CN109899800A - Based on the compound thermal cracking gasification treatment process of house refuse and system - Google Patents
Based on the compound thermal cracking gasification treatment process of house refuse and system Download PDFInfo
- Publication number
- CN109899800A CN109899800A CN201910034585.1A CN201910034585A CN109899800A CN 109899800 A CN109899800 A CN 109899800A CN 201910034585 A CN201910034585 A CN 201910034585A CN 109899800 A CN109899800 A CN 109899800A
- Authority
- CN
- China
- Prior art keywords
- cracker
- drier
- thermal cracking
- dry
- cracking
- 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.)
- Pending
Links
- 238000004227 thermal cracking Methods 0.000 title claims abstract description 86
- 238000000034 method Methods 0.000 title claims abstract description 59
- 238000002309 gasification Methods 0.000 title claims abstract description 54
- 230000008569 process Effects 0.000 title claims abstract description 44
- 150000001875 compounds Chemical class 0.000 title claims abstract description 31
- 239000000463 material Substances 0.000 claims abstract description 69
- 239000010813 municipal solid waste Substances 0.000 claims abstract description 60
- 238000005336 cracking Methods 0.000 claims abstract description 41
- 239000007788 liquid Substances 0.000 claims abstract description 31
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical group [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims abstract description 25
- 238000001035 drying Methods 0.000 claims abstract description 25
- 238000012545 processing Methods 0.000 claims abstract description 25
- 238000000926 separation method Methods 0.000 claims abstract description 21
- 239000007787 solid Substances 0.000 claims abstract description 10
- 238000001291 vacuum drying Methods 0.000 claims abstract description 7
- 238000002352 steam pyrolysis Methods 0.000 claims abstract description 4
- 229910052751 metal Inorganic materials 0.000 claims abstract description 3
- 239000002184 metal Substances 0.000 claims abstract description 3
- 238000002485 combustion reaction Methods 0.000 claims description 51
- 239000007789 gas Substances 0.000 claims description 49
- 238000000197 pyrolysis Methods 0.000 claims description 31
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 18
- 239000001301 oxygen Substances 0.000 claims description 18
- 229910052760 oxygen Inorganic materials 0.000 claims description 18
- 239000002737 fuel gas Substances 0.000 claims description 13
- 230000005611 electricity Effects 0.000 claims description 12
- 238000000855 fermentation Methods 0.000 claims description 4
- 230000004151 fermentation Effects 0.000 claims description 4
- 238000000746 purification Methods 0.000 claims description 2
- 230000000694 effects Effects 0.000 abstract description 7
- 230000009467 reduction Effects 0.000 abstract description 4
- 230000008676 import Effects 0.000 description 16
- 239000000126 substance Substances 0.000 description 12
- 238000005979 thermal decomposition reaction Methods 0.000 description 11
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 11
- 238000006243 chemical reaction Methods 0.000 description 9
- 230000005540 biological transmission Effects 0.000 description 7
- 239000003337 fertilizer Substances 0.000 description 7
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 6
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 6
- 239000000203 mixture Substances 0.000 description 6
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 5
- 238000010586 diagram Methods 0.000 description 5
- 229910002092 carbon dioxide Inorganic materials 0.000 description 4
- 238000007599 discharging Methods 0.000 description 4
- 239000007769 metal material Substances 0.000 description 4
- QTBSBXVTEAMEQO-UHFFFAOYSA-N Acetic acid Chemical compound CC(O)=O QTBSBXVTEAMEQO-UHFFFAOYSA-N 0.000 description 3
- CSCPPACGZOOCGX-UHFFFAOYSA-N Acetone Chemical compound CC(C)=O CSCPPACGZOOCGX-UHFFFAOYSA-N 0.000 description 3
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 description 3
- 238000010521 absorption reaction Methods 0.000 description 3
- 238000010504 bond cleavage reaction Methods 0.000 description 3
- 239000003638 chemical reducing agent Substances 0.000 description 3
- 239000002361 compost Substances 0.000 description 3
- 230000007797 corrosion Effects 0.000 description 3
- 238000005260 corrosion Methods 0.000 description 3
- 239000003546 flue gas Substances 0.000 description 3
- 238000010438 heat treatment Methods 0.000 description 3
- 150000002500 ions Chemical class 0.000 description 3
- 229910052742 iron Inorganic materials 0.000 description 3
- 238000012423 maintenance Methods 0.000 description 3
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 3
- 230000020477 pH reduction Effects 0.000 description 3
- 238000010248 power generation Methods 0.000 description 3
- 238000004064 recycling Methods 0.000 description 3
- 230000007017 scission Effects 0.000 description 3
- 239000002689 soil Substances 0.000 description 3
- 239000007921 spray Substances 0.000 description 3
- 229910001220 stainless steel Inorganic materials 0.000 description 3
- 239000010935 stainless steel Substances 0.000 description 3
- HGUFODBRKLSHSI-UHFFFAOYSA-N 2,3,7,8-tetrachloro-dibenzo-p-dioxin Chemical compound O1C2=CC(Cl)=C(Cl)C=C2OC2=C1C=C(Cl)C(Cl)=C2 HGUFODBRKLSHSI-UHFFFAOYSA-N 0.000 description 2
- 239000010963 304 stainless steel Substances 0.000 description 2
- IKHGUXGNUITLKF-UHFFFAOYSA-N Acetaldehyde Chemical compound CC=O IKHGUXGNUITLKF-UHFFFAOYSA-N 0.000 description 2
- 229910000589 SAE 304 stainless steel Inorganic materials 0.000 description 2
- GWEVSGVZZGPLCZ-UHFFFAOYSA-N Titan oxide Chemical compound O=[Ti]=O GWEVSGVZZGPLCZ-UHFFFAOYSA-N 0.000 description 2
- 239000004566 building material Substances 0.000 description 2
- 229910052799 carbon Inorganic materials 0.000 description 2
- 239000001569 carbon dioxide Substances 0.000 description 2
- 229910002091 carbon monoxide Inorganic materials 0.000 description 2
- 230000008859 change Effects 0.000 description 2
- 230000007547 defect Effects 0.000 description 2
- 238000011161 development Methods 0.000 description 2
- 238000005265 energy consumption Methods 0.000 description 2
- 239000004744 fabric Substances 0.000 description 2
- 229910001385 heavy metal Inorganic materials 0.000 description 2
- 239000001257 hydrogen Substances 0.000 description 2
- 229910052739 hydrogen Inorganic materials 0.000 description 2
- 238000010409 ironing Methods 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- 239000005416 organic matter Substances 0.000 description 2
- 238000003672 processing method Methods 0.000 description 2
- 238000010926 purge Methods 0.000 description 2
- 239000002910 solid waste Substances 0.000 description 2
- 239000011364 vaporized material Substances 0.000 description 2
- 206010002660 Anoxia Diseases 0.000 description 1
- 241000976983 Anoxia Species 0.000 description 1
- 206010013786 Dry skin Diseases 0.000 description 1
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 1
- 206010021143 Hypoxia Diseases 0.000 description 1
- 229910000831 Steel Inorganic materials 0.000 description 1
- 230000007953 anoxia Effects 0.000 description 1
- 239000012298 atmosphere Substances 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 239000006229 carbon black Substances 0.000 description 1
- 238000004140 cleaning Methods 0.000 description 1
- 239000000571 coke Substances 0.000 description 1
- 239000000567 combustion gas Substances 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 238000013461 design Methods 0.000 description 1
- 230000001066 destructive effect Effects 0.000 description 1
- 230000029087 digestion Effects 0.000 description 1
- 238000009826 distribution Methods 0.000 description 1
- 239000010791 domestic waste Substances 0.000 description 1
- 230000005518 electrochemistry Effects 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 238000004880 explosion Methods 0.000 description 1
- 238000010304 firing Methods 0.000 description 1
- 238000005189 flocculation Methods 0.000 description 1
- 230000016615 flocculation Effects 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- 239000000295 fuel oil Substances 0.000 description 1
- 150000002431 hydrogen Chemical class 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 230000010354 integration Effects 0.000 description 1
- 108010028930 invariant chain Proteins 0.000 description 1
- 238000011068 loading method Methods 0.000 description 1
- VUZPPFZMUPKLLV-UHFFFAOYSA-N methane;hydrate Chemical compound C.O VUZPPFZMUPKLLV-UHFFFAOYSA-N 0.000 description 1
- 239000010812 mixed waste Substances 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 239000003960 organic solvent Substances 0.000 description 1
- 238000007254 oxidation reaction Methods 0.000 description 1
- 230000000505 pernicious effect Effects 0.000 description 1
- 238000009272 plasma gasification Methods 0.000 description 1
- 239000004033 plastic Substances 0.000 description 1
- 229920003023 plastic Polymers 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 238000011160 research Methods 0.000 description 1
- 238000007789 sealing Methods 0.000 description 1
- 239000002904 solvent Substances 0.000 description 1
- 238000010025 steaming Methods 0.000 description 1
- 239000010959 steel Substances 0.000 description 1
- 238000003860 storage Methods 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
- 239000011269 tar Substances 0.000 description 1
- 238000012360 testing method Methods 0.000 description 1
- 239000004408 titanium dioxide Substances 0.000 description 1
- 238000012546 transfer Methods 0.000 description 1
- 230000001131 transforming effect Effects 0.000 description 1
- 238000009834 vaporization Methods 0.000 description 1
- 230000008016 vaporization Effects 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
Classifications
-
- 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
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
- Y02P20/129—Energy recovery, e.g. by cogeneration, H2recovery or pressure recovery turbines
Landscapes
- Gasification And Melting Of Waste (AREA)
- Processing Of Solid Wastes (AREA)
Abstract
The invention discloses compound thermal cracking gasification treatment process and system is based on, the technique is the following steps are included: (1) pre-processes: by rubbish by broken bag processing, then by the metal removal in the rubbish after broken bag；(2) be crushed: the refuse breaking after will be processed is at the material for being less than 20mm；(3) it is separated by solid-liquid separation: being separated by solid-liquid separation by broken material；(4) dry thermal cracking: by the multistage continuous vacuum drying technique for the different temperatures gradient that the solid refuse being separated by solid-liquid separation enters to, it is suitable for the state for carrying out thermal cracking gasification that house refuse moisture content, which is dropped to,；Material after drying enters different temperatures gradient continuous multi-stage thermal cracking process and carries out steam pyrolysis gasification；(5) carbon residue after step (4) cracking, carries out carbon residue burning；(6) lime-ash of after-flame excludes outside furnace.Treatment process and system provided by the invention can greatly improve house refuse thermal cracking gasification effect, while energy saving, the investment reduction of energy, save processing cost.
Description
Technical field
The present invention relates to technical field of domestic garbage treatment more particularly to a kind of refuse pyrolysis gasification process technique and it is
System.
Background technique
With the fast development of urbanization process, the processing of domestic waste, which has become, restricts each urban sustainable development hair
The problem of exhibition.According to statistics, domestic rubbish is mainly based on landfill, burning and compost.Landfill is current main processing ways, is accounted for
Than nearly half, burning accounts for 12% or so, and compost still has 30% house refuse to fail to handle less than 10%.These processing methods
Defect is obvious, and landfill method occupies a large amount of soils, easily pollutes to atmosphere, soil, water body, hidden peril of explosion of hiding.Incineration method fortune
Row processing cost is high, is especially easy to produce dioxin harmful substance, becomes new pollution sources.Compost fertilizer quality is not achieved
Fertilizer quality standard, the heavy metal contained in rubbish can also cause new pollution to soil.Therefore current processing mode restricts
Large-scale popularization and application.A kind of not secondary pollution, economic and practical processing technique, is current domestic rubbish disposal city
What field was badly in need of.
Pyrolysismethod is the thermal instability using organic matter in garbage, carries out heating steaming to it under anaerobic or anoxia condition
It evaporates, so that organic matter is generated cracking, form various new gases, liquid and solid after condensing, therefrom extract fuel oil, combustible gas
Process.It is pyrolyzed chemical structure, physical aspect and the temperature of pyrolysis and speed that yield depends on raw material.Pyrolysismethod and incineration method
It is two entirely different processes.Burning is an exothermic process, and is pyrolyzed and needs to absorb amount of heat.The primary product of burning
Carbon dioxide and water, and the primary product being pyrolyzed is flammable low molecular compound: gaseous hydrogen, methane, carbon monoxide,
The organic matters such as methanol, acetone, acetic acid, the acetaldehyde of liquid and tar, solvent naphtha etc..Solid mainly coke and carbon black.
The difficult point of refuse pyrolysis destructive gasifying technicalization: rubbish is a kind of mixture, the thermal decomposition temperature of different material first
Degree is different, and thermal decomposition behavior is also different, so the control of thermal decomposition operations condition is very difficult, can not even carry out sometimes.Its
Secondary, component of refuse, moisture often change, and operating condition is unstable, therefore often laboratory stage is very effective, and one arrives industry
Stage just becomes very complicated, and processing cost also increases considerably.Again, if mixing water content of matter is excessive, especially China is existing
The rubbish in stage is mainly garbage, and moisture is very high, and the heat balance of thermal decomposition is just relatively difficult, and thermal decomposition institute is recoverable
Fuel gas is not only few, but also calorific value is also low, therefore the economy thermally decomposed must give one's full attention to.In last rubbish some plastics or
Rubber pyrolysis will generate some pernicious gases, this technically brings bigger difficulty to thermal decomposition.In short, urban refuse thermal decomposition
Processing, though there are various researchs or test report in western developed country, since component of refuse is extremely complex, moisture, group poling
The operation of unstable mixed waste, Yao Wending is not easy very much.Capital cost, running cost, maintenance expense are high, and the fuel gas of recycling has
When calorific value it is low, therefore using being subject to certain restrictions.
Summary of the invention
The present invention is to solve the defect and deficiency of the prior art, is provided a kind of based at the compound thermal cracking gasification of house refuse
Science and engineering skill and system using the compound thermal cracking gasification processing method and system, then are equipped with special matched integrated compound thermal
After solving gasification furnace, house refuse thermal cracking gasification effect can be greatly improved, at the same can energy saving, investment reduction, at saving
Manage cost.
To achieve the above object, the technical solution adopted by the present invention is that being based on compound thermal cracking gasification treatment process, including
Following steps:
(1) it pre-processes: by rubbish by broken bag processing, then by the metal removal in the rubbish after broken bag；
(2) be crushed: the refuse breaking after will be processed is at the material for being less than 20mm；
(3) it is separated by solid-liquid separation: being separated by solid-liquid separation by broken material；
(4) the multistage continuous vacuum of different temperatures gradient dry thermal cracking: is entered to by the solid refuse being separated by solid-liquid separation
Drying process, the material after drying enter different temperatures gradient continuous multi-stage thermal cracking process and carry out steam pyrolysis gas
Change；
(5) carbon residue after step (4) cracking, carries out carbon residue burning；
(6) lime-ash of after-flame excludes outside furnace.
The side for using different temperatures gradient continuous multi-stage dry for the high problem of garbage water content, the present invention
Method, it is suitable for the state for carrying out thermal cracking gasification that house refuse moisture content, which is dropped to,.The characteristics of for house refuse complicated component, this
Invention can realize that rubbish is effectively handled using the method for different temperatures ladder thermal cracking.
As the preferred embodiment of the compound thermal cracking gasification treatment process of the present invention, the multistage continuous vacuum is dry
Drying process is dry using at least two-stage, and the continuous multi-stage thermal cracking process is using at least two-stage thermal cracking.
As the preferred embodiment of the compound thermal cracking gasification treatment process of the present invention, the multistage continuous vacuum drying work
Skill uses three-level continuous vacuum drying, and the dry temperature of the first order is 250 DEG C, and the dry temperature in the second level is 300 DEG C, third
The dry temperature of grade is 350 DEG C~450 DEG C；The continuous multi-stage thermal cracking process uses continuous three-level thermal cracking, the first order
The temperature of thermal cracking is 450 DEG C~650 DEG C, and the temperature of second level thermal cracking is 650 DEG C~750 DEG C, the temperature of third level thermal cracking
750 DEG C~850 DEG C of degree.Wherein, the temperature of cracking technologies at different levels by remaining carbonizable substance in material burn caused by heat with
The ratio of the amount of vaporized material controls.The present invention can solve life rubbish by the drying process equipped with different temperatures gradient
The high problem of rubbish moisture content, it is suitable for the state for carrying out thermal cracking gasification that realization, which drops to house refuse moisture content,.Simultaneously as
Rubbish is a kind of mixture, and the thermal decomposition temperature of different material is different, and thermal decomposition behavior is also different, and therefore, the present invention uses three
The ladder thermal cracking process of grade (high, medium and low) different temperatures.
As the preferred embodiment of the compound thermal cracking gasification treatment process of the present invention, the carbon residue ignition temperature is 850
DEG C~950 DEG C.Ignition temperature is controlled by the ratio of the quality of carbonizable substance remaining in material and the amount of oxygen supply.
Dry heat as the preferred embodiment of the compound thermal cracking gasification treatment process of the present invention, in the step (4)
It cracks and is carried out in integral type thermal splitting system with the carbon residue burning in step (5)；The integral type thermal splitting system includes
Furnace body, the furnace body are equipped with combustion chamber and at least one set of dry cracking apparatus,
The combustion chamber is equipped with input end, exhaust end and lime-ash output end, and the combustion chamber is equipped with gasifier,
The dry cracking apparatus includes drier and about at least two parallel rows of about at least two arranged in parallel
The cracker of cloth, each cracker are respectively positioned on the lower section of each drier, the combustion chamber be arranged in the bottom of furnace body and
Positioned at the lower section of each cracker；
Two neighbouring driers are connected, and two neighbouring crackers are connected, close to institute
The drier for stating cracker is connected with the cracker close to the drier,
Positioned at the top drier be equipped with feed inlet, positioned at bottom cracker be equipped with discharge port, it is described go out
Material mouth is connected with the input end, is equipped with exhaust outlet on each drier and each cracker.
Drying thermal cracking of the invention and carbon residue burning is carried out in integral type thermal splitting system, wherein material into
Enter in furnace with rise and pyrolysis gas convection current, reach dry materials, the material after drying drops to gasification layer, by vapor from
Son vaporization；Pyrolysis gas rises, and furnace body is discharged from exhaust outlet；Carbon residue declines the fuel gas buring that burned device sprays, and generates high temperature, combustion
Burn the energy consumption in the high temperature maintenance furnace generated；Pyrolysis gas is introduced into burner combustion, realizes energy circulation.It can be significantly
House refuse thermal cracking gasification effect, while energy saving, the investment reduction of energy are improved, processing cost is saved.
As the preferred embodiment of the compound thermal cracking gasification treatment process of the present invention, between the step (1) and (2) also
Ferment including step (1a): rubbish entered rubbish warehouse, by 2~4 days acidifying fermentations；, sent out by 3 days rapid acidifications
Ferment, rubbish become soft, alleviate to equipment attrition.And it is easy to be separated by solid-liquid separation.
The dry vapor generated, is discharged into steam generating system in the step (4), further heats；What cracking generated
Cracked gas a part enters carbon residue combustion chambers burn, and the heat of generation enters multistage heat exchange using another part for thermal cracking
Device is discharged into gas purge system, and power generation etc. is otherwise utilized after purification.
It successively include pretreatment system by processing direction the present invention also provides compound thermal cracking gasification processing system is based on
I, integral type pyrolysis furnace system II, auxiliary system III；The integral type pyrolysis furnace system II includes furnace body, and the furnace body is equipped with
Combustion chamber and at least one set of dry cracking apparatus,
The combustion chamber is equipped with input end, exhaust end and lime-ash output end, and the combustion chamber is equipped with gasifier,
The dry cracking apparatus includes drier and about at least two parallel rows of about at least two arranged in parallel
The cracker of cloth, each cracker are respectively positioned on the lower section of each drier, the combustion chamber be arranged in the bottom of furnace body and
Positioned at the lower section of each cracker；
Two neighbouring driers are connected, and two neighbouring crackers are connected, close to institute
The drier for stating cracker is connected with the cracker close to the drier,
Positioned at the top drier be equipped with feed inlet, positioned at bottom cracker be equipped with discharge port, it is described go out
Material mouth is connected with the input end, is equipped with exhaust outlet on each drier and each cracker.
Preferably, the dry cracking apparatus includes three driers, respectively the first drier, the second drier and the
Three driers, first drier are located at the top of second drier, and it is dry that second drier is located at the third
The top of dry device,
The dry cracking apparatus includes three crackers, respectively the first cracker, the second cracker and third cracking
Device, first cracker are arranged in the lower section of the third drier and are located at the top of second cracker, and described the
Two crackers are located at the top of the third cracker, and the third cracker is located at the top of the combustion chamber.
Preferably, the operating temperature of the first drying tube is 250 DEG C, and the operating temperature of second level drying tube is 300 DEG C, third
The operating temperature of grade drying tube is 350 DEG C~450 DEG C, and the operating temperature of first order heat cracker is 450 DEG C~650 DEG C, second
The operating temperature of grade heat cracker is 650 DEG C~750 DEG C, and the operating temperature of third level heat cracker is 750 DEG C~850 DEG C.
Preferably, the auxiliary system III includes multi-stage heat-exchanger, steam generator, combustible gas purifying system, richness
Oxygen system；The dry vapor generated of each drier enters steam generator and further heats, and each pyrolysis apparatus generates
Fuel gas enter in multi-stage heat-exchanger, by multi-stage heat-exchanger, steam generator, treated that gas enters to
In combustible gas purifying system；The oxygen enrichment system is used to provide oxygen to the carbon residue in combustion chamber；
Preferably, enter electricity generation system IV by combustible gas purifying system purified gas；The lime-ash of combustion chamber after-flame
It excludes outside furnace, is conveyed to following resourceization and utilizes system V.
Beneficial effects of the present invention: provided by the invention to be based on the compound thermal cracking gasification treatment process of house refuse and be
System, the compound thermal cracking gas chemical industry skill that the present invention uses, using the method that different temperatures gradient continuous multi-stage is dry, by life rubbish
It is suitable for the state for carrying out thermal cracking gasification that rubbish moisture content, which drops to, and the characteristics of for house refuse complicated component, the present invention is not using
The method of synthermal ladder thermal cracking can realize that rubbish is effectively handled.The compound thermal cracking gasification processing system of offer of the invention
After system is using the compound pyrolysis gasification furnace of integration, house refuse thermal cracking gasification effect can be greatly improved, while energy can be saved
Source, investment reduction save processing cost.
Detailed description of the invention
Fig. 1 is compound thermal cracking gasification process flow diagram of the invention；
Fig. 2 is the structural schematic diagram of integral type pyrolysis furnace system II of the present invention；
Fig. 3 is the cross-sectional structure schematic diagram of integral type pyrolysis furnace system II of the present invention；
Fig. 4 is the side view of integral type pyrolysis furnace system II of the present invention；
Fig. 5 is the structural schematic diagram of integral type pyrolysis furnace system II and auxiliary system III of the invention.
Specific embodiment
The present invention is further described in detail with reference to the accompanying drawing, these attached drawings are simplified schematic diagram, only
The basic structure that the invention is illustrated in a schematic way, the direction of this specific implementation is using the direction Fig. 1 as standard.
Embodiment 1
A kind of embodiment based on the compound thermal cracking gasification processing system of house refuse of the invention, as shown in Figure 1, described
Thermal cracking gasification processing system includes pretreatment system I, integral type pyrolysis furnace system II, auxiliary system III, electricity generation system IV, and
Following resourceization utilizes system V.
Pretreatment system I includes that house refuse is unloaded platform, household garbage bag-breaking machine, strong magnetic automatic discharging iron remover, rubbish
Rubbish warehouse, driving grab bucket, crusher, solid-liquid separating machine；The cram packer for being first filled up with rubbish opens platform of unloading, and overturning is unloaded
Rubbish is passed through household garbage bag-breaking machine, will load in mixture the polybag broken bag of rubbish by vehicle, makes rubbish tiling on a moving belt, rubbish
Communicated band conveying, below too strong magnetic automatic discharging iron remover, the ironware in rubbish is removed by automatic de-ironing device, then ironware
It is transported to specific store case, carries out steel recycling.
Rubbish enters rubbish warehouse, and the rubbish warehouse of the present embodiment is solid anaerobic digestion cabin, and rubbish is in this residence time
It is 2~4 days, preferably 3 days, ferments by 3 days rapid acidifications, rubbish becomes soft, thus can reduce to equipment attrition, and
And be easy to be separated by solid-liquid separation, the rubbish of acidified processing, it grabs bucket via driving, is delivered to crusher, is broken into and is less than
The material of 20mm.Enter solid-liquid separating machine by broken material, is separated by solid-liquid separation.Liquid after separation, a part return spray
To rubbish warehouse, a part enters liquid fertilizer system.
By the solid waste of separation of solid and liquid, it is delivered in integral type pyrolysis system II, as shown in figs. 2 to 4, integral type heat
Solving furnace system II includes furnace body 1, and furnace body 1 is equipped with combustion chamber 2 and at least one set of dry cracking apparatus, and combustion chamber 2 is equipped with import
End 21, exhaust end 22 and lime-ash output end 23, combustion chamber 2 are equipped with gasifier 27, and dry cracking apparatus includes at least two
The drier 4 of lower arranged in parallel and the cracker 5 of about at least two arranged in parallel, each cracker 5 are respectively positioned on each drier 4
Lower section, combustion chamber 2 are arranged in the bottom of furnace body 1 and are located at the lower section of each cracker 5, and two neighbouring driers 4 are connected
Logical, two neighbouring crackers 5 are connected, and the drier 4 close to cracker 5 is connected with the cracker 5 close to drier 4
Logical, the drier 4 positioned at the top is equipped with feed inlet 411, is equipped with discharge port 532, discharging positioned at the cracker 5 of bottom
Mouth 532 is connected with input end 21, is equipped with exhaust outlet 6 on each drier 4 and each cracker 5.
Enter in the drier 4 for being located at the top after drying by the solid waste of separation of solid and liquid from feed inlet 411, material
In moisture be evaporated, the dry vapor generated is discharged from the exhaust outlet 6 on drier 4, is discharged into steam generating system, into
The heating of one step.Because neighbouring two driers 4 are connected, material falls into next drying from the drier 4 for being located at the top
In device 4, by redrying, moisture is further evaporated, and is equally discharged by exhaust outlet 6.Repeatedly until material is from last
It is fallen into cracker 5 in one drier 4, heat scission reaction occurs.Drier 4 presses different temperatures gradient, and temperature is from down to height
Arrangement, each cracker 5 can be sequentially arranged in the lower section of each drier 4 from temperature down to height by different temperature gradients downwards.Object
Low temperature pyrogenation substance in the material thermal cracking in the cracker 5 being connected to drier 4, the fuel gas of generation is from the cracker 5
On exhaust outlet 6 enter auxiliary system III in multi-stage heat-exchanger, in the present embodiment, it is also possible to which pipeline is connected to the exhaust outlet
6 into combustion chamber 2, convenient for the recycling of pyrolysis gas, increases the calorific value of burning, energy saving, and solves flue gas emission
Pollution problem.After repeatedly being dried multiple heat scission reaction occurs for material.The fuel gas that 5 thermal cracking of cracker generates,
A part returns to combustion chamber 2 and burns, and the heat of generation is used for thermal cracking.Power generation etc. is otherwise utilized after a part can purify.
After material falls into the cracker 5 positioned at bottom and heat scission reaction occurs.Material enters combustion chamber 2 along discharge port 532
In.Carbon residue declines the fuel gas buring that burned device sprays, and generates high temperature, and the high temperature for generation of burning maintains the energy consumption in furnace.
Gasifier 27 is equipped in combustion chamber 2, gasifier 27 can promote material to gasify, and have and improve calorific value, increase intensity of fire, energy-saving ring
The using effect of guarantor.In the present embodiment, gasifier 27 is preferably plasma gasification device, be can produce with high purity, cleaning flammable
Gas.The carbon dioxide generated that burns is discharged from exhaust end 22, it is preferable that the top of furnace body 1 is arranged in exhaust end 22.Combustion chamber
2 two sides are equipped with burner 24, convenient for by the remaining carbonizable substance full combustion in material, the residue after burning is exported from lime-ash
23 discharge of end, user can place trolley 3 in lime-ash output end 23, for loading residue.
II key reaction of integral type pyrolysis system of the invention is as follows:
(1) steam transforming is reacted
C+H2O=CO+H2-132KJ/mol；
(2) water gas shift reaction
CO+H2O=CO2+H2+42KJ/mol；
(3) partial oxidation reaction
C+0.5O2=CO+111KJ/mol；
(4) methanation reaction
CO+2H2=CH4+74KJ/mol；
(5) Boudouard reacts
C+CO2=CO-172KJ/mol.
Without adding auxiliary fuel after pyrolysis system operation of the invention, can maintain to operate normally.
II structure of integral type pyrolysis system of the invention is simple, reduces the volume of equipment, is particularly suitable for the heat of rubbish
Gasification process is solved, for the high problem of garbage water content, using more than two-stage continuous drying method, by house refuse
It is suitable for the state for carrying out thermal cracking gasification that moisture content, which drops to,.The characteristics of for house refuse complicated component, using different temperatures rank
The cracker 5 of ladder carries out thermal cracking process.Thermal cracking gasification furnace structure provided by the invention is simple, and the setting of drier 4 is cracking
The top of device 5, the operating temperature that cracker 5 needs is higher, and the operating temperature that drier 4 needs is lower.When furnace body 1 works,
Heat rises from the bottom up, and the thermal energy that cracker 5 passes over can be absorbed in drier 4, and rubbish thermal oxide generation is highly utilized
Calorific value, reduce the waste of heat.Material is carried out using more than two driers 4 and more than two crackers 5 multiple
Dry and pyrolysis, improves the calorific value of pyrolysis gas, increases the efficiency of material pyrolysis, strengthens thermal cracking gasification effect.?
In actual production, the feeding device for having sealing function can be placed at feed inlet 411, which only has a charging
Mouth 411, which is located on the drier 4 of the top, and cracking gas and other driers 4 are almost in contact with less than the external world
Air, a possibility that oxygen is entered in other driers 4 or cracker 5 is reduced, to generate dioxin etc. when reducing reaction
A possibility that harmful substance.
Wherein, the shape of each drier 4 and each cracker 5 is tubulose, and each drier 4 and the equal level of each cracker 5 are worn
On furnace body 1.The tubular design of drier 4 and cracker 5 is conducive to keep higher temperature in drier 4 or cracker 5,
Reach preferable heat-transfer effect, accelerate dry materials and promotes the progress of pyrolytic reaction.
Particularly, dry cracking apparatus includes three driers 4, respectively the first drier 41,42 and of the second drier
Third drier 43, the first drier 41 are located at the top of the second drier 42, and the second drier 42 is located at third drier 43
Top, dry cracking apparatus includes three crackers 5, respectively the first cracker 51, the second cracker 52 and third cracking
Device 53, the first cracker 51 are arranged in the lower section of third drier 43 and are located at the top of the second cracker 52, the second cracker
52 are located at the top of third cracker 53, and third cracker 53 is located at the top of combustion chamber 2.In the present embodiment, first is dry
The operating temperature of device 41 is 250 DEG C, and the operating temperature of the second drier 42 is 300 DEG C, and the operating temperature of third drier 43 is
350 DEG C~450 DEG C, the operating temperature of the first cracker 51 is 450 DEG C~650 DEG C, and the operating temperature of the second cracker 52 is 650
DEG C~750 DEG C, 750 DEG C~850 DEG C of third cracking tube operating temperature, the operating temperature of combustion chamber 2 is 850 DEG C~950 DEG C.Its
In, the ratio of the amount of temperature heat caused by carbonizable substance burning remaining in material and vaporized material of each cracker 5
The ignition temperature of example control, combustion chamber 2 is controlled by the ratio of the quality of carbonizable substance remaining in material and the amount of oxygen supply.In reality
In, user can be set as needed the quantity of drier 4 and cracker 5.The present invention is by being equipped with different temperatures ladder
The drier of degree can solve the problems, such as that garbage water content is high, and it is suitable for carrying out heat that realization, which drops to house refuse moisture content,
Crack the state of gasification.Simultaneously as rubbish is a kind of mixture, the thermal decomposition temperature of different material is different, thermal decomposition behavior
Also different, therefore, the present invention uses the ladder thermal cracking process of three-level (high, medium and low) different temperatures.
Further, the first drier 41, the second drier 42, third drier 43, the cracking of the first cracker 51, second
Device 52 and third cracker 53 all have two ends in left and right, and feed inlet 411 is located at the end of left and right two of the first drier 41
Wherein one end upside, the downside of the other end of the first drier 41 is equipped with first outlet 412, the second drier 42 and first
The upside for exporting the corresponding one end in 412 positions is equipped with the first import 421, and first outlet 412 is connected with the first import 421, with
Realize that the first drier 41 is connected with the second drier 42, the downside of the other end of the second drier 42 is equipped with second outlet
422, the upside of the one end corresponding with 422 position of second outlet of third drier 43 is equipped with the second import 431, second outlet 422
Be connected with the second import 431, with realize the second drier 42 be connected with third drier 43, third drier 43 it is another
The downside at end is equipped with third outlet 432, and the upside of the first cracker 51 one end corresponding with third 432 positions of outlet is equipped with third
Import 511, third outlet 432 is connected with third import 511, to realize that third drier 43 is connected with the first cracker 51
Logical, the downside of the other end of the first cracker 51 is equipped with the 4th outlet 512,512 positions pair of the second cracker 52 and the 4th outlet
The upside of the one end answered is equipped with the 4th import 521, and the 4th outlet 512 is connected with the 4th import 521, to realize the first cracker
51 are connected with the second cracker 52, and the downside of the other end of the second cracker 52 is equipped with the 5th outlet 522, third cracker 53
The upside of one end corresponding with the 5th 522 positions of outlet is equipped with the 5th import 531, and the 5th outlet 522 is connected with the 5th import 531
Logical, to realize that the second cracker 52 is connected with third cracker 53, discharge port 532 is located at the other end of third cracker 53
Downside.
The material being broken enters the first drier 41 from feed inlet 411, and the moisture in material is heated to form vapor,
It is discharged from the exhaust outlet 6 of the first drier 41, material is dry into second through the first import 421 from first outlet 412 after being dried
By redrying in dry device 42, likewise, the moisture in material is further evaporated, from 6 row of exhaust outlet of the second drier 42
Out.Material is discharged from second outlet 422, enters in third drier 43 through the second import 431, the moisture in material is thoroughly steamed
Hair is discharged from the exhaust outlet 6 of third drier 43.The material of over dry enters first through third import 511 from third outlet 432 and splits
It solves in device 51, low temperature pyrogenation substance in material by thermal cracking, is generating fuel gas, and user's available pipe is by each cracking
The exhaust outlet 6 of device 5 is connected with combustion chamber 2, burns so that fuel gas is introduced into combustion chamber 2, pyrolysis gas is made full use of to increase
The combustion efficiency of strong combustion chamber 2.Material, which enters in the second cracker 52 from the 4th outlet 512 through the 4th import 521, realizes medium temperature
Cracking then enters in third cracker 53 through the 5th import 531 from the 5th outlet 522 and realizes Pintsch process.By three-level heat
The remaining material of cracking is discharged from discharge port 532, enters in combustion chamber 2 from input end 21 and is sufficiently burned.It drier 4 and splits
The inlet and outlet of solution device 5 is divided into both ends, so that material will can be just discharged by entire drier 4 or entire cracker 5,
Be conducive to the abundant dry or sufficiently pyrolysis of material.
In addition, each drier 4 and each cracker 5 are equipped with the material propulsion device for pushing material to advance.Due to dry
Dry device 4 and cracker 5 are tubular structure, and the advance of material needs the promotion of material propulsion device, and next stage of being allowed for access is dry
In dry device 4 or cracker 5 or combustion chamber 2.Material propulsion device includes driving device, transmission device 8 and propeller 7, driving dress
The input terminal set is electrically connected with external power supply, and the output end of driving device is connected with the input terminal of transmission device 8, transmission device
8 output end is connected with propeller 7, and in the operating condition, driving device driving transmission device 8 rotates, to drive propeller 7
Rotation, to push material to advance.After powering on, driving device driving transmission device 8 is rotated, so that propeller 7 works, is pushed
Material advances.In the present embodiment, driving device is motor, and transmission device 8 can be speed reducer, and propeller 7 is helical blade,
The output end of motor and the input terminal of speed reducer connect, and the output end of speed reducer and the center of helical blade connect.In other realities
It applies in example, can also be driven by pulley drive, hydraulic drive or the modes such as pneumatic, there are many transmission devices 8, without being limited thereto
Example, propeller 7 can be ribbon or blade etc., and the material of propeller 7 is necessary for high temperature resistant material.
Preferably, combustion chamber 2 is equipped with steam gasification nozzle 25.Vapor is sprayed into sufficiently combustion by steam gasification nozzle 25
In the substance of burning, promote material that further gasification reaction occurs, the carbon monoxide and hydrogen of generation can be introduced by pipeline to be fired
With overheavy firing in burner 24.It is highly preferred that can be used pipeline by the exhaust outlet 6 and steam gasification nozzle on each drier 4
25 connections, make full use of the moisture being evaporated in material, environmental protection and energy saving.
Fire grate 26 is equipped in combustion chamber 2, material is evenly distributed on fire grate 26, each more objects that can burn in combustion chamber 2
Material, guarantees the full combustion of material.
It is noted that as shown in figure 3, the quantity of dry cracking apparatus is two groups.In the present embodiment, two groups of dryings
Cracking apparatus is all provided with there are three drier 4 and three crackers 5.Two groups of dry cracking apparatus can be run simultaneously, can also be wrong
ETAD expected time of arrival and departure operation.When wherein one group of dry cracking apparatus needs repairing, another group of dry cracking apparatus can be at working condition,
Guarantee not shut down in plant maintenance, carry out garbage disposal work can as usual.
In addition, the material of drier 4 is the corrosion-resistant metal materials that can bear 500 DEG C or more high temperature, the material of cracker 5
For the corrosion-resistant metal materials that can bear 1000 DEG C or more high temperature.In view of rubbish has corrosivity, therefore preferably with corrosion-resistant
Material.The highest operating temperature of drier 4 is 450 DEG C, is able to satisfy using the metal material that can bear 500 DEG C or more high temperature dry
Dry device running temperature requirement, likewise, the highest operating temperature of cracker be 950 DEG C, therefore select can bear 1000 DEG C with
The metal material of upper high temperature.In the present embodiment, drying tube 4 selects 304 stainless steel seamless pipes, and cracking tube 4 selects 2520 resistance to height
Warm stainless steel tube, wall thickness 16mm, 2520 stainless steel tubes can high temperature resistant to 1300 DEG C, can work in the environment of 1150 DEG C for a long time
Make.304 stainless steel tubes and 2520 stainless steel tube price material benefits, can reduce the cost of thermal cracking gasification oven.
As shown in figure 5, auxiliary system III includes multi-stage heat-exchanger 90, steam generator 91, combustible gas purifying system,
Oxygen enrichment system, wherein the dry vapor generated of each drier 4 enters steam generator 91 further by exhaust outlet 6
Heating, the fuel gas that each pyrolysis apparatus 5 generates enter in multi-stage heat-exchanger 91 from the exhaust outlet 6 on the cracker 5, preferably
Ground, the gas to be gasified by 27 material of gasifier can connect multi-stage heat-exchanger 91, and the titanium dioxide generated of burning by pipeline
Carbon enters in multi-stage heat-exchanger 91 from exhaust end 22, and by multi-stage heat-exchanger 90, treated for steam generator 91
Gas enters in combustible gas purifying system；Combustible gas purifying system includes exhaust gas absorption device 92, steam-water separator 93, ion
Clarifier 94, fuel gas are initially entered to exhaust gas absorption device 92, and exhaust gas absorption device 92 contains organic solvent, for absorbing
Exhaust gas in gas, gas after treatment, which enters in steam-water separator 92, realizes steam-water separation, removes extra moisture, can
Combustion gas body enters ion purifier 94 and is further purified, to generate purity is high, clean fuel gas, generation it is flammable
Gas is generated electricity using gas electricity generator for generating electricity, avoids the high pressure of high steam boiler power generation, inefficiency problem.It is oxygen-enriched
System is used to provide oxygen to combustion chamber 2, and carbon residue uses oxygen-enriched combusting, greatly reduces the yield of flue gas, richness of the invention
Oxygen system uses three-level embrane method oxygen technique, and oxygen cost processed can be greatly reduced.
Present invention multi-stage heat-exchanger 90 mentioned above, steam generator 91, combustible gas purifying system, oxygen enrichment system
It is all made of prior art realization, does not do excessive description herein.
Electricity generation system IV is made of gas electricity generator and distribution system.Pass through the purified combustible gas of ion purifier 94
Body is generated electricity for generating electricity using gas electricity generator.Following resourceization is using system V by building materials manufacturing system (brickmaking) and liquid
Fertilizer system composition.The lime-ash of 2 after-flame of combustion chamber excludes to be conveyed to auxiliary building materials (brickmaking) system outside furnace.By solid-liquid point
The percolate of the percolate and auxiliary system III isolated from device enters subsequent liquid fertilizer system, first by percolate
Heavy metal is deviate from through electrochemistry flocculation system, then is handled through biotechnology, liquid fertilizer is made.
Embodiment 2
A kind of embodiment based on the compound thermal cracking gasification treatment process of house refuse of the invention, comprising the following steps:
(1) it pre-processes: rubbish being handled by broken bag, the polybag broken bag of rubbish, the communicated band after broken bag will be loaded in mixture
Conveying, below too strong magnetic automatic discharging iron remover, the ironware in rubbish is removed by automatic de-ironing device, and then ironware is transported to specially
With storage box, it is recycled；
(2) ferment: rubbish entered rubbish warehouse, and is 2~4 days in this residence time, by 2~4 days rapid acidifications
Fermentation, rubbish become soft, to can reduce to equipment attrition, and are easy to be separated by solid-liquid separation；
(3) be crushed: the rubbish of acidified processing grabs bucket via driving, is delivered to crusher, is broken into less than 20mm's
Material；
(4) it is separated by solid-liquid separation: entering solid-liquid separating machine by broken material, be separated by solid-liquid separation, the liquid after separation, one
Part, which is returned, is sprayed onto rubbish warehouse, and a part enters liquid fertilizer system.
(5) dry thermal cracking: the multistage for the different temperatures gradient that the solid refuse by separation of solid and liquid enters to is continuous true
Empty drying process, it is suitable for the state for carrying out thermal cracking gasification that house refuse moisture content, which is dropped to,；Material after drying enters
Different temperatures gradient continuous multi-stage thermal cracking process carries out steam pyrolysis gasification；
(6) carbon residue after step (5) cracking is discharged into carbon residue combustion chamber, while the dry water generated of step (5) steams
Gas is discharged into steam generating system, further heats；Cracked gas a part that cracking generates enters carbon residue burning, the heat of generation
Amount is used for thermal cracking, and another part enters multi-stage heat-exchanger, is discharged into gas purge system；
(7) lime-ash of after-flame excludes outside furnace, and purified combustible gas is input to electricity generation system.
Drying thermal cracking in the step (5) carries out in the integral type pyrolysis system II that the present invention implements in 1；Institute
It is dry using at least two-stage to state multistage continuous vacuum drying technique, the present embodiment uses three-level continuous vacuum drying, and the first order is dry
Dry temperature is 250 DEG C, and the dry temperature in the second level is 300 DEG C, and the dry temperature of the third level is 350 DEG C~450 DEG C, described
Continuous multi-stage thermal cracking process using at least two-stage thermal cracking, the present embodiment uses continuous three-level thermal cracking process, the first order
The temperature of thermal cracking is 450 DEG C~650 DEG C, and the temperature of second level thermal cracking is 650 DEG C~750 DEG C, the temperature of third level thermal cracking
750 DEG C~850 DEG C of degree；
Carbon residue burning in (6) carries out in integral type pyrolysis system II with thermal cracking dry in step (5), residual
The operating temperature of carbon burning is 850 DEG C~950 DEG C.The carbon residue burning process uses oxygen-enriched combusting, can greatly reduce flue gas
Yield.
The foregoing is merely illustrative of the preferred embodiments of the present invention, is not intended to limit the invention, all in essence of the invention
Within mind and principle, any modification, equivalent substitution, improvement and etc. done be should be included within the scope of the present invention.
Claims (10)
1. being based on compound thermal cracking gasification treatment process, which comprises the following steps:
(1) it pre-processes: by rubbish by broken bag processing, then by the metal removal in the rubbish after broken bag；
(2) be crushed: the refuse breaking after will be processed is at the material for being less than 20mm；
(3) it is separated by solid-liquid separation: being separated by solid-liquid separation by broken material；
(4) dry thermal cracking: entering to the multistage continuous vacuum drying of different temperatures gradient by the solid refuse being separated by solid-liquid separation,
Material after drying enters different temperatures gradient continuous multi-stage thermal cracking process and carries out steam pyrolysis gasification；
(5) carbon residue after step (4) cracking, carries out carbon residue burning；
(6) lime-ash of after-flame excludes outside furnace.
2. compound thermal cracking gasification treatment process according to claim 1, which is characterized in that described multistage continuous true
Empty drying process is dry using at least two-stage, and the continuous multi-stage thermal cracking process is using at least two-stage thermal cracking.
3. compound thermal cracking gasification treatment process according to claim 2, which is characterized in that the multistage continuous vacuum is dry
Drying process uses three-level continuous vacuum drying, and the dry temperature of the first order is 250 DEG C, and the dry temperature in the second level is 300 DEG C,
The dry temperature of the third level is 350 DEG C~450 DEG C；The continuous multi-stage thermal cracking process uses continuous three-level thermal cracking, the
The temperature of level-one thermal cracking is 450 DEG C~650 DEG C, and the temperature of second level thermal cracking is 650 DEG C~750 DEG C, third level thermal cracking
750 DEG C~850 DEG C of temperature.
4. compound thermal cracking gasification treatment process according to claim 1, which is characterized in that the carbon residue ignition temperature is
850 DEG C~950 DEG C.
Drying thermal cracking and step 5. compound thermal cracking gasification treatment process according to claim 1, in the step (4)
Suddenly the carbon residue burning in (5) carries out in integral type thermal splitting system；The integral type thermal splitting system includes furnace body, described
Furnace body is equipped with combustion chamber and at least one set of dry cracking apparatus,
The combustion chamber is equipped with input end, exhaust end and lime-ash output end, and the combustion chamber is equipped with gasifier,
The dry cracking apparatus includes the drier and about at least two arranged in parallel of about at least two arranged in parallel
Cracker, each cracker are respectively positioned on the lower section of each drier, and the combustion chamber is arranged in the bottom of furnace body and is located at
The lower section of each cracker；
Two neighbouring driers are connected, and two neighbouring crackers are connected, and split close to described
The drier for solving device is connected with the cracker close to the drier,
Drier positioned at the top is equipped with feed inlet, and the cracker positioned at bottom is equipped with discharge port, the discharge port
It is connected with the input end, is equipped with exhaust outlet on each drier and each cracker.
6. compound thermal cracking gasification treatment process according to claim 1, which is characterized in that the step (1) and (2) it
Between further include step (1a) fermentation: rubbish entered rubbish warehouse, by 2~4 days acidifying fermentations；
The dry vapor generated, is discharged into steam generating system in the step (4), further heats；Crack the cracking generated
Gas a part enters carbon residue burning, and the heat of generation is used for thermal cracking, and another part enters multi-stage heat-exchanger, is discharged into gas
Body purification system.
7. be based on compound thermal cracking gasification processing system, which is characterized in that by processing direction successively include pretreatment system I, one
Body formula is pyrolyzed furnace system II, auxiliary system III；The integral type pyrolysis furnace system II includes furnace body, and the furnace body is equipped with burning
Room and at least one set of dry cracking apparatus,
The combustion chamber is equipped with input end, exhaust end and lime-ash output end, and the combustion chamber is equipped with gasifier,
The dry cracking apparatus includes the drier and about at least two arranged in parallel of about at least two arranged in parallel
Cracker, each cracker are respectively positioned on the lower section of each drier, and the combustion chamber is arranged in the bottom of furnace body and is located at
The lower section of each cracker；
Two neighbouring driers are connected, and two neighbouring crackers are connected, and split close to described
The drier for solving device is connected with the cracker close to the drier,
Drier positioned at the top is equipped with feed inlet, and the cracker positioned at bottom is equipped with discharge port, the discharge port
It is connected with the input end, is equipped with exhaust outlet on each drier and each cracker.
8. according to claim 7 be based on compound thermal cracking gasification processing system, which is characterized in that the dry cracking is set
Standby includes three driers, respectively the first drier, the second drier and third drier, and first drier is located at institute
The top of the second drier is stated, second drier is located at the top of the third drier,
The dry cracking apparatus includes three crackers, respectively the first cracker, the second cracker and third cracker, institute
It states the first cracker the lower section of the third drier is arranged in and is located at the top of second cracker, second cracking
Device is located at the top of the third cracker, and the third cracker is located at the top of the combustion chamber.
9. according to claim 8 be based on compound thermal cracking gasification processing system, which is characterized in that the work of the first drying tube
Making temperature is 250 DEG C, and the operating temperature of second level drying tube is 300 DEG C, the operating temperature of third level drying tube is 350 DEG C~
450 DEG C, the operating temperature of first order heat cracker is 450 DEG C~650 DEG C, and the operating temperature of second level heat cracker is 650 DEG C
~750 DEG C, the operating temperature of third level heat cracker is 750 DEG C~850 DEG C.
10. according to claim 7 be based on compound thermal cracking gasification processing system, which is characterized in that the auxiliary system
III includes multi-stage heat-exchanger, steam generator, combustible gas purifying system, oxygen enrichment system；Each drier is dry to be produced
Raw vapor enters steam generator and further heats, and the fuel gas that each pyrolysis apparatus generates enters multi-stage heat-exchanger
In, by multi-stage heat-exchanger, steam generator, treated that gas enters in combustible gas purifying system；The oxygen-enriched system
It unites for providing oxygen to the carbon residue in combustion chamber；
Preferably, enter electricity generation system IV by combustible gas purifying system purified gas；The lime-ash of combustion chamber after-flame excludes
Outside furnace, it is conveyed to following resourceization and utilizes system V.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201910034585.1A CN109899800A (en) | 2019-01-14 | 2019-01-14 | Based on the compound thermal cracking gasification treatment process of house refuse and system |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201910034585.1A CN109899800A (en) | 2019-01-14 | 2019-01-14 | Based on the compound thermal cracking gasification treatment process of house refuse and system |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN109899800A true CN109899800A (en) | 2019-06-18 |
Family
ID=66943793
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201910034585.1A Pending CN109899800A (en) | 2019-01-14 | 2019-01-14 | Based on the compound thermal cracking gasification treatment process of house refuse and system |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN109899800A (en) |
Cited By (13)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109609189A (en) * | 2018-12-14 | 2019-04-12 | 西安交通大学 | A waste gasifier and a waste gasification method based thereon |
| CN110529859A (en) * | 2019-09-16 | 2019-12-03 | 徐飞 | A kind of solid waste material treating device |
| CN111019711A (en) * | 2019-12-16 | 2020-04-17 | 武汉科技大学 | Thermal cracking gasification process for household garbage |
| CN111139096A (en) * | 2020-01-08 | 2020-05-12 | 润电能源科学技术有限公司 | Household garbage treatment system and household garbage treatment method thereof |
| CN112268279A (en) * | 2020-10-15 | 2021-01-26 | 深圳市捷晶能源科技有限公司 | An intelligent thermal cracking treatment method and system for slag solid waste |
| CN112300817A (en) * | 2019-12-05 | 2021-02-02 | 上海敏建环保科技有限公司 | Pyrolysis gasification method for household garbage |
| CN112619562A (en) * | 2020-11-27 | 2021-04-09 | 深圳市捷晶能源科技有限公司 | Thermal cracking system and thermal cracking method |
| CN112619561A (en) * | 2020-11-27 | 2021-04-09 | 深圳市捷晶能源科技有限公司 | Heavy metal-containing material treatment system and treatment method thereof |
| CN112728548A (en) * | 2020-12-22 | 2021-04-30 | 华中科技大学 | Gradient temperature-changing type equipment and method for removing tar by garbage heat |
| CN113087337A (en) * | 2021-04-06 | 2021-07-09 | 深圳市捷晶能源科技有限公司 | Sludge treatment system |
| CN113280348A (en) * | 2021-05-27 | 2021-08-20 | 巴彦淖尔市汇利锅炉制造有限责任公司 | Multifunctional garbage incinerator |
| CN113531538A (en) * | 2021-06-08 | 2021-10-22 | 湖南省欣洁环保科技有限公司 | Household garbage treatment method and system |
| CN118960382A (en) * | 2024-09-18 | 2024-11-15 | 阜新成泰环保科技有限公司 | A method and device for supplying air to a reaction zone in a rotary kiln through the kiln wall |
Citations (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH11211042A (en) * | 1998-01-29 | 1999-08-06 | Meidensha Corp | Method and apparatus for treating halogen containing material |
| CN1621743A (en) * | 2003-11-26 | 2005-06-01 | 中国科学院力学研究所 | Plasma multi-stage cracking technology and apparatus capable of processing multiple organic wastes simultaneously |
| WO2006117824A1 (en) * | 2005-05-02 | 2006-11-09 | Pyrolb S.R.L. | Integrated process for waste treatment by pyrolysis and related plant |
| CN104534476A (en) * | 2014-12-29 | 2015-04-22 | 派石新能源技术开发(北京)有限公司 | Destructive distillation method and device for organic solid waste harmless treatment |
| CN205299538U (en) * | 2016-01-19 | 2016-06-08 | 河南华天环保科技有限公司 | Vertical rotatory domestic waste of superelevation multistage burns gasification equipment |
| CN106085511A (en) * | 2016-06-08 | 2016-11-09 | 北京神雾环境能源科技集团股份有限公司 | A kind of rubbish charcoal resource and the method and system of raising pyrolysis gas calorific value |
| CN106287733A (en) * | 2016-08-11 | 2017-01-04 | 赛能杰高新技术股份有限公司 | One way of life waste disposal method |
| CN106391673A (en) * | 2016-11-30 | 2017-02-15 | 北京神雾环境能源科技集团股份有限公司 | System and method for treating household garbage |
| CN107225142A (en) * | 2016-03-25 | 2017-10-03 | 周鼎力 | A kind of energy-saving rubbish destructive distillation combustion gas and the method for fuel gas generation |
| CN109185887A (en) * | 2018-09-14 | 2019-01-11 | 广西博世科环保科技股份有限公司 | A kind of house refuse coupling desiccation pyrolysis processing technique and processing system |
-
2019
- 2019-01-14 CN CN201910034585.1A patent/CN109899800A/en active Pending
Patent Citations (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH11211042A (en) * | 1998-01-29 | 1999-08-06 | Meidensha Corp | Method and apparatus for treating halogen containing material |
| CN1621743A (en) * | 2003-11-26 | 2005-06-01 | 中国科学院力学研究所 | Plasma multi-stage cracking technology and apparatus capable of processing multiple organic wastes simultaneously |
| WO2006117824A1 (en) * | 2005-05-02 | 2006-11-09 | Pyrolb S.R.L. | Integrated process for waste treatment by pyrolysis and related plant |
| CN104534476A (en) * | 2014-12-29 | 2015-04-22 | 派石新能源技术开发(北京)有限公司 | Destructive distillation method and device for organic solid waste harmless treatment |
| CN205299538U (en) * | 2016-01-19 | 2016-06-08 | 河南华天环保科技有限公司 | Vertical rotatory domestic waste of superelevation multistage burns gasification equipment |
| CN107225142A (en) * | 2016-03-25 | 2017-10-03 | 周鼎力 | A kind of energy-saving rubbish destructive distillation combustion gas and the method for fuel gas generation |
| CN106085511A (en) * | 2016-06-08 | 2016-11-09 | 北京神雾环境能源科技集团股份有限公司 | A kind of rubbish charcoal resource and the method and system of raising pyrolysis gas calorific value |
| CN106287733A (en) * | 2016-08-11 | 2017-01-04 | 赛能杰高新技术股份有限公司 | One way of life waste disposal method |
| CN106391673A (en) * | 2016-11-30 | 2017-02-15 | 北京神雾环境能源科技集团股份有限公司 | System and method for treating household garbage |
| CN109185887A (en) * | 2018-09-14 | 2019-01-11 | 广西博世科环保科技股份有限公司 | A kind of house refuse coupling desiccation pyrolysis processing technique and processing system |
Cited By (17)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109609189A (en) * | 2018-12-14 | 2019-04-12 | 西安交通大学 | A waste gasifier and a waste gasification method based thereon |
| CN110529859A (en) * | 2019-09-16 | 2019-12-03 | 徐飞 | A kind of solid waste material treating device |
| CN112300817A (en) * | 2019-12-05 | 2021-02-02 | 上海敏建环保科技有限公司 | Pyrolysis gasification method for household garbage |
| CN111019711B (en) * | 2019-12-16 | 2021-09-14 | 武汉科技大学 | Thermal cracking gasification process for household garbage |
| CN111019711A (en) * | 2019-12-16 | 2020-04-17 | 武汉科技大学 | Thermal cracking gasification process for household garbage |
| CN111139096A (en) * | 2020-01-08 | 2020-05-12 | 润电能源科学技术有限公司 | Household garbage treatment system and household garbage treatment method thereof |
| CN112268279A (en) * | 2020-10-15 | 2021-01-26 | 深圳市捷晶能源科技有限公司 | An intelligent thermal cracking treatment method and system for slag solid waste |
| CN112619562A (en) * | 2020-11-27 | 2021-04-09 | 深圳市捷晶能源科技有限公司 | Thermal cracking system and thermal cracking method |
| CN112619561A (en) * | 2020-11-27 | 2021-04-09 | 深圳市捷晶能源科技有限公司 | Heavy metal-containing material treatment system and treatment method thereof |
| CN112619562B (en) * | 2020-11-27 | 2021-10-29 | 深圳市捷晶能源科技有限公司 | Thermal cracking system and thermal cracking method |
| CN112728548A (en) * | 2020-12-22 | 2021-04-30 | 华中科技大学 | Gradient temperature-changing type equipment and method for removing tar by garbage heat |
| CN113087337A (en) * | 2021-04-06 | 2021-07-09 | 深圳市捷晶能源科技有限公司 | Sludge treatment system |
| CN113087337B (en) * | 2021-04-06 | 2022-03-08 | 深圳市捷晶能源科技有限公司 | Sludge treatment system |
| CN113280348A (en) * | 2021-05-27 | 2021-08-20 | 巴彦淖尔市汇利锅炉制造有限责任公司 | Multifunctional garbage incinerator |
| CN113531538A (en) * | 2021-06-08 | 2021-10-22 | 湖南省欣洁环保科技有限公司 | Household garbage treatment method and system |
| CN118960382A (en) * | 2024-09-18 | 2024-11-15 | 阜新成泰环保科技有限公司 | A method and device for supplying air to a reaction zone in a rotary kiln through the kiln wall |
| CN118960382B (en) * | 2024-09-18 | 2025-12-09 | 阜新成泰环保科技有限公司 | Method and device for supplying air to reaction zone in kiln through kiln wall of rotary kiln |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN109899800A (en) | Based on the compound thermal cracking gasification treatment process of house refuse and system | |
| US20170218274A1 (en) | Waste Incinerator | |
| US20200002630A1 (en) | Pyrolysis processing of solid waste from a water treatment plant | |
| CN104028547B (en) | Municipal solid waste extreme decrement and highly resourceful treatment process and municipal solid waste extreme decrement and highly resourceful treatment device | |
| CN102322630A (en) | The macromolecular substances high-efficiency cleaning uses method and device | |
| CN103666505A (en) | Equipment for reducing and transforming household garbage or organic waste into energy resources | |
| CN107513389B (en) | Carbonizing device capable of treating garbage | |
| CN103045273A (en) | Method and equipment for preparing fuel from household garbage for suppressing dioxin | |
| CN102329656B (en) | Downdraft biomass gasification reaction chamber and gasification process thereof | |
| CN102746903A (en) | Large-scale domestic garbage dry distillation and gasification furnace without exhaust gas or dioxin emission | |
| CN106734080A (en) | The system and method for processing solid waste | |
| CN108315056A (en) | From tar removing formula biomass gasification reaction system and method | |
| CN201072128Y (en) | Biomass gasification electric generating apparatus of gas control type thermal decomposition system | |
| CN102329654B (en) | Biomass gasification device and process | |
| CN101962558B (en) | Biomass combustible gas high-temperature oxygen-free reinforced dry-distillation pyrolysis plant | |
| CN101191059B (en) | Dynamics gasification furnace and exhaust heat boiler composed by the same | |
| CN113000557A (en) | Brown gas pyrolysis hazardous solid waste treatment technology system and application method thereof | |
| EP1222428A1 (en) | Process and system for recovering energy from carbon-containing materials | |
| CN206405159U (en) | The system for handling solid waste | |
| CN105505474B (en) | Combined pyrolytic gasification furnace | |
| CN101974351A (en) | Scale fixed bed biomass gasification power generation production technology and complete equipment | |
| CN110358586A (en) | One kind returning to formula organic waste pyrolysis system and its refuse pyrolysis technique | |
| CN214937226U (en) | System for handle organic solid useless | |
| CN212362032U (en) | Garbage pyrolysis gasification coupling blast furnace slag treatment system | |
| CZ295171B6 (en) | Three-zone gasifier having a bypass and intended for gasification of biomass of vegetable origin |
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 | ||
| RJ01 | Rejection of invention patent application after publication | ||
| RJ01 | Rejection of invention patent application after publication |
Application publication date: 20190618 |