CN105728439B - The system and method for handling organic waste - Google Patents
The system and method for handling organic waste Download PDFInfo
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- CN105728439B CN105728439B CN201610211589.9A CN201610211589A CN105728439B CN 105728439 B CN105728439 B CN 105728439B CN 201610211589 A CN201610211589 A CN 201610211589A CN 105728439 B CN105728439 B CN 105728439B
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- oil gas
- organic waste
- heat exchange
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- pyrolysis
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- 239000010815 organic waste Substances 0.000 title claims abstract description 181
- 238000000034 method Methods 0.000 title claims abstract description 58
- 238000000197 pyrolysis Methods 0.000 claims abstract description 141
- 239000002296 pyrolytic carbon Substances 0.000 claims abstract description 78
- 238000006243 chemical reaction Methods 0.000 claims abstract description 40
- 238000007233 catalytic pyrolysis Methods 0.000 claims abstract description 35
- 239000000779 smoke Substances 0.000 claims abstract description 23
- 230000005855 radiation Effects 0.000 claims abstract description 13
- 239000007789 gas Substances 0.000 claims description 280
- 238000012545 processing Methods 0.000 claims description 59
- 238000001035 drying Methods 0.000 claims description 43
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims description 42
- 239000003546 flue gas Substances 0.000 claims description 42
- 239000003054 catalyst Substances 0.000 claims description 40
- 239000010813 municipal solid waste Substances 0.000 claims description 38
- 238000007599 discharging Methods 0.000 claims description 23
- 238000010791 quenching Methods 0.000 claims description 19
- 230000000171 quenching effect Effects 0.000 claims description 19
- 239000000446 fuel Substances 0.000 claims description 18
- 238000006555 catalytic reaction Methods 0.000 claims description 14
- 239000000571 coke Substances 0.000 claims description 14
- 238000001816 cooling Methods 0.000 claims description 8
- 230000008859 change Effects 0.000 claims description 7
- 239000004744 fabric Substances 0.000 claims description 7
- 239000003610 charcoal Substances 0.000 claims description 4
- 238000003756 stirring Methods 0.000 claims description 4
- 230000008676 import Effects 0.000 claims description 3
- 239000002245 particle Substances 0.000 abstract description 7
- 238000012546 transfer Methods 0.000 abstract description 7
- 239000003208 petroleum Substances 0.000 abstract description 3
- 230000008569 process Effects 0.000 description 25
- 239000010410 layer Substances 0.000 description 23
- 238000005265 energy consumption Methods 0.000 description 12
- 239000000463 material Substances 0.000 description 12
- 239000000567 combustion gas Substances 0.000 description 10
- 238000009825 accumulation Methods 0.000 description 8
- 239000002918 waste heat Substances 0.000 description 8
- 238000004939 coking Methods 0.000 description 6
- 238000010586 diagram Methods 0.000 description 6
- 238000005516 engineering process Methods 0.000 description 6
- 238000005979 thermal decomposition reaction Methods 0.000 description 6
- 230000033228 biological regulation Effects 0.000 description 5
- 230000008901 benefit Effects 0.000 description 4
- 238000002485 combustion reaction Methods 0.000 description 4
- 230000000694 effects Effects 0.000 description 4
- 238000004519 manufacturing process Methods 0.000 description 4
- 230000004044 response Effects 0.000 description 4
- HGUFODBRKLSHSI-UHFFFAOYSA-N 2,3,7,8-tetrachloro-dibenzo-p-dioxin Chemical compound O1C2=CC(Cl)=C(Cl)C=C2OC2=C1C=C(Cl)C(Cl)=C2 HGUFODBRKLSHSI-UHFFFAOYSA-N 0.000 description 3
- 230000000903 blocking effect Effects 0.000 description 3
- 239000002361 compost Substances 0.000 description 3
- 238000010438 heat treatment Methods 0.000 description 3
- 239000000203 mixture Substances 0.000 description 3
- BWHMMNNQKKPAPP-UHFFFAOYSA-L potassium carbonate Substances [K+].[K+].[O-]C([O-])=O BWHMMNNQKKPAPP-UHFFFAOYSA-L 0.000 description 3
- 239000004215 Carbon black (E152) Substances 0.000 description 2
- 239000000969 carrier Substances 0.000 description 2
- 239000003795 chemical substances by application Substances 0.000 description 2
- 235000019504 cigarettes Nutrition 0.000 description 2
- 238000005336 cracking Methods 0.000 description 2
- 238000009826 distribution Methods 0.000 description 2
- 239000000428 dust Substances 0.000 description 2
- 238000005338 heat storage Methods 0.000 description 2
- 229930195733 hydrocarbon Natural products 0.000 description 2
- 150000002430 hydrocarbons Chemical class 0.000 description 2
- 238000009434 installation Methods 0.000 description 2
- 230000003993 interaction Effects 0.000 description 2
- 229910000027 potassium carbonate Inorganic materials 0.000 description 2
- 239000000843 powder Substances 0.000 description 2
- 238000010926 purge Methods 0.000 description 2
- 238000000746 purification Methods 0.000 description 2
- 238000004064 recycling Methods 0.000 description 2
- 238000000926 separation method Methods 0.000 description 2
- CDBYLPFSWZWCQE-UHFFFAOYSA-L sodium carbonate Substances [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 description 2
- 229910000029 sodium carbonate Inorganic materials 0.000 description 2
- 239000002689 soil Substances 0.000 description 2
- 239000007787 solid Substances 0.000 description 2
- 238000003860 storage Methods 0.000 description 2
- 241001391944 Commicarpus scandens Species 0.000 description 1
- 241000196324 Embryophyta Species 0.000 description 1
- 230000003416 augmentation Effects 0.000 description 1
- 238000007664 blowing Methods 0.000 description 1
- 230000003197 catalytic effect Effects 0.000 description 1
- 230000007423 decrease Effects 0.000 description 1
- 230000000994 depressogenic effect Effects 0.000 description 1
- 238000011161 development Methods 0.000 description 1
- 230000005802 health problem Effects 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 239000011229 interlayer Substances 0.000 description 1
- 238000011068 loading method Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000001172 regenerating effect Effects 0.000 description 1
- 239000007921 spray Substances 0.000 description 1
- 238000005507 spraying Methods 0.000 description 1
- 238000010025 steaming Methods 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 230000001988 toxicity Effects 0.000 description 1
- 231100000419 toxicity Toxicity 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 1
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B09—DISPOSAL OF SOLID WASTE; RECLAMATION OF CONTAMINATED SOIL
- B09B—DISPOSAL OF SOLID WASTE
- B09B3/00—Destroying solid waste or transforming solid waste into something useful or harmless
- B09B3/40—Destroying solid waste or transforming solid waste into something useful or harmless involving thermal treatment, e.g. evaporation
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B09—DISPOSAL OF SOLID WASTE; RECLAMATION OF CONTAMINATED SOIL
- B09B—DISPOSAL OF SOLID WASTE
- B09B5/00—Operations not covered by a single other subclass or by a single other group in this subclass
Landscapes
- Engineering & Computer Science (AREA)
- Environmental & Geological Engineering (AREA)
- Physics & Mathematics (AREA)
- Thermal Sciences (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
- Separation, Recovery Or Treatment Of Waste Materials Containing Plastics (AREA)
Abstract
The invention discloses a kind of system and method for handling organic waste, the system includes：Catalytic pyrolysis reaction device, first-class heat exchanger and secondary heat exchanger, wherein, pyrolytic carbon outlet on catalytic pyrolysis reaction device is connected with the pyrolytic carbon entrance in first-class heat exchanger, the exhanst gas outlet of radiant tube is connected with the smoke inlet in first-class heat exchanger in catalytic pyrolysis reaction device, pyrolysis oil gas vent on catalytic pyrolysis reaction device is connected with the pyrolysis oil gas entrance on secondary heat exchanger, and the one-level heat exchange smoke inlet on secondary heat exchanger is connected with the one-level heat exchange exhanst gas outlet in first-class heat exchanger.The system can realize the efficiently and directionally pyrolysis of organic waste, and petroleum resources caused by pyrolysis can be exported rapidly, it is high to be pyrolyzed oil quality, light components content is high in pyrolysis oil, other reactor is using radiant tube and along the short transverse multi-tier arrangement of reactor, add and conducted heat between particular radiation pipe between particle, heat transfer efficiency is high.
Description
Technical field
The invention belongs to chemical technology field, and specifically, the present invention relates to a kind of system for handling organic waste and side
Method.
Background technology
With rapid economic development, the continuous quickening of urbanization process, the continuous improvement of living standards of the people, all come therewith
House refuse problem be also on the rise.According to relevant report, China's daily output quantity of refuse is about 4,000,000 tons, wherein more than seventy percent
It is organic waste.Garbage disposal problem will turn into the sixty-four dollar question that will face of China and urgent problem to be solved it
One.
At present, the processing mode of domestic organic garbage is mainly with burning, compost, landfill, recycling etc..Wherein, rubbish
Burning can produce violent in toxicity dioxin, while dioxin removal cost is high, and burning method not only causes certain environment and health
Problem, also result in certain economic loss；Garbage compost is primarily adapted for use in kitchen garbage, because China's rubbish is not classified,
Garbage compost processing time is longer simultaneously, can only alleviate garbage problem；Garbage loading embeading can change soil property, produce underground heat, enter
And cause soil can not growing plant；The refuse classification in China is in elementary step, the unexecuted refuse classification of most area.
Organic waste contains substantial amounts of petroleum resources, and it, which is extracted, can produce huge economic benefit while solve
Refuse pollution problem.It is organic waste recycling, innoxious, the maximally effective side of minimizing that domestic organic garbage is carried out into pyrolysis
Formula, while also produced without dioxin.
At present, on the market the problem of refuse pyrolysis treatment device generally existing treating capacity is relatively low, high energy consumption.Therefore, mesh
Preceding existing organic garbage treatment technology is further improved.
The content of the invention
It is contemplated that at least solves one of technical problem in correlation technique to a certain extent.Therefore, the present invention
One purpose is to propose a kind of system and method for handling organic waste, and the system can realize the High Efficiency Thermal of organic waste
Solution, and petroleum resources caused by pyrolysis can be exported rapidly, pyrolysis oil quality is high, and light components content is high in pyrolysis oil,
Other reactor is added and passed between particular radiation pipe between particle using radiant tube and along the short transverse multi-tier arrangement of reactor
Heat, heat transfer efficiency are high.
In one aspect of the invention, the present invention proposes a kind of system for handling organic waste, according to the reality of the present invention
Example is applied, the system includes：
Catalytic pyrolysis reaction device, first-class heat exchanger and secondary heat exchanger,
Wherein, the catalytic pyrolysis reaction device includes：
Organic waste entrance, steam inlet, pyrolysis oil gas vent, pyrolytic carbon outlet；
The organic waste entrance is located at the top center of the reactor；
The pyrolysis oil gas vent is located in the side wall of the reactor；
The steam inlet is located on the pyrolysis oil gas vent, and the steam inlet and the pyrolysis oil gas vent
Connection；
The pyrolytic carbon outlet is positioned at the bottom of the reactor；
Catalyst transport, the catalyst transport stretch to the inside reactor by the side wall of the reactor,
The port of export of the catalyst transport is provided with blast cap, and the port of export of the catalyst transport is located at the organic waste and entered
The underface of mouth, and the blast cap is relative with the organic waste entrance；
Radiant tube, the radiant tube is in short transverse multi-tier arrangement of the inside of the reactor along the reactor, often
Layer has more radiant tubes parallel to each other in the horizontal direction；
Discharge, the discharge are arranged in the reactor and are connected with the pyrolysis oil gas vent；
Oil gas exports pipeline, and the oil gas export pipeline is communicated to the discharge, and the oil gas exports pipeline
Through hole is provided with tube wall；
Agitating device, the agitating device includes agitating shaft and the multiple puddlers being connected on the agitating shaft, described
Agitating shaft extend into the inside of the reactor by pyrolytic carbon outlet and be configured to can be in the reactor internal rotation；
The first-class heat exchanger has pyrolytic carbon outlet and one-level heat exchange flue gas after smoke inlet, pyrolytic carbon entrance, heat exchange
Outlet, the smoke inlet are connected with the exhanst gas outlet on the radiant tube, and the pyrolytic carbon entrance exports with the pyrolytic carbon
It is connected；
The secondary heat exchanger has pyrolysis oil gas entrance, one-level heat exchange smoke inlet, one-level heat exchange oil gas vent and two
Level heat exchange exhanst gas outlet, the pyrolysis oil gas entrance are connected with the pyrolysis oil gas vent, one-level heat exchange smoke inlet and
The one-level heat exchange exhanst gas outlet is connected.
Thus, the system of processing organic waste according to embodiments of the present invention uses the side that cloth gas is combined with catalyst
Formula, it is the high-efficiency thermal decomposition that organic waste can be achieved without the mixed processes of catalyst and organic waste, secondly by every spoke
Penetrate pipe lower end and be respectively provided with two quick delivery lines of oil gas, reduce residence time of the pyrolysis oil in burner hearth, reduce secondary response
Occur, and blow and rotate coke removing appts using steam, avoid radiant tube upper end coking phenomenon and oil gas blocks, and then improve
Pyrolysis efficiency and pyrolysis oily yield, using tar light oil content in the pyrolysis oil of the system production more than 60%, in addition, should
Without complicated machinery in system, inside reactor each point temperature is flexibly adjustable, has the characteristics that technological process is simple, is easy to extensive
Industrialized production.
In addition, the system of processing organic waste according to the above embodiment of the present invention can also have technology additional as follows
Feature：
In some embodiments of the invention, short transverse laminates of the oil gas export pipeline along the reactor
Put, every layer has more oil gas export pipelines parallel to each other in the horizontal direction.Thus, it is possible to further improve in reactor
Oil gas export efficiency.
In some embodiments of the invention, the oil gas export pipeline is arranged in parallel with the radiant tube, and the spoke
Penetrate the respective left and right sides of pipe and be symmetrically arranged with two oil gas export pipelines.Thus, it is possible to further improve the oil in reactor
Conductance goes out efficiency.
In some embodiments of the invention, the spacing of the oil gas export pipeline and the tube wall of the neighbouring radiant tube
From export pipe diameter d for the oil gas 1/2-3 times.
In some embodiments of the invention, multiple through holes are provided with the tube wall of the oil gas export pipeline.Thus, may be used
Further to improve the export efficiency of the oil gas in reactor.
In some embodiments of the invention, the through hole uniformly divides on the length direction of oil gas export pipeline
Cloth.
In some embodiments of the invention, baffle plate, the baffle plate are respectively arranged with the both sides tube wall of the radiant tube
Positioned at the top of oil gas export pipeline, and cover whole vertical projections of the oil gas export pipeline.Thus, not only can be with
Effectively prevent oil gas from quickly exporting the blocking of pipeline, and the material scattering of whereabouts can be pyrolyzed efficiency so as to improve material.
In some embodiments of the invention, the baffle plate is from the phase tangent line of the vertical section of the tube wall of the radiant tube
Starting point, the vertical section of the oil gas export pipeline is extended downward at an angle.
In some embodiments of the invention, 40-90 degree is the angle ranging from, without 90 degree.
In some embodiments of the invention, oil gas export pipeline is communicated to discharge described in same root described in same layer.
In some embodiments of the invention, there are one or more puddler, and puddler in the top of every layer of radiant tube
Vertical range with radiant tube is 20~300mm.Thereby, it is possible to augmentation of heat transfer effect.Pyrolytic tar is for example, puddler can be situated between
Between radiation tube layer and oil gas export pipe layers.
In some embodiments of the invention, the puddler is perpendicular to the agitating shaft, and along the agitating shaft
Length direction is spaced apart.
In some embodiments of the invention, adjacent projections of the puddler on the same cross section of the agitating shaft
At an angle.
In some embodiments of the present invention, the port of export of the catalyst transport is located under the organic waste entrance
Side, the distance of the blast cap and the organic waste entrance is 200~500mm.Thus it is easy to break up organic waste, improves catalysis
Agent and the reaction efficiency of organic waste.
In some embodiments of the present invention, the blast cap is cowl, and has multiple through holes on blast cap.Thus it is easy to
The wind of different directions is formed, helps breaing up for organic waste.
In some embodiments of the invention, the system of the processing organic waste further comprises：One-level turns round kiln drying
There is organic waste import, secondary heat exchange smoke inlet and one-level to dry organic waste for dry device, the one-level rotary kiln
Outlet, the secondary heat exchange smoke inlet are connected with the secondary heat exchange exhanst gas outlet；Two-stage rotary kiln drier, the two level
Rotary kiln have one-level heat exchange oil gas entrance, one-level dry organic waste entrance, the outlet of secondary drying organic waste and
Secondary heat exchange oil gas vent, the one-level heat exchange oil gas entrance are connected with one-level heat exchange oil gas vent, and the one-level is dried
Organic waste entrance is dried organic waste outlet with the one-level and is connected；Feed bin, the feed bin have charging aperture and discharging opening, institute
Charging aperture is stated with secondary drying organic waste outlet to be connected；Feed auger, the feed auger are fed with the first spiral
Mouth and the first spiral discharging mouth, first screw feed en-trance are connected with the discharging opening, the first spiral discharging mouth and institute
Organic waste entrance is stated to be connected；Discharge spiral, and the discharging spiral has the second screw feed en-trance and the second spiral discharging mouth, institute
State the second screw feed en-trance with pyrolytic carbon outlet to be connected, the second spiral discharging mouth is connected with the pyrolytic carbon entrance.
Thus, by the way that the waste heat for being catalyzed flue gas, pyrolysis oil gas and pyrolytic carbon caused by pyrolysis to be used to organic waste be dried place
Reason, can not only significantly improve the utilization rate of energy consumption, and can significantly improve the pyrolysis efficiency of organic waste.
In some embodiments of the invention, the system of the processing organic waste further comprises：Purifier, it is described
There is purifier oil gas entrance, pyrolysis oil export and clean gas outlet, the oil gas entrance to go out with the secondary heat exchange oil gas
Mouth is connected, and the clean gas outlet is connected with the fuel inlet on the radiant tube；Steam generator, the steam generating appliances
Have purified gas entrance and steam (vapor) outlet, the purified gas entrance is connected with the clean gas outlet, the steam (vapor) outlet with it is described
Steam inlet is connected.Thus, by will isolated pyrolysis oil and net again after pyrolysis oil gas is exchanged heat caused by catalysis pyrolysis
Change gas, and used the purified gas as the fuel of radiant tube and steam generator, fuel cost can be significantly reduced.
In some embodiments of the invention, the system of the processing organic waste further comprises：Coke quenching device, it is described
Coke quenching device has pyrolytic carbon entrance and the outlet of cooling pyrolytic carbon after heat exchange, after the heat exchange after pyrolytic carbon entrance and the heat exchange
Pyrolytic carbon outlet is connected.
In another aspect of the invention, the present invention proposes a kind of method for handling organic waste.According to the present invention's
Embodiment, this method are carried out using the system of above-mentioned processing organic waste.According to a particular embodiment of the invention, the party
Method includes：
(1) organic waste and catalyst are respectively fed to carry out catalysis pyrolysis in the catalytic pyrolysis reaction device, so as to
Obtain being pyrolyzed oil gas and pyrolytic carbon；
(2) flue gas caused by the pyrolytic carbon and the radiant tube is supplied into the first-class heat exchanger into progress one-level to change
Heat treatment, so that pyrolytic carbon after exchange heat and one-level exchange heat flue gas；
(3) the pyrolysis oil gas and one-level heat exchange flue gas are supplied and secondary heat exchange is carried out into the secondary heat exchanger
Processing, to obtain one-level heat exchange oil gas and secondary heat exchange flue gas.
Thus, the method for processing organic waste according to embodiments of the present invention uses the side that cloth gas is combined with catalyst
Formula, it is the high-efficiency thermal decomposition that organic waste can be achieved without the mixed processes of catalyst and organic waste, secondly by every spoke
Penetrate pipe lower end and be respectively provided with two quick delivery lines of oil gas, reduce residence time of the pyrolysis oil in burner hearth, reduce secondary response
Occur, and blow and rotate coke removing appts using steam, avoid radiant tube upper end coking phenomenon and oil gas blocks, and then improve
Pyrolysis efficiency and pyrolysis oily yield, using tar light oil content in the pyrolysis oil of the system production more than 60%, in addition, should
Without complicated machinery in system, inside reactor each point temperature is flexibly adjustable, has the characteristics that technological process is simple, is easy to extensive
Industrialized production.
In addition, the method for processing organic waste according to the above embodiment of the present invention can also have technology additional as follows
Feature：
In some embodiments of the invention, the method for the processing organic waste further comprises：(4) have by described
Before machine rubbish and catalyst are respectively fed to carry out catalysis pyrolysis in the catalytic pyrolysis reaction device, the two level is changed in advance
Heat smoke and the organic waste are supplied into the one-level rotary kiln to be carried out at one-level drying to the organic waste
Reason, organic waste is dried to obtain one-level；(5) by the one-level exchange heat oil gas and the one-level dry organic waste supply to
Secondary drying processing is carried out in the two-stage rotary kiln drier, to obtain secondary drying rubbish and secondary heat exchange oil gas；(6)
The secondary drying organic waste is supplied into the feed bin and stored, and by described in secondary drying organic waste warp
Feed auger is supplied into the catalytic pyrolysis reaction device.Thus, by the way that flue gas caused by pyrolysis, pyrolysis oil gas and heat will be catalyzed
The waste heat of solution charcoal is used to organic waste be dried processing, can not only significantly improve the utilization rate of energy consumption, and can show
Write the pyrolysis efficiency for improving organic waste.
In some embodiments of the invention, the method for the processing organic waste further comprises：(7) by the two level
Heat exchange oil gas supplies purified treatment is carried out into the purifier, to obtain pyrolysis oil and purified gas, and by the purification
Part supply to the radiant tube of gas uses as fuel；(8) another part of the purified gas is supplied to the steaming
Burning produces steam in vapour generator, and the steam is supplied into the discharge through the steam inlet.Thus, pass through
Catalysis is pyrolyzed isolated pyrolysis oil and purified gas, and the purified gas is made respectively again after caused pyrolysis oil gas is exchanged heat
Used for the fuel of radiant tube and steam generator, fuel cost can be significantly reduced.
In some embodiments of the invention, the method for the processing organic waste further comprises：(9) by the heat exchange
Pyrolytic carbon, which is supplied into the coke quenching device, afterwards carries out quenching processing, to obtain cooling down pyrolytic carbon.
The additional aspect and advantage of the present invention will be set forth in part in the description, and will partly become from the following description
Obtain substantially, or recognized by the practice of the present invention.
Brief description of the drawings
Fig. 1 is the system structure diagram of processing organic waste according to an embodiment of the invention；
Fig. 2 is oil gas export pipeline and radiant tube in the system of processing organic waste according to an embodiment of the invention
Front view；
Fig. 3 is the top view of the agitating device in the system of processing organic waste according to an embodiment of the invention；
Fig. 4 is the system structure diagram according to the processing organic waste of further embodiment of the present invention；
Fig. 5 is the system structure diagram according to the processing organic waste of another embodiment of the invention；
Fig. 6 is the method flow schematic diagram of processing organic waste according to an embodiment of the invention；
Fig. 7 is the method flow schematic diagram according to the processing organic waste of further embodiment of the present invention；
Fig. 8 is the method flow schematic diagram according to the processing organic waste of another embodiment of the invention.
Embodiment
Embodiments of the invention are described below in detail, the example of the embodiment is shown in the drawings, wherein from beginning to end
Same or similar label represents same or similar element or the element with same or like function.Below with reference to attached
The embodiment of figure description is exemplary, it is intended to for explaining the present invention, and is not considered as limiting the invention.
In the description of the invention, it is to be understood that term " " center ", " longitudinal direction ", " transverse direction ", " length ", " width ",
" thickness ", " on ", " under ", "front", "rear", "left", "right", " vertical ", " level ", " top ", " bottom ", " interior ", " outer ", " up time
The orientation or position relationship of the instruction such as pin ", " counterclockwise ", " axial direction ", " radial direction ", " circumference " be based on orientation shown in the drawings or
Position relationship, it is for only for ease of and describes the present invention and simplify description, rather than indicates or imply that signified device or element must
There must be specific orientation, with specific azimuth configuration and operation, therefore be not considered as limiting the invention.
In addition, term " first ", " second " are only used for describing purpose, and it is not intended that instruction or hint relative importance
Or the implicit quantity for indicating indicated technical characteristic.Thus, define " first ", the feature of " second " can be expressed or
Implicitly include at least one this feature.In the description of the invention, " multiple " are meant that at least two, such as two, three
It is individual etc., unless otherwise specifically defined.
In the present invention, unless otherwise clearly defined and limited, term " installation ", " connected ", " connection ", " fixation " etc.
Term should be interpreted broadly, for example, it may be fixedly connected or be detachably connected, or integrally；Can be that machinery connects
Connect or electrically connect；Can be joined directly together, can also be indirectly connected by intermediary, can be in two elements
The connection in portion or the interaction relationship of two elements, limited unless otherwise clear and definite.For one of ordinary skill in the art
For, the concrete meaning of above-mentioned term in the present invention can be understood as the case may be.
In the present invention, unless otherwise clearly defined and limited, fisrt feature can be with "above" or "below" second feature
It is that the first and second features directly contact, or the first and second features pass through intermediary mediate contact.Moreover, fisrt feature exists
Second feature " on ", " top " and " above " but fisrt feature are directly over second feature or oblique upper, or be merely representative of
Fisrt feature level height is higher than second feature.Fisrt feature second feature " under ", " lower section " and " below " can be
One feature is immediately below second feature or obliquely downward, or is merely representative of fisrt feature level height and is less than second feature.
In one aspect of the invention, the present invention proposes a kind of system for handling organic waste.Below with reference to Fig. 1 to this
The system of the lower processing rubbish of inventive embodiments is described in detail.According to an embodiment of the invention, the system includes：Catalytic thermal
Solve reactor 100, first-class heat exchanger 200 and secondary heat exchanger 300.
According to an embodiment of the invention, catalytic pyrolysis reaction device 100 include organic garbage inlet 101, steam inlet 102,
It is pyrolyzed oil gas vent 103, pyrolytic carbon outlet 104, catalyst transport 11, radiant tube 12, discharge 13, oil gas export pipeline 14
With agitating device 15.
According to an embodiment of the invention, organic waste entrance 101 is located at the top center of reactor 100, and is suitable to
Organic waste is supplied into catalytic pyrolysis reaction device.
According to an embodiment of the invention, the particle diameter of organic waste is not particularly restricted, and those skilled in the art can root
Selected according to being actually needed, according to a particular embodiment of the invention, the particle diameter of organic waste can be 0.1mm~10mm.By
This, can significantly improve the pyrolysis efficiency of organic waste.
According to an embodiment of the invention, pyrolysis oil gas vent 103 is located in the side wall of reactor 100, and suitable for that will be pyrolyzed
Pyrolysis oil conductance goes out reactor caused by process, and according to a particular embodiment of the invention, pyrolysis oil gas vent 103 can be more
It is individual, and multiple pyrolysis oil gas vents 103 are distributed in the side wall of reactor.
According to an embodiment of the invention, steam inlet 102 be located at pyrolysis oil gas vent 103 on, and steam inlet 102 with
Pyrolysis oil gas vent 103 connects, and supplies steam suitable for being exported to oil gas in pipeline 14, so as to effectively avoid oil gas from exporting
The blocking of pipeline, according to a particular embodiment of the invention, steam inlet 102 can be multiple, and one is pyrolyzed oil gas vent
On can be correspondingly arranged on a steam inlet.
According to an embodiment of the invention, pyrolytic carbon outlet 104 is arranged on the bottom of reactor 100, and suitable for pyrolysis is given birth to
Into pyrolytic carbon discharge reactor.
According to an embodiment of the invention, catalyst transport 11 stretches to inside reactor by the side wall of reactor, catalysis
The port of export of agent delivery pipe is provided with blast cap 16, and the port of export of catalyst transport is located at the underface of organic waste entrance 101,
So that blast cap 16 is relative with the organic waste entrance 101 of reactor.Thus, added by the catalyst transport into reactor
Catalyst is advantageously implemented catalyst and mixed with the uniform of material.Specifically, catalyst can be selected from CaO, MgO, Na2CO3With
K2CO3At least one of.
According to a particular embodiment of the invention, the blast cap 16 of the port of export of catalyst transport 11 is located at organic waste entrance
101 underface, and the hole of blast cap 16 is upward.It is possible thereby to the organic waste of whereabouts is broken up, so that organic rubbish
Rubbish is uniformly pyrolyzed, in addition, inventor also found that catalyst is not only well mixed with organic waste and can also had by the way of spraying into
Effect breaks up material, makes its even drop down.Preferably, the distance of blast cap 16 and organic waste entrance 101 is 200~500mm.Thus
Pyrolysis efficiency can be further improved, and then improves pyrolysis oily yield.
According to a particular embodiment of the invention, blast cap 16 can be cowl, and have multiple through holes on blast cap 16.By
This can form the wind of different directions, help breaing up for organic waste, be advantageous to improve pyrolysis oily yield.
According to an embodiment of the invention, radiant tube 12 is in short transverse laminates of the inside of reactor along reactor
Put, every layer has more radiant tubes parallel to each other in the horizontal direction, according to a particular embodiment of the invention, in the horizontal direction
Upper radiant tube parallel to each other is uniformly distributed, it is preferable that the radiant tube arranged along the short transverse of reactor it is parallel to each other and
It is staggeredly arranged.According to the specific example of the present invention, the caliber of radiant tube can be 100~300mm.According to the implementation of the present invention
Example, the horizontal range between adjacent radiation pipe outer wall be 200~500mm, the vertical distance between adjacent radiation pipe outer wall is 200~
700mm.It is to be understood that the horizontal range between adjacent radiation pipe outer wall can be understood as on same layer between radiation pipe outer wall
Distance, and the vertical distance between adjacent radiation pipe outer wall can be understood as above and below adjacent between the adjacent radiation pipe outer wall of two interlayers
Distance.
According to an embodiment of the invention, the number of plies of multilayer radiant tube can be 10-25 layers.Inventor's discovery, this kind of structure
Arrangement can make it that reactor temperature field distribution is uniform, so as to significantly improve the pyrolysis efficiency of organic waste.
According to an embodiment of the invention, radiant tube can be unidirectional regenerative gas heat accumulation type radiant tube, that is, pass through accumulation of heat
Heat caused by combustion gas is carried out heat supply by formula radiant tube body in a manner of radiating.According to a particular embodiment of the invention,
Gas control valve (not shown) can be provided with heat accumulation type radiant tube.It is thus, it is possible to logical by adjusting gas control valve regulation
The flow for entering the combustion gas of heat accumulation type radiant tube comes etc. to realize the accurate temperature controlling to pyrolytic process, so as to significantly improve organic rubbish
The pyrolysis efficiency of rubbish, and then improve the yield of pyrolysis oil.
Specifically, radiant tube extend into reactor from the side of sidewall of reactor and runs through reactor in the horizontal direction,
Another side wall that pipe stretches into reactor from the side of sidewall of reactor and passes reactor in the horizontal direction is penetrated, and is radiated
Sidewall of reactor is stretched out at the both ends of pipe, wherein, the fuel inlet on radiant tube is located at one end that reactor is stretched out on radiant tube,
Exhanst gas outlet on radiant tube is located at the other end that reactor is stretched out on radiant tube, or fuel inlet and flue gas on radiant tube
The same one end of outlet on radiant tube.Flow of combustion gas of radiant tube etc. is passed through by adjustment to realize to the accurate of pyrolytic process
Temperature control, and radiant tube is using the combustion system periodically to commutate so that and the temperature field of single radiant tube is more or less the same in 30 DEG C, from
And ensure the uniformity of reactor temperature field, such as by adjust be passed through radiant tube combustion gas flow reactor on
The regulation temperature range of the radiant tube in section region is 500~800 DEG C, ensures the abundant pyrolysis of organic waste, is passed through by adjustment
The flow of the combustion gas of radiant tube make it that the regulation temperature range of the radiant tube in hypomere region in reactor is 450~650 DEG C, so as to
The organic waste that further a heating part is not pyrolyzed completely.
According to a particular embodiment of the invention, discharge 13 is arranged in reactor 100 and with being pyrolyzed the phase of oil gas vent 103
Connection.Thus, the export efficiency of pyrolysis oil gas can be significantly improved using discharge, so as to improve pyrolysis oil gas yield.
According to an embodiment of the invention, through hole is provided with the tube wall of oil gas export pipeline 14, according to the specific of the present invention
Embodiment, oil gas export short transverse multi-tier arrangement of the pipeline 14 along reactor, and every layer has more in the horizontal direction each other
Parallel oil gas export pipeline.
According to a particular embodiment of the invention, oil gas export pipeline 14 is arranged in parallel with radiant tube 12, and radiant tube 12
The left and right sides is symmetrically arranged with two oil gas export pipelines 14.Inventor has found, by installing oil gas every radiant tube both sides
Pipeline is exported, oil gas caused by pyrolysis exports pipeline by oil gas and exported rapidly, so as to restrained effectively the secondary of oil gas
Cracking, and then the yield of pyrolysis oil is improved, it is good in economic efficiency.According to the specific example of the present invention, oil gas exports the caliber of pipeline
Can be 30~80mm.
According to a particular embodiment of the invention, as shown in Fig. 2 the tube wall of oil gas export pipeline 14 and neighbouring radiant tube 12
Between distance be that oil gas exports pipe diameter d 1/2-3 times.It is possible thereby to pyrolysis oil caused by exporting at once, avoids pyrolysis oil
Cracking, improve pyrolysis oily yield.
According to a particular embodiment of the invention, multiple through holes are provided with the tube wall of oil gas export pipeline 14, it is preferable that more
Individual through hole is uniformly distributed on the length direction of oil gas export pipeline 14.It is possible thereby to it is easy to be pyrolyzed the quick export of oil gas.
According to an embodiment of the invention, agitating device 15 includes agitating shaft 17 and the multiple stirrings being connected on agitating shaft 17
Bar 18, so as to which agitating shaft 17 drives puddler 18 to rotate under the driving of motor, according to a particular embodiment of the invention, stir
Mix axle 17 and rotatably extend into inside reactor from pyrolytic carbon outlet 104.Invention is found, is stirred by being set in reactor
Device, puddler is during back rotation is carried out, it is possible to prevente effectively from the coking of radiation pipe surface, and then avoid because of radiant tube knot
It is burnt and reduce heat transfer efficiency, so as to strengthen heat-transfer effect.
According to a particular embodiment of the invention, there are one or more puddler, and puddler in the top of every layer of radiant tube
Vertical range with radiant tube is 20~300mm.It is possible thereby to avoid the upper coking of radiant tube, ensure equipment normal operation.Example
Such as, puddler can be between radiation tube layer and oil gas export pipe layers.
According to a particular embodiment of the invention, puddler 18 is perpendicular to agitating shaft 17, and along the length side of agitating shaft 17
To being spaced apart.
According to a particular embodiment of the invention, adjacent projections of the puddler 18 on the same cross section of agitating shaft 17 are in one
Determine angle.For example, as shown in figure 3, the angle, θ can be 0~90 degree (being free of end value), preferably 30~90 degree (are free of 90
Degree).Thus, it is possible to so that puddler effectively loosens inside reactor organic waste, so as to quickly export pyrolysis oil gas.
Specifically, the length of central stirring shaft can be 1-18m, detachable puddler vertical interval can be 0.4-1m, and the number of plies can be
11-26 layers.
According to a particular embodiment of the invention, same layer oil gas export pipeline 14 can be connected by same root discharge 13
To same pyrolysis oil gas vent 103, i.e. same layer oil gas export pipeline 14 and same pyrolysis oil gas vent 103 connects respectively
Same root discharge 13.It is possible thereby to which oil gas is collected, simplify technique and improve pyrolysis oily yield, while can be led in order to oil gas
Go out.
According to a particular embodiment of the invention, adjacent two layers or more layer oil gas export pipeline 14 can by two or
The discharge 13 of more roots is communicated to same pyrolysis oil gas vent 103, the i.e. root of the number of plies of oil gas export pipeline and discharge
Number is identical, and the oil gas export pipeline of same layer is connected by a discharge with same pyrolysis oil gas vent, and more collection
Tracheae is finally collected to same pyrolysis oil gas vent, such as shown in figure 1, the oil gas export pipeline 14 of multilayer passes through a collection
Tracheae 13 is communicated to same pyrolysis oil gas vent 103.
According to an embodiment of the invention, the bottom of reactor can be in back taper.Thus, it is possible to so that pyrogenous origin heat
Solution charcoal smoothly discharges reactor.
According to a particular embodiment of the invention, as shown in Fig. 2 gear can be respectively arranged with the both sides tube wall of radiant tube 12
Plate 19, baffle plate 19 are located at the top of oil gas export pipeline 14, and cover whole vertical projections of oil gas export pipeline 14.By
Baffle plate 19 is set on the both sides tube wall of radiant tube 12, rubbing oil gas delivery line road during material decline, Jin Eryan can be prevented
The life-span in long oil gas delivery line road；And baffle plate 19 can also play the drainage to material, prevent material be stuck in radiant tube with
Between oil gas export pipeline, feed blocking is caused.
According to a particular embodiment of the invention, as shown in Fig. 2 baffle plate 19 is from the vertical section A of the tube wall of radiant tube 12
(A1) phase tangent line is starting point, and α extends downward into the vertical section B (B1) of oil gas export pipeline 14 at an angle, and angle [alpha] is
40-90 degree, without 90 degree.So that the shortest length of baffle plate is can to block oil gas export pipeline.
According to an embodiment of the invention, after first-class heat exchanger 200 has smoke inlet 201, pyrolytic carbon entrance 202, heat exchange
Pyrolytic carbon outlet 203 and one-level heat exchange exhanst gas outlet 204, smoke inlet 201 and the exhanst gas outlet (not shown) phase on radiant tube
Even, pyrolytic carbon entrance 202 is connected with pyrolytic carbon outlet 104, and is suitable to caused pyrolytic carbon and spoke in catalytic pyrolysis reaction device
Penetrate caused flue gas in pipe and carry out one-level heat exchange processing, exchanged heat flue gas so as to pyrolytic carbon after exchange heat and one-level.Thus,
By the way that flue gas caused by caused pyrolytic carbon in catalytic pyrolysis reaction device and radiant tube is exchanged heat, the waste heat of pyrolytic carbon is passed
Flue gas is passed, then the dried medium using the flue gas after heat exchange as subsequent process, so as to realize to the cold of pyrolytic carbon
But the efficient utilization of pyrolytic carbon sensible heat is realized while, and then reduces energy consumption.
According to an embodiment of the invention, secondary heat exchanger 300 has pyrolysis oil gas entrance 301, one-level heat exchange smoke inlet
302nd, one-level heat exchange oil gas vent 303 and secondary heat exchange exhanst gas outlet 304, pyrolysis oil gas entrance 301 and pyrolysis oil gas vent 103
It is connected, one-level heat exchange smoke inlet 302 is connected with one-level heat exchange exhanst gas outlet 204, and one suitable for first-class heat exchanger is obtained
Level heat exchange flue gas carries out heat exchange processing with pyrolysis oil gas caused by catalytic pyrolysis reaction device, so as to obtain one-level heat exchange oil gas
With secondary heat exchange flue gas.Thus, by the way that the waste heat for being pyrolyzed oil gas is passed into one-level heat exchange flue gas, then by gained secondary heat exchange
Flue gas and one-level heat exchange oil gas respectively as subsequent process dried medium, it is possible to achieve pyrolysis oil gas sensible heat efficient utilization,
And then further reduce energy consumption.
The system of processing organic waste according to embodiments of the present invention by the way of cloth gas is combined with catalyst, without
The mixed processes of catalyst and organic waste are the high-efficiency thermal decomposition that organic waste can be achieved, and are by using multigroup radiant tube
Pyrolytic process provides thermal source, can realize the accurate control to pyrolytic process by adjusting the flow for the combustion gas that be passed through radiant tube
Temperature, and radiant tube ensure that the uniformity in temperature field, so as to significantly improve the heat of organic waste by heat storage type combustion
Efficiency is solved, and then improves the yield of pyrolysis oil, while more traditional use gas heat carrier or solid thermal carriers hot as pyrolysis
The pyrolytic reaction device in source is compared, and catalytic pyrolysis reaction device of the invention need not set preheating unit and carrier separative element,
So as to greatly simplify pyrolytic reaction technological process, and then significantly reduce dust content in the fault rate of device and gained pyrolysis oil
It is relatively low, and exhaust gas temperature is low, and secondly the present invention can be produced pyrolysis by arranging that oil gas exports pipeline in the bottom of radiant tube
Raw oil gas exports rapidly, so as to restrained effectively the second pyrolysis of oil gas, and then improves the yield of pyrolysis oil, and be pyrolyzed
Gas is not diluted by gas heat carrier, and pyrolysis gas calorific value is high, good in economic efficiency, sets agitating device to match somebody with somebody again by reactor
Radiant tube is closed, puddler is during back rotation is carried out so that the organic waste of accumulation is loosened, and increases the organic rubbish of accumulation
Voidage between rubbish, reduce the pressure drop that pyrolysis oil gas passes through organic waste layer so that caused pyrolysis oil gas can pass rapidly through
Organic waste layer reaches oil gas delivery line, and caused pyrolysis oil gas can be exported by oil gas delivery line in time, and can be avoided
The coking of radiant tube upper end, so as to avoid influence heat transfer efficiency, additionally by by pyrolytic carbon caused by pyrolytic process and pyrolysis oil gas
With radiant tube caused by flue gas exchanged heat, increase economic efficiency.
With reference to figure 4, the system of processing rubbish according to embodiments of the present invention further comprises：One-level rotary kiln
400th, two-stage rotary kiln drier 500, feed bin 600, feed auger 700 and discharging spiral 800.
According to an embodiment of the invention, one-level rotary kiln 400 has organic waste import 401, secondary heat exchange cigarette
Gas entrance 402 and one-level dry organic waste outlet 403, secondary heat exchange smoke inlet 402 and the phase of secondary heat exchange exhanst gas outlet 304
Even, and it is suitable to before being respectively fed to carry out catalysis pyrolysis in catalytic pyrolysis reaction device by organic waste and catalyst, in advance
Secondary heat exchange flue gas will be used to carry out one-level drying process to organic waste, organic waste is dried so as to obtain one-level.By
This, by the way that organic waste is dried the waste heat of internal system heat smoke, can dry effect significantly improving organic waste
The utilization rate of thermal decomposition product sensible heat is improved while rate, and then reduces system energy consumption.
According to an embodiment of the invention, there is two-stage rotary kiln drier 500 one-level heat exchange oil gas entrance 501, one-level to do
Dry organic waste entrance 502, secondary drying organic waste outlet 503 and secondary heat exchange oil gas vent 504, one-level heat exchange oil gas enter
Mouth 501 is connected with one-level heat exchange oil gas vent 204, and one-level is dried organic waste entrance 502 and exported with one-level drying organic waste
403 are connected, and processing is dried suitable for drying organic waste to one-level using one-level heat exchange oil gas, so as to obtain two level
Dry organic waste and secondary heat exchange oil gas.Thus, it is possible to reduce system while organic waste pyrolysis efficiency is further improved
System energy consumption.
According to an embodiment of the invention, feed bin 600 has charging aperture 601 and discharging opening 602, and charging aperture 601 is done with two level
Dry organic waste outlet 503 is connected, and the secondary drying organic waste obtained suitable for storage two-stage rotary kiln drier.
According to an embodiment of the invention, feed auger 700 has the first screw feed en-trance 701 and the first spiral discharging mouth
702, the first screw feed en-trance 701 is connected with discharging opening 602, and the first spiral discharging mouth 702 is connected with organic waste entrance 101,
And carried out suitable for being supplied the secondary drying organic waste being stored in feed bin by feed auger into catalytic pyrolysis reaction device
Pyrolysis processing.Thus, it is possible to significantly improve the powder feeding efficiency of organic waste.
According to an embodiment of the invention, discharging spiral 800 has the second screw feed en-trance 801 and the second spiral discharging mouth
802, the second screw feed en-trance 801 is connected with pyrolytic carbon outlet 104, the second spiral discharging mouth 802 and the phase of pyrolytic carbon entrance 202
Even, and suitable for by the pyrolytic carbon that catalytic pyrolysis reaction device obtains by the spiral that discharges supply to and heat exchanger in.Thus, it is possible to
Significantly improve the discharging efficiency of pyrolytic carbon.
With reference to figure 5, the system of processing rubbish according to embodiments of the present invention further comprises：Purifier 900, steam hair
Raw device 1000 and coke quenching device 1100.
According to an embodiment of the invention, there is purifier 900 oil gas entrance 901, pyrolysis oil export 902 and purified gas to go out
Mouth 903, oil gas entrance 901 is connected with secondary heat exchange oil gas vent 504, clean gas outlet 903 and the fuel inlet on radiant tube
(not shown) is connected, and suitable for carrying out purified treatment to the secondary heat exchange oil gas obtained in two-stage rotary kiln drier, so as to
To obtain pyrolysis oil and purified gas, and the part supply of gained purified gas is used to radiant tube as fuel.Thus, pass through
Caused pyrolysis gas is purified after Oil-gas Separation will be pyrolyzed caused by internal system, and using gained purified gas as radiant tube
Fuel uses, and can significantly reduce the dependence to be refueled to outside.It should be noted that those skilled in the art can basis
It is actually needed and the particular type of purifier is selected.
According to an embodiment of the invention, steam generator 1000 has purified gas entrance 1001 and steam (vapor) outlet 1002, only
To change gas entrance 1001 with clean gas outlet 903 to be connected, steam (vapor) outlet 1002 is connected with steam inlet 102, and suitable for purification is filled
The another part for the purified gas for putting to obtain is burnt to be heated to water, so as to obtain steam, and gained steam is passed through
Steam inlet is supplied into discharge.Thus, periodically commutated and sprayed into discharge by steam caused by steam generator, gone forward side by side
Enter oil gas export pipeline, and then avoid oil gas from exporting line clogging.According to a particular embodiment of the invention, steam generator replaces
The vapor (steam) temperature for purging oil gas export pipeline is 300~500 DEG C, switching time 30s-600s.Thus, it is possible to further subtract
Few pyrolysis oil reduces the generation of secondary response in the residence time of burner hearth, and then significantly improves oil gas and quickly export efficiency, improves
Hydrocarbon yield.
According to an embodiment of the invention, pyrolytic carbon entrance 1101 goes out with cooling pyrolytic carbon after coke quenching device 1100 has heat exchange
Mouth 1102, pyrolytic carbon entrance 1101 is connected with pyrolytic carbon outlet 203 after heat exchange after heat exchange, and is carried out suitable for pyrolytic carbon after exchanging heat
Quenching is handled, so as to obtain cooling down pyrolytic carbon.It should be noted that those skilled in the art can be according to being actually needed pair
The condition of quenching processing is selected.
As described above, the system of processing organic waste according to embodiments of the present invention, which can have, is selected from the advantages of following extremely
It is one of few：
The system temperature of processing organic waste according to embodiments of the present invention is flexibly controllable, complicated suitable for processes composition
Organic waste, it is applied widely；
The system of processing organic waste according to embodiments of the present invention is using the method for rubbish catalysis pyrolysis, obtained pyrolysis
Gas yield is high, calorific value is high；Obtained pyrolysis oil composition is simple；
The system product sensible heat of processing organic waste according to embodiments of the present invention efficiently utilizes, and reduces energy consumption, organic rubbish
It is internal system supply that rubbish, which dries heat,；
The system of processing organic waste according to embodiments of the present invention is using the conjunction depressed with cloth of catalyst jetting device
Method, without adding the mixed processes of catalyst and material；
The system addition of processing organic waste according to embodiments of the present invention rotates coke removing appts, avoids radiant tube upper end from tying
Burnt phenomenon；
The system of processing organic waste according to embodiments of the present invention uses steam blowing oil gas delivery line, avoids oil gas from leading
Go out blockage.
In another aspect of the invention, the present invention proposes a kind of method for handling organic waste.According to the present invention's
Embodiment, this method are carried out using the system of above-mentioned processing organic waste.Below with reference to Fig. 6-8 pairs of embodiment of the present invention
The method of processing organic waste is described in detail.According to a particular embodiment of the invention, this method includes：
S100：Organic waste and catalyst are respectively fed to carry out catalysis pyrolysis in catalytic pyrolysis reaction device
According to an embodiment of the invention, organic waste and catalyst are respectively fed to be urged in catalytic pyrolysis reaction device
Change pyrolysis, so as to obtain being pyrolyzed oil gas and pyrolytic carbon.
According to an embodiment of the invention, the particle diameter of organic waste is not particularly restricted, and those skilled in the art can root
Selected according to being actually needed, according to a particular embodiment of the invention, the particle diameter of organic waste can be 0.1mm~10mm.By
This, can significantly improve the pyrolysis efficiency of organic waste.Specifically, catalyst can be selected from CaO, MgO, Na2CO3And K2CO3
At least one of.
Specifically, accurate temperature controlling of the realization such as flow of combustion gas of radiant tube to pyrolytic process can be passed through by adjustment,
And radiant tube is using the combustion system periodically to commutate so that the temperature field of single radiant tube is more or less the same in 30 DEG C, so as to protect
Demonstrate,prove epimere area in the uniformity of reactor temperature field, such as the flow reactor for the combustion gas for being passed through radiant tube by adjustment
The regulation temperature range of the radiant tube in domain is 500~800 DEG C, ensures the abundant pyrolysis of organic waste, and radiation is passed through by adjustment
The flow of the combustion gas of pipe make it that the regulation temperature range of the radiant tube in hypomere region in reactor is 450~650 DEG C, so as to enter one
The organic waste that a step heating part is not pyrolyzed completely.
S200：Flue gas caused by pyrolytic carbon and radiant tube is supplied into first-class heat exchanger and carries out one-level heat exchange processing
According to an embodiment of the invention, by caused by burning in caused pyrolytic carbon in catalytic pyrolysis reaction device and radiant tube
Flue gas, which is supplied into first-class heat exchanger, carries out one-level heat exchange processing, is exchanged heat cigarette so as to pyrolytic carbon after exchange heat and one-level
Gas.Thus, by the way that flue gas caused by caused pyrolytic carbon in catalytic pyrolysis reaction device and radiant tube is exchanged heat, by pyrolytic carbon
Waste heat pass to flue gas, the then dried medium using the flue gas after heat exchange as subsequent process, so as to realize to heat
The efficient utilization of pyrolytic carbon sensible heat is realized while the cooling for solving charcoal, and then reduces energy consumption.
S300：Pyrolysis oil gas and one-level heat exchange flue gas are supplied into secondary heat exchanger and carries out secondary heat exchange processing
According to an embodiment of the invention, will be obtained in catalytic pyrolysis reaction device in caused pyrolysis oil gas and first-class heat exchanger
One-level heat exchange flue gas supply into secondary heat exchanger carry out secondary heat exchange processing, so as to obtain one-level heat exchange oil gas and two
Level heat exchange flue gas.Thus, by the way that the waste heat for being pyrolyzed oil gas is passed into one-level heat exchange flue gas, then by gained secondary heat exchange flue gas
Dried medium with one-level heat exchange oil gas respectively as subsequent process, it is possible to achieve the efficient utilization of pyrolysis oil gas sensible heat, and then
Further reduce energy consumption.
The method of processing organic waste according to embodiments of the present invention by the way of cloth gas is combined with catalyst, without
The mixed processes of catalyst and organic waste are the high-efficiency thermal decomposition that organic waste can be achieved, and are by using multigroup radiant tube
Pyrolytic process provides thermal source, can realize the accurate control to pyrolytic process by adjusting the flow for the combustion gas that be passed through radiant tube
Temperature, and radiant tube ensure that the uniformity in temperature field, so as to significantly improve the heat of organic waste by heat storage type combustion
Efficiency is solved, and then improves the yield of pyrolysis oil, while more traditional use gas heat carrier or solid thermal carriers hot as pyrolysis
The pyrolytic reaction device in source is compared, and catalytic pyrolysis reaction device of the invention need not set preheating unit and carrier separative element,
So as to greatly simplify pyrolytic reaction technological process, and then significantly reduce dust content in the fault rate of device and gained pyrolysis oil
It is relatively low, and exhaust gas temperature is low, and secondly the present invention can be produced pyrolysis by arranging that oil gas exports pipeline in the bottom of radiant tube
Raw oil gas exports rapidly, so as to restrained effectively the second pyrolysis of oil gas, and then improves the yield of pyrolysis oil, and be pyrolyzed
Gas is not diluted by gas heat carrier, and pyrolysis gas calorific value is high, good in economic efficiency, sets agitating device to match somebody with somebody again by reactor
Radiant tube is closed, puddler is during back rotation is carried out so that the organic waste of accumulation is loosened, and increases the organic rubbish of accumulation
Voidage between rubbish, reduce the pressure drop that pyrolysis oil gas passes through organic waste layer so that caused pyrolysis oil gas can pass rapidly through
Organic waste layer reaches oil gas delivery line, and caused pyrolysis oil gas can be exported by oil gas delivery line in time, and can be avoided
The coking of radiant tube upper end, so as to avoid influence heat transfer efficiency, additionally by by pyrolytic carbon caused by pyrolytic process and pyrolysis oil gas
With radiant tube caused by flue gas exchanged heat, increase economic efficiency.
With reference to figure 7, the method for processing rubbish according to embodiments of the present invention further comprises：
S400：Before organic waste and catalyst are respectively fed to carry out catalysis pyrolysis in catalytic pyrolysis reaction device,
Secondary heat exchange flue gas and organic waste are supplied into one-level rotary kiln in advance organic waste is carried out at one-level drying
Reason
According to an embodiment of the invention, organic waste and catalyst are being respectively fed to carry out in catalytic pyrolysis reaction device
Before catalysis pyrolysis, secondary heat exchange flue gas and organic waste that secondary heat exchanger obtains are supplied to one-level rotary kiln drying in advance
One-level drying process is carried out to organic waste in device, organic waste is dried so as to obtain one-level.Thus, by by system
Organic waste is dried the waste heat of portion's heat smoke, and pyrolysis can be improved while organic waste drying efficiency is significantly improved
The utilization rate of product sensible heat, and then reduce system energy consumption.
S500：One-level heat exchange oil gas and one-level drying organic waste are supplied and carries out two level into two-stage rotary kiln drier
Drying process
According to an embodiment of the invention, by the one-level obtained in secondary heat exchanger heat exchange oil gas and one-level rotary kiln
In obtained one-level dry organic waste and supply into two-stage rotary kiln drier and carry out secondary drying processing, so as to obtain
Secondary drying rubbish and secondary heat exchange oil gas.Thus, it is possible to reduce system while organic waste pyrolysis efficiency is further improved
System energy consumption.
S600：Secondary drying organic waste is supplied and stored into feed bin, and by secondary drying organic waste through entering
Material spiral is supplied into catalytic pyrolysis reaction device
According to an embodiment of the invention, the secondary drying organic waste obtained in two-stage rotary kiln drier is supplied to material
Stored in storehouse, and secondary drying organic waste is supplied into catalytic pyrolysis reaction device through feed auger.It is thus, it is possible to aobvious
Write the powder feeding efficiency for improving organic waste.
With reference to figure 8, the method for processing rubbish according to embodiments of the present invention further comprises：
S700：Secondary heat exchange oil gas is supplied into purifier and carries out purified treatment, and a part for purified gas is supplied
Used to radiant tube as fuel
According to an embodiment of the invention, the secondary heat exchange oil gas that two-stage rotary kiln drier obtains is supplied to purifier
Middle carry out purified treatment, so as to obtain pyrolysis oil and purified gas, and a part for gained purified gas is supplied to radiant tube
Used as fuel.Thus, purified by caused pyrolysis gas after being pyrolyzed Oil-gas Separation caused by internal system, and will
Gained purified gas uses as the fuel of radiant tube, can significantly reduce the dependence to be refueled to outside.It should be noted that
Those skilled in the art can select according to the particular type being actually needed to purifier.
S800：Another part of purified gas is supplied into steam generator burning and produces steam, and by steam through steam
Entrance is supplied into discharge
According to an embodiment of the invention, another part of purified gas obtained by purifier is supplied and fired into steam generator
Burn and produce steam, and gained steam is supplied into discharge through steam inlet.Thus, steam caused by steam generator is passed through
Periodically commutation is sprayed into discharge, and enters oil gas export pipeline, and then avoids oil gas from exporting line clogging.According to the present invention's
Specific embodiment, the vapor (steam) temperature of steam generator alternately purging oil gas export pipeline is 300~500 DEG C, and switching time is
30s-600s.Thus, it is possible to further reduce pyrolysis oil in the residence time of burner hearth, the generation of secondary response is reduced, and then
Significantly improve oil gas and quickly export efficiency, improve hydrocarbon yield.
S900：Pyrolytic carbon after heat exchange is supplied into coke quenching device and carries out quenching processing
According to an embodiment of the invention, pyrolytic carbon after the heat exchange obtained in first-class heat exchanger is supplied to enter into coke quenching device
Row quenching is handled, so as to obtain cooling down pyrolytic carbon.It should be noted that those skilled in the art can be according to being actually needed
The condition of quenching processing is selected.
It should be noted that the feature and advantage described by the above-mentioned system for processing organic waste are equally applicable to this
The method for handling organic waste, here is omitted.
Below with reference to specific embodiment, present invention is described, it is necessary to which explanation, these embodiments are only to describe
Property, without limiting the invention in any way.
Embodiment
Organic waste is handled using the system of the processing organic waste shown in Fig. 5, first by organic waste (particle diameter
0.5-5mm, moisture content 45%) to one-level drying process is carried out into one-level rotary kiln, obtaining one-level drying has for supply
Machine rubbish (moisture content 17%), and gained one-level drying organic waste is supplied into two-stage rotary kiln drier and carries out two level
Drying process, secondary drying organic waste (moisture content 8%) is obtained, and gained secondary drying organic waste is delivered to feed bin and deposited
Storage, and the secondary drying organic waste being stored in feed bin is delivered in catalytic pyrolysis reaction device (pyrolysis temperature through feed auger
600 DEG C of degree), while through catalyst transport sprays into reactor catalyst CaO (straying quatity is organic waste quality
5%) organic waste catalytic pyrolysis reaction, takes place, the pyrolysis oil gas (550 DEG C) for reacting to obtain is arranged by pyrolysis oil gas vent
Go out, pyrolytic carbon (500 DEG C) is exported discharge by pyrolytic carbon and supplied through the spiral that discharges into first-class heat exchanger and fuel in radiant tube
(50 DEG C) progress one-level heat exchange of flue gas caused by burning, pyrolytic carbon (300 DEG C) and one-level heat exchange flue gas (140 after being exchanged heat
DEG C), then one-level heat exchange flue gas is supplied to secondary heat exchanger with pyrolysis oil gas and exchanged heat, obtains secondary heat exchange flue gas (200
DEG C) and one-level heat exchange oil gas (350 DEG C), then using secondary heat exchange flue gas as the dried medium of one-level rotary kiln to having
Processing is dried in machine rubbish, one-level is dried using one-level heat exchange oil gas as the dried medium of two-stage rotary kiln drier organic
Drying garbage processing, then pyrolytic carbon after heat exchange is supplied into coke quenching device and carries out quenching processing, then by gained two level heat
Solution oil gas, which is supplied into purifier, carries out purified treatment, is purified gas and pyrolysis oil, and a part for purified gas is supplied
Used to radiant tube as fuel, another part of purified gas, which is supplied into steam generator, carries out burning generation steam, and will
Gained steam is supplied into discharge through steam inlet.
The catalysis thermal decomposition product distribution of the rubbish of table 1
In the description of the invention, it is to be understood that term " " center ", " longitudinal direction ", " transverse direction ", " length ", " width ",
" thickness ", " on ", " under ", "front", "rear", "left", "right", " vertical ", " level ", " top ", " bottom " " interior ", " outer ", " up time
The orientation or position relationship of the instruction such as pin ", " counterclockwise ", " axial direction ", " radial direction ", " circumference " be based on orientation shown in the drawings or
Position relationship, it is for only for ease of and describes the present invention and simplify description, rather than indicates or imply that signified device or element must
There must be specific orientation, with specific azimuth configuration and operation, therefore be not considered as limiting the invention.
In addition, term " first ", " second " are only used for describing purpose, and it is not intended that instruction or hint relative importance
Or the implicit quantity for indicating indicated technical characteristic.Thus, define " first ", the feature of " second " can be expressed or
Implicitly include one or more this feature.In the description of the invention, " multiple " are meant that two or more,
Unless otherwise specifically defined.
In the present invention, unless otherwise clearly defined and limited, term " installation ", " connected ", " connection ", " fixation " etc.
Term should be interpreted broadly, for example, it may be fixedly connected or be detachably connected, or integrally；Can be that machinery connects
Connect or electrically connect；Can be joined directly together, can also be indirectly connected by intermediary, can be in two elements
The connection in portion or the interaction relationship of two elements.For the ordinary skill in the art, can be according to specific feelings
Condition understands the concrete meaning of above-mentioned term in the present invention.
In the present invention, unless otherwise clearly defined and limited, fisrt feature can be with "above" or "below" second feature
It is that the first and second features directly contact, or the first and second features pass through intermediary mediate contact.Moreover, fisrt feature exists
Second feature " on ", " top " and " above " but fisrt feature are directly over second feature or oblique upper, or be merely representative of
Fisrt feature level height is higher than second feature.Fisrt feature second feature " under ", " lower section " and " below " can be
One feature is immediately below second feature or obliquely downward, or is merely representative of fisrt feature level height and is less than second feature.
In the description of this specification, reference term " one embodiment ", " some embodiments ", " example ", " specifically show
The description of example " or " some examples " etc. means specific features, structure, material or the spy for combining the embodiment or example description
Point is contained at least one embodiment or example of the present invention.In this manual, to the schematic representation of above-mentioned term not
Identical embodiment or example must be directed to.Moreover, specific features, structure, material or the feature of description can be any
Combined in an appropriate manner in individual or multiple embodiments or example.In addition, in the case of not conflicting, the technology of this area
Different embodiments or example and the feature of different embodiments or example described in this specification can be combined by personnel
And combination.
Although embodiments of the invention have been shown and described above, it is to be understood that above-described embodiment is example
Property, it is impossible to limitation of the present invention is interpreted as, one of ordinary skill in the art within the scope of the invention can be to above-mentioned
Embodiment is changed, changed, replacing and modification.
Claims (20)
- A kind of 1. system for handling organic waste, it is characterised in that including：Catalytic pyrolysis reaction device, first-class heat exchanger and two level Heat exchanger,Wherein, the catalytic pyrolysis reaction device includes：Organic waste entrance, steam inlet, pyrolysis oil gas vent, pyrolytic carbon outlet；The organic waste entrance is located at the top center of the reactor；The pyrolysis oil gas vent is located in the side wall of the reactor；The steam inlet is on the pyrolysis oil gas vent, and the steam inlet and the pyrolysis oil gas outlet；The pyrolytic carbon outlet is positioned at the bottom of the reactor；Catalyst transport, the catalyst transport stretches to the inside reactor by the side wall of the reactor, described The port of export of catalyst transport is provided with blast cap, and the port of export of the catalyst transport is located at the organic waste entrance Underface, and the blast cap is relative with the organic waste entrance；Radiant tube, the radiant tube is in short transverse multi-tier arrangement of the inside of the reactor along the reactor, every layer of tool There are more radiant tubes parallel to each other in the horizontal direction；Discharge, the discharge are arranged in the reactor and are connected with the pyrolysis oil gas vent；Oil gas exports pipeline, and the oil gas export pipeline is communicated to the discharge, and the tube wall of oil gas export pipeline On be provided with through hole；Agitating device, the agitating device include agitating shaft and the multiple puddlers being connected on the agitating shaft, the stirring Axle extend into the inside of the reactor by pyrolytic carbon outlet and be configured to can be in the reactor internal rotation；The first-class heat exchanger has pyrolytic carbon outlet and one-level heat exchange exhanst gas outlet after smoke inlet, pyrolytic carbon entrance, heat exchange, The smoke inlet is connected with the exhanst gas outlet on the radiant tube, and the pyrolytic carbon entrance is connected with pyrolytic carbon outlet；There is the secondary heat exchanger pyrolysis oil gas entrance, one-level heat exchange smoke inlet, one-level heat exchange oil gas vent and two level to change Heat smoke exports, and the pyrolysis oil gas entrance is connected with the pyrolysis oil gas vent, the one-level exchange heat smoke inlet with it is described One-level heat exchange exhanst gas outlet is connected.
- 2. system according to claim 1, it is characterised in that height side of the oil gas export pipeline along the reactor To multi-tier arrangement, every layer has more oil gas export pipelines parallel to each other in the horizontal direction.
- 3. system according to claim 2, it is characterised in that the oil gas exports pipeline cloth parallel with the radiant tube Put, and the respective left and right sides of the radiant tube is symmetrically arranged with two oil gas export pipelines.
- 4. system according to claim 3, it is characterised in that the oil gas export pipeline and the neighbouring radiant tube Distance is that the oil gas exports pipe diameter d between tube wall 1/2-3 times.
- 5. according to the system any one of claim 1-4, it is provided with the tube wall of the oil gas export pipeline multiple logical Hole.
- 6. system according to claim 5, it is characterised in that length direction of the through hole in oil gas export pipeline On be uniformly distributed.
- 7. system according to claim 1, it is characterised in that be respectively arranged with gear on the both sides tube wall of the radiant tube Plate, the baffle plate are located at the top of oil gas export pipeline, and cover whole vertical projections of the oil gas export pipeline.
- 8. system according to claim 7, it is characterised in that the baffle plate is from the vertical section of the tube wall of the radiant tube Phase tangent line be starting point, extend downward into the vertical section of oil gas export pipeline at an angle.
- 9. system according to claim 8, it is characterised in that 40-90 degree is the angle ranging from, without 90 degree.
- 10. system according to claim 2, it is characterised in that oil gas export pipeline is communicated to same root described in same layer The discharge.
- 11. system according to claim 2, it is characterised in that the puddler is between radiation tube layer and oil gas delivery line Between channel layer.
- 12. system according to claim 1, it is characterised in that the distance of the blast cap and the organic waste entrance is 200~500mm.
- 13. system according to claim 12, it is characterised in that the blast cap is cowl, and is had on blast cap more Individual through hole.
- 14. system according to claim 1, it is characterised in that further comprise：One-level rotary kiln, the one-level rotary kiln have organic waste import, secondary heat exchange smoke inlet and One-level dries organic waste outlet, and the secondary heat exchange smoke inlet is connected with the secondary heat exchange exhanst gas outlet；Two-stage rotary kiln drier, the two-stage rotary kiln drying appliance have one-level heat exchange oil gas entrance, one-level to dry organic rubbish Rubbish entrance, the outlet of secondary drying organic waste and secondary heat exchange oil gas vent, the one-level heat exchange oil gas entrance and the one-level Heat exchange oil gas vent is connected, and the one-level, which dries organic waste entrance and dries organic waste with the one-level and export, to be connected；Feed bin, the feed bin have charging aperture and discharging opening, and the charging aperture is connected with secondary drying organic waste outlet；Feed auger, the feed auger have the first screw feed en-trance and the first spiral discharging mouth, the first spiral charging Mouth is connected with the discharging opening, and the first spiral discharging mouth is connected with the organic waste entrance；Discharge spiral, and the discharging spiral has the second screw feed en-trance and the second spiral discharging mouth, the second spiral charging Mouth is connected with pyrolytic carbon outlet, and the second spiral discharging mouth is connected with the pyrolytic carbon entrance.
- 15. system according to claim 14, it is characterised in that further comprise：Purifier, the purifier have oil gas entrance, pyrolysis oil export and clean gas outlet, the oil gas entrance and institute State secondary heat exchange oil gas vent to be connected, the clean gas outlet is connected with the fuel inlet on the radiant tube；Steam generator, the steam generator have purified gas entrance and a steam (vapor) outlet, the purified gas entrance with it is described net Change gas outlet to be connected, the steam (vapor) outlet is connected with the steam inlet.
- 16. system according to claim 1, it is characterised in that further comprise：Coke quenching device, the coke quenching device have pyrolytic carbon entrance and the outlet of cooling pyrolytic carbon after heat exchange, are pyrolyzed after the heat exchange Charcoal entrance is connected with pyrolytic carbon outlet after the heat exchange.
- 17. a kind of method that system using described in claim any one of 1-16 handles organic waste, it is characterised in that bag Include：(1) organic waste and catalyst are respectively fed to carry out catalysis pyrolysis in the catalytic pyrolysis reaction device, to obtain It is pyrolyzed oil gas and pyrolytic carbon；(2) flue gas caused by the pyrolytic carbon and the radiant tube is supplied into the first-class heat exchanger and carried out at one-level heat exchange Reason, so that pyrolytic carbon after exchange heat and one-level exchange heat flue gas；(3) the pyrolysis oil gas and one-level heat exchange flue gas are supplied into the secondary heat exchanger and carried out at secondary heat exchange Reason, to obtain one-level heat exchange oil gas and secondary heat exchange flue gas.
- 18. according to the method for claim 17, it is characterised in that further comprise：(4) before being respectively fed to carry out catalysis pyrolysis in catalytic pyrolysis reaction device by the organic waste and catalyst, in advance First the secondary heat exchange flue gas and the organic waste are supplied into one-level rotary kiln the organic waste is carried out One-level drying process, organic waste is dried to obtain one-level；(5) one-level heat exchange oil gas and one-level drying organic waste are supplied and carries out two into two-stage rotary kiln drier Level drying process, to obtain secondary drying rubbish and secondary heat exchange oil gas；(6) the secondary drying organic waste is supplied and stored into feed bin, and the secondary drying organic waste is passed through Feed auger is supplied into the catalytic pyrolysis reaction device.
- 19. according to the method for claim 18, it is characterised in that further comprise：(7) the secondary heat exchange oil gas is supplied into purifier and carries out purified treatment, to obtain pyrolysis oil and purified gas, And part supply to the radiant tube of the purified gas is used as fuel；(8) another part of the purified gas is supplied into steam generator burning and produces steam, and by the steam through institute Steam inlet is stated to supply into the discharge.
- 20. according to the method for claim 19, it is characterised in that further comprise：(9) pyrolytic carbon after the heat exchange is supplied into coke quenching device and carries out quenching processing, to obtain cooling down pyrolytic carbon.
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| CN201610211589.9A CN105728439B (en) | 2016-04-06 | 2016-04-06 | The system and method for handling organic waste |
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| CN201610211589.9A CN105728439B (en) | 2016-04-06 | 2016-04-06 | The system and method for handling organic waste |
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Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1090219A (en) * | 1992-11-13 | 1994-08-03 | 福斯特·惠勒能源公司 | Fluidized-bed reactor and system with and using method |
| JP2002180061A (en) * | 2000-12-18 | 2002-06-26 | Tokyo Yogyo Co Ltd | Carbonization oven and carbonization oven unit |
| CN2697475Y (en) * | 2004-03-01 | 2005-05-04 | 天津大学 | Screened pyrolyzing treatment furnace for domestic refuse |
| CN2733186Y (en) * | 2004-09-03 | 2005-10-12 | 刘谦 | Vertical thermal dissociation incinerator structure |
| CN101761928A (en) * | 2010-01-11 | 2010-06-30 | 中信重工机械股份有限公司 | Incineration treatment method for domestic refuse |
| CN201871374U (en) * | 2010-11-24 | 2011-06-22 | 杨健 | Pyrolytic oxidizing reaction kettle for household garbage |
| CN205628880U (en) * | 2016-04-06 | 2016-10-12 | 北京神雾环境能源科技集团股份有限公司 | System for handle organic rubbish |
Family Cites Families (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| KR101342893B1 (en) * | 2011-12-14 | 2014-01-06 | 한국하이테크 주식회사 | Low-temperature carbonization of organic waste, the device |
-
2016
- 2016-04-06 CN CN201610211589.9A patent/CN105728439B/en active Active
Patent Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1090219A (en) * | 1992-11-13 | 1994-08-03 | 福斯特·惠勒能源公司 | Fluidized-bed reactor and system with and using method |
| JP2002180061A (en) * | 2000-12-18 | 2002-06-26 | Tokyo Yogyo Co Ltd | Carbonization oven and carbonization oven unit |
| CN2697475Y (en) * | 2004-03-01 | 2005-05-04 | 天津大学 | Screened pyrolyzing treatment furnace for domestic refuse |
| CN2733186Y (en) * | 2004-09-03 | 2005-10-12 | 刘谦 | Vertical thermal dissociation incinerator structure |
| CN101761928A (en) * | 2010-01-11 | 2010-06-30 | 中信重工机械股份有限公司 | Incineration treatment method for domestic refuse |
| CN201871374U (en) * | 2010-11-24 | 2011-06-22 | 杨健 | Pyrolytic oxidizing reaction kettle for household garbage |
| CN205628880U (en) * | 2016-04-06 | 2016-10-12 | 北京神雾环境能源科技集团股份有限公司 | System for handle organic rubbish |
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