CN109099437A - A kind of waste total system and its processing method - Google Patents
A kind of waste total system and its processing method Download PDFInfo
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- CN109099437A CN109099437A CN201811114420.7A CN201811114420A CN109099437A CN 109099437 A CN109099437 A CN 109099437A CN 201811114420 A CN201811114420 A CN 201811114420A CN 109099437 A CN109099437 A CN 109099437A
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- waste
- flue gas
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- gas
- combustion furnace
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- 239000002699 waste material Substances 0.000 title claims abstract description 49
- 238000003672 processing method Methods 0.000 title claims abstract description 7
- 239000003546 flue gas Substances 0.000 claims abstract description 84
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims abstract description 81
- 238000002485 combustion reaction Methods 0.000 claims abstract description 32
- 239000002912 waste gas Substances 0.000 claims abstract description 29
- 239000007789 gas Substances 0.000 claims abstract description 22
- 238000002309 gasification Methods 0.000 claims abstract description 17
- 238000000034 method Methods 0.000 claims abstract description 14
- 150000003839 salts Chemical group 0.000 claims abstract description 13
- 239000000428 dust Substances 0.000 claims abstract description 11
- 239000010808 liquid waste Substances 0.000 claims abstract description 9
- 239000002245 particle Substances 0.000 claims abstract description 6
- 239000012535 impurity Substances 0.000 claims abstract description 5
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 33
- 238000010521 absorption reaction Methods 0.000 claims description 29
- 238000006243 chemical reaction Methods 0.000 claims description 17
- 238000005554 pickling Methods 0.000 claims description 17
- 239000003518 caustics Substances 0.000 claims description 16
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 claims description 13
- 239000000835 fiber Substances 0.000 claims description 12
- 239000012716 precipitator Substances 0.000 claims description 12
- 239000003595 mist Substances 0.000 claims description 11
- 239000012530 fluid Substances 0.000 claims description 9
- 239000002918 waste heat Substances 0.000 claims description 9
- 238000004140 cleaning Methods 0.000 claims description 5
- 239000007921 spray Substances 0.000 claims description 5
- 238000010828 elution Methods 0.000 claims description 4
- 238000005453 pelletization Methods 0.000 claims description 4
- 238000000889 atomisation Methods 0.000 claims description 3
- 239000003517 fume Substances 0.000 claims description 3
- 238000002156 mixing Methods 0.000 claims description 3
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 abstract description 8
- 239000007788 liquid Substances 0.000 abstract description 7
- 238000004064 recycling Methods 0.000 abstract description 5
- 239000000377 silicon dioxide Substances 0.000 abstract description 5
- 239000007787 solid Substances 0.000 abstract description 4
- 238000000926 separation method Methods 0.000 abstract description 2
- 239000012071 phase Substances 0.000 abstract 2
- 239000008247 solid mixture Substances 0.000 abstract 1
- 239000007790 solid phase Substances 0.000 abstract 1
- 238000005979 thermal decomposition reaction Methods 0.000 abstract 1
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 description 34
- 239000000243 solution Substances 0.000 description 19
- 239000002253 acid Substances 0.000 description 8
- 239000002920 hazardous waste Substances 0.000 description 8
- KVGZZAHHUNAVKZ-UHFFFAOYSA-N 1,4-Dioxin Chemical compound O1C=COC=C1 KVGZZAHHUNAVKZ-UHFFFAOYSA-N 0.000 description 7
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 6
- 238000012545 processing Methods 0.000 description 6
- 239000000047 product Substances 0.000 description 5
- 235000019504 cigarettes Nutrition 0.000 description 4
- 238000001816 cooling Methods 0.000 description 4
- 230000000694 effects Effects 0.000 description 4
- 239000004744 fabric Substances 0.000 description 3
- 229910001385 heavy metal Inorganic materials 0.000 description 3
- 239000003345 natural gas Substances 0.000 description 3
- 230000007935 neutral effect Effects 0.000 description 3
- 238000006386 neutralization reaction Methods 0.000 description 3
- 230000008569 process Effects 0.000 description 3
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 2
- 239000012267 brine Substances 0.000 description 2
- 230000008859 change Effects 0.000 description 2
- 229910052681 coesite Inorganic materials 0.000 description 2
- 229910052906 cristobalite Inorganic materials 0.000 description 2
- 238000000354 decomposition reaction Methods 0.000 description 2
- 239000002283 diesel fuel Substances 0.000 description 2
- 238000001035 drying Methods 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 239000000446 fuel Substances 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- 230000009965 odorless effect Effects 0.000 description 2
- 230000003647 oxidation Effects 0.000 description 2
- 238000007254 oxidation reaction Methods 0.000 description 2
- 239000013618 particulate matter Substances 0.000 description 2
- 230000000704 physical effect Effects 0.000 description 2
- 238000000197 pyrolysis Methods 0.000 description 2
- 230000008929 regeneration Effects 0.000 description 2
- 238000011069 regeneration method Methods 0.000 description 2
- HPALAKNZSZLMCH-UHFFFAOYSA-M sodium;chloride;hydrate Chemical compound O.[Na+].[Cl-] HPALAKNZSZLMCH-UHFFFAOYSA-M 0.000 description 2
- 229910052682 stishovite Inorganic materials 0.000 description 2
- 239000013589 supplement Substances 0.000 description 2
- 229910052905 tridymite Inorganic materials 0.000 description 2
- 238000005406 washing Methods 0.000 description 2
- 241001274216 Naso Species 0.000 description 1
- 239000000809 air pollutant Substances 0.000 description 1
- 231100001243 air pollutant Toxicity 0.000 description 1
- 239000003513 alkali Substances 0.000 description 1
- 238000013459 approach Methods 0.000 description 1
- 239000007864 aqueous solution Substances 0.000 description 1
- 230000008901 benefit Effects 0.000 description 1
- 230000033228 biological regulation Effects 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 238000004364 calculation method Methods 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- NEHMKBQYUWJMIP-UHFFFAOYSA-N chloromethane Chemical class ClC NEHMKBQYUWJMIP-UHFFFAOYSA-N 0.000 description 1
- 238000009833 condensation Methods 0.000 description 1
- 230000005494 condensation Effects 0.000 description 1
- 238000011109 contamination Methods 0.000 description 1
- 125000004122 cyclic group Chemical group 0.000 description 1
- 230000006378 damage Effects 0.000 description 1
- 230000007423 decrease Effects 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 238000010612 desalination reaction Methods 0.000 description 1
- 238000001514 detection method Methods 0.000 description 1
- 238000011161 development Methods 0.000 description 1
- 230000018109 developmental process Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 150000002013 dioxins Chemical class 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 238000012850 discrimination method Methods 0.000 description 1
- 239000006185 dispersion Substances 0.000 description 1
- 238000004090 dissolution Methods 0.000 description 1
- 239000003344 environmental pollutant Substances 0.000 description 1
- 238000001704 evaporation Methods 0.000 description 1
- 230000008020 evaporation Effects 0.000 description 1
- 239000002737 fuel gas Substances 0.000 description 1
- 230000036541 health Effects 0.000 description 1
- QAOWNCQODCNURD-UHFFFAOYSA-M hydrogensulfate Chemical compound OS([O-])(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-M 0.000 description 1
- 239000002440 industrial waste Substances 0.000 description 1
- 230000007774 longterm Effects 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 229910052751 metal Inorganic materials 0.000 description 1
- 239000002184 metal Substances 0.000 description 1
- 150000002736 metal compounds Chemical class 0.000 description 1
- 230000003020 moisturizing effect Effects 0.000 description 1
- 230000003472 neutralizing effect Effects 0.000 description 1
- 235000021110 pickles Nutrition 0.000 description 1
- 231100000719 pollutant Toxicity 0.000 description 1
- 238000004321 preservation Methods 0.000 description 1
- 238000003825 pressing Methods 0.000 description 1
- 230000009257 reactivity Effects 0.000 description 1
- 230000000630 rising effect Effects 0.000 description 1
- 229920006395 saturated elastomer Polymers 0.000 description 1
- 238000005201 scrubbing Methods 0.000 description 1
- 239000002893 slag Substances 0.000 description 1
- 239000000779 smoke Substances 0.000 description 1
- 239000002910 solid waste Substances 0.000 description 1
- 238000003860 storage Methods 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 230000009469 supplementation Effects 0.000 description 1
- 230000001502 supplementing effect Effects 0.000 description 1
- 230000004083 survival effect Effects 0.000 description 1
- 230000002194 synthesizing effect Effects 0.000 description 1
- 238000012360 testing method Methods 0.000 description 1
- 238000002207 thermal evaporation Methods 0.000 description 1
- 231100000331 toxic Toxicity 0.000 description 1
- 230000002588 toxic effect Effects 0.000 description 1
- 238000009834 vaporization Methods 0.000 description 1
- 230000008016 vaporization Effects 0.000 description 1
- 239000002351 wastewater Substances 0.000 description 1
Classifications
-
- 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
- F23G5/20—Incineration of waste; Incinerator constructions; Details, accessories or control therefor having rotating or oscillating drums
-
- 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
-
- 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
- F23G7/00—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals
- F23G7/06—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals of waste gases or noxious gases, e.g. exhaust gases
-
- 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
- F23J15/06—Arrangements of devices for treating smoke or fumes of coolers
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
- F23G2203/00—Furnace arrangements
- F23G2203/20—Rotary drum furnace
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
- F23G2206/00—Waste heat recuperation
- F23G2206/20—Waste heat recuperation using the heat in association with another installation
- F23G2206/203—Waste heat recuperation using the heat in association with another installation with a power/heat generating installation
-
- 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
- Y02E20/12—Heat utilisation in combustion or incineration of waste
Abstract
The invention discloses a kind of waste total system and its processing methods.Method includes the following steps: waste residue is delivered in rotary kiln by (1), the gas-solid mixture of burning, thermal decomposition, generation is separated by cyclone dust collectors, and gas phase enters in waste gas combustion furnace, and solid phase is directly carried out except unlap；(2) salt bearing liquid wastes are delivered in gasification burner, are vaporized, subsequently into incinerator；(3) exhaust gas and salt-free waste liquid are passed directly into waste gas combustion furnace, are burned；(4) flue-gas temperature obtained by step (3) is made to be down to 200~250 DEG C in 1~3s, the SiO then contained in recovered flue gas2Particle, gas phase enter back into bag filter and carry out the separation of gas-solid essence；(5) HCl in flue gas obtained by collection step (4)；Then the impurity in flue gas is further removed, is finally discharged.The method of the present invention can effectively be handled trade waste, it is made to meet discharge standard, and the silica in capable of recycling the waste.
Description
Technical field
The invention belongs to Waste Disposal Technology fields, and in particular to a kind of waste total system and its processing side
Method.
Background technique
Hazardous waste, which refers to, is included in National Hazard waste register, or is recognized according to the hazardous waste discrimination method of national regulation
The fixed waste with hazard property, so-called hazard property are primarily referred to as toxic, explosivity, inflammability, corrosivity, chemistry
Reactivity, infectiousness, radioactivity etc.；It therefore, include the above-mentioned above hazard profile of one or more, and with its distinctive property pair
The substance that environment generates pollution is just hazardous waste.
As society and expanding economy, industrial waste especially hazardous waste yield and type are increasing, have drawn
Play the very big concern of government and the public；The discharge everywhere and unreasonable disposition of hazardous waste, can endanger people's health, long-term product
Tired seriously to destroy ecological environment for the survival of mankind, extent of the destruction is much larger than house refuse；Currently, hazardous waste has become
For the protrusion public hazards of worldwide range, active development new technology, new process, new equipment carry out the centralized management to hazardous waste
It is disposed with science, reducing and eliminate contamination hazard has been the task of top priority.
Summary of the invention
For above-mentioned deficiency in the prior art, the present invention provides a kind of waste total system and its processing side
Method can effectively handle the waste with hazard property, reach corresponding discharge standard.
To achieve the above object, the technical solution adopted by the present invention to solve the technical problems is:
A kind of waste total system, including rotary kiln, gasification burner and exhaust treatment system；
The exhaust treatment system include the waste gas combustion furnace being sequentially communicated, dust pelletizing system, absorption tower, elution Tower System with
And mist water separator；The rotary kiln and gasification burner are connected to waste gas combustion furnace.
Further, dust pelletizing system includes the fiber bag precipitator and wet dedusting tower being sequentially communicated；The wet dust removal
Two heat exchangers engaged therewith are provided at tower.
Further, it is additionally provided with the waste heat boiler being connected between waste gas combustion furnace and fiber bag precipitator and half dry type is anti-
Answer tower.
Further, absorption tower is three-level pickling absorption tower, and is provided with three heat exchangers engaged therewith.
Further, elution Tower System includes the water scrubber and caustic wash tower being sequentially communicated.
The method that waste is handled using above system, comprising the following steps:
(1) waste residue is delivered in rotary kiln, rotary kiln is rotated with the revolving speed of 1~3r/min, in 800~850 DEG C of item
It burns under part, the flue gas of generation enters in waste gas combustion furnace；
(2) salt bearing liquid wastes are delivered in gasification burner, are vaporized in 450~700 DEG C, then gas phase enters waste gas combustion furnace
In；
(3) by exhaust gas and not, salt bearing liquid wastes are passed directly into waste gas combustion furnace, with gained in step (1) and step (2)
Product mixing, then burns under conditions of 1100~1200 DEG C, -100Pa~100Pa, and the flue gas generated after burning is passed through remaining
In heat boiler, so that flue-gas temperature is reduced to 500~550 DEG C；
(4) flue gas obtained by step (3) is passed through in half dry type reaction tower, its temperature is made to be down to 200~230 in 1~3s
DEG C, it is then successively passed through again into fiber bag precipitator and wet dedusting tower, the SiO contained in recovered flue gas2Particle, and make cigarette
Temperature degree is down to 50~70 DEG C；
(5) flue gas obtained by step (4) is passed through three-level pickling absorption tower, collects the HCl in flue gas；Then again by flue gas after
It is continuous to be passed through into water scrubber and caustic wash tower, the impurity in flue gas is further removed, is discharged after being handled finally by mist water separator.
Further, waste is the waste of generation during organosilicon reaction.
Further, the revolving speed of rotary kiln is 2r/min in step (1), and temperature is 800 DEG C, and pressure is -64Pa.
Further, the flue gas temperature-fall period in half dry type reaction tower again in step (4) are as follows:
Water source is conveyed into half dry type reaction tower by the two-fluid spray nozzle at the top of half dry type reaction tower, and makes water source mist
To change, the lye droplet being atomized is acted on by upward hot fume, the high-density region that a droplet suspends is formed near the nozzle,
Temperature is cooled to rapidly 200 DEG C or so in 1s when flue gas passes through this region.
Further, the cleaning solution in step (5) in caustic wash tower is NaOH solution and NaSO3Solution is 1 according to volume ratio:
The mixed liquor that 1 ratio mixes.
The invention has the benefit that
1, under conditions of -100~100Pa, the ignition temperature in waste gas combustion furnace reaches 1100~1200 DEG C, makes to burn
More completely, achieve the effect that smokeless, odorless, without secondary pollution；Also, the mixed gas waste gas combustion furnace residence time is greater than 2 seconds,
So that micro-content organism therein and dioxin are sufficiently decomposed, decomposition efficiency is more than 99.99%, it is ensured that enters hazardous waste
Full combustion is complete.
2, the flue gas that waste gas combustion furnace generates after burning enters in waste heat boiler, can effectively recycle in flue gas
Thermal energy, and the temperature of flue gas is reduced, it is convenient for subsequent processing.
3, the high-density region that lye droplet suspends is formed in half dry type reaction tower, temperature exists when flue gas passes through this region
200 DEG C or so are reduced to from 500 DEG C rapidly in 1s, to restrained effectively the regeneration of dioxin；It is had in flue gas simultaneously
The droplet that is also injected into of some Mars extinguish, the equipment to protect subsequent fiber bag precipitator and remaining non-refractory.
4, fiber bag precipitator can remove the heavy metal that partially dissociates in the fine solid particle and flue gas being detained in flue gas
Object is closed, heavy metal and dioxins concentration in flue gas are reduced.
5, the HCl in flue gas is recycled by three-level pickling absorption tower, the acid solution recycled, a part as at
Product output, remaining can be delivered to again in three-level pickling absorption tower, to continue as the absorbing liquid in three-level pickling absorption tower
HCl recycling is carried out to subsequent flue gas.
6, through the invention in system and method, it is ensured that the waste generated in production process can be safe and stable
Burning, and HCl and SiO in recovered flue gas can be recycled2, meanwhile, the content of the impurity such as dioxin in flue gas can be reduced, cigarette is made
Gas reaches discharge standard.
Detailed description of the invention
Fig. 1 is the functional block diagram of this system.
Wherein, 1, rotary kiln；2, gasification burner；3, waste gas combustion furnace；4, waste heat boiler；5, half dry type reaction tower；6, cloth bag
Formula deduster；7, wet dedusting tower；8, heat exchanger；9, absorption tower；10, water scrubber；11, caustic wash tower；12, mist water separator；13,
Cyclone separator.
Specific embodiment
A specific embodiment of the invention is described below, in order to facilitate understanding by those skilled in the art this hair
It is bright, it should be apparent that the present invention is not limited to the ranges of specific embodiment, for those skilled in the art,
As long as various change is in the spirit and scope of the present invention that the attached claims limit and determine, these variations are aobvious and easy
See, all are using the innovation and creation of present inventive concept in the column of protection.
Embodiment 1
As shown in Figure 1, the waste total system, including rotary kiln 1, gasification burner 2, cyclone separator 13 and useless
Gas processing system；Wherein, rotary kiln 1 and gasification burner 2 are connected to cyclone separator 13 respectively, cyclone separator 13 and exhaust-gas treatment
System connectivity.
The waste total system is additionally provided with the waste material collocation area cooperated with rotary kiln 1, and physical property is different
Waste material is premixed, collocation charging.
As shown in Figure 1, the exhaust treatment system includes that the waste gas combustion furnace 3, waste heat boiler 4, half dry type that are sequentially communicated are anti-
Answer tower 5, fiber bag precipitator 6, wet dedusting tower 7, absorption tower 9, water scrubber 10 and caustic wash tower 11；Wherein, waste gas combustion furnace 3
It is connected to cyclone separator 13.
Also, rotary kiln 1, gasification burner 2, cyclone separator 13, waste gas combustion furnace 3, waste heat boiler 4, half dry type reaction tower 5
And 6 bottom of fiber bag precipitator, it is connected to the silica collector for receiving silica.
As shown in Figure 1, being respectively arranged with heat exchanger 8 engaged therewith at wet dedusting tower 7 and absorption tower 9, wherein wet
Two heat exchangers 8 are provided at formula gas wash tower 7, a normal use, one spare；Three heat exchangers are provided at absorption tower 9
8, also, the absorption tower 9 is three-level pickling absorption tower.
As shown in Figure 1, be also communicated with mist water separator 12 at caustic wash tower 11, for through treated the cigarette of caustic wash tower 11
Gas carries out water mist separation, then the air-introduced machine guidance discharge through being connected to mist water separator 12 again.
Embodiment 2
The method that waste is handled using system described in embodiment 1, comprising the following steps:
(1) after waste residue being packaged, transport to feed zone, and waste material collocation area is provided at feed zone, not by physical property
Same waste material is premixed, collocation charging；The waste material matched is delivered to incineration area, and solid waste is promoted to by bucket elevator
Hopper, waste material enter feed chute, are sent into rotary kiln by hydraulic feeder；
(2) after waste residue enters rotary kiln, temperature be 800~850 DEG C, revolving speed be 1~3r/min (according to actual condition into
Row adjust, be more difficult to decompose speed demand it is lower), pressure be -90Pa in the state of, along rotary kiln tilt angle (generally
3 °~5 °) and direction of rotation slowly move, gradually by drying, pyrolysis and gasification, the flue gas of generation enter in waste gas combustion furnace into
Row is handled in next step.
According to burning 3T1E (temperature, time, vortex, coefficient of excess) principle, so that clinker fills in furnace body combustion chamber
Point oxidation, pyrolysis, burning, and furnace body with per minute several turns revolving speed rotation (be configured with frequency converter, can be according to the heat of waste residue
It is worth the revolving speed of variable frequency adjustment rotary kiln), it by moisture content height, kills in following waste residue automatic turning, on one side by heated drying, on one side
By the revolution of rotary kiln, make the broken dispersion of material, waste residue is decomposed in the back segment of stove；
Waste residue smoulder in rotary kiln, using the rotation of rotary kiln and the gradient of kiln body itself, waste residue fires on one side
It burns and enters kiln tail portion on one side, finally fall into hydrolock dragveyer, export lime-ash through conveyer；And the flue gas generated is burned useless
It is further burned in gas incinerator, temperature increases to 1100~1200 DEG C under auxiliary fuel, keeps burning more complete, reaches nothing
Cigarette, effect odorless, without secondary pollution, also, the flue gas entered in waste gas combustion furnace is needed in its burning indoor residence time
Greater than 2 seconds, so that the micro-content organism and dioxin in flue gas are sufficiently decomposed, decomposition efficiency was more than 99.99%, it is ensured that combustion
It burns down complete.
(3) after the pressurized pump pressurization of salt bearing liquid wastes, gasification burner is sent by waste water spray gun；Furnace temperature control is vaporized in 450-
Between 700 DEG C；Waste liquid evaporates in gasification burner, vaporizes vapor of the formation containing particulate matter, and then high-temperature cyclone dust extractor will
Particulate matter therein is removed, waste gas combustion furnace is entered back into and carries out high temperature incineration oxidation processes, temperature is 800~850 DEG C；And it is precipitated
Salt mainly deposit to vaporization furnace bottom with Granular forms；The bottom of gasification burner is provided with a set of water cooling scraper slagging machine；
Its salt slag deposited after the cooling of water cooling scraper slagging machine by being discharged；Also, booster burners are provided on gasification burner；With
To control the fire box temperature in gasification burner.
(4) exhaust gas that is come out from factory technics device and salt bearing liquid wastes can be fed directly in waste gas combustion furnace；It is free of
Bisulfate waste liquor is first transported to the waste liquid tank on waste gas combustion furnace, by booster pump be delivered to the waste liquid burner in waste gas combustion furnace into
Row atomization is burned；And the natural gas how much measured or diesel oil are required supplementation with according to theoretical calculation exhaust gas liquid and can be only achieved and stablize burning
Condition.
Natural gas is entering hearth combustion by burner into fuel gas pipeline behind battery limit (BL), and fuel is mainly carrying out baker, rising
It is used when mild heat preservation operation；After flue gas puts into normal table burning, natural gas or diesel oil stopping are come into operation, chloromethanes is utilized
Tail gas independently burns, and provides stable heat source for the not strong flue gas of other flammabilities.
Salt bearing liquid wastes are not decomposed at high temperature, are aoxidized, and generate CO2、H2O、HCl、SiO2Deng also a large amount of in generation flue gas
N2The superfluous O with part2And the Cl of micro free state2(the Cl of these free states2Alkali and Na are used after into caustic wash tower2SO3
Solution absorbs it)
(5) vapor of waste residue generates flue gas, salt bearing liquid wastes generation is together with the product in step (4) in burned waste gas
The incineration temperature of burning in furnace, waste gas combustion furnace is controlled at 1100 DEG C~1200 DEG C or so.
(6) high-temperature flue gas come out in incinerator, first by waste heat boiler thermal energy recycling most of in flue gas, thus
The saturated vapor for generating 1.0MpaG is incorporated to pipe network；After waste heat boiler, flue-gas temperature is also down to 500-550 DEG C by 1150 DEG C
Left and right.
And it is the chance for reducing dioxin and synthesizing again, it is necessary to reduce flue gas in 240~500 DEG C of residence time, need
Flue gas is set quickly to be cooled to 240 DEG C hereinafter, the measure " chilling " taken, detailed process are as follows:
Flue gas after cooling enters half dry type reaction tower；Wherein, force (forcing) pump supplies clear water as needed, reacted top of tower
Two-fluid spray nozzle is sent into reaction tower, and aqueous solution is atomized into subtle droplet by two-fluid spray nozzle, and the droplet being atomized is by upward
Hot fume effect forms the high-density region that a droplet suspends near the nozzle, and when flue gas passes through this region, temperature is in 1s
200 DEG C or so are reduced to from 500 DEG C rapidly, to restrained effectively the regeneration of dioxin；Some fire in flue gas simultaneously
The water mist that star is injected into extinguishes, and protects subsequent cloth bag not to be burned, the flying dust of generation is collected into flying dust working area of temporary library etc.
Wait outward transport processing.
(7) flue gas subsequently enters fiber bag precipitator, is partially swum with removing in the fine solid particle and flue gas being detained in flue gas
From heavy metal compound；The active carbon being blown in the pipeline weight (as needed) for entering fiber bag precipitator, adsorbing in flue gas
Metal and dioxin, dust and active carbon powder under intercepting through cloth bag are discharged outside bag filter with star-shaped dust-discharging valve.
(8) then pass through pipeline by the purified flue gas of fiber bag precipitator and enter wet dedusting tower, in wet type tower dedusting
In tower, flue gas is directly in contact with the circulation concentrated hydrochloric acid of atomisation, and the moisture and HCl in hydrochloric acid are by thermal evaporation, heat absorption, simultaneously
Heat transmitting of the hydrochloric acid solution between flue gas itself is recycled, also reduces rapidly the temperature of flue gas.
By wet dedusting tower, flue-gas temperature is reduced to 70 DEG C or so from 200 DEG C；Gas wash tower be furnished with two heat exchangers, one
Platform works normally, and one spare, and the heat in circulation fluid is then taken away by heat exchanger heat exchange.
In wet dedusting tower, flue gas goes in the same direction with cyclic absorption hydrochloric acid solution, at this point, the HCl gas in flue gas will not
The water in hydrochloric acid for being dissolved in hydrochloric acid solution, and recycling, which can evaporate, to be become vapor and enters hydrochloric acid absorption tower；To being carried in flue gas
SiO2Carry out hydraulic dust-removing.With the operation of incinerator, solid content is gradually increased in circulation fluid, in order to avoid circulation fluid at
For gel, circulation fluid periodically should be drained into neutralization pond.Wet dedusting tower circulation fluid supplement absorption tower under tower concentrated hydrochloric acid, allow its not
It absorbs or absorbs HCl gas in flue gas less, only wash away entrained with dust in flue gas.
(9) flue gas after dedusting enters pickling absorption tower, is substantially free of SiO in flue gas at this time2Particle, therefore can be with
The hydrochloric acid of relative clean is obtained in pickling absorption tower.Pickling absorption tower is three-level pickling absorption tower, and flue gas and circulation acid solution are inverse
Xiang Erhang divides upper, middle and lower three-level to absorb.At this point, the HCl gas in flue gas is dissolved in acid solution, water vapour is condensed into water.
Three-level pickling absorption tower is furnished with three heat exchangers (upper, middle and lower respectively matches one), due to the dissolution of HCl gas and water vapour
Condensation is all exothermic reaction, and the heat that they are released is taken away by the heat exchanger on circulating absorption solution pipeline.Also, by three-level pickling
The hydrochloric acid that absorb the bottom of the tower comes out, as finished acid, a part are exported as finished product, acid solution needed for can supplementing water scrubber, or
Acid solution needed for other devices；Rest part turns again to three-level pickling absorption tower, to supplement the circulation acid solution in it.
(10) flue gas come out from three-level pickling absorption tower, HCl content therein has substantially reduced, subsequently into washing
Tower further decreases HCl content in flue gas.The water that water scrubber comes out can be recycled in tower reactor, while water scrubber tower reactor
Also it can be three-level pickling absorption tower moisturizing, absorb recycling HCl to greatest extent, reduce water usage.
(11) flue gas subsequently enters neutralization scrubbing tower, i.e. caustic wash tower, and NaOH and NaSO is configured in caustic wash tower3Mixing
Solution efficiently carries out final carrying out washing treatment as cleaning solution, by the cleaning solution in caustic wash tower to flue gas, in flue gas
The Cl of remaining few HCl and free state2It neutralizes, becomes salt water discharge, flue gas emission is made to be up to state standards.
When the cleaning solution in caustic wash tower tower reactor storage tank becomes to approach neutral salt water after wash cycle after a period of time
When neutral brine is replaced.Acid pickle in neutral brine and wet dedusting tower enters neutralization pond, molten after neutralizing filters pressing
Liquid enters triple effect evaporation former pond and is evaporated desalination；It is recycled, caustic wash tower treated flue gas is separated by fog
After device removes water mist, the processing that the Litter in entire production process is completed to atmosphere is arranged through chimney from air-introduced machine.
The flue gas that detects that treated through the invention according to emission standard of air pollutants for boilers (GB13271-2014),
The testing result of its nuisance content is shown in Table 1.
1 flue gas nuisance content of table
By the detection data of table 1 it is found that the content of every pollutant reaches in flue gas after the method for the present invention is handled
Discharge standard is even far below discharge standard, thus illustrates, the method for the present invention can effective purifying smoke, remove flue gas
In impurity content.
Claims (10)
1. a kind of waste total system, which is characterized in that including rotary kiln, gasification burner and exhaust treatment system；
The exhaust treatment system includes the waste gas combustion furnace being sequentially communicated, dust pelletizing system, absorption tower, elution Tower System and mist
Separator；The rotary kiln and gasification burner are connected to waste gas combustion furnace.
2. waste total system according to claim 1, which is characterized in that the dust pelletizing system includes successively connecting
Logical fiber bag precipitator and wet dedusting tower；Two heat exchangers engaged therewith are provided at the wet dedusting tower.
3. waste total system according to claim 2, which is characterized in that the waste gas combustion furnace and cloth-bag type
The waste heat boiler and half dry type reaction tower of connection are additionally provided between deduster.
4. waste total system according to claim 3, which is characterized in that the absorption tower is three-level pickling suction
Tower is received, and is provided with three heat exchangers engaged therewith.
5. waste total system according to claim 4, which is characterized in that the elution Tower System includes successively
The water scrubber and caustic wash tower of connection.
6. the method handled using system described in claim 5 waste, which comprises the following steps:
(1) waste residue is delivered in rotary kiln, rotary kiln is rotated with the revolving speed of 1~3r/min, under conditions of 800~850 DEG C
Burning, the flue gas of generation enter in waste gas combustion furnace；
(2) salt bearing liquid wastes are delivered in gasification burner, are vaporized in 450~700 DEG C, then gas phase enters in waste gas combustion furnace；
(3) by exhaust gas and not, salt bearing liquid wastes are passed directly into waste gas combustion furnace, with products therefrom in step (1) and step (2)
Mixing, then burns under conditions of 1100~1200 DEG C, -100Pa~100Pa, the flue gas generated after burning is passed through waste heat pot
In furnace, so that flue-gas temperature is reduced to 500~550 DEG C；
(4) flue gas obtained by step (3) is passed through in half dry type reaction tower, so that its temperature is down to 200~230 DEG C in 1~3s, so
It is successively passed through again into fiber bag precipitator and wet dedusting tower afterwards, the SiO contained in recovered flue gas2Particle, and make flue gas temperature
Degree is down to 50~70 DEG C；
(5) flue gas obtained by step (4) is passed through three-level pickling absorption tower, collects the HCl in flue gas；Then again flue gas is continued to lead to
Enter into water scrubber and caustic wash tower, further removes the impurity in flue gas, be discharged after being handled finally by mist water separator.
7. processing method according to claim 6, which is characterized in that the waste is generation during organosilicon reaction
Waste.
8. processing method according to claim 6, which is characterized in that the revolving speed of rotary kiln described in step (1) is 2r/
Min, temperature are 800 DEG C, and pressure is -64Pa.
9. processing method according to claim 6, which is characterized in that flue gas is again in half dry type reaction tower in step (4)
Temperature-fall period are as follows:
Water source is conveyed into half dry type reaction tower by the two-fluid spray nozzle at the top of half dry type reaction tower, and is atomized water source, quilt
The droplet of atomization is acted on by upward hot fume, forms the high-density region that a droplet suspends near the nozzle, and flue gas passes through
Temperature is cooled to rapidly 200 DEG C or so in 1s when this region.
10. processing method according to claim 6, which is characterized in that the cleaning solution in caustic wash tower described in step (5) is
NaOH solution and NaSO3The mixed liquor that solution is mixed according to the ratio that volume ratio is 1:1.
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| CN112555857A (en) * | 2020-12-24 | 2021-03-26 | 南京化学工业园天宇固体废物处置有限公司 | Even collocation feed arrangement of hazardous waste |
| CN112845515A (en) * | 2020-12-30 | 2021-05-28 | 中科院过程工程研究所南京绿色制造产业创新研究院 | Method for treating pyrolysis flue gas of solid waste |
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