CN110081445B - Liquid dangerous waste incineration system and incineration process thereof - Google Patents
Liquid dangerous waste incineration system and incineration process thereof Download PDFInfo
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- CN110081445B CN110081445B CN201910451976.3A CN201910451976A CN110081445B CN 110081445 B CN110081445 B CN 110081445B CN 201910451976 A CN201910451976 A CN 201910451976A CN 110081445 B CN110081445 B CN 110081445B
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- flue gas
- tower
- waste
- incineration
- bag filter
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- 239000007788 liquid Substances 0.000 title claims abstract description 87
- 238000004056 waste incineration Methods 0.000 title claims abstract description 20
- 238000000034 method Methods 0.000 title claims abstract description 17
- 239000003546 flue gas Substances 0.000 claims abstract description 110
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims abstract description 108
- 239000002699 waste material Substances 0.000 claims abstract description 57
- 239000002918 waste heat Substances 0.000 claims abstract description 43
- 238000010791 quenching Methods 0.000 claims abstract description 31
- 230000000171 quenching effect Effects 0.000 claims abstract description 29
- 238000006243 chemical reaction Methods 0.000 claims abstract description 28
- 238000000746 purification Methods 0.000 claims abstract description 25
- 239000000872 buffer Substances 0.000 claims abstract description 22
- 238000001816 cooling Methods 0.000 claims abstract description 16
- 239000007921 spray Substances 0.000 claims description 47
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 42
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 31
- UIIMBOGNXHQVGW-UHFFFAOYSA-M Sodium bicarbonate Chemical compound [Na+].OC([O-])=O UIIMBOGNXHQVGW-UHFFFAOYSA-M 0.000 claims description 30
- 238000006386 neutralization reaction Methods 0.000 claims description 28
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 claims description 23
- 239000002253 acid Substances 0.000 claims description 20
- VHUUQVKOLVNVRT-UHFFFAOYSA-N Ammonium hydroxide Chemical compound [NH4+].[OH-] VHUUQVKOLVNVRT-UHFFFAOYSA-N 0.000 claims description 19
- 235000011114 ammonium hydroxide Nutrition 0.000 claims description 19
- 239000000779 smoke Substances 0.000 claims description 19
- 238000003860 storage Methods 0.000 claims description 19
- 229910000030 sodium bicarbonate Inorganic materials 0.000 claims description 17
- 238000001704 evaporation Methods 0.000 claims description 15
- 230000008020 evaporation Effects 0.000 claims description 15
- 235000017557 sodium bicarbonate Nutrition 0.000 claims description 13
- 238000005554 pickling Methods 0.000 claims description 10
- 239000000295 fuel oil Substances 0.000 claims description 9
- 239000007789 gas Substances 0.000 claims description 9
- 239000002920 hazardous waste Substances 0.000 claims description 9
- 238000005406 washing Methods 0.000 claims description 9
- 239000003595 mist Substances 0.000 claims description 7
- 238000010438 heat treatment Methods 0.000 claims description 6
- 238000005507 spraying Methods 0.000 claims description 3
- 239000003517 fume Substances 0.000 claims description 2
- 230000014759 maintenance of location Effects 0.000 claims 1
- 230000009931 harmful effect Effects 0.000 abstract description 7
- 239000000126 substance Substances 0.000 abstract description 5
- 230000009897 systematic effect Effects 0.000 abstract description 3
- 238000009834 vaporization Methods 0.000 abstract description 2
- 230000008016 vaporization Effects 0.000 abstract description 2
- 208000028659 discharge Diseases 0.000 abstract 2
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 21
- 229910021529 ammonia Inorganic materials 0.000 description 14
- 239000000428 dust Substances 0.000 description 11
- MWUXSHHQAYIFBG-UHFFFAOYSA-N nitrogen oxide Inorganic materials O=[N] MWUXSHHQAYIFBG-UHFFFAOYSA-N 0.000 description 6
- 238000005303 weighing Methods 0.000 description 6
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 5
- 239000003344 environmental pollutant Substances 0.000 description 5
- 231100000719 pollutant Toxicity 0.000 description 5
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 4
- 230000008901 benefit Effects 0.000 description 4
- 230000007797 corrosion Effects 0.000 description 4
- 238000005260 corrosion Methods 0.000 description 4
- 238000007599 discharging Methods 0.000 description 4
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 4
- 239000001301 oxygen Substances 0.000 description 4
- 229910052760 oxygen Inorganic materials 0.000 description 4
- 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 description 3
- 239000000463 material Substances 0.000 description 3
- KRHYYFGTRYWZRS-UHFFFAOYSA-N Fluorane Chemical compound F KRHYYFGTRYWZRS-UHFFFAOYSA-N 0.000 description 2
- RAHZWNYVWXNFOC-UHFFFAOYSA-N Sulphur dioxide Chemical compound O=S=O RAHZWNYVWXNFOC-UHFFFAOYSA-N 0.000 description 2
- 238000004140 cleaning Methods 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 229910001385 heavy metal Inorganic materials 0.000 description 2
- 239000012535 impurity Substances 0.000 description 2
- 239000010808 liquid waste Substances 0.000 description 2
- 239000003345 natural gas Substances 0.000 description 2
- 229910052757 nitrogen Inorganic materials 0.000 description 2
- 239000003921 oil Substances 0.000 description 2
- 229920006395 saturated elastomer Polymers 0.000 description 2
- 159000000000 sodium salts Chemical class 0.000 description 2
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 description 1
- XSQUKJJJFZCRTK-UHFFFAOYSA-N Urea Chemical compound NC(N)=O XSQUKJJJFZCRTK-UHFFFAOYSA-N 0.000 description 1
- 238000004378 air conditioning Methods 0.000 description 1
- 239000003513 alkali Substances 0.000 description 1
- 239000002585 base Substances 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 239000004202 carbamide Substances 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 239000003638 chemical reducing agent Substances 0.000 description 1
- 238000002485 combustion reaction Methods 0.000 description 1
- 238000010276 construction Methods 0.000 description 1
- 238000005536 corrosion prevention Methods 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 229910001873 dinitrogen Inorganic materials 0.000 description 1
- 238000001914 filtration Methods 0.000 description 1
- 239000000383 hazardous chemical Substances 0.000 description 1
- IXCSERBJSXMMFS-UHFFFAOYSA-N hydrogen chloride Substances Cl.Cl IXCSERBJSXMMFS-UHFFFAOYSA-N 0.000 description 1
- 229910000041 hydrogen chloride Inorganic materials 0.000 description 1
- 230000007774 longterm Effects 0.000 description 1
- 235000016709 nutrition Nutrition 0.000 description 1
- 230000003647 oxidation Effects 0.000 description 1
- 238000007254 oxidation reaction Methods 0.000 description 1
- 239000002245 particle Substances 0.000 description 1
- 230000009257 reactivity Effects 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 238000011160 research Methods 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 239000010865 sewage Substances 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 239000013589 supplement Substances 0.000 description 1
- 238000003786 synthesis reaction Methods 0.000 description 1
- 231100001234 toxic pollutant Toxicity 0.000 description 1
- 230000001988 toxicity Effects 0.000 description 1
- 231100000419 toxicity Toxicity 0.000 description 1
Classifications
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
- F23G5/00—Incineration of waste; Incinerator constructions; Details, accessories or control therefor
- F23G5/44—Details; Accessories
- F23G5/46—Recuperation of heat
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
- F23G5/00—Incineration of waste; Incinerator constructions; Details, accessories or control therefor
- F23G5/44—Details; Accessories
- F23G5/48—Preventing corrosion
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
- F23G7/00—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals
- F23G7/04—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals of waste liquors, e.g. sulfite liquors
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES
- F23J15/00—Arrangements of devices for treating smoke or fumes
- F23J15/02—Arrangements of devices for treating smoke or fumes of purifiers, e.g. for removing noxious material
- F23J15/022—Arrangements of devices for treating smoke or fumes of purifiers, e.g. for removing noxious material for removing solid particulate material from the gasflow
- F23J15/025—Arrangements of devices for treating smoke or fumes of purifiers, e.g. for removing noxious material for removing solid particulate material from the gasflow using filters
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES
- F23J15/00—Arrangements of devices for treating smoke or fumes
- F23J15/02—Arrangements of devices for treating smoke or fumes of purifiers, e.g. for removing noxious material
- F23J15/04—Arrangements of devices for treating smoke or fumes of purifiers, e.g. for removing noxious material using washing fluids
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES
- F23J15/00—Arrangements of devices for treating smoke or fumes
- F23J15/06—Arrangements of devices for treating smoke or fumes of coolers
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES
- F23J15/00—Arrangements of devices for treating smoke or fumes
- F23J15/08—Arrangements of devices for treating smoke or fumes of heaters
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES
- F23J2217/00—Intercepting solids
- F23J2217/10—Intercepting solids by filters
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E20/00—Combustion technologies with mitigation potential
- Y02E20/30—Technologies for a more efficient combustion or heat usage
Landscapes
- Engineering & Computer Science (AREA)
- Mechanical Engineering (AREA)
- General Engineering & Computer Science (AREA)
- Environmental & Geological Engineering (AREA)
- Treating Waste Gases (AREA)
Abstract
The invention belongs to the technical field of waste incineration, and particularly relates to a liquid dangerous waste incineration system which comprises an incineration unit, a flue gas purification unit and a flue gas discharge unit. The incineration unit comprises a buffer tank group, an incinerator, an exhaust-heat boiler and a pollution discharge tank, the flue gas purification unit comprises a quenching tower, a dry reaction tower and a bag filter I, and the flue gas emission unit comprises a denitration reactor and a chimney; the liquid dangerous waste incineration process comprises a next incineration stage, a waste heat cooling stage, a flue gas purification stage and a flue gas discharge stage. According to the invention, the vertical incinerator is adopted to heat the waste liquid to high temperature for vaporization, then the waste liquid is recycled by heat in the flue gas collected by the waste heat boiler, and then the flue gas is subjected to a systematic purification process step by step through equipment such as a quenching tower, a dry reaction tower, a bag filter and the like in the flue gas purification unit once, so that harmful substances in the flue gas can be effectively removed, and finally the flue gas discharged through a chimney reaches the national standard, and the method is environment-friendly and energy-saving and has wider application prospect.
Description
Technical Field
The invention belongs to the technical field of waste incineration, and particularly relates to a liquid dangerous waste incineration system and an incineration process thereof.
Background
The liquid dangerous waste mainly refers to harmful liquid waste, including high-concentration liquid waste acid, waste alkali and the like, and has one or more dangerous characteristics of corrosiveness, toxicity, inflammability, reactivity or infectivity and the like. The water resource is rich in solid pollutants, aerobic pollutants, nutritional pollutants, acid-base pollutants, toxic pollutants and the like in the using process, so that the original use value is lost, and the water resource can be greatly damaged by random discharge and also can be liquid dangerous waste. Such liquid dangerous materials, if directly discharged, have harmful effects on the environment or human health, so that the treatment before the discharge of the liquid dangerous materials is of great importance.
Disclosure of Invention
Aiming at various defects in the prior art, the inventor researches and designs a liquid hazardous waste incineration system and an incineration process thereof in long-term practice, so that liquid hazardous substances can be purified and then discharged, the energy is saved, the environment is protected, and the economic benefit of enterprises is improved.
In order to achieve the above purpose, the present invention provides the following technical solutions: a liquid dangerous waste incineration system comprises an incineration unit, a flue gas purification unit and a flue gas discharge unit. One end of the flue gas purifying unit is connected with the incineration unit, and the other end of the flue gas purifying unit is connected with the flue gas discharging unit; the incineration unit comprises a buffer tank group, an incinerator, a waste heat boiler and a sewage tank; the upper part of the incinerator is provided with a spray gun group, and one side of the incinerator is provided with a heat exchanger and an air adjusting fan; the heat exchanger is connected with a heat exchange fan; the top of the waste heat boiler is provided with a steam collecting tank, the top of the steam collecting tank is provided with a sub-cylinder, and a white smoke heater I is arranged between the sub-cylinder and the steam collecting tank; a denitration spray gun is arranged at one side of the waste heat boiler and is connected with a denitration liquid storage tank; the flue gas purification unit comprises a quenching tower, a dry reaction tower and a bag filter I, wherein the inlet of the quenching tower is connected with the waste heat boiler, the outlet of the quenching tower is connected with the inlet of the dry reaction tower, and the outlet of the dry reaction tower is connected with the inlet of the bag filter I; the outlet of the bag filter I is connected with the inlet of the pickling tower, the outlet of the pickling tower is connected with the inlet of the neutralization tower, and the outlet of the neutralization tower is connected with the inlet of the bag filter II; a white smoke heater II is arranged between the neutralization tower and the bag filter II; the flue gas discharge unit comprises a denitration reactor and a chimney, an ammonia water evaporation tank is connected to the inlet of the denitration reactor, and the outlet of the denitration reactor is connected with the chimney.
Further, the buffer tank group comprises a low-calorific-value waste liquid buffer tank, a medium-calorific-value waste liquid buffer tank and a high-calorific-value waste liquid buffer tank; the spray gun group comprises a low heat value waste liquid spray gun, a medium heat value waste liquid spray gun and a high heat value waste liquid spray gun.
Further, a fuel oil storage device is arranged beside the incinerator and is connected with the incinerator through a fuel oil spray gun arranged on the incinerator; the lower part of the incinerator is also provided with an incinerator water seal box.
Further, the branch cylinder is connected with the softening water tank and the deoxidizing cabinet; a steam condenser is also arranged between the sub-cylinder and the softening water tank; and a waste heat boiler water seal box is arranged below the waste heat boiler.
Further, a water mist spray gun is arranged at one side of the quenching tower, and the lower end of the water mist spray gun is connected with a spray gun cooling fan; two sides of the dry reaction tower are respectively connected with a baking soda storage bin and an active carbon storage bin through pipelines; the bottom of the bag filter I is connected with the spiral conveyor I, and the lower end of the bag filter II is connected with the spiral conveyor II; the inlet of the neutralization tower is connected with a sodium hydroxide tank; the flue gas purification unit is also provided with a plurality of ash collectors.
Further, an induced draft fan is arranged between the denitration reactor and the bag filter II; an ammonia water tank is arranged on one side of the ammonia water evaporation tank, ammonia water is conveyed into the ammonia water evaporation tank through an ammonia water conveying pump, the ammonia water evaporation tank is also connected with an electric heater, and the electric heater is connected with a heating fan.
The invention also provides a liquid hazardous waste incineration process, which comprises the following steps:
s1, an incineration stage: spraying the waste liquid into a vertical incinerator through a waste liquid spray gun for incineration to generate flue gas;
s2, waste heat cooling stage: the flue gas from the incinerator enters a waste heat boiler for cooling;
S3, flue gas purification: the flue gas from the waste heat boiler enters a quenching tower for cooling, enters a dry reaction tower after passing through the quenching tower, enters a bag filter I for dedusting after passing through the dry reaction tower, enters an acid washing tower for preliminary deacidification after passing through the bag filter I, enters a neutralization tower for further deacidification after preliminary deacidification, and enters a bag filter II for dedusting after passing through the neutralization tower;
s4: fume emission stage: and the flue gas from the bag filter II enters a denitration reactor for denitration, and is discharged through a chimney.
Further, in the step S1, the incineration temperature is 1000 degrees celsius, and the residence time of the waste liquid in the incinerator is more than 2 seconds.
Further, in step S2, the flue gas enters the first return chamber in the waste heat boiler, the temperature of the flue gas is reduced to 950 ℃, and then enters the second return chamber, and the temperature is reduced to 500 ℃.
Further, the flue gas in the step S3 enters a quenching tower, clean water is sprayed into the quenching tower to cool the flue gas to 200 ℃ within 1 second; and in the step S3, the flue gas enters a precooler for preliminary cooling after being dedusted by a bag filter I, then enters an acid washing tower for preliminary deacidification, the temperature of the flue gas in the acid washing tower is reduced to 75 ℃, the flue gas discharged from the acid washing tower enters a neutralization tower, 20% sodium hydroxide solution is sprayed into the neutralization tower to react with acid gas in the flue gas, the flue gas discharged from the neutralization tower is defogged by a demister, and then enters a bag filter II for dedusting again after being heated to 190 ℃ by a white flue heater.
The beneficial effects of the invention are as follows:
(1) The waste liquid treatment system has the advantages that the combination of the incineration unit, the smoke purification unit and the smoke emission unit is adopted, the waste heat generated by incineration of waste liquid is collected by the waste heat boiler and is supplied to other auxiliary equipment in the system, meanwhile, the smoke is heated to the dew point by the white smoke heater, corrosion to system equipment is reduced, dangerous matters in the waste liquid can be effectively purified, energy is saved, and economic benefits of enterprises are improved.
(2) The waste liquid is heated to high temperature by adopting the vertical incinerator, heat in the flue gas is collected through the waste heat boiler for recycling, then the flue gas is subjected to a systematic purification process step by step through equipment such as a quenching tower, a dry reaction tower, a bag filter and the like in the flue gas purification unit at one time, harmful substances in the flue gas can be effectively removed, and finally the flue gas discharged through a chimney reaches the national standard, so that the method is environment-friendly and energy-saving and has wider application prospect.
Drawings
FIG. 1 is a schematic view of the overall construction of the incineration system of the present invention;
FIG. 2 is a schematic view of an incineration unit according to the present invention;
FIG. 3 is a schematic view of an incinerator of the present invention;
FIG. 4 is an enlarged view of a portion of the incinerator of the present invention;
FIG. 5 is a schematic view of a waste heat boiler of the present invention;
FIG. 6 is an enlarged view of a portion of the waste heat boiler of the present invention;
FIG. 7 is a schematic diagram of a flue gas cleaning unit according to the present invention;
FIG. 8 is a schematic diagram of a baking soda silo of the present invention;
FIG. 9 is a schematic view of a quench tower of the present invention;
fig. 10 is a schematic view of a smoke evacuation cell of the present invention.
In the accompanying drawings: 10-incineration unit, 20-flue gas purification unit, 30-flue gas emission unit, 11-buffer tank group, 111-low heat value waste liquid buffer tank, 112-medium heat value waste liquid buffer tank, 113-high heat value waste liquid buffer tank, 12-spray gun group, 121-low heat value waste liquid spray gun, 122-medium heat value waste liquid spray gun, 123-high heat value waste liquid spray gun, 13-combustion-supporting oil storage device, 131-combustion-supporting oil spray gun, 14-incinerator, 141-heat exchanger, 142-heat exchange fan, 143-adjusting air fan, 144-incinerator water seal box, 15-waste heat boiler, 151-denitration spray gun, 1511-denitration liquid storage tank, 1512-denitration liquid pump, 152-steam collection tank, 153-split cylinder, 1531-softening water tank 1532-deoxidizing cabinet, 1533-white smoke heater I, 1534-steam condenser, 154-waste heat boiler water seal box, 155-blowdown tank, 21-quench tower, 211-spray gun, 212-spray gun cooling fan, 22-dry reaction tower, 221-baking soda storage bin, 222-baking soda dust remover, 223-baking soda weighing device, 224-baking soda fan, 225-activated carbon storage bin, 226-activated carbon dust remover, 227-activated carbon weighing device, 228-activated carbon fan, 23-bag filter I, 231-screw conveyor I, 24-pickling tower, 241-sodium hydroxide tank, 25-neutralization tower, 26-bag filter II, 261-screw conveyor II, 27-ash collector, 31-induced draft fan, 32-denitration reactor, 33-ammonia evaporation tank, 331-ammonia tank, 332-ammonia delivery pump, 333-electric heater, 334-heating fan, 34-chimney.
Detailed Description
In order to make the technical solution of the present application better understood by those skilled in the art, the technical solution of the present application will be clearly and completely described below with reference to the accompanying drawings. Based on the embodiments of the present application, other similar embodiments, which may be obtained by those of ordinary skill in the art without making any inventive effort, should fall within the scope of the present application. In addition, directional words such as "upper", "lower", "left", "right", and the like, which are used in the following embodiments, are merely directions with reference to the drawings, and thus, the directional words used are intended to illustrate, not to limit, the application. Furthermore, the terms "first," "second," "third," and the like are used for descriptive purposes only and are not to be construed as indicating or implying relative importance.
In the description of the present invention, it should also be noted that, unless explicitly specified and limited otherwise, the terms "mounted," "connected," and "connected" are to be construed broadly, and may be either fixedly connected, detachably connected, or integrally connected, for example; can be mechanically or electrically connected; can be directly connected or indirectly connected through an intermediate medium. The specific meaning of the above terms in the present invention can be understood as appropriate by those of ordinary skill in the art.
The invention will be further described with reference to the drawings and preferred embodiments.
Referring to fig. 1, there is an overall schematic view of the liquid hazardous waste incineration system of the present invention, which includes an incineration unit 10, a flue gas purification unit 20, and a flue gas discharge unit 30. The smoke purifying unit 20 has one end connected to the incineration unit 10 and the other end connected to the smoke discharging unit 30. The dangerous materials to be incinerated pass through the incineration unit 10, then pass through the smoke purification unit 20, and finally the purified smoke is discharged by the smoke discharge unit 30.
Referring to fig. 2 to 6, the incineration unit 10 includes a buffer tank group 11, an incinerator 14, and a waste heat boiler 15. The buffer tank group 11 includes a low-heat-value waste liquid buffer tank 111, a medium-heat-value waste liquid buffer tank 112, and a high-heat-value waste liquid buffer tank 113, all of which convey waste liquids of different temperatures to the incinerator 14 through pipes. The incineration unit 10 is further provided with a blowdown tank 155 which collects impurities generated from the incineration unit 10 and periodically discharges them.
A lance set 12 is provided at the upper part of the incinerator 14. The spray gun set 12 comprises a low heat value waste liquid spray gun 121, a medium heat value waste liquid spray gun 122 and a high heat value waste liquid spray gun 123, which respectively atomize the waste liquid with different temperatures and then spray the atomized waste liquid into the incinerator 14, so that the waste liquid can be fully mixed with the air in the incinerator, and the combustion is more thorough. A fuel oil storage device 13 is arranged beside the incinerator 14, natural gas or fuel oil is stored in the fuel oil storage device, and the natural gas or the fuel oil is sprayed into the incinerator through a fuel oil spray gun 131 arranged on the incinerator 14.
A heat exchanger 141 is provided near the incinerator 14, and the heat exchanger 141 is connected to a heat exchange fan 142. The heat exchange fan 142 heats the air in the heat exchanger 141, and the heated air is supplied to the incinerator 14 to supplement the waste liquid in the incinerator with hot air. An air conditioning fan 143 is also provided beside the incinerator 14, which can adjust the air quantity according to the air pressure in the incinerator, so that the waste liquid is incinerated with sufficient oxygen.
An incinerator water seal box 144 is also connected to the lower part of the incinerator 14, and can collect the residue and ash generated after the waste liquid in the incinerator is burned out, and the residue and ash are discharged periodically after being quenched and cooled by water.
Referring to fig. 2, 5 and 6, the waste heat boiler 15 converts heat energy released from the incineration of the waste liquid into saturated or superheated steam, and a steam collecting tank 152 is provided at the top thereof. The steam collecting tank 152 collects the steam and delivers the steam to the separation cylinder 153. The sub-cylinder 153 is connected with a demineralized water tank 1531 and a deoxidizing cabinet 1532. In addition to the demineralized water tank 1531 and the oxygen tank 1532, the tap cylinder 153 may be connected to any process auxiliary equipment requiring thermal energy. A white smoke heater I1533 is also provided between the steam cylinder 153 and the steam collection tank 152, which heats the flue gas above the dew point, reducing the corrosion of the flue gas to the pipes. The demineralized water tank 1531 provides demineralized water to the system, pumps water through the water pump into the tank, and delivers it to the deoxygenated tank 1532 to prevent scaling thereof. A steam condenser 1534 is further provided between the steam dividing cylinder 153 and the demineralized water tank 1531, which converts the high temperature steam into condensed water and transfers the condensed water to the demineralized water tank for use, thereby preventing the demineralized water tank from being damaged by the high temperature steam. The deoxidizing cabinet 1532 removes oxygen from the softened water and then transfers the oxygen to the waste heat boiler 153, thereby preventing oxidation of the apparatus at high temperature.
A denitration spray gun 151 is provided beside the waste heat boiler 15, and is connected with a denitration liquid storage tank 1511, and denitration liquid is conveyed to the denitration spray gun 151 through a denitration liquid pump 1512. The denitration liquid generally adopts ammonia, urea or hydro-ammonia acid as a reducing agent, and is sprayed into a waste heat boiler through a denitration spray gun 151, so that the denitration liquid is rapidly decomposed into ammonia gas at high temperature, and reacts with nitrogen oxides in the flue gas to generate nitrogen gas and water, so that nitrogen elements in the flue gas are effectively removed.
A waste heat boiler water seal box 154 is arranged below the waste heat boiler 15, and can collect the residue and the residual ash generated after the waste liquid in the waste heat boiler is burned out, and the residue and the residual ash are discharged periodically after being quenched and cooled by water.
Referring to fig. 7 to 9, the flue gas cleaning unit 20 includes a quenching tower 21, a dry reaction tower 22, and a bag filter I23. The inlet of the quenching tower 21 is connected with the waste heat boiler 15, and the outlet is connected with the inlet of the dry reaction tower 22. The outlet of the dry reaction tower 22 is connected with the inlet of the bag filter I23 through a pipeline.
A water mist spray gun 211 is arranged on one side of the quenching tower 21, and atomized water is sprayed into the quenching tower through the water mist spray gun 211 and mixed with high-temperature flue gas in the quenching tower 21, so that the temperature of the flue gas is rapidly reduced. The lower end of the water mist spray gun 211 is connected with a spray gun cooling fan 212, and cooling air is blown into the spray gun to reduce the temperature of the spray gun.
Two sides of the dry reaction tower 22 are respectively connected with a baking soda storage bin 221 and an activated carbon storage bin 225 through pipelines, and the baking soda and the activated carbon are respectively conveyed to the dry reaction tower 22. The activated carbon can adsorb heavy metals, dioxin and other harmful substances in the flue gas, and the baking soda can react with the acid gas to form dust-like sodium salt. The baking soda warehouse 221 is provided with a baking soda dust remover 222 at the top and a baking soda weighing device 223 at the bottom, and a baking soda fan 224 is arranged beside the baking soda weighing device 223 to blow air into the conveying pipeline to blow baking soda into the dry reaction tower 22. The activated carbon storage bin 225 is provided with an activated carbon dust collector 226 at the top and an activated carbon weighing device 227 at the bottom, and an activated carbon blower 228 is arranged beside the activated carbon weighing device 227 to blow air into the conveying pipeline to blow activated carbon into the dry reaction tower 22.
The bag filter I23 filters dust in the flue gas, and the bottom of the bag filter I23 is connected with the screw conveyor I231 which can convey the dust in the bag filter I23 out.
The outlet of the bag filter I23 is connected with the inlet of the pickling tower 24 through a pipeline, water is sprayed into the pickling tower 24, and soluble acid gas is further dissolved, so that the content of the acid gas in the flue gas is reduced. The outlet of the pickling tower 24 is connected to the inlet of the neutralization tower 25 by a pipe. A sodium hydroxide tank 241 is connected to the inlet pipe of the neutralization tower 25, which provides the neutralization tower 25 with a 20% sodium hydroxide solution, which is again neutralized with the acid gases in the flue gas.
The outlet of the neutralization tower 25 is connected with the inlet of the bag filter II 26 through a pipeline, the flue gas enters the bag filter II 26 for further dust removal, and the lower end of the bag filter II 26 is connected with the screw conveyor II 262 which is used for conveying out dust in the bag filter II. A white smoke heater II 261 is arranged between the neutralization tower 25 and the bag filter II 26, and heats the smoke passing through the neutralization tower to be above the dew point, so that the corrosion of the smoke to a pipeline and a chimney is reduced, the diffusivity of pollutants is improved, and the technical requirements of equipment such as the pipeline and the like on corrosion prevention are reduced.
Ash collectors 27 for collecting and periodically discharging impurities generated after the purification of the flue gas are provided at the lower ends of the quenching tower 21, the dry reaction tower 22, the bag filter I23 and the bag filter II 26.
Referring to fig. 10, the flue gas discharge unit 30 includes a de-marketing reactor 32 and a stack 34. An induced draft fan 31 is arranged between the denitration reactor 32 and the bag filter II 26, so that the negative pressure state between the incinerator 14 and the induced draft fan 31 can be realized, and the flue gas can be smoothly conveyed until the flue gas is discharged out of the system.
An ammonia evaporation tank 33 is further connected to the inlet pipe of the denitration reactor 32 to provide ammonia vapor for the denitration reactor 32, and the ammonia vapor reacts with nitrogen oxides in the flue gas in the denitration reactor 32 to remove nitrogen elements in the flue gas.
An ammonia water tank 331 is provided beside the ammonia water evaporation tank 33, and ammonia water is fed into the ammonia water evaporation tank 33 by an ammonia water feed pump 332. An electric heater 333 is arranged beside the ammonia evaporation tank 33, the electric heater 333 is connected with a heating fan 334, the heating fan 334 blows air into the electric heater 333, the electric heater 333 heats the air and then introduces the air into the ammonia evaporation tank 33, and ammonia in the ammonia evaporation tank 33 is heated by hot air to be changed into ammonia steam for use in the ammonia steam co-denitration reactor 32. The flue gas which is treated by the denitration reactor 32 and reaches the national standard is discharged through a chimney 34.
The embodiment of the invention also provides a liquid dangerous waste incineration method, which comprises the following steps of
Step S1, the waste liquid is transported to a temporary storage warehouse by a special vehicle, is pumped to a buffer tank group by the waste liquid pump, is stored in the buffer tank, and is sprayed into the vertical incinerator by a waste liquid spray gun after multi-stage filtration. The incinerator is internally divided into a low-temperature section and a temperature-increasing section from top to bottom, the incineration temperature of the temperature-increasing section is 1000 ℃, the residence time of waste liquid in the incinerator is more than 2 seconds, and the waste liquid is conveyed to a waste heat boiler from an outlet of the incinerator.
Step S2, flue gas from the incinerator enters a first return chamber in the waste heat boiler, the temperature of the flue gas is reduced to 950 ℃, then enters a second return chamber, the temperature of the flue gas is reduced to 500 ℃, and saturated steam generated by heat of the flue gas is collected by a steam collecting tank and is used by other auxiliary equipment of the system.
And S3, enabling the flue gas from the waste heat boiler to enter a quenching tower, spraying clear water into the quenching tower to cool the flue gas to 200 ℃ within 1 second so as to reduce the re-synthesis of dioxin.
And S4, enabling the flue gas cooled by the quenching tower to enter a dry reaction tower, enabling activated carbon in the dry reaction tower to adsorb heavy metals, dioxin and other harmful substances in the flue gas, and enabling sodium bicarbonate to react with acid gas to form dust-like sodium salt.
And S5, after part of acid gas is removed by the dry reaction tower, the flue gas enters a bag filter I for dust removal, and ash in the flue gas flies through a screw conveyor I and is conveyed to an ash collector 27.
And S6, enabling the flue gas subjected to dust removal by the bag filter I to enter a precooler (not shown in the figure) for preliminary cooling, then entering a pickling tower for preliminary deacidification, cooling to 75 ℃ in the pickling tower, and removing part of hydrogen chloride, sulfur dioxide and hydrofluoric acid.
And S7, the flue gas from the acid washing tower enters a neutralization tower for further deacidification, 20% sodium hydroxide solution is sprayed into the neutralization tower to react with acid gas in the flue gas, and the temperature of the flue gas is reduced to 70 ℃.
And S8, demisting the flue gas from the neutralization tower through a demister (not shown in the figure), heating to 190 ℃ through a white flue gas heater, then entering a bag filter II for dedusting again, thoroughly removing dust particles, entering a denitration reactor for denitration, and finally discharging through a chimney.
The liquid dangerous waste incineration system adopts the combination of the incineration unit, the flue gas purification unit and the flue gas emission unit, utilizes the waste heat boiler to collect heat generated by incineration waste liquid and supply the heat to other auxiliary equipment in the system, and simultaneously utilizes the white flue gas heater to heat the flue gas to the dew point, thereby reducing corrosion to system equipment, effectively purifying waste liquid dangerous matters, saving energy and improving economic benefits of enterprises.
In addition, the liquid dangerous waste incineration method adopts the vertical incinerator to heat the waste liquid to high temperature for vaporization, then the waste liquid is recycled by heat in the flue gas collected by the waste heat boiler, and then the flue gas is subjected to a systematic purification process step by step through equipment such as a quenching tower, a dry reaction tower, a bag filter and the like in the flue gas purification unit at one time, so that harmful substances in the flue gas can be effectively removed, and finally the flue gas discharged through a chimney reaches the national standard, thereby being environment-friendly and energy-saving and having wider application prospect.
The foregoing detailed description of the application has been presented for purposes of illustration and description, but is not intended to limit the scope of the application, i.e., the application is not limited to the details shown and described.
Claims (7)
1. The liquid dangerous waste incineration system comprises an incineration unit (10), a flue gas purification unit (20) and a flue gas discharge unit (30), and is characterized in that one end of the flue gas purification unit (20) is connected with the incineration unit (10), and the other end of the flue gas purification unit is connected with the flue gas discharge unit (30);
The incineration unit (10) comprises a buffer tank group (11), an incinerator (14), a waste heat boiler (15) and a pollution discharge tank (155); the upper part of the incinerator (14) is provided with a spray gun group (12), and one side of the incinerator (14) is provided with a heat exchanger (141) and an air adjusting fan (143); the heat exchanger (141) is connected with a heat exchange fan (142);
the top of the waste heat boiler (15) is provided with a steam collecting tank (152), the top of the steam collecting tank (152) is provided with a branch cylinder (153), and a white smoke heater I (1533) is arranged between the branch cylinder (153) and the steam collecting tank (152); a denitration spray gun (151) is arranged on one side of the waste heat boiler (15), and the denitration spray gun (151) is connected with a denitration liquid storage tank (1511);
The flue gas purification unit (20) comprises a quenching tower (21), a dry reaction tower (22) and a bag filter I (23); the inlet of the quenching tower (21) is connected with the waste heat boiler (15), and the outlet of the quenching tower is connected with the inlet of the dry reaction tower (22); the outlet of the dry reaction tower (22) is connected with the inlet of the bag filter I (23); the outlet of the bag filter I (23) is connected with the inlet of the pickling tower (24); the outlet of the pickling tower (24) is connected with the inlet of the neutralization tower (25); the outlet of the neutralization tower (25) is connected with the inlet of the bag filter II (26); a white smoke heater II (261) is arranged between the neutralization tower (25) and the bag filter II (26);
the flue gas discharge unit (30) comprises a denitration reactor (32) and a chimney (34), and an ammonia water evaporation tank (33) is connected to the inlet of the denitration reactor (32); the outlet of the out-of-stock reactor (32) is connected with a chimney (34);
the buffer tank group (11) comprises a low-heat-value waste liquid buffer tank (111), a medium-heat-value waste liquid buffer tank (112) and a high-heat-value waste liquid buffer tank (113); the spray gun group (12) comprises a low-heat-value waste liquid spray gun (121), a medium-heat-value waste liquid spray gun (122) and a high-heat-value waste liquid spray gun (123);
a fuel oil storage device (13) is arranged beside the incinerator (14), and is connected with the incinerator (14) through a fuel oil spray gun (131) arranged on the incinerator (14); the lower part of the incinerator (14) is also provided with an incinerator water seal box (144);
The branch cylinder (153) is connected with a softening water tank (1531) and an deoxidizing cabinet (1532); a steam condenser (1534) is also arranged between the branch cylinder (153) and the softening water tank (1531); a waste heat boiler water seal box (154) is arranged below the waste heat boiler (15).
2. The liquid hazardous waste incineration system according to claim 1, wherein a water mist spray gun (211) is arranged at one side of the quenching tower (21), and a spray gun cooling fan (212) is connected to the lower end of the water mist spray gun (211); two sides of the dry reaction tower (22) are respectively connected with a baking soda storage bin (221) and an activated carbon storage bin (225) through pipelines; the bottom of the bag filter I (23) is connected with the screw conveyor I (231), and the lower end of the bag filter II (26) is connected with the screw conveyor II (262); an inlet of the neutralization tower (25) is connected with a sodium hydroxide tank (241); the flue gas purification unit (20) is also provided with a plurality of ash collectors (27).
3. A liquid hazardous waste incineration system according to claim 2, characterised in that an induced draft fan (31) is arranged between the denitrification reactor (32) and the bag filter II (26); an ammonia water tank (331) is arranged on one side of the ammonia water evaporation tank (33), ammonia water is conveyed into the ammonia water evaporation tank (33) through an ammonia water conveying pump (332), the ammonia water evaporation tank (33) is further connected with an electric heater (333), and the electric heater (333) is connected with a heating fan (334).
4. A liquid hazardous waste incineration process, characterized in that the liquid hazardous waste incineration process is applicable to the liquid hazardous waste incineration system according to any one of claims 1 to 3, comprising the steps of:
s1, an incineration stage: spraying the waste liquid into a vertical incinerator through a waste liquid spray gun for incineration to generate flue gas;
s2, waste heat cooling stage: the flue gas from the incinerator enters a waste heat boiler for cooling;
S3, flue gas purification: the flue gas from the waste heat boiler enters a quenching tower for cooling, enters a dry reaction tower after passing through the quenching tower, enters a bag filter I for dedusting after passing through the dry reaction tower, enters an acid washing tower for preliminary deacidification after passing through the bag filter I, enters a neutralization tower for further deacidification after preliminary deacidification, and enters a bag filter II for dedusting after passing through the neutralization tower;
s4: fume emission stage: and the flue gas from the bag filter II enters a denitration reactor for denitration, and is discharged through a chimney.
5. The process according to claim 4, wherein the incineration temperature is 1000 ℃ and the retention time of the waste liquid in the incinerator is more than 2 seconds.
6. The process of claim 4, wherein in step S2, the flue gas enters the first return chamber in the waste heat boiler, the temperature of the flue gas is reduced to 950 ℃, and then the temperature of the flue gas enters the second return chamber to 500 ℃.
7. The process for incinerating liquid hazardous waste according to claim 4, wherein the flue gas in the step S3 enters a quenching tower, and clean water is sprayed into the quenching tower to cool the flue gas to 200 ℃ within 1 second; and in the step S3, the flue gas enters a precooler for preliminary cooling after being dedusted by a bag filter I, then enters an acid washing tower for preliminary deacidification, the temperature of the flue gas in the acid washing tower is reduced to 75 ℃, the flue gas discharged from the acid washing tower enters a neutralization tower, 20% sodium hydroxide solution is sprayed into the neutralization tower to react with acid gas in the flue gas, the flue gas discharged from the neutralization tower is defogged by a demister, and then enters a bag filter II for dedusting again after being heated to 190 ℃ by a white flue heater.
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| CN110645583A (en) * | 2019-11-06 | 2020-01-03 | 北京首创环境科技有限公司 | Ultra-clean emission treatment system and method for hazardous waste incineration flue gas |
| CN113464959B (en) * | 2021-07-02 | 2023-05-09 | 深圳星河环境股份有限公司 | Incineration system and technology suitable for medium and low heat value waste liquid |
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