 11 months and 9 days of an incineration system of a certain hazardous waste comprehensive treatment center, and the content of each component is 8.09 percent of oxygen content, 5.3mg/m 3 percent of smoke dust, 3 percent of SO 2 mg/m, 3 percent of NO X mg/m, 1.3mg/m 3 percent of HCl, 0.05mg/m 3 percent of HF, 0.0155mg/m 3 percent of Hg, 1.1 × 10 -5 mg/m 3 percent of Cd, 2 × 10 -4 mg/m 3 percent of As, 2 × 10 -4 mg/m 3 percent of Pb, 3.6 × 10 - 3 mg/m 3 percent of Cr, Sn, Cu, Sb, 0.0382mg/m 3 percent of dioxin, and 0.012ng/m 3 percent of dioxin.
Claims (8)
1. The utility model provides a hazardous waste burns ultra-clean discharge system of flue gas which characterized in that includes: the system comprises an SNCR high-temperature denitration system, a quench tower, a dry type deacidification system, a bag type dust collector, a double-tower double-circulation wet type deacidification system, a honeycomb tube type wet type electric demister, a flue gas reheater and an induced air discharge system;
The flue for feeding high-temperature flue gas (1) is communicated with a waste heat boiler (2), an SNCR high-temperature denitration system (4) is arranged in the waste heat boiler (2), the inlet pipe of a urea solution (3) is connected with the SNCR high-temperature denitration system (4) to enable the high-temperature flue gas and urea to be mixed and react in the first return stroke of the waste heat boiler (2), the gas outlet of the waste heat boiler (2) is connected with the side surface of the upper part of a quench tower (6) through a pipeline, a double-fluid spraying system (7) is arranged on the upper top surface inside the quench tower (6), the ash outlet at the lower part of the quench tower (6) is connected with an ash conveying device (8), the gas outlet of the quench tower (6) is connected with a dry deacidification tower (9) through a pipeline, the dry deacidification tower (9) is respectively connected with the inlet pipe of lime powder (10) and the inlet pipe of activated carbon powder (11), the gas outlet of the dry deacidification tower (9) is connected with the gas inlet of a bag type dust remover, an ash bucket (13) is arranged at the lower part of the bag-type dust collector (12), an air outlet of the bag-type dust collector (12) is connected with an air inlet of a precooler (14), the precooler (14) is washed and cooled by alkaline aqueous solution, a primary washing water (15) is formed at a liquid outlet at the lower end of the precooler (14), and the primary washing water (15) is stored in a primary washing water tank and is recycled as the alkaline aqueous solution of the precooler (14); the air outlet of the precooler (14) is connected with the air inlet of the washing tower (18), the washing tower (18) adopts alkaline aqueous solution for washing, a liquid outlet at the lower end of the washing tower (18) forms secondary washing water (17), and the secondary washing water (17) is stored in a secondary washing water tank and is recycled as the alkaline aqueous solution of the washing tower (18); a gas outlet of the washing tower (18) is connected with a honeycomb tube type wet electric demister (19), a gas outlet of the honeycomb tube type wet electric demister (19) is connected with a gas inlet of a tube side of a flue gas reheater (20), the gas outlet of the tube side of the flue gas reheater (20) is connected with a chimney (22) through a draught fan (5), and the discharged flue gas (23) of the chimney (22) can be monitored on line and is discharged into the atmosphere after reaching the standard; the shell side air inlet of the flue gas reheater (20) is connected with the saturated low-pressure steam (21) outlet of the waste heat boiler (2) through a pipeline and a valve, and the shell side air outlet (16) of the flue gas reheater (20) is connected with a chimney (22).
2. The ultra-clean exhaust system for hazardous waste incineration flue gas according to claim 1, comprising: the bag-type dust collector (12) adopts a multistage parallel series structure, and an ash bucket (13) is arranged below each bag-type dust collector.
3. the ultra-clean exhaust system for hazardous waste incineration flue gas according to claim 1, comprising: the bag type dust collector (12) is a low-filtering-speed bag type dust collector.
4. The ultra-clean exhaust system for hazardous waste incineration flue gas according to claim 1, comprising: the lime powder and the activated carbon powder are stored in respective storage bins, are proportioned by a disc feeder and are added from the middle upper part of the dry deacidification tower through a Roots blower.
5. The ultra-clean exhaust system for hazardous waste incineration flue gas according to claim 1, comprising: the precooler is designed in a hollow structure; the washing tower adopts a multilayer flow-through sieve plate tower.
6. The ultra-clean exhaust system for hazardous waste incineration flue gas according to claim 1, comprising: the pH value of the secondary washing water in the washing tower is not lower than that of the primary washing water in the precooler, preferably, the pH value of the secondary washing water is 8-9, and the pH value of the primary washing water is 7-8.
7. Method for ultra-clean emission of hazardous waste incineration flue gas using the system according to any of claims 1-6, characterized in that it comprises the following:
The method comprises the following steps that high-temperature flue gas passes through an SNCR (selective non-catalytic reduction) high-temperature denitration system in a first return stroke of a waste heat boiler, urea solution is fully mixed with the flue gas through an injection device, and NO x component and urea are subjected to reduction reaction at the high temperature of 950-1000 ℃;
After passing through the waste heat boiler, the flue gas enters a quenching tower from the upper part through a flue in order to prevent the dioxin from being synthesized again in the cooling process; a double-fluid spraying system arranged at the upper part of the quenching tower generates atomized water drops to rapidly cool the flue gas;
The cooled flue gas enters a dry type deacidification system, slaked lime powder and activated carbon powder are added at the dry type deacidification system, and the flue gas enters a dry type deacidification strengthening section, so that part of acid gas is removed in the dry type deacidification system, and pollutants such as dioxin, heavy metals and the like are effectively adsorbed;
The flue gas carries slaked lime powder and activated carbon powder added in the dry deacidification system to enter a bag type dust collector together, and in the dust collector, lime and activated carbon form a stable secondary reaction filter layer on the surface of a filter bag by controlling a lower filtering air speed, so that the reaction efficiency of a dry deacidification agent and the activated carbon is improved; when the running resistance of the bag-type dust collector is increased, compressed air is used for cleaning dust, and the dust is blown out from the back of the filter bag, so that the smoke dust falls off to a lower dust hopper;
After cloth bag dust removal, the flue gas enters a double-tower double-circulation wet type deacidification system, namely a precooler and a washing tower, and acid gas in the flue gas is deeply removed by spraying sodium hydroxide or sodium carbonate solution as a deacidification agent;
The flue gas after wet deacidification enters a honeycomb tube type wet electric demister firstly to remove impurities such as fine particles, acid mist, aerosol and the like, so that the corrosion of the wet flue gas to a chimney is delayed, and the impurity content in tail gas emission can be reduced; and the residual water is gasified by a flue gas reheater and finally enters the atmosphere through an induced air discharge system.
8. The method of claim 7, wherein the circulating water TDS is controlled to 150000mg/L by passing through a precooler and a washing tower in sequence, thereby increasing the salt discharge concentration and avoiding the blockage in the tower.
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| CN114177760A (en) * | 2022-02-16 | 2022-03-15 | 浙江百能科技有限公司 | System and method for oxidizing active oxygen in hazardous waste incineration flue gas and integrally discharging hazardous waste incineration flue gas in ultralow emission mode |
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Application publication date: 20191210 |