CN107388262B - A kind of harmlessness disposing method of comprehensive utilization of high saliferous chemical engineering sludge - Google Patents
A kind of harmlessness disposing method of comprehensive utilization of high saliferous chemical engineering sludge Download PDFInfo
- Publication number
- CN107388262B CN107388262B CN201710621099.0A CN201710621099A CN107388262B CN 107388262 B CN107388262 B CN 107388262B CN 201710621099 A CN201710621099 A CN 201710621099A CN 107388262 B CN107388262 B CN 107388262B
- Authority
- CN
- China
- Prior art keywords
- outlet
- tank
- entrance
- agitator tank
- section
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
- 239000010802 sludge Substances 0.000 title claims abstract description 46
- 238000000034 method Methods 0.000 title claims abstract description 38
- 238000003889 chemical engineering Methods 0.000 title claims abstract description 37
- 150000003839 salts Chemical class 0.000 claims abstract description 61
- 238000009825 accumulation Methods 0.000 claims abstract description 20
- 125000004122 cyclic group Chemical group 0.000 claims abstract description 19
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 51
- 239000000203 mixture Substances 0.000 claims description 45
- 239000007788 liquid Substances 0.000 claims description 43
- 238000012546 transfer Methods 0.000 claims description 42
- 239000007789 gas Substances 0.000 claims description 40
- 239000003546 flue gas Substances 0.000 claims description 38
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims description 36
- 238000002386 leaching Methods 0.000 claims description 33
- 239000000463 material Substances 0.000 claims description 33
- 239000000446 fuel Substances 0.000 claims description 25
- 238000004064 recycling Methods 0.000 claims description 25
- 239000007787 solid Substances 0.000 claims description 24
- 238000011084 recovery Methods 0.000 claims description 23
- 239000002028 Biomass Substances 0.000 claims description 19
- 239000000779 smoke Substances 0.000 claims description 18
- 238000005303 weighing Methods 0.000 claims description 18
- 238000000746 purification Methods 0.000 claims description 17
- 239000002699 waste material Substances 0.000 claims description 16
- 230000006835 compression Effects 0.000 claims description 15
- 238000007906 compression Methods 0.000 claims description 15
- 239000002904 solvent Substances 0.000 claims description 15
- 239000012452 mother liquor Substances 0.000 claims description 14
- 239000000428 dust Substances 0.000 claims description 13
- 238000001816 cooling Methods 0.000 claims description 12
- 238000003756 stirring Methods 0.000 claims description 12
- 239000000725 suspension Substances 0.000 claims description 12
- 235000008733 Citrus aurantifolia Nutrition 0.000 claims description 11
- 235000011941 Tilia x europaea Nutrition 0.000 claims description 11
- 239000004571 lime Substances 0.000 claims description 11
- 239000002562 thickening agent Substances 0.000 claims description 11
- 239000004744 fabric Substances 0.000 claims description 10
- 239000007921 spray Substances 0.000 claims description 10
- 238000000498 ball milling Methods 0.000 claims description 9
- 238000012545 processing Methods 0.000 claims description 6
- 230000008569 process Effects 0.000 claims description 5
- 238000003825 pressing Methods 0.000 claims description 4
- 239000003795 chemical substances by application Substances 0.000 claims description 3
- 238000000227 grinding Methods 0.000 claims description 2
- 238000005086 pumping Methods 0.000 claims description 2
- 238000005119 centrifugation Methods 0.000 claims 1
- 230000001276 controlling effect Effects 0.000 claims 1
- 230000001105 regulatory effect Effects 0.000 claims 1
- 230000000694 effects Effects 0.000 abstract description 19
- 238000007363 ring formation reaction Methods 0.000 abstract description 9
- 238000005054 agglomeration Methods 0.000 abstract description 6
- 230000002776 aggregation Effects 0.000 abstract description 6
- 238000012423 maintenance Methods 0.000 abstract description 4
- 238000004134 energy conservation Methods 0.000 abstract description 2
- 230000007613 environmental effect Effects 0.000 abstract description 2
- 238000009270 solid waste treatment Methods 0.000 abstract description 2
- 239000000126 substance Substances 0.000 description 13
- 239000012535 impurity Substances 0.000 description 10
- 239000002893 slag Substances 0.000 description 9
- 238000005265 energy consumption Methods 0.000 description 8
- 238000005406 washing Methods 0.000 description 8
- 230000035699 permeability Effects 0.000 description 7
- 238000010586 diagram Methods 0.000 description 5
- 238000004519 manufacturing process Methods 0.000 description 5
- 231100000331 toxic Toxicity 0.000 description 5
- 230000002588 toxic effect Effects 0.000 description 5
- 230000008901 benefit Effects 0.000 description 4
- 239000006227 byproduct Substances 0.000 description 4
- 230000007547 defect Effects 0.000 description 4
- 238000001035 drying Methods 0.000 description 4
- 238000010304 firing Methods 0.000 description 4
- 238000002844 melting Methods 0.000 description 4
- 230000008018 melting Effects 0.000 description 4
- 235000019504 cigarettes Nutrition 0.000 description 3
- 238000007599 discharging Methods 0.000 description 3
- 238000001704 evaporation Methods 0.000 description 3
- 230000008020 evaporation Effects 0.000 description 3
- 238000000926 separation method Methods 0.000 description 3
- 239000002689 soil Substances 0.000 description 3
- 239000011449 brick Substances 0.000 description 2
- 238000009833 condensation Methods 0.000 description 2
- 230000005494 condensation Effects 0.000 description 2
- 238000013461 design Methods 0.000 description 2
- 238000011161 development Methods 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 239000000706 filtrate Substances 0.000 description 2
- 238000010438 heat treatment Methods 0.000 description 2
- 239000000155 melt Substances 0.000 description 2
- 238000002156 mixing Methods 0.000 description 2
- 239000003960 organic solvent Substances 0.000 description 2
- 239000000575 pesticide Substances 0.000 description 2
- 238000007789 sealing Methods 0.000 description 2
- 239000002344 surface layer Substances 0.000 description 2
- 239000002912 waste gas Substances 0.000 description 2
- NWZSZGALRFJKBT-KNIFDHDWSA-N (2s)-2,6-diaminohexanoic acid;(2s)-2-hydroxybutanedioic acid Chemical compound OC(=O)[C@@H](O)CC(O)=O.NCCCC[C@H](N)C(O)=O NWZSZGALRFJKBT-KNIFDHDWSA-N 0.000 description 1
- 239000005562 Glyphosate Substances 0.000 description 1
- 239000003513 alkali Substances 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 238000004939 coking Methods 0.000 description 1
- 238000002485 combustion reaction Methods 0.000 description 1
- 230000007423 decrease Effects 0.000 description 1
- 230000003247 decreasing effect Effects 0.000 description 1
- 230000009977 dual effect Effects 0.000 description 1
- XDDAORKBJWWYJS-UHFFFAOYSA-N glyphosate Chemical compound OC(=O)CNCP(O)(O)=O XDDAORKBJWWYJS-UHFFFAOYSA-N 0.000 description 1
- 229940097068 glyphosate Drugs 0.000 description 1
- 239000008187 granular material Substances 0.000 description 1
- 238000003837 high-temperature calcination Methods 0.000 description 1
- IKDUDTNKRLTJSI-UHFFFAOYSA-N hydrazine monohydrate Substances O.NN IKDUDTNKRLTJSI-UHFFFAOYSA-N 0.000 description 1
- 230000008676 import Effects 0.000 description 1
- 239000013067 intermediate product Substances 0.000 description 1
- -1 it is mobile Substances 0.000 description 1
- 239000005416 organic matter Substances 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 231100000614 poison Toxicity 0.000 description 1
- 230000007096 poisonous effect Effects 0.000 description 1
- 239000000047 product Substances 0.000 description 1
- 238000012797 qualification Methods 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 238000012958 reprocessing Methods 0.000 description 1
- 238000012827 research and development Methods 0.000 description 1
- 230000003068 static effect Effects 0.000 description 1
- 238000010025 steaming Methods 0.000 description 1
- 238000012360 testing method Methods 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
- F23G7/00—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F9/00—Multistage treatment of water, waste water or sewage
-
- 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
- F23G5/02—Incineration of waste; Incinerator constructions; Details, accessories or control therefor with pretreatment
- F23G5/033—Incineration of waste; Incinerator constructions; Details, accessories or control therefor with pretreatment comminuting or crushing
-
- 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
- F23G5/02—Incineration of waste; Incinerator constructions; Details, accessories or control therefor with pretreatment
- F23G5/04—Incineration of waste; Incinerator constructions; Details, accessories or control therefor with pretreatment drying
-
- 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
- F23G5/50—Control or safety arrangements
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/001—Processes for the treatment of water whereby the filtration technique is of importance
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/02—Treatment of water, waste water, or sewage by heating
- C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/02—Treatment of water, waste water, or sewage by heating
- C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
- C02F1/041—Treatment of water, waste water, or sewage by heating by distillation or evaporation by means of vapour compression
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/38—Treatment of water, waste water, or sewage by centrifugal separation
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/66—Treatment of water, waste water, or sewage by neutralisation; pH adjustment
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
- C02F2001/5218—Crystallization
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2301/00—General aspects of water treatment
- C02F2301/04—Flow arrangements
- C02F2301/046—Recirculation with an external loop
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2301/00—General aspects of water treatment
- C02F2301/08—Multistage treatments, e.g. repetition of the same process step under different conditions
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
- F23G2203/00—Furnace arrangements
- F23G2203/80—Furnaces with other means for moving the waste through the combustion zone
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
- F23G2205/00—Waste feed arrangements
- F23G2205/12—Waste feed arrangements using conveyors
- F23G2205/121—Screw conveyor
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
- F23G2209/00—Specific waste
- F23G2209/12—Sludge, slurries or mixtures of liquids
Landscapes
- Engineering & Computer Science (AREA)
- Mechanical Engineering (AREA)
- General Engineering & Computer Science (AREA)
- Environmental & Geological Engineering (AREA)
- Life Sciences & Earth Sciences (AREA)
- Hydrology & Water Resources (AREA)
- Water Supply & Treatment (AREA)
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Treatment Of Sludge (AREA)
Abstract
The invention belongs to Solid Waste Treatment technical fields, more particularly to a kind of harmlessness disposing method of comprehensive utilization of high saliferous chemical engineering sludge, the method burns reclaimer using negative-pressure cyclic accumulation of heat, maintenance and replacement are easy, equipment use cost is cheap, it can be realized the harmlessness disposing of high saliferous chemical engineering sludge, recycle the salt in sludge, and high saliferous chemical engineering sludge can be overcome to melt under the high temperature conditions, ring formation, agglomeration etc. cause the technical problem of serious damage to incinerator, improve burning effect, energy conservation and environmental protection.
Description
Technical field
The invention belongs to Solid Waste Treatment technical fields, and in particular to a kind of harmlessness disposing of high saliferous chemical engineering sludge
Method of comprehensive utilization.
Background technique
High saliferous chemical engineering sludge refer to industrial processes generate containing organic matter, other poisonous and harmful substances and
Moisture, and the sludge based on inorganic abraum salt, in the production process of many fine chemistry industries, chemical pesticide product or intermediate,
4~5 tons will will be generated containing toxic harmful with the generation of a large amount of high saliferous chemical engineering sludges, such as 1 ton of hydrazine hydrate of every production
The high saliferous chemical engineering sludge of by-product of substance is learned, 1 ton of glyphosate pesticide of every production then generates 1.1~1.4 tons and contains toxic harmful chemicals
The high saliferous chemical engineering sludge of the by-product of substance, with the development of many important fine chemistry industries and intermediate product, height is dirty containing salt chemical engineering
The amount of mud is also being continuously increased, and becomes the big bottleneck for hindering industry development.
High saliferous chemical engineering sludge easily agglomerates on the one hand because containing moisture, and processing difficulty is big；On the other hand again because having containing toxic
Evil chemical substance, cannot be used directly as the raw material of industry, thus at present major part enterprise processing mode mainly have it is following several
Kind: salt slag water or organic solvent washing are washed away the impurity in salt slag by 1. desalinization of soil by flooding or leaching method as far as possible, and treated, and salt is used to join alkali
Industry, but the method is only applicable to the by-product salt slag that impurity content is few and impurity composition is single, and the water or organic solvent of washing
There are the secondary pollutions such as reprocessing, in addition, the impurity in by-product salt slag is difficult to clean, residual quantity is also unstable, it is difficult to
Realize industrialization；2. salt slag high-temperature process is made the organic impurities contained in salt slag resolve into gas at high temperature by high-temperature process method
To achieve the purpose that remove organic impurities, but the key of the method is the research and development of resolving device, and the current country has report to use back
The Thermal Equipments such as rotary kiln, fluidized bed furnace carry out 800 DEG C or more high-temperature calcination processing, but there are the nothings in high saliferous chemical engineering sludge for the method
Melting, ring formation, agglomeration easily occur at high temperature for machine salt, cause equipment to be unable to operate normally and wait engineering problems, it is difficult to realize industry
Change；3. landfill or tipping are directly toppled over the outdoor stockpiling of salt slag or into rivers, but the method is simple and crude, stores up for a long time
Salt slag does not only take up a large amount of soils, also constitutes grave danger to environment, and the soluble-salt of these high saliferous chemical engineering sludges and has
Malicious harmful chemical such as with rain water runoff, can serious salinization surrounding soil, destroy surrounding vegetation, deteriorate water quality, polluted source,
It constitutes a serious threat to people's lives.
Therefore, harmless treatment is carried out to these high saliferous chemical engineering sludges and carries out resource utilization, become industry urgency
Significant problem to be solved.
Summary of the invention
In view of the foregoing drawbacks, the object of the present invention is to provide a kind of comprehensive utilizations of the harmlessness disposing of high saliferous chemical engineering sludge
Method, the method can be realized the harmlessness disposing of high saliferous chemical engineering sludge, recycle the salt in sludge, and height can be overcome to contain
Salt chemical engineering sludge melts under the high temperature conditions, ring formation, agglomeration etc. cause the technical problem of serious damage to incinerator, improves and burns
Effect, energy conservation and environmental protection.
For achieving the above object, the present invention the following technical schemes are provided:
A kind of harmlessness disposing method of comprehensive utilization of high saliferous chemical engineering sludge, comprising the following steps:
Step 1: it is 3-12mm that high saliferous chemical engineering sludge, which is crushed to partial size, and sludge is pressed with lime, chaff shell, biomass fuel
It is mixed to prepare mixture according to the ratio of mass ratio 40-80:0-5:10-20:10-35, the partial size of the chaff shell is 2-8mm, described
Biomass fuel partial size be 1-8mm, calorific value be 4500-6500 kilocalorie；
Step 2: step 1 gains are delivered in negative-pressure cyclic accumulation of heat burning reclaimer and carry out burning recovery processing,
The thickness of step 1 gains is no more than 900mm, and the speed of conveying is 0-2m/s, and recycling is burned in the negative-pressure cyclic accumulation of heat
Equipment includes hybrid system, car-type incineration system, exhausting system, smoke circulating system, salt recovery system, conveyer system and cigarette
Gas purification system, it is characterised in that:
The hybrid system includes multiple feed bins, weighing balance, mixed stirring device, and the discharge port of the feed bin is directed at metering
The weighing plate of title, the weighing plate of the weighing balance and the feed inlet of mixed stirring device are corresponding, the discharge port of mixed stirring device
Connect conveyer system, lime, chaff shell and the biomass fuel in feed bin after weighing balance weighs, be sent into mixed stirring device with
High saliferous chemical engineering sludge is mixed to obtain mixture described in step 1, and communicated system is sent into car-type incineration system；
The car-type incineration system includes auger type distributor, preheating cover, track and the series connection platform moved in orbit
Vehicle, the track are divided into cloth section, preheating igniting section, incineration section and cooling section, the auger type distributor from front to back
Interior to be equipped with material scattering device, the cloth section of respective carter, the preheating cover is interior to be equipped with igniter, and the preheating cover is equipped with exhaust gas
Import and fuel nozzle, the preheating igniting section of respective carter, step 1 gained mixture is through auger type distributor cloth in series connection platform
Che Shang, material loosening degree are suitable for that series connection trolley marches to preheating and covers corresponding preheating igniting section, are passed through through exhaust gas inlet useless
Gas is to the material pre-heating temperature elevation on trolley, igniter fire, and firing temperature is 800 DEG C -900 DEG C, can either avoid mixture without
The defect that method is lighted, and can be avoided the defect that the excessively high caused energy consumption of temperature is high, the melting of mixture surface layer influences gas permeability；Institute
The mobile design burned of series connection trolley is stated, high saliferous chemical engineering sludge can be overcome to melt under the high temperature conditions, ring formation, agglomeration etc. pair
The breaking-up of incinerator, high saliferous sludge burns on more mutually indepedent, series connection trolleys, and realizes trolley by track
Incinerator is moved out, it is then broken to trolley discharging, will not only breaking-up be generated to incinerator, but also burning effect is more preferable；This
Outside, trolley structure is simple, and maintenance replacement is easy, and equipment life is long, and use cost is cheap；The incineration section top of the track and cigarette
The gas circulatory system is tightly connected, and the preheating igniting section of the track, the lower section of incineration section and cooling section and exhausting system sealing connect
It connects；
The exhausting system includes the pumping being tightly connected below multiple preheating igniting sections, incineration section and cooling section with track
Fan housing, each draught hood connects a set of air draft pipeline being made of exhaust column and exhaust fan, between the exhaust column and exhaust fan
Equipped with steam-water separator, the water outlet end of the steam-water separator is connected to salt recovery system, and steam-water separator will be burned and be generated
Flue gas and condensed water separated, the condensed water isolated enters in salt recovery system through water outlet end to be utilized again, separation
Flue gas out enters smoke circulating system through exhaust fan, with the tail end and cigarette of the air draft pipeline being connected to below track preheating igniting section
The connection of gas purification system will be discharged into atmosphere after the waste gas purification that interior second-time burning is covered in preheating is up to standard, below track incineration section
The tail end of the air draft pipeline of connection is connected to next stage smoke circulating system, is carried out to the material in next stage smoke circulating system
Preheating and drying makes full use of the thermal energy in exhaust gas, reduces energy consumption, with the afterbody air draft pipeline being connected to below track incineration section
Outlet be connected to exhaust gas inlet, preheating not only was dried to the material in preheating cover, but also by exhaust gas progress second-time burning depth
Processing is connected to the air draft pipeline being connected to below track cooling section with sinter machine discharge end dedusting device；
The smoke circulating system includes multiple flue gas covers connecting with the incineration section upper seal of track, each flue gas
Exhaust gas entrance and fresh air is equipped on cover to connect with entrance, the exhaust gas entrance of the flue gas cover and the tail end of upper level air draft pipeline
Logical, the flue gas that the harmful substance in mixed material is decomposed to form in high temperature incineration enters air draft pipeline through draught hood, send under
Level-one flue gas cover completes drying and preheating to back segment mixed material；
The salt recovery system includes that successively the ball-milling device of piping connection, leaching wash mill, pH adjust tank, MVR
Device (also known as steam mechanical recompression device) and equipment for separating liquid from solid, the ball-milling device is by ball mill, entrance and ball mill
The water spray dust collecting box of outlet and several waste residue feed bins composition, the entrance of the waste residue feed bin and going out for water spray dust collecting box
Mouth connection, the outlet of the waste residue feed bin are connected to wash mill is leached, and car-type incineration system burns the residue generated through ball
Grinding machine is crushed to partial size no more than 100 mesh, can sufficiently expose the salt being wrapped in residue, improve and leach washing effect, enter
It is stored after dust removal process to waste residue feed bin in water spray dust collecting box；The leaching wash mill includes multistage by agitator tank, filters pressing
The leaching wash of machine and transfer tank composition, in every grade of leachings wash, agitator tank outlet is connected to filter press entrance, pressure
The solid outlet of filter is connected to the agitator tank material inlet that next stage leaches wash, the liquid outlet of filter press and transfer
The connection of tank entrance, the first order leaches the outlet of the transfer tank of wash and pH adjusts tank and is connected to, other leaching washing groups at different levels
The outlet of the transfer tank of part is connected to the agitator tank leaching solvent entrance that upper level leaches wash, and the first order leaches washing group
It is leached simultaneously with the outlet of the water outlet end of the steam-water separator of exhausting system and next stage the disengaging colvent inlet of the agitator tank of part
The outlet of wash transfer tank, the pH, which is adjusted, is equipped with pH meter and pH agent addition box in tank, adjusts pH and adjusts in tank
Liquid pH to 7-8；The MVR device includes heater, crystallizer, separator, vapour compression machine and suspension thickener, it is described plus
Hot device is connect with crystallizer, provides hot steam heat supply for crystallizer, the top of the crystallizer passes through separator and both vapor compression
Machine connection, the lower part of the crystallizer are connected to suspension thickener, and the outlet of the vapour compression machine is connected to heater, pH tune
Liquid in section tank is pumped into the crystallizer of MVR device, and in the case where heater is for heat effect, liquid moisture is constantly evaporated to water steaming
Gas, the vapor enter vapour compression machine by separator, under vapour compression machine compression, improve the vapor
Pressure and temperature is again introduced into heater as heat source, can not only recycle the thermal energy of the vapor, moreover it is possible to omit
The condensation procedure and equipment of the vapor are precipitated salt after liquid evaporation concentration in crystallizer and obtain solidliquid mixture, described solid
Liquid mixture is pumped into suspension thickener；The equipment for separating liquid from solid includes centrifuge, salt recycling can and mother liquor tank, the centrifuge
Entrance connect with the outlet in suspension thickener, the solid outlet of the centrifuge is connected to salt recycling can, the centrifuge
Liquid outlet be connected to mother liquor tank, the mother liquor tank by valve control pump with leaching wash mill and MVR device be connected to,
It completes to be separated by solid-liquid separation under centrifuge effect, isolated solid enters salt recycling can, can be used in deicing salt etc., purity is high, nothing
Environment toxic side effects, isolated liquid enter mother liquor tank and carry out purity detecting, and blowback leaching is washed if impurity content is unqualified
Device is washed, if impurity content qualification in blowback MVR device, remaining salt in mother liquor tank can either be reused, realize zero-emission
It puts, and can ensure to recycle the purity of salt；
The escape pipe of the flue gas purification device is connected to chimney by exhaust fan, will purify exhaust gas up to standard and is discharged.
Method according to the present invention, high saliferous chemical engineering sludge, lime, chaff shell and biomass fuel described in step 1
Mass ratio be 50-80:1-5:10-15:10-35.
The inventors discovered that high saliferous chemical engineering sludge, lime, chaff shell and biomass fuel mass ratio mixture is burnt
It is larger to burn influential effect, as above-mentioned four 40-80:0-5 in mass ratio；The ratio of 10-20:10-35, especially in mass ratio
When the ratio mixing of 50-80:1-5:10-15:10-35, the obtained horizontal appropriate, inorganic salts of mixture good permeability, calorific value melt
Melt, ring formation, agglomerate less, burning is abundant.
In addition, the partial size of chaff shell and biomass fuel is also very big on the influence of the property of mixture, when chaff shell or biomass fuel
When material partial size is more than 8mm, mixture gas permeability obtained is excessively good, and burning velocity is too fast, and large granular materials are unable to get adequately
Burning；When chaff shell partial size is less than 2mm or biomass fuel partial size is less than 1mm, phase between mixture material and material obtained
Mutual adhesion, the poor air permeability of the bed of material, firing rate decline influence burning effect；The present inventor passes through largely test discovery, when
When chaff shell partial size is 2-8mm and biomass fuel partial size is 1-8mm, mixture good permeability obtained, calorific value water both can guarantee
It is flat appropriate, and inorganic salts melting, ring formation, caking phenomenon can be reduced, burning is abundant.
Method according to the present invention, mixture described in step 2 is with a thickness of 300-900mm.
The present inventors have additionally discovered that when mixture is sent into the incinerator of negative-pressure cyclic accumulation of heat recovery system, thickness and traveling
Speed also has a significant impact to burning effect, when thickness is more than 900mm or travel speed is more than 2m/s, the gas permeability of mixture
Not enough, it can not burn sufficiently, influence burning effect；If thickness is lower than 300mm, the accumulation of heat effect of mixture is poor, is unable to fully
Burning；Only control mixture with a thickness of 300-900mm, and travel speed is 0-2m/s, especially for 0.2-1.5m/s when,
Not only it can guarantee that mixture burned sufficiently, but also inorganic salts melting, ring formation, caking phenomenon can be effectively reduced, and improved the warp of fixed-end forces
Benefit of helping and treatment effeciency, while can ensure the stable operation of system.
Method according to the present invention, leaching wash mill described in step 2 include the first agitator tank, the first filters pressing
In machine, the first transfer tank, the second agitator tank, the second filter press, the second transfer tank, third agitator tank, third filter press and third
Turn tank, the material inlet of first agitator tank is connect with waste residue bin outlet, the leaching solvent entrance of first agitator tank
It exports and connects with the water outlet end of the steam-water separator of exhausting system, realize the recycling for burning the condensed water generated, it is described
The outlet of first agitator tank is connected to the first filter press, and the material of the solid outlet and the second agitator tank of first filter press enters
Mouthful connection, the liquid outlet of first filter press is connected to the entrance of the first transfer tank, the outlet of the first transfer tank and
PH adjusts tank connection, and the liquid salt content that the first filter press filters out is high, about 15%-20%, can significantly reduce subsequent MVR dress
The energy consumption for being concentrated by evaporation filtrate is set, the efficiency and benefit of salt recycling are improved；The outlet of second agitator tank and the second filter press
Connection, the solid outlet of second filter press are connected to the entrance of third agitator tank, the liquid outlet of second filter press
It being connected to the entrance of the second transfer tank, the outlet of the second transfer tank is connected to the leaching solvent entrance of the first agitator tank, the
Two transfer pot liquids flow back to the first agitator tank as residue leaching solvent, can either further recycle remaining in incineration residue
Salinity, and can be realized the recycling of recycling water, it is economic and environment-friendly；The outlet of the third agitator tank and third filter press connect
It connects, the solid outlet of the third filter press is stacked pond with filter residue and connect, and the filter residue moisture content through three-level countercurrent washing is less than
30%, salt content is less than 0.5%, nonhazardous substance, can be directly used as brick or light wall board material, economic and environment-friendly, and described
The liquid outlet of three filter presses is connected to third transfer tank, the outlet of the third transfer tank and the leaching solvent of the second agitator tank
Entrance connection, similarly, third transfer pot liquid flows back to the second agitator tank as residue leaching solvent, can either further return
Remaining salinity in incineration residue is received, and can be realized the recycling of recycling water, it is economic and environment-friendly.
The fresh air of method according to the present invention, flue gas device described in step 2 is equipped with blast pipe tune with entrance
Valve is saved, the amount of allocating of fresh air is controlled by controlling its aperture.
Method of the invention, using negative-pressure cyclic accumulation of heat burn reclaimer the characteristics of, add certain supplies, come
The disposition to high saliferous sludge is realized, its main feature is that the same of burning disposal can carried out to the harmful substance in high saliferous sludge
When, on the one hand using series connection trolley mobile the characteristics of burning, overcome high saliferous chemical engineering sludge to melt under the high temperature conditions, ring formation,
The breaking-up to incinerator such as agglomeration, improves burning effect；On the other hand the characteristics of being preheated using incinerator when burning is realized
Thermal energy recycling, specific advantage are as follows:
1, reclaimer is burned using negative-pressure cyclic accumulation of heat, incinerator is connected by multiple mutually independent burning trolleys
Composition, it is mobile, and material is static, high saliferous sludge can melt on the car under the high temperature conditions, after discharging is broken
It collects, will not generate coking etc. to incinerator influences, to influence the effect of burning and the service life of equipment and use function；
2, the burning trolley structure used is simple, and maintenance and replacement are easy, and equipment use cost is cheap；
3, since high saliferous sludge calorific value is extremely low, and contain harmful serious a small amount of organic substance, when burning must add
A large amount of auxiliary fuel, energy consumption is high, burns recovery technology using negative-pressure cyclic accumulation of heat of the invention, effective use upper materials are burnt
It burns the high-temperature steam generated lower part material is dried and preheated, improves burning disposal and obtain special efficacy rate, reduce energy consumption；
4, it burns the flue gas generated and on the one hand passes through extractor fan and flue gas device recycling heat energy, on the one hand in exhausting
It is run in the sealing pipeline of device and flue gas device, flue gas purification device is finally entered after dual firing chamber's advanced treating, is not generated
Secondary pollution is able to achieve cleanly production；
5, smoke multistage circulation secondary combustion technology is used, the harmful components in gas are effectively addressed, fire simultaneously
The oxygen content of exhaust gas is utilized effectively during burning, therefore new intake is greatly decreased, and then it is total to largely reduce flue gas emission
Amount can reduce 60% or more compared with generally burning mode flue gas emission total amount；
6, water, gas, the slag discharged is up to state standards.
Detailed description of the invention
Fig. 1 is the structural schematic diagram that reclaimer is burned in negative-pressure cyclic accumulation of heat of the present invention；
Fig. 2 is the structural schematic diagram that reclaimer hybrid system is burned in negative-pressure cyclic accumulation of heat of the present invention；
Fig. 3 is that reclaimer car-type incineration system, exhausting system, flue gas recirculation system are burned in negative-pressure cyclic accumulation of heat of the present invention
The structural schematic diagram of system, salt recovery system and flue gas purification system；
Fig. 4 is the structural schematic diagram that reclaimer salt recovery system salt recovery system is burned in negative-pressure cyclic accumulation of heat of the present invention,
Wherein ball-milling device, leaching wash mill and pH, which adjust tank, enlarged structure；
Fig. 5 is the structural schematic diagram that reclaimer salt recovery system salt recovery system is burned in negative-pressure cyclic accumulation of heat of the present invention,
Wherein MVR device and equipment for separating liquid from solid are by enlarged structure；
In figure,
1- hybrid system, 11- feed bin, 12- weighing balance, 13- mixed stirring device；
2- car-type incineration system, 20- auger type distributor, 21- preheating cover, 22- track, 23- series connection trolley, 24- object
Expect dispersing device, 25- igniter, 26- exhaust gas inlet, 27- fuel nozzle；
3- exhausting system, 31- draught hood, 32- exhaust column, 33- exhaust fan, 34- steam-water separator；
4- smoke circulating system, 41- flue gas cover, 42- exhaust gas entrance, 43- fresh air match entrance；
5- salt recovery system, 51- ball-milling device, 511- ball mill, 512- water spray dust collecting box, 513- waste residue feed bin, 52-
Leach wash mill, the first agitator tank of 521-, the first filter press of 522-, 523- the first transfer tank, the second agitator tank of 524-, 525-
Second filter press, 526- the second transfer tank, 527- third agitator tank, 528- third filter press, 529- third transfer tank, 53-pH
Adjusting tank, 54-MVR device, 541- heater, 542- crystallizer, 543- separator, 544- vapour compression machine, 545- suspension are thick
Thick device, 55- equipment for separating liquid from solid, 551- centrifuge, 552- salt recycling can, 553- mother liquor tank；
6- conveyer system；
7- flue gas purification system.
Specific embodiment
Reclaimer is burned in 1 negative-pressure cyclic accumulation of heat of embodiment
As shown in Figs. 1-5, it includes hybrid system 1 that reclaimer is burned in negative-pressure cyclic accumulation of heat of the invention, and car-type burns
System 2, exhausting system 3, smoke circulating system 4, salt recovery system 5, conveyer system 6 and flue gas purification system 7, the mixed stocker
System 1 includes multiple feed bins 11, weighing balance 12, mixed stirring device 13, the title of the discharge port alignment weighing balance 12 of the feed bin 11
Disk is measured, the weighing plate of the weighing balance 12 is corresponding with the feed inlet of mixed stirring device 13, the discharge port of mixed stirring device 13
Conveyer system 6 is connected, lime, chaff shell and the biomass fuel in feed bin 11 are sent into and dress are mixed after the weighing of weighing balance 12
It sets and is mixed to obtain mixture described in step 1 with high saliferous chemical engineering sludge in 13, communicated system 6 is sent into car-type and is burned
In system 2；
The car-type incineration system 2 includes auger type distributor 20, preheating cover 21, track 22 and moves on track 22
Series connection trolley 23, the track 22 is divided into cloth section, preheating igniting section, incineration section and cooling section from front to back, described
Material scattering device 24 is equipped in auger type distributor 20, the cloth section of respective carter 22, the preheating cover 21 is interior to be equipped with igniter
25, the preheating cover 21 is equipped with exhaust gas inlet 26 and fuel nozzle 27, the preheating igniting section of respective carter 22, step 1 gained
For mixture through 20 cloth of auger type distributor on series connection trolley 23, material loosening degree is suitable for that series connection trolley 23 marches to pre-
Heat 21 corresponding preheating igniting sections of cover, the exhaust gas being passed through through exhaust gas inlet 26 is to the material pre-heating temperature elevation on trolley, igniter 25
Igniting, firing temperature are 800 DEG C -900 DEG C, the defect that can either avoid mixture that from can not lighting, and it is excessively high to can be avoided temperature
Caused energy consumption is high, mixture surface layer melts the defect for influencing gas permeability；The mobile design burned of series connection trolley 23, can
High saliferous chemical engineering sludge is overcome to melt under the high temperature conditions, the breaking-up of ring formation, agglomeration etc. to incinerator, high saliferous sludge is in Duo Tai
Independently of each other, it is burned on the trolley being connected in series, and realizes that trolley moves out incinerator by track 22, then to trolley discharging
It is broken, will not only breaking-up be generated to incinerator, but also burning effect is more preferable；In addition, trolley structure is simple, maintenance replacement is held
Easily, equipment life is long, and use cost is cheap；It is tightly connected above the incineration section of the track 22 with smoke circulating system 4, it is described
The preheating igniting section of track 22, the lower section of incineration section and cooling section and exhausting system 3 are tightly connected；
The exhausting system 3 includes being tightly connected below multiple preheating igniting sections, incineration section and cooling section with track 22
Draught hood 31, each draught hood 31 connects a set of air draft pipeline being made of exhaust column 32 and exhaust fan 33, the exhaust column
Steam-water separator 34 is equipped between 32 and exhaust fan 33, the water outlet end of the steam-water separator 34 is connected to salt recovery system 5,
Steam-water separator 34 will burn the flue gas generated and condensed water separates, and the condensed water isolated enters salt through water outlet end and returns
It is utilized again in receipts system 5, the flue gas isolated enters smoke circulating system 4 through exhaust fan 33, with 22 preheating igniting section of track
The tail end of the air draft pipeline of lower section connection is connected to flue gas purification system 7, by the waste gas purification of the second-time burning in preheating cover 21
It is discharged into atmosphere after up to standard, connects with the tail end for the air draft pipeline being connected to below 22 incineration section of track with next stage smoke circulating system 4
It is logical, preheating and drying is carried out to the material in next stage smoke circulating system 4, makes full use of the thermal energy in exhaust gas, reduces energy consumption, with
The outlet for the afterbody air draft pipeline being connected to below 22 incineration section of track is connected to exhaust gas inlet 26, both in preheating cover 21
Preheating is dried in material, and exhaust gas is carried out second-time burning advanced treating, with the exhaust column being connected to below 22 cooling section of track
Road is connected to sinter machine discharge end dedusting device；
The smoke circulating system 4 includes multiple flue gas covers 41 connecting with the incineration section upper seal of track 22, often
Exhaust gas entrance 42 and fresh air are equipped in a flue gas cover 41 with entrance 43, the exhaust gas entrance 42 and upper level of the flue gas cover 41 are taken out
The tail end of air pipe line is connected to, the flue gas that the harmful substance in mixed material is decomposed to form in high temperature incineration, through draught hood 31 into
Enter air draft pipeline, send to next stage flue gas cover 41, complete the drying and preheating to back segment mixed material；
The salt recovery system 5 includes ball-milling device 51, leaches wash mill 52, pH adjusting tank 53,54 and of MVR device
Equipment for separating liquid from solid 55, the ball-milling device 51 are gathered dust by the water spray of 511 outlet of ball mill 511, entrance and ball mill
Case 512 and several waste residue feed bins 513 composition, the entrance of the waste residue feed bin 513 and the outlet of water spray dust collecting box 512,
The outlet of the waste residue feed bin 513 is connected to wash mill 52 is leached, and car-type incineration system 2 burns the residue generated through ball milling
Machine 511 is crushed to partial size no more than 100 mesh, can sufficiently expose the salt being wrapped in residue, improve and leach washing effect, enter
It is stored after dust removal process to waste residue feed bin 513 in water spray dust collecting box 512；The leaching wash mill 52 includes the first agitator tank
521, the first filter press 522, the first transfer tank 523, the second agitator tank 524, the second filter press 525, the second transfer tank 526,
Three agitator tanks 527, third filter press 528 and third transfer tank 529, the material inlet and waste residue material of first agitator tank 521
The outlet of storehouse 513 connection, the water of the steam-water separator 34 of the leaching solvent entrance and exhausting system 3 of first agitator tank 521 go out
Mouth brings out mouth connection, realizes the recycling for burning the condensed water generated, the outlet and the first filters pressing of first agitator tank 521
Machine 522 is connected to, and the solid outlet of first filter press 522 is connected to the material inlet of the second agitator tank 524, first pressure
The liquid outlet of filter 522 is connected to the entrance of the first transfer tank 523, and the outlet of the first transfer tank 523 and pH adjust tank
53 connections, the liquid salt content that the first filter press filters out is high, about 15%-20%, can significantly reduce subsequent MVR device 54 and steam
The energy consumption of hair concentration filtrate, improves the efficiency and benefit of salt recycling；The outlet of second agitator tank 524 and the second filter press
525 connections, the solid outlet of second filter press 525 are connected to the entrance of third agitator tank 527, second filter press
525 liquid outlet is connected to the entrance of the second transfer tank 526, the outlet of the second transfer tank 526 and the first agitator tank 521
The connection of leaching solvent entrance, liquid flows back to the first agitator tank 521 and is used as residue leaching solvent in the second transfer tank 526, can
Remaining salinity in enough further recycling incineration residues, and can be realized the recycling of recycling water, it is economic and environment-friendly；Described
The outlet of three agitator tanks 527 is connect with third filter press 528, and the solid outlet and filter residue of the third filter press 528 stack pond
Connection, the filter residue moisture content through three-level countercurrent washing is less than 30%, and less than 0.5%, nonhazardous substance can be used directly salt content
Make brick or light wall board material, economic and environment-friendly, the liquid outlet of the third filter press 528 is connected to third transfer tank 529, institute
The outlet for stating third transfer tank 529 is connected to the leaching solvent entrance of the second agitator tank 524, similarly, in third transfer tank 526
Liquid flows back to the second agitator tank 521 and is used as residue leaching solvent, can either further recycle remaining salinity in incineration residue, again
It can be realized the recycling of recycling water, it is economic and environment-friendly；The pH, which is adjusted, is equipped with pH meter and pH agent addition box in tank 53, adjust
PH adjusts the liquid pH to 7-8 in tank 53；The MVR device 54 includes heater 541, crystallizer 542, separator 543, steam
Compressor 544 and suspension thickener 545, the heater 541 are connect with crystallizer 542, provide hot steam confession for crystallizer 542
Heat, the top of the crystallizer 542 are connected to by separator 543 with vapour compression machine 544, the lower part of the crystallizer 542 and
Suspension thickener 545 is connected to, and the outlet of the vapour compression machine 544 is connected to heater 541, and pH adjusts the liquid pump in tank 53
Enter in the crystallizer 542 of MVR device 54, in the case where heater 541 is for heat effect, liquid moisture is constantly evaporated to vapor, described
Vapor improves the vapor under 544 compression of vapour compression machine into vapour compression machine 544 by separator 543
Pressure and temperature, be again introduced into heater 541 as heat source, the thermal energy of the vapor can not only be recycled, also
The condensation procedure and equipment of the vapor can be omitted, salt is precipitated after liquid evaporation concentration in crystallizer 542 and obtains solid-liquid mixing
Object, the solidliquid mixture are pumped into suspension thickener 545；The equipment for separating liquid from solid 55 includes centrifuge 551, salt recycling can
552 and mother liquor tank 553, the entrance of the centrifuge connect in suspension thickener 545 outlet, the centrifuge 551 is consolidated
Body outlet is connected to salt recycling can 552, and the liquid outlet of the centrifuge 551 is connected to mother liquor tank 553, the mother liquor tank
553 are connected to by valve control pump with leaching wash mill 52 and MVR device 54, complete solid-liquid point under the effect of centrifuge 551
From, isolated solid enters salt recycling can 552, it can be used in deicing salt etc., purity is high, without environment toxic side effects, separation
Liquid enters mother liquor tank 547 and carries out purity detecting, and wash mill 52 is leached in blowback if impurity content is unqualified, if impurity content
It is qualified then in blowback MVR device 54, can either reuse remaining salt in mother liquor tank 553, realize zero-emission, and can ensure
Recycle the purity of salt.
The escape pipe of the flue gas purification device 7 is connected to chimney by exhaust fan, will purify exhaust gas up to standard and is discharged.
The comprehensive utilization of the high saliferous chemical engineering sludge of embodiment 2
Step 1: high saliferous chemical engineering sludge is crushed to partial size 3-12mm, sludge and lime, chaff shell, biomass fuel according to
The ratio of mass ratio 45:5:15:35 is mixed to prepare mixture, and the partial size of the chaff shell is 2-8mm, the biomass fuel
Partial size is 1-8mm, and calorific value is 5000 kilocalories；
Step 2: the resulting mixture of step 1 being sent into negative-pressure cyclic accumulation of heat described in embodiment 1 and burns reclaimer
In car-type incineration system, the mixture with a thickness of 500mm, the travel speed 0.16m/s of mixture, igniting is burned, warp
The exhaust gas that flue gas purification device 7 is discharged meets 2000 standard of European Union, and the salt rate of recovery 90%, purity (content of organics) is less than 1%.
The comprehensive utilization of the high saliferous chemical engineering sludge of embodiment 3
Step 1: high saliferous chemical engineering sludge is crushed to partial size 4-10mm, sludge and lime, chaff shell, biomass fuel according to
The ratio of mass ratio 60:2:10:28 is mixed to prepare mixture, and the partial size of the chaff shell is 2-8mm, the biomass fuel
Partial size is 1-8mm, and calorific value is 5000 kilocalories；
Step 2: the resulting mixture of step 1 being sent into negative-pressure cyclic accumulation of heat described in embodiment 1 and burns reclaimer
In car-type incineration system, the mixture with a thickness of 700mm, the travel speed 0.08m/s of mixture, igniting is burned, warp
The exhaust gas that flue gas purification device 7 is discharged meets 2000 standard of European Union, and the salt rate of recovery 92%, purity (content of organics) is less than 1%.
The comprehensive utilization of the high saliferous chemical engineering sludge of embodiment 4
Step 1: high saliferous chemical engineering sludge is crushed to partial size 5-8mm, sludge and lime, chaff shell, biomass fuel according to
The ratio of mass ratio 75:0:10:15 is mixed to prepare mixture, and the partial size of the chaff shell is 2-8mm, the biomass fuel
Partial size is 1-8mm, and calorific value is 5000 kilocalories；
Step 2: the resulting mixture of step 1 being sent into negative-pressure cyclic accumulation of heat described in embodiment 1 and burns reclaimer
In car-type incineration system, the mixture with a thickness of 900mm, the travel speed 0.05m/s of mixture, igniting is burned, warp
The exhaust gas that flue gas purification device 7 is discharged meets 2000 standard of European Union, and the salt rate of recovery 86%, purity (content of organics) is less than 1%.
Claims (10)
1. a kind of harmlessness disposing method of comprehensive utilization of high saliferous chemical engineering sludge, comprising the following steps:
Step 1: it is 3-12mm mesh that high saliferous chemical engineering sludge, which is crushed to partial size, with lime, chaff shell, biomass fuel according to quality
Ratio than 40-80:0-5:10-20:10-35 is mixed to prepare mixture, and the partial size of the chaff shell is 2-8mm, the biology
The partial size of matter fuel is 1-8mm, and calorific value is 4500-6500 kilocalorie；
Step 2: step 1 gains are delivered in negative-pressure cyclic accumulation of heat burning reclaimer and carry out burning recovery processing, it is described
The thickness of step 1 gains is no more than 900mm, and the speed of conveying is 0-2m/s, and reclaimer is burned in the negative-pressure cyclic accumulation of heat
Including hybrid system (1), car-type incineration system (2), exhausting system (3), smoke circulating system (4), salt recovery system (5),
Conveyer system (6) and flue gas purification system (7)；
The hybrid system (1) includes multiple feed bins (11), weighing balance (12), mixed stirring device (13), the feed bin (11)
Discharge port alignment weighing balance (12) weighing plate, the charging of the weighing plate of the weighing balance (12) and mixed stirring device (13)
Mouth is corresponding, and the discharge port of the mixed stirring device (13) connects conveyer system (6), lime, chaff shell and the life in feed bin (11)
Biomass fuel is sent into mixed stirring device (13) after weighing balance (12) weigh and is mixed to obtain with high saliferous chemical engineering sludge
Mixture described in step 1, communicated system (6) are sent into car-type incineration system (2)；
The car-type incineration system (2) includes distributing device (20), preheating cover (21), track (22) and moves on track (22)
Series connection trolley (23), the track (22) is divided into cloth section, preheating igniting section, incineration section and cooling section from front to back,
The cloth section of distributing device (20) respective carter (22), the preheating cover (21) is interior to be equipped with igniter (25), the preheating cover
(21) be equipped with exhaust gas inlet (26) and fuel nozzle (27), the preheating igniting section of respective carter (22), the track (22)
It is tightly connected with smoke circulating system (4) above incineration section, the preheating igniting section of the track (22), incineration section and cooling section
Lower section and exhausting system (3) are tightly connected；
The exhausting system (3) includes being tightly connected below multiple preheating igniting sections, incineration section and cooling section with track (22)
Draught hood (31), each draught hood (31) connects a set of air draft pipeline being made of exhaust column (32) and exhaust fan (33), institute
State between exhaust column (32) and exhaust fan (33) be equipped with steam-water separator (34), the water outlet end of the steam-water separator (34) with
Salt recovery system (5) connection；
The smoke circulating system (4) includes the flue gas cover (41) that multiple incineration section upper seals with track (22) are connect, often
Exhaust gas entrance (42) and fresh air are equipped on a flue gas cover (41) with entrance (43), the exhaust gas entrance (42) of the flue gas cover (41)
It is connected to the tail end of upper level air draft pipeline；
The salt recovery system (5) includes the ball-milling device (51) of successively piping connection, leaches wash mill (52), pH adjusting tank
(53), MVR device (54) and equipment for separating liquid from solid (55)；
The escape pipe of the flue gas purification system (7) is connected to chimney by exhaust fan, will purify exhaust gas up to standard and is discharged.
2. the method as described in claim 1, it is characterised in that: high saliferous chemical engineering sludge described in step 1, lime, chaff shell and
The mass ratio of biomass fuel is 50-80:1-5:10-15:10-35；Mixture described in step 2 with a thickness of 300-900mm,
Travel speed is 0.2-1.5m/s.
3. the method as described in claim 1, it is characterised in that: the ball-milling device (51) is by ball mill (511), entrance and ball
The water spray dust collecting box (512) and several waste residue feed bins (513) of grinding machine (511) outlet form, the waste residue feed bin (513)
Entrance and water spray dust collecting box (512) outlet, the outlet of the waste residue feed bin (513) and leach wash mill (52)
Connection, into dust removal process in water spray dust collecting box (512) after storage to waste residue feed bin (513).
4. the method as described in claim 1, it is characterised in that: the leaching wash mill (52) include it is multistage by agitator tank,
The leaching wash of filter press and transfer tank composition, in every grade of leachings wash, agitator tank outlet and filter press entrance company
Logical, the solid outlet of filter press is connected to the agitator tank material inlet that next stage leaches wash, the liquid outlet of filter press
It is connected to transfer tank entrance, the first order leaches the outlet of the transfer tank of wash and pH adjusts tank (53) and is connected to, other at different levels
The outlet for leaching the transfer tank of wash is connected to the agitator tank leaching solvent entrance that upper level leaches wash, the first order
Leach the disengaging colvent inlet of the agitator tank of wash while the water outlet end with the steam-water separator (34) of exhausting system (3)
Outlet and next stage leach the outlet of wash transfer tank.
5. method as claimed in claim 4, it is characterised in that: the leaching wash mill (52) includes the first agitator tank
(521), the first filter press (522), the first transfer tank (523), the second agitator tank (524), the second filter press (525), in second
Turn tank (526), third agitator tank (527), third filter press (528) and third transfer tank (529), first agitator tank
(521) material inlet and waste residue feed bin (513) outlet connects, the leaching solvent entrance and pumping of first agitator tank (521)
The water outlet end of the steam-water separator (34) of wind system (3) exports connection, the outlet of first agitator tank (521) and the first pressure
Filter (522) connection, the solid outlet of first filter press (522) are connected to the material inlet of the second agitator tank (524), institute
The liquid outlet for stating the first filter press (522) is connected to the entrance of the first transfer tank (523), the first transfer tank (523)
Outlet is connected to pH adjusting tank (53), and the outlet of second agitator tank (524) is connect with the second filter press (525), and described the
The solid outlet of two filter presses (525) is connected to the entrance of third agitator tank (527), the liquid of second filter press (525)
Outlet is connected to the entrance of the second transfer tank (526), outlet and the first agitator tank (521) of the second transfer tank (526)
The connection of leaching solvent entrance, the outlet of the third agitator tank (527) are connect with third filter press (528), the third filters pressing
The solid outlet of machine (528) is stacked pond with filter residue and is connect, the liquid outlet and third transfer tank of the third filter press (528)
(529) it is connected to, the outlet of the third transfer tank (529) is connected to the leaching solvent entrance of the second agitator tank (524).
6. the method as described in claim 1, it is characterised in that: the pH, which is adjusted, is equipped with pH meter and pH agent addition in tank (53)
Box adjusts the liquid pH to 7-8 in pH adjusting tank (53).
7. the method as described in claim 1, it is characterised in that: the MVR device (54) includes heater (541), crystallizer
(542), separator (543), vapour compression machine (544) and suspension thickener (545), the heater (541) and crystallizer
(542) connect, provide hot steam heat supply for crystallizer (542), the top of the crystallizer (542) by separator (543) with
Vapour compression machine (544) connection, the lower part of the crystallizer (542) are connected to suspension thickener (545), the vapour compression machine
(544) outlet is connected to heater (541).
8. the method for claim 7, it is characterised in that: the equipment for separating liquid from solid (55) includes centrifuge (551), salt
The entrance of recycling can (552) and mother liquor tank (553), the centrifuge is connect with the outlet of suspension thickener (545), the centrifugation
The solid outlet of machine (551) is connected to salt recycling can (552), and the liquid outlet of the centrifuge (551) and mother liquor tank (553) are even
Logical, the mother liquor tank (553) is connected to by valve control pump with leaching wash mill (52) and MVR device (54).
9. such as described in any item methods of claim 1-8, it is characterised in that: be connected to track (22) preheating igniting section lower section
The tail end of air draft pipeline be connected to flue gas purification system (7), with the tail for the air draft pipeline being connected to below track (22) incineration section
End is connected to next stage smoke circulating system (4), and the afterbody air draft pipeline being connected to track (22) incineration section lower section goes out
Mouth is connected to exhaust gas inlet (26), is connected to the air draft pipeline being connected to below track (22) cooling section with sinter machine discharge end dedusting device.
10. such as described in any item methods of claim 1-8, it is characterised in that: the distributing device (20) is spiral cloth
Device, interior to be equipped with material scattering device (24), the cloth section of respective carter (22)；Smoke circulating system described in step 2 (4) it is new
Wind is equipped with blast pipe regulating valve with entrance, and the amount of allocating of fresh air is controlled by controlling its aperture.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201710621099.0A CN107388262B (en) | 2017-07-27 | 2017-07-27 | A kind of harmlessness disposing method of comprehensive utilization of high saliferous chemical engineering sludge |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201710621099.0A CN107388262B (en) | 2017-07-27 | 2017-07-27 | A kind of harmlessness disposing method of comprehensive utilization of high saliferous chemical engineering sludge |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN107388262A CN107388262A (en) | 2017-11-24 |
| CN107388262B true CN107388262B (en) | 2018-12-04 |
Family
ID=60342203
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201710621099.0A Active CN107388262B (en) | 2017-07-27 | 2017-07-27 | A kind of harmlessness disposing method of comprehensive utilization of high saliferous chemical engineering sludge |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN107388262B (en) |
Families Citing this family (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2019062350A1 (en) * | 2017-09-26 | 2019-04-04 | 重庆盎瑞悦科技有限公司 | Harmless treatment method and system for domestic sludge |
| CN109502941A (en) * | 2018-12-28 | 2019-03-22 | 重庆盎瑞悦科技有限公司 | Cooperate with cement plant using the method for self- propagating pyrolysis installation processing sludge |
| CN109519928A (en) * | 2018-12-28 | 2019-03-26 | 重庆盎瑞悦科技有限公司 | Method and system containing organic materialization work abraum salt are handled using self- propagating pyrolysismethod |
| CN113307512B (en) * | 2021-05-07 | 2022-05-27 | 北京卡卢金热风炉技术有限公司 | Lime preparation device and lime preparation method |
| CN115520881A (en) * | 2022-10-13 | 2022-12-27 | 中国天辰工程有限公司 | Resource utilization method and system for waste salt with high content of organic matters |
Family Cites Families (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US20080072807A1 (en) * | 2006-09-22 | 2008-03-27 | Brookes David R | Gasifier and Incinerator for Biomass Sludge Destruction |
| CN103822213B (en) * | 2014-03-19 | 2015-10-28 | 大连容大资源循环利用咨询设计有限公司 | The dehydration of a kind of municipal sludge heat, waste heat drying and fluidized incineration integral process and system |
| US20150338094A1 (en) * | 2014-05-23 | 2015-11-26 | Wei-Hsuan Liu | Waste energy recovery system |
| CN205048449U (en) * | 2015-03-17 | 2016-02-24 | 南京工程学院 | Processing system of grate type waste incinerator multifuel combustion mud |
| CN105819644B (en) * | 2016-05-25 | 2019-05-03 | 北京航纳科技有限公司 | A kind of oily sludge innocuity disposal system and method |
-
2017
- 2017-07-27 CN CN201710621099.0A patent/CN107388262B/en active Active
Also Published As
| Publication number | Publication date |
|---|---|
| CN107388262A (en) | 2017-11-24 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN107388262B (en) | A kind of harmlessness disposing method of comprehensive utilization of high saliferous chemical engineering sludge | |
| CN106914474B (en) | A kind of Processes and apparatus of industrial waste salt decomposition carbonization harmless treatment | |
| CN207238730U (en) | Reclaimer is burned in a kind of negative-pressure cyclic accumulation of heat that harmlessness disposing is carried out to high saliferous chemical engineering sludge | |
| US6337302B1 (en) | Method for producing activated carbon from carbon black | |
| CN108892349A (en) | A kind of sludge drying and incineration system and its treatment process | |
| CN107030093A (en) | One kind combines washing and plasma fusion handles flying ash system | |
| CN111270077B (en) | System and method for disposing dust collection ash of steel plant by using chain plate type high-temperature reduction furnace | |
| RU2494128C2 (en) | Device for producing soot from rubber wastes | |
| CN112845504B (en) | Household garbage resource utilization treatment process | |
| CN108036323A (en) | The system and method that cement kiln cooperates with multifuel combustion garbage flying ash and sludge eco-cement | |
| CN106958827A (en) | A kind of dangerous waste incinerator slag total system | |
| CN116283338B (en) | System and method for firing ceramsite by using waste incineration fly ash | |
| CN108443889A (en) | A kind of discarded metal catalyst and organic sludge coprocessing device and method | |
| CN109824271A (en) | It handles the method for house refuse and implements its system | |
| JPS63502253A (en) | Methods and apparatus for neutralizing acid fumes, especially those arising from the combustion of residues | |
| CN105753344A (en) | Device and method for producing cement raw material from waste fly ash | |
| CN110043909A (en) | A kind of chemical engineering sludge burning process | |
| CN212285251U (en) | Dust collecting system for steel plant disposed by mesh belt type suspension combined reduction furnace | |
| CN111282961B (en) | System and method for disposing dust collection ash of steel plant by using mesh belt type suspension combined reduction furnace | |
| CN205635475U (en) | Organic garbage pyrolytic system | |
| CN105754622A (en) | Organic garbage pyrolysis system and application thereof | |
| EP3029372A1 (en) | Plant and process for recovering energy from organic matrix waste material | |
| CN105885884A (en) | Organic waste pyrolysis system and application thereof | |
| CN212451569U (en) | High-efficient ore deposit heat is useless circulation reprocessing and is utilized system admittedly | |
| CN216137437U (en) | System for resourceful treatment waste incineration fly ash |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant | ||
| TR01 | Transfer of patent right |
Effective date of registration: 20190307 Address after: 400080 Workshop Building 9, No. 16 Shilin Avenue, Dadukou District, Chongqing Patentee after: Chongqing Jinshengyue Intelligent Equipment Co.,Ltd. Address before: 400080 Tian'an Digital City, Dadukou District, Chongqing City, 4 buildings 703 Patentee before: CHONGQING ANGRUIYUE SCIENCE AND TECHNOLOGY Co.,Ltd. |
|
| TR01 | Transfer of patent right | ||
| TR01 | Transfer of patent right |
Effective date of registration: 20190517 Address after: 4 blocks 7-3, 7-4 and 7-5, 101 Cuibai Road, Chunhui Road, Dadukou District, Chongqing, 400084 Patentee after: CHONGQING ANGRUIYUE SCIENCE AND TECHNOLOGY Co.,Ltd. Address before: 400080 Workshop Building 9, No. 16 Shilin Avenue, Dadukou District, Chongqing Patentee before: Chongqing Jinshengyue Intelligent Equipment Co.,Ltd. |
|
| TR01 | Transfer of patent right | ||
| PP01 | Preservation of patent right |
Effective date of registration: 20190805 Granted publication date: 20181204 |
|
| PP01 | Preservation of patent right | ||
| PD01 | Discharge of preservation of patent |
Date of cancellation: 20190916 Granted publication date: 20181204 |
|
| PD01 | Discharge of preservation of patent | ||
| PE01 | Entry into force of the registration of the contract for pledge of patent right |
Denomination of invention: A comprehensive utilization method for harmless disposal of high salinity chemical sludge Granted publication date: 20181204 Pledgee: Chongqing Rural Commercial Bank Co.,Ltd. Dadukou Branch Pledgor: CHONGQING ANGRUIYUE SCIENCE AND TECHNOLOGY Co.,Ltd. Registration number: Y2024500000041 |
|
| PE01 | Entry into force of the registration of the contract for pledge of patent right |