CN104560072B - Thermal decomposition of organic wastes system and method for pyrolysis - Google Patents
Thermal decomposition of organic wastes system and method for pyrolysis Download PDFInfo
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- CN104560072B CN104560072B CN201410831821.XA CN201410831821A CN104560072B CN 104560072 B CN104560072 B CN 104560072B CN 201410831821 A CN201410831821 A CN 201410831821A CN 104560072 B CN104560072 B CN 104560072B
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- 238000000197 pyrolysis Methods 0.000 title claims abstract description 251
- 239000010815 organic waste Substances 0.000 title claims abstract description 57
- 238000000034 method Methods 0.000 title claims abstract description 49
- 238000005979 thermal decomposition reaction Methods 0.000 title claims abstract description 37
- 239000004744 fabric Substances 0.000 claims abstract description 69
- 238000001816 cooling Methods 0.000 claims abstract description 46
- 239000007787 solid Substances 0.000 claims abstract description 30
- 238000003860 storage Methods 0.000 claims abstract description 18
- 239000007789 gas Substances 0.000 claims description 213
- 238000002485 combustion reaction Methods 0.000 claims description 31
- 239000000047 product Substances 0.000 claims description 27
- 239000000463 material Substances 0.000 claims description 25
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims description 24
- 239000003546 flue gas Substances 0.000 claims description 23
- 230000008569 process Effects 0.000 claims description 23
- 238000005338 heat storage Methods 0.000 claims description 20
- 238000010438 heat treatment Methods 0.000 claims description 17
- 238000001035 drying Methods 0.000 claims description 15
- 239000002245 particle Substances 0.000 claims description 14
- 239000012265 solid product Substances 0.000 claims description 14
- 238000009825 accumulation Methods 0.000 claims description 12
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 claims description 10
- 239000000779 smoke Substances 0.000 claims description 9
- 238000000926 separation method Methods 0.000 claims description 8
- XSQUKJJJFZCRTK-UHFFFAOYSA-N Urea Chemical compound NC(N)=O XSQUKJJJFZCRTK-UHFFFAOYSA-N 0.000 claims description 7
- 239000004202 carbamide Substances 0.000 claims description 7
- 239000003054 catalyst Substances 0.000 claims description 6
- 229910021529 ammonia Inorganic materials 0.000 claims description 5
- 238000009413 insulation Methods 0.000 claims description 5
- 238000006555 catalytic reaction Methods 0.000 claims description 4
- 238000005192 partition Methods 0.000 claims description 4
- 239000007921 spray Substances 0.000 claims description 3
- 238000005507 spraying Methods 0.000 claims description 3
- 239000003921 oil Substances 0.000 description 52
- 238000006243 chemical reaction Methods 0.000 description 16
- 239000002994 raw material Substances 0.000 description 9
- 230000000694 effects Effects 0.000 description 7
- 238000005265 energy consumption Methods 0.000 description 7
- 239000003610 charcoal Substances 0.000 description 6
- 238000010586 diagram Methods 0.000 description 6
- 238000005516 engineering process Methods 0.000 description 6
- 239000007788 liquid Substances 0.000 description 5
- 239000010813 municipal solid waste Substances 0.000 description 5
- 235000003642 hunger Nutrition 0.000 description 4
- 230000037351 starvation Effects 0.000 description 4
- 210000000498 stratum granulosum Anatomy 0.000 description 4
- 229910052799 carbon Inorganic materials 0.000 description 3
- 239000000567 combustion gas Substances 0.000 description 3
- 239000000203 mixture Substances 0.000 description 3
- 239000002699 waste material Substances 0.000 description 3
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 2
- 238000004458 analytical method Methods 0.000 description 2
- 230000008859 change Effects 0.000 description 2
- 238000004140 cleaning Methods 0.000 description 2
- 239000001257 hydrogen Substances 0.000 description 2
- 229910052739 hydrogen Inorganic materials 0.000 description 2
- 230000008676 import Effects 0.000 description 2
- 239000004615 ingredient Substances 0.000 description 2
- 230000007774 longterm Effects 0.000 description 2
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 2
- 239000005416 organic matter Substances 0.000 description 2
- 238000004064 recycling Methods 0.000 description 2
- 239000002918 waste heat Substances 0.000 description 2
- 239000002028 Biomass Substances 0.000 description 1
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 1
- PFRUBEOIWWEFOL-UHFFFAOYSA-N [N].[S] Chemical compound [N].[S] PFRUBEOIWWEFOL-UHFFFAOYSA-N 0.000 description 1
- 230000009471 action Effects 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 239000006229 carbon black Substances 0.000 description 1
- 229910002091 carbon monoxide Inorganic materials 0.000 description 1
- 235000019504 cigarettes Nutrition 0.000 description 1
- 230000001112 coagulating effect Effects 0.000 description 1
- 239000003245 coal Substances 0.000 description 1
- 239000002361 compost Substances 0.000 description 1
- 230000001351 cycling effect Effects 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 150000002013 dioxins Chemical class 0.000 description 1
- 238000010304 firing Methods 0.000 description 1
- 239000003500 flue dust Substances 0.000 description 1
- 239000002737 fuel gas Substances 0.000 description 1
- 239000000295 fuel oil Substances 0.000 description 1
- 229930195733 hydrocarbon Natural products 0.000 description 1
- 150000002430 hydrocarbons Chemical class 0.000 description 1
- 150000002431 hydrogen Chemical class 0.000 description 1
- 238000009434 installation Methods 0.000 description 1
- 230000003993 interaction Effects 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000000505 pernicious effect Effects 0.000 description 1
- FGIUAXJPYTZDNR-UHFFFAOYSA-N potassium nitrate Chemical compound [K+].[O-][N+]([O-])=O FGIUAXJPYTZDNR-UHFFFAOYSA-N 0.000 description 1
- 238000002203 pretreatment Methods 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 239000002296 pyrolytic carbon Substances 0.000 description 1
- 238000010791 quenching Methods 0.000 description 1
- 230000000171 quenching effect Effects 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 238000009738 saturating Methods 0.000 description 1
- 239000010802 sludge Substances 0.000 description 1
- 229910001220 stainless steel Inorganic materials 0.000 description 1
- 239000010935 stainless steel Substances 0.000 description 1
- 231100001234 toxic pollutant Toxicity 0.000 description 1
- 239000010920 waste tyre Substances 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
- C10B53/00—Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
- C10B49/00—Destructive distillation of solid carbonaceous materials by direct heating with heat-carrying agents including the partial combustion of the solid material to be treated
- C10B49/02—Destructive distillation of solid carbonaceous materials by direct heating with heat-carrying agents including the partial combustion of the solid material to be treated with hot gases or vapours, e.g. hot gases obtained by partial combustion of the charge
- C10B49/04—Destructive distillation of solid carbonaceous materials by direct heating with heat-carrying agents including the partial combustion of the solid material to be treated with hot gases or vapours, e.g. hot gases obtained by partial combustion of the charge while moving the solid material to be treated
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
- C10B57/00—Other carbonising or coking processes; Features of destructive distillation processes in general
- C10B57/08—Non-mechanical pretreatment of the charge, e.g. desulfurization
- C10B57/10—Drying
Landscapes
- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Materials Engineering (AREA)
- Organic Chemistry (AREA)
- Combustion & Propulsion (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Gasification And Melting Of Waste (AREA)
- Processing Of Solid Wastes (AREA)
Abstract
The present invention provides a kind of thermal decomposition of organic wastes system and method for pyrolysis, wherein, thermal decomposition of organic wastes system includes：Breaker, drier, revolving bed pyrolysis oven, pyrolysis solids treatment device, cooling and purifier, oil storage tank and heat accumulating type rotary heat exchanger, wherein, revolving bed pyrolysis oven is suitable for carrying out pyrolysis processing to pyrolysis feed, and there is cloth tray rotatable, for holding pyrolysis feed in revolving bed pyrolysis oven, pyrolysis chamber, the heat supply chamber below cloth tray that cloth tray will be separated into above cloth tray in revolving bed pyrolysis oven, wherein, there is the through hole that multiple connections are pyrolyzed chamber and heat supply chamber in cloth tray；Heat accumulating type rotary heat exchanger is respectively with cooling down and the hot air intake of purifier and revolving bed pyrolysis oven is connected, for being used for pyrolysis processing after fixed gas is heated.Thus effectively organic waste can be pyrolyzed using the thermal decomposition of organic wastes system of the above embodiment of the present invention.
Description
Technical field
The present invention relates to pyrolysis arts, and specifically, the present invention relates to a kind of thermal decomposition of organic wastes systems and pyrolysis side
Method.
Background technology
For a large amount of discarded objects in the current whole world, the main method landfill of traditional processing discarded object, compost, three kinds of burning
Technology, but with the increasing fast of discarded object, these three technologies increasingly show its defect, and such as landfill occupies tract, heap
Fertile method treating capacity is small, efficiency is low, burns and easily generates secondary pollution, can generate pernicious gas, particularly generate bioxin
(Dioxins) toxic pollutant, and be to cause one of haze weather origin cause of formation, make it interrupted in terms of commercial Application.
Pyrolytic technique is that organic matter is heated to 500~1000 DEG C in the state of anaerobic or anoxic, makes solid carbon object
(coal, biomass, rubbish, waste tire, waste and old organic matter, organic sludge etc.), be converted into combustion gas (pyrolysis gas), fuel oil and
The depot energy based on pyrolytic carbon.With gas heat pyrolytic technique in, be mostly used high-temperature flue gas as heating carrier directly into
Enter in pyrolysis oven and conduct heat through material bed realize, be back to use for product pyrolysis gas in pyrolytic process as gas heating carrier
Technology is rare to be referred to.
The content of the invention
It is contemplated that it solves at least some of the technical problems in related technologies.For this purpose, the present invention
One purpose is to propose a kind of efficient, the thermal decomposition of organic wastes system and be pyrolyzed using the system that low energy consumption of pyrolysis
The method of organic waste.
Thermal decomposition of organic wastes system according to embodiments of the present invention, including：Breaker, the breaker is suitable for will
The organic waste carries out break process, obtains granular pyrolysis feed；Drier, the drier and the broken dress
It puts and is connected and suitable for carrying out drying and processing to the pyrolysis feed Jing Guo the break process；Revolving bed pyrolysis oven, the revolving bed
Pyrolysis oven is connected with the drier and suitable for carrying out pyrolysis processing, and tool in the revolving bed pyrolysis oven to the pyrolysis feed
There is cloth tray rotatable, for holding the pyrolysis feed, the cloth tray will be separated into the revolving bed pyrolysis oven
Pyrolysis chamber, the heat supply chamber below the cloth tray above the cloth tray, wherein, have in the cloth tray
There is the through hole of multiple connections pyrolysis chamber and heat supply chamber, the heat supply chamber has hot air intake, the pyrolysis chamber
Room has feed inlet and gas outlet, and the feed inlet is connected with the pretreatment unit；It is pyrolyzed solids treatment device, the solid
Product processing device is connected with the solid outlet；Cooling and purifier, the cooling and purifier and the gas outlet
It is connected, oil and fixed gas is obtained so that the oil gas product generated in the pyrolysis chamber is carried out Oil-gas Separation；Oil storage tank, it is described
Oil storage tank is connected with the cooling and purifier；Heat accumulating type rotary heat exchanger, the heat accumulating type rotary heat exchanger respectively with institute
It states cooling with the hot air intake of purifier and the revolving bed pyrolysis oven to be connected, for using after the fixed gas is heated
In the pyrolysis processing.
Thermal decomposition of organic wastes system according to embodiments of the present invention, wherein revolving bed pyrolysis oven use the side of gas heat supply
Method, first hot gas out of, hot air intake enters cloth tray lower part heat supply chamber, secondly, hot gas from the bottom of cloth tray equably
Into multiple through holes in cloth tray, and through the pyrolysis feed layer in cloth tray, heat exchange is come into full contact with pyrolysis feed, thus
Pyrolytic reaction occurs in the environment of starvation for pyrolysis feed.The revolving bed pyrolysis oven with said structure uses gas as a result,
Body mode of heating, and hot gas is made to penetrate material bed from the bottom of pyrolysis feed layer so that pyrolysis feed reaches pyrolysis temperature, thus
Hot gas can be caused to be come into full contact with raw material inside the layer of pyrolysis feed layer, further improve heat source and the contact surface of pyrolysis feed
Product, so as to improve the degree of being heated evenly of pyrolysis feed.Therefore, using the thermal decomposition of organic wastes system of the above embodiment of the present invention
The pyrolysis efficiency and degree of pyrolysis of pyrolysis material can be improved.
In addition, thermal decomposition of organic wastes system according to the present invention also has following additional technical feature：
Specifically, the heat accumulating type rotary heat exchanger includes：Insulation shell defines chamber, the shell in the housing
Body has first entrance, first outlet, second entrance and second outlet；Partition plate, the partition plate are located in the chamber and by institutes
It states chamber and is separated into accumulation of heat chamber and heat release chamber；Heat storage, the heat storage are located at middle part and the accumulation of heat of the heat release chamber
The second outlet is formed at the middle part of chamber, the top of the heat release chamber, and the lower part of the heat release chamber forms described second
Combustion chamber is formed at entrance, the top of the accumulation of heat chamber, and combustion chamber is turned on first entrance, the lower part of the accumulation of heat chamber
First outlet is formed, wherein, the first entrance is connected with the cooling and purifier with fixed gas described in receiving portion, institute
Second entrance is stated to be connected to receive fixed gas described in another part, the second outlet and the hot gas with cooling and purifier
Import is connected.The heat exchange efficiency between gas can be significantly improved using above-mentioned heat accumulating type rotary heat exchanger.
Further, the heat accumulating type rotary heat exchanger includes denitration catalyst reative cell.
Further, the denitration catalyst reative cell includes：Spray ammonia or urea grid, ammonia or urea and SCR catalytic reactions
Room.
Further, the thermal decomposition of organic wastes system further includes smoke eliminator, the smoke eliminator with
The drier is connected.Thus the direct exhaust emission environment of flue gas is avoided.
Preferentially, the through hole in the cloth tray be circular hole and/or fin square hole, wherein, a diameter of the 2 of the circular hole
~6 millimeters, the long side of the fin square hole is 10~15 millimeters, broadside is 3~5 millimeters.It is possible thereby to significantly improve hot gas
The efficiency being threaded through, and then improve and the heat transfer effect of pyrolysis feed.
According to the second aspect of the invention, the invention also provides using foregoing thermal decomposition of organic wastes system into
The method of row pyrolysis organic waste, including：
The organic waste is subjected to break process using the breaker, obtains granular pyrolysis feed；
Drying and processing is carried out to the pyrolysis feed Jing Guo the break process using drier；
Will by drying and processing the pyrolysis feed particle from the revolving bed pyrolysis oven pyrolysis chamber described in into
Material mouth carries out cloth in the cloth tray, and is passed through hot gas into the heat supply chamber from the hot air intake, makes the heat
Solution feed particles are pyrolyzed, and obtain solid product and oil gas product；
The solid product is handled and collected in the pyrolysis solids treatment device；
The oil gas product is subjected to Oil-gas Separation processing in the cooling and purifier, to obtain oily and not coagulate
Gas, and the oil is stored in the oil storage tank；
In fixed gas described in the combustion chamber Indoor Combustion part of the heat accumulating type rotary heat exchanger or outside for combustible gas releasing
Heat fixed gas described in another part is heated, and by the fixed gas after heating be used for the pyrolysis.
In some embodiments of the invention, it is used to heat after the combustion chamber Indoor Combustion of the heat accumulating type rotary heat exchanger
The temperature of the high-temperature flue gas of fixed gas is 600~950 degrees Celsius.
In some embodiments of the invention, the temperature of the fixed gas after heating is 550~850 degrees Celsius.
In some embodiments of the invention, when the pyrolysis processing is that progress 1~3 is small under 550~800 degrees Celsius.
Description of the drawings
Fig. 1 is the structure diagram of thermal decomposition of organic wastes system according to an embodiment of the invention.
Fig. 2 is the structure diagram of revolving bed pyrolysis oven according to an embodiment of the invention.
Fig. 3 is the structure diagram of cloth tray in revolving bed pyrolysis oven according to an embodiment of the invention.
Fig. 4 is the structure diagram of heat accumulating type rotary heat exchanger according to an embodiment of the invention.
Fig. 5 is the structure diagram of heat accumulating type rotary heat exchanger in accordance with another embodiment of the present invention.
Fig. 6 is the structure diagram of thermal decomposition of organic wastes system in accordance with another embodiment of the present invention.
Fig. 7 is the flow chart of method for pyrolysis in accordance with another embodiment of the present invention.
Specific embodiment
The embodiment of the present invention is 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 has the function of same or like element.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 present 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 instructions such as pin ", " counterclockwise ", " axial direction ", " radial direction ", " circumferential direction " be based on orientation shown in the drawings or
Position relationship is for only for ease of the description present invention and simplifies description rather than instruction 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 description purpose, and it is not intended that instruction or hint relative importance
Or the implicit quantity for indicating indicated technical characteristic.Define " first " as a result, the feature of " second " can be expressed or
Implicitly include one or more this feature.In the description of the present 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 being fixedly connected or being detachably connected or integral；Can be that machinery connects
It connects or is electrically connected；It can be directly connected, can also be indirectly connected by intermediary, can be in two elements
The connection in portion or the interaction relationship of two elements.It 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 contact directly or the first and second features pass through intermediary mediate contact.Moreover, fisrt feature exists
Second feature " on ", " top " and " above " but fisrt feature 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 less than second feature.
According to an aspect of the present invention, the present invention proposes a kind of thermal decomposition of organic wastes system.It is real according to the present invention
The thermal decomposition of organic wastes system of example is applied, including：Breaker, breaker are suitable for organic waste carrying out break process,
Obtain granular pyrolysis feed；Drier, drier are connected with breaker and suitable for former to the pyrolysis Jing Guo break process
Material carries out drying and processing；Revolving bed pyrolysis oven, revolving bed pyrolysis oven is suitable for carrying out the pyrolysis feed pyrolysis processing, and rotates
There is cloth tray rotatable, for holding pyrolysis feed in bed pyrolysis oven, cloth tray will be separated into revolving bed pyrolysis oven
Pyrolysis chamber, the heat supply chamber below cloth tray above cloth tray, wherein, there are multiple connection heat in cloth tray
The through hole of chamber and heat supply chamber is solved, heat supply chamber has hot air intake, and there is pyrolysis chamber feed inlet, gas outlet and solid to go out
Mouthful；Solids treatment device is pyrolyzed, pyrolysis solids treatment device is connected with solid outlet；Cooling and purifier, cooling and purification
Device is connected with gas outlet, and oil and fixed gas are obtained to be pyrolyzed the oil gas product generated in chamber progress Oil-gas Separation；Storage
Oil tank, oil storage tank are connected with cooling and purifier；Heat accumulating type rotary heat exchanger, heat accumulating type rotary heat exchanger respectively with cooling and
The hot air intake of purifier and revolving bed pyrolysis oven is connected, for after fixed gas is heated for pyrolysis processing.
Thermal decomposition of organic wastes system according to embodiments of the present invention, wherein revolving bed pyrolysis oven use the side of gas heat supply
Method, first hot gas out of, hot air intake enters cloth tray lower part heat supply chamber, secondly, hot gas from the bottom of cloth tray equably
Into multiple through holes in cloth tray, and through the pyrolysis feed layer in cloth tray, heat exchange is come into full contact with pyrolysis feed, thus
Pyrolytic reaction occurs in the environment of starvation for pyrolysis feed.The revolving bed pyrolysis oven with said structure uses gas as a result,
Body mode of heating can make hot gas penetrate material bed from the bottom of pyrolysis feed layer so that pyrolysis feed reaches pyrolysis temperature, by
This can cause hot gas to be come into full contact with raw material inside the layer of pyrolysis feed layer, further improve contact of the heat source with pyrolysis feed
Area, so as to improve the degree of being heated evenly of pyrolysis feed.Therefore, using the thermal decomposition of organic wastes system of the above embodiment of the present invention
System can improve the pyrolysis efficiency and degree of pyrolysis of pyrolysis material.
The thermal decomposition of organic wastes system 100 of the above embodiment of the present invention is described in detail below with reference to Fig. 1-Fig. 5.Using this
Waste materials containing carbon can be pyrolyzed into solid matter such as carbon black, pyrolysis oil and pyrolysis gas etc. completely by thermal decomposition of organic wastes system 100
Useful products.
Thermal decomposition of organic wastes system 100 according to embodiments of the present invention, as shown in Figure 1, including：Breaker 10 is done
Dry device 20, revolving bed pyrolysis oven 30, pyrolysis solids treatment device 40, cooling and purifier 50, oil storage tank 60, heat accumulating type rotation
Heat exchanger 70.
According to a particular embodiment of the invention, as shown in Figure 1, breaker 10 is suitable for organic waste carrying out broken place
Reason, obtains granular pyrolysis feed；Drier 20 is connected with breaker 10 and suitable for former to the pyrolysis Jing Guo break process
Material carries out drying and processing.Organic waste before being effectively pyrolyzed using breaker 10 and drier 20 as a result, is carried out
Pre-treatment removes moisture therein, to improve pyrolysis efficiency.
According to a particular embodiment of the invention, as shown in Fig. 2, have in revolving bed pyrolysis oven 30 it is rotatable, for containing
Put the cloth tray 31 of pyrolysis feed, cloth tray by the pyrolysis chamber 32 being separated into revolving bed pyrolysis oven above cloth tray,
Heat supply chamber 33 below cloth tray.The ring-shaped structure that cloth tray is arranged horizontally, heat supply chamber are arranged horizontally
Circular cavity, wherein, there is the through hole 311 that multiple connections are pyrolyzed chamber and heat supply chamber in cloth tray 31 as shown in Figure 3,
Heat supply chamber has hot air intake 34, and the hot air intake 34 is multiple, is evenly distributed in the annulus of heat supply chamber cavity
Inside, pyrolysis chamber have feed inlet (not shown), gas outlet 35 and solid outlet (not shown)；It is pyrolyzed solids treatment device 40
It is connected with solid outlet (not shown).According to a particular embodiment of the invention, above-mentioned revolving bed pyrolysis oven 30 is suitable for former to pyrolysis
Material carries out pyrolysis processing.
According to a particular embodiment of the invention, the through hole 311 in above-mentioned revolving bed pyrolysis oven 30 in cloth tray 31 can be
Circular hole and/or fin square hole.According to a particular embodiment of the invention, the diameter of circular hole can be 2~6 millimeters, fin side
The long side in hole can be 10~15 millimeters, broadside can be 3~5 millimeters.It therefore can by using the through hole with above-mentioned size
To prevent pyrolysis feed from draining in heat supply chamber, while hot gas can be significantly improved and enter the pyrolysis indoor rate of chamber, Jin Erti
High hot gas improves pyrolysis efficiency to the efficiency of heating surface of pyrolysis material.
According to a particular embodiment of the invention, cloth tray is preferably that circular hole and the aperture that there is aperture to be preferably 4 millimeters are 3
The stainless steel plate of the fin square hole (not provided in figure) of * 12 millimeters of millimeter.Thus be more conducive to cloth tray bottom 550~
800 degrees Celsius of hot gas is directly contacted by circular hole and/or fin square hole with the material in cloth tray.Through hole hole in cloth tray
The selection of footpath size should have beneficial to gas through pyrolysis feed layer and be effectively prevented from pyrolysis feed and fall on cloth tray by this hole
Under heat supply chamber.Therefore, the selection of through-hole aperture size is determined by pyrolysis feed granular size in cloth tray, pyrolysis feed
The selection gist of grain diameter is obtained by actual production, and material difficulty is interior when 2 is small after material particular diameter is more than 30 millimeters
Pyrolysis is saturating, and individual layer material pyrolysis time is short when material particular diameter is less than 5 millimeters, but fabric thickness is limited, because the thicker bed of material
Make bed of material air resistance bigger than normal, unfavorable gas passes through, and is also unfavorable for the pyrolysis of upper materials.Therefore, pyrolysis feed optimum grain-diameter
For 5~30 millimeters, fabric thickness is preferably 50~400 millimeters, and through hole is 4 millimeters of circular hole in the cloth tray of revolving bed pyrolysis oven
And/or the fin square hole that aperture is 3 millimeters * 12 millimeters is optimal.It is possible thereby to significantly improve pyrolysis efficiency.
According to a particular embodiment of the invention, the temperature for being provided to the indoor hot gas of heat supply chamber can be 550~850 Celsius
Degree it is possible thereby to provide enough heats to pyrolysis feed and pyrolysis chamber, and then improves pyrolysis efficiency.Tool according to the present invention
Body embodiment, the interior temperature for carrying out pyrolysis processing of pyrolysis chamber is 480~800 degrees Celsius.Therefore it provides temperature is 550~850
Degree Celsius hot gas to heat supply chamber can be effectively ensured pyrolysis feed reach 480~800 degrees Celsius concurrently give birth to pyrolytic reactions.
According to a particular embodiment of the invention, above-mentioned revolving bed pyrolysis oven is using hot gas as heat source, and from the bottom of pyrolysis feed
The mode of heating that portion passes through it is possible thereby to significantly improve the contact area of hot gas and pyrolysis feed, enables in particular to and pyrolysis feed
Pyrolysis feed contact inside layer improves the degree of being heated evenly of pyrolysis feed, therefore, using the rotation with said structure feature
Bed pyrolysis oven can significantly improve pyrolysis efficiency.
Thermal decomposition of organic wastes system according to the above embodiment of the present invention can also include：Cooling and purifier 50,
Oil storage tank 60.Cooling and purifier 50 are connected with gas outlet 35, and oil is carried out to be pyrolyzed the oil gas product generated in chamber
The isolated oil of gas and fixed gas；Oil storage tank 60 is connected with cooling and purifier 50, for storing isolated oil.
According to a particular embodiment of the invention, the oil gas product that pyrolysis generates in revolving bed pyrolysis oven is from pyrolysis chamber roof
Gas outlet be discharged into cooling and purifier 50, the oil after cooling in oil gas product forms liquid oil and does not coagulate
Thus gas separates oil gas product, liquid oil is stored in oil storage tank 60.
According to a particular embodiment of the invention, thermal decomposition of organic wastes system can also include：Heat accumulating type rotary heat exchanger
70, heat accumulating type rotary heat exchanger 70 is connected respectively with cooling and the hot air intake 34 of purifier 50 and revolving bed pyrolysis oven 30,
For after fixed gas is heated for pyrolysis processing.Therefore, pyrolysis can be generated by heat accumulating type rotary heat exchanger 70
Fixed gas heated after return for pyrolytic reaction.Thus the thermal decomposition of organic wastes system of the above embodiment of the present invention is used
System can significantly improve energy utilization rate, reduce pyrolysis energy consumption.
According to a particular embodiment of the invention, as shown in figure 4, above-mentioned heat accumulating type rotary heat exchanger 70 specifically includes following group
Part：Insulation shell 71, housing have first entrance 72, second entrance 73, first outlet 74 and second outlet 75, first entrance 72
It is connected with cooling and purifier 70 with receiving portion fixed gas, second entrance 73 is connected to receive with cooling and purifier 40
Another part fixed gas, second outlet 75 are connected with hot air intake 14, and one or more pairs of heat storages 76, multipair heat storage is located at shell
In body 71；Combustion chamber 77, combustion chamber is located in the insulation shell and closes on the first entrance, and combustion chamber is suitable for
Part fixed gas burning.
First entrance 72 (high-temperature flue gas entry) front end of above-mentioned heat accumulating type rotary heat exchanger 70 has combustion chamber as a result,
77, pyrolysis generates the obtained part fixed gas generation high-temperature flue gas that can burn directly in combustion chamber 77 and enters heat storage 76 and change
Heat can also be burnt in combustion chamber 77 as combustion gas instead of fixed gas by external world's offer combustible gas and obtain high-temperature flue gas, may be used also
It is exchanged heat with directly entering heat storage 76 by external world's offer high-temperature flue gas.
According to a particular embodiment of the invention, the concrete operating principle of heat accumulating type rotary heat exchanger 70 is as shown in figure 5, accumulation of heat
When formula rotary heat exchanger 70 is run, the axis rotary motion along longitudinal direction of heat storage 76, other each equipment are stationary, part fixed gas from
When first entrance 72 enters burning in combustion chamber 77 and passes through heat storage 76, heat storage 76 starts accumulation of heat, and heat storage 76 is continuous
Heating, when the heat storage 76 after accumulation of heat heating rotates to opposite side, another part fixed gas of room temperature enters from opposite side second
Mouth 73 enters in heat storage 76, during fixed gas is by heat storage 76, exchanges heat with heat storage 76, room temperature fixed gas is continuous
Heating is finally left in the entrance revolving bed pyrolysis oven of heat accumulating type rotary heat exchanger 70 from second outlet 75 and is used to be pyrolyzed.With accumulation of heat
The continuous rotary motion of axis, combustion parts fixed gas reach Continuous Heat Transfer effect to body 76 with another room temperature fixed gas along longitudinal direction.Root
According to specific embodiments of the present invention, the part fixed gas of burning can also by it is outer for high-temperature flue gas substitute directly releasing heat or
Person is substituted by outer for fuel gas, and heat is released after burning.Therefore, above-mentioned heat accumulating type rotary heat exchanger 70 to fixed gas into
The adaptability of row preheating is stronger.
In addition, it can also be added in as requested in heat accumulating type rotary heat exchanger using above-mentioned heat accumulating type rotary heat exchanger corresponding
Catalyst, change fixed gas gas ingredient come meet pyrolysis requirement, also denitration process can be directly carried out to flue gas, after reduction
Section process cost of investment.
The fixed gas that can be generated as a result, by using above-mentioned heat accumulating type rotary heat exchanger 70 to pyrolysis heats, into
And it is used for the pyrolytic reaction of the pyrolysis feed in revolving bed pyrolysis oven.It is possible thereby to it will generate in thermal decomposition of organic wastes system
Fixed gas returns to the heat source for thermal decomposition of organic wastes system, can significantly reduce energy consumption.
According to a particular embodiment of the invention, the mainly reproducibility gas of the hydro carbons containing low-carbon is pyrolyzed in the fixed gas of generation
Body, including carbon monoxide, hydrogen and methane etc..Therefore, the combustion parts in the combustion chamber 77 of heat accumulating type rotary heat exchanger 70
Fixed gas can release amount of heat for preheating another part fixed gas, this save outer for combustible gas, saving energy consumption.Separately
Outside, using heat source of the fixed gas that pyrolysis generates as pyrolytic reaction in itself, the progress of pyrolytic reaction is not interfered with not only, not yet
It can influence the quality of fixed gas, it is ensured that the calorific value of fixed gas.According to a particular embodiment of the invention, using gas heat carrier, heat
Solution raw material is heated evenly, and temperature plateau, fluctuation range is small, easy to control.Thus there is the organic waste of said structure of the present invention
Pyrolysis system improves utilization rate of heat value, and equipment investment is few, easily operated.
As shown in figure 5, according to a particular embodiment of the invention, above-mentioned heat accumulating type rotary heat exchanger 70 still further comprises de-
Nitre catalytic reaction, out of stock reative cell are located in the insulation shell and close on the first outlet 74.It is according to the present invention specific
Embodiment, denitration catalyst reative cell include：Ammonia-spraying grid or spray urea grid 78, ammonia or urea and SCR catalytic reaction chambers 79.Its
In, ammonia or urea are provided by import 781.It is possible thereby to directly carry out denitration process to flue gas, back segment process cost of investment is reduced.
As shown in fig. 6, according to a particular embodiment of the invention, above-mentioned thermal decomposition of organic wastes system further comprises：Cigarette
Air purifying apparatus 80 and chimney 90, smoke eliminator 80 are connected with drier 20, drier 20 and heat accumulating type rotary heat exchanger
70 first outlet 74 is connected；Chimney 90 is connected with smoke eliminator 80.It is possible thereby to first with heat accumulating type rotating heat transfer
After the heat of the flue gas of discharge carries out drying and processing to organic waste in device 70, then purified in smoke eliminator 80
Processing chimney 90 discharge, by, avoid pollution environment.
According to another aspect of the present invention, the invention also provides a kind of sides being pyrolyzed using above-mentioned pyrolysis system
Method.Specifically include the following steps：The organic waste is subjected to break process using breaker, obtains granular pyrolysis
Raw material；Drying and processing is carried out to the pyrolysis feed Jing Guo break process using drier；It will be by the pyrolysis of drying and processing
Feed particles from the feed inlet of the pyrolysis chamber of revolving bed pyrolysis oven to cloth tray on carry out cloth, and from hot air intake to heat supply
Hot gas is passed through in chamber, is pyrolyzed pyrolysis feed particle, obtains solid product and oil gas product；In pyrolysis solids treatment dress
It puts and interior solid product is handled and collected；Oil gas product is subjected to Oil-gas Separation processing in cooling and purifier, with
Just oil and fixed gas are obtained, and oil is stored in the oil storage tank；In the combustion chamber Indoor Combustion of heat accumulating type rotary heat exchanger
Part fixed gas outside heats another part fixed gas for combustible gas liberated heat, and by not coagulating after heating
Gas is used to be pyrolyzed.
The method that method for pyrolysis according to embodiments of the present invention, wherein revolving bed pyrolysis oven use gas heat supply, it is hot first
Gas is out of, hot air intake enters cloth tray lower part heat supply chamber, and secondly, hot gas is from the bottom of cloth tray evenly into cloth
Multiple through holes on disk, and through the pyrolysis feed layer in cloth tray, heat exchange is come into full contact with pyrolysis feed, thus pyrolysis feed
Pyrolytic reaction occurs in the environment of starvation.As a result, using having above-mentioned revolving bed pyrolysis oven, hot gas can be made from pyrolysis
The bottom of raw material layer penetrates material bed so that pyrolysis feed reaches pyrolysis temperature, it is possible thereby to so that hot gas and pyrolysis feed layer
The internal raw material of layer comes into full contact with, and further improves the contact area of heat source and pyrolysis feed, so as to improve the heated of pyrolysis feed
The uniformity.Therefore, the pyrolysis efficiency of pyrolysis material and pyrolysis journey can be improved using the method for pyrolysis of the above embodiment of the present invention
Degree.
Method for pyrolysis according to embodiments of the present invention is described in detail below with reference to Fig. 7.
(1) pretreatment of raw material
First, will be obtained wait the organic waste being pyrolyzed after pretreatment can be as the pyrolysis feed of pyrolysis.Pretreatment
It can include following one or more steps：
Break process：Organic waste is subjected to break process.
Drying and processing：The hot organic waste crushed is dried before revolving bed pyrolysis oven is entered
Dry, the temperature of drying can be 120~280 degrees Celsius.The use of more extensive solid drying machine is at present rotary dryer, does
Dry heat source can be the heat smoke from heat accumulating type rotary heat exchanger, by inversely with organic waste direct contact heat transfer,
So as to fulfill the drying of organic waste.
(2) pyrolysis processing is carried out in revolving bed pyrolysis oven
Secondly, by the pyrolysis feed particle that above-mentioned pretreatment obtains from revolving bed pyrolysis oven pyrolysis chamber feed inlet to
Cloth is carried out in cloth tray, hot gas is passed through into heat supply chamber from hot air intake, is pyrolyzed pyrolysis feed particle, consolidate
Body product and oil gas product.
According to a particular embodiment of the invention, above-mentioned pretreated pyrolysis feed particle is passed through on revolving bed pyrolysis oven
Portion's feed inlet enters entrance storehouse, and in revolving bed pyrolysis oven under the effect of cloth scraper plate, pyrolysis feed particle is existed by equably cloth
Pyrolysis feed stratum granulosum is formed in revolving bed pyrolysis oven cloth tray.According to a particular embodiment of the invention, pyrolysis feed stratum granulosum
Thickness can be related according to the hole size in the particle size and cloth tray of pyrolysis feed particle, specifically, should be appropriate
Relation between three is controlled, inventor has found, when pyrolysis feed optimum grain-diameter is 5~30 millimeters, fabric thickness is preferably 50~
400 millimeters, the fin that through hole is 4 millimeters of circular hole and/or aperture is 3 millimeters * 12 millimeters in the cloth tray of revolving bed pyrolysis oven
Shape square hole.It is possible thereby to ensure hot gas through the rate of through hole and pyrolysis feed stratum granulosum, and then improve and pyrolysis feed particle
It comes into full contact with, improves the pyrolysis feed particles by heat uniformity, improve pyrolysis efficiency.
According to a particular embodiment of the invention, the temperature of the anti-raw pyrolytic reaction of above-mentioned pyrolysis feed is Celsius for 480~800
Degree, and only need at such a temperature 1~3 it is small when can be pyrolyzed completely.It is possible thereby to significantly improve pyrolysis efficiency.
(3) heat source presentation mode
Further, heat source is supplied into revolving bed pyrolysis oven and carries out pyrolytic reaction.Another specific reality according to the present invention
Example is applied, heat source can provide as follows.For example, made using the fixed gas generated in revolving bed pyrolysis oven after preheating
For heat source, wherein, preheating may be employed part fixed gas or be carried out outside for combustible gas and high-temperature flue gas.
According to a particular embodiment of the invention, supply fixed gas after preheating as heat source by the use of outer.First, driving
During stove, external flammable gas generates high-temperature flue gas in the burning Indoor Combustion of heat accumulating type rotary heat exchanger, also can directly be carried by the external world
For high-temperature flue gas, pass through the high-temperature flue gas entry of heat accumulating type rotary heat exchanger and fixed gas entrance respectively with fixed gas outside room temperature
Heat accumulating type rotary heat exchanger is redirected back into, is exchanged heat in the rotation heat storage in heat accumulating type rotary heat exchanger, the height of generation
Warm fixed gas enters the cloth tray bottom of revolving bed pyrolysis oven, is evenly distributed on high temperature fixed gas by furnace bottom gas distributor
In the heat supply chamber of cloth tray bottom, then high temperature fixed gas is used as gas heat carrier by the through hole in cloth tray from bottom to top
Through the pyrolysis feed stratum granulosum in cloth tray, with pyrolysis feed direct contact heat transfer, pyrolysis feed is in the environment of starvation
Under be pyrolyzed, be that 5~30 millimeters of material is heated to 550~800 degrees Celsius of pyrolysis temperature by grain size.By pyrolysis feed destructive distillation
Into gas, liquid, solid body carbonaceous products, the solid product after being pyrolyzed leaves revolving bed by revolving bed pyrolysis oven solid outlet and is pyrolyzed
Stove.
According to a particular embodiment of the invention, above-mentioned method for pyrolysis further includes：It is not coagulated what is generated in revolving bed pyrolysis oven
Gas is used to be pyrolyzed after being heated in heat accumulating type rotary heat exchanger.It is possible thereby to the fixed gas that pyrolysis generates is utilized to return for heat
Solution reaction, can not only save energy consumption, while not interfere with the ingredient of fixed gas, it is ensured that and fixed gas can continue cycling through utilization,
So that utmostly sinking is inexpensive.
According to a particular embodiment of the invention, above-mentioned method for pyrolysis further includes：In the combustion chamber of heat accumulating type rotary heat exchanger
Indoor Combustion part fixed gas outside heats another part fixed gas for combustible gas liberated heat, and will heating
Fixed gas afterwards is used to be pyrolyzed.It is possible thereby to further improve the utilization rate of fixed gas, while eliminate outer for combustible gas, saving
Energy consumption.In addition, using heat source of the fixed gas that pyrolysis generates as pyrolytic reaction in itself, do not interfere with not only pyrolytic reaction into
Row will not influence the quality of fixed gas, it is ensured that the calorific value of fixed gas.According to a particular embodiment of the invention, using air heat
Carrier, pyrolysis feed are heated evenly, and temperature plateau, fluctuation range is small, easy to control.Thus it is organic with said structure of the present invention
Pyrolysis of waste system improves utilization rate of heat value, and equipment investment is few, in operation.
According to a particular embodiment of the invention, in the above-mentioned fixed gas as heat accumulating type rotary heat exchanger heat source, for firing
The gas volume ratio for burning exothermic part fixed gas and another part fixed gas can be 1:1.Both can adjust in special circumstances
The volume ratio 1 of gas:3.Part fixed gas also directly can in a combustion chamber be burnt by outer for combustible gas instead of fixed gas.
According to a particular embodiment of the invention, do not coagulated after the combustion chamber Indoor Combustion of heat accumulating type rotary heat exchanger for heating
The temperature of the high-temperature flue gas of gas is 600~950 degrees Celsius, and flue-gas temperature is down to less than 300 degrees Celsius after heat storage exchanges heat,
The temperature of the above-mentioned fixed gas heat source for revolving bed pyrolysis oven obtained by heat accumulating type rotary heat exchanger is 550~850, by
Pyrolysis feed fully can be heated to 550~800 degrees Celsius of generation pyrolytic reactions by this.Further, the entrance after cooling
In gas cleaning unit, flue dust and nitrogen sulfur compound are removed, flue gas outside chimney by arranging after reaching discharge standard.
Another specific embodiment according to the present invention is used to heat fixed gas after the interior burning of heat accumulating type rotary heat exchanger
The temperature of high-temperature flue gas is 700~950 degrees Celsius, and flue-gas temperature is down to less than 300 degrees Celsius after heat storage exchanges heat, above-mentioned
The temperature of the fixed gas heat source for revolving bed pyrolysis oven obtained by heat accumulating type rotating commutator is 600~850 degrees Celsius,
It is possible thereby to pyrolysis feed is fully heated to 580~750 degrees Celsius of generation pyrolytic reactions.
(4) solid product is handled
According to a particular embodiment of the invention, solid product is handled and collected in pyrolysis solids treatment device.
Specifically, the solid product after being pyrolyzed in revolving bed pyrolysis oven enters pyrolysis under the action of the spiral that discharges by feed opening
Solids treatment device is cooled down.The cooling procedure of solid product can pass through the quenching or cold with water-cooling jacket spiral of spraying
But, solid product is cooled to less than 80 degrees Celsius by 450 DEG C -750 degrees Celsius, product enters solid resultant product collection storehouse after cooling
Middle storage.Obtained high-temperature steam is cooled down to send to afterheat boiler system recycling.
(5) oil gas product is handled
According to a particular embodiment of the invention, by the oil gas product generated in revolving bed pyrolysis oven in cooling and purifier
Interior progress Oil-gas Separation processing, to obtain oil and fixed gas, and oil is stored in oil storage tank.Specific reality according to the present invention
Example is applied, the temperature of rear oil gas product is reduced to less than 28 degrees Celsius into cooling and clean unit, and portion gas is condensed into liquid
Body.The oil product that obtains further deep processing or directly can be sold, the fixed gas obtained after cooling and purifying outside after liquid separation
It can be used for the heat source of heat accumulating type rotary heat exchanger after preheating.It is possible thereby to significantly reduce energy consumption.
The thermal decomposition of organic wastes system of the above embodiment of the present invention and utilization system pyrolysis organic waste as a result,
Method can bring following advantageous effect：
(1) using fixed gas as heat source, so as to not influence the quality of pyrolysis gas, it is ensured that fixed gas calorific value.
(2) using gas heat carrier, rubbish is heated evenly temperature plateau, and fluctuation range is small, easy to control.
(3) heat storage is commonly used in smoke pre-heating air, and selects heat accumulating type rotating commutator, can be as needed, with one
The burning Indoor Combustion that the fixed gas that partial thermal decomposition generates is set in heat accumulating type rotating commutator provides the heat source of system,
On the one hand, resulting high-temperature flue gas preheats fixed gas that another part pyrolysis generates or other gases (such as hydrogen, CO
Deng) heat source is used as, adaptability is stronger.
(4) other heat exchange mode heat transfer effects are better than using separate unit heat accumulating type rotating commutator heat transfer effect, and
Heat accumulating type rotating commutator exhanst gas outlet adds denitrification apparatus, directly by the use of flue-gas temperature as denitration reaction temperature, structure letter
Single, denitration effect is good, reduces back segment process cost of investment.
Embodiment 1
The somewhere autumn house refuse (garbage raw material analysis data are shown in Table 1) of granularity 5mm~120mm, is connected with 1.6t/h
Continuous to be sent into revolving bed, with fixed gas direct contact heat transfer that temperature is 800 DEG C or so and being pyrolyzed at 680 DEG C, generation is hot
Solid object containing charcoal, oil vapour and combustible gas, obtained hot solids object containing charcoal temperature are cold into cooling system progress for 620 DEG C or so
But heat is recycled, solid object containing charcoal after cooling is sent into storage bin.The oil gas of generation and the fixed gas mixture of heat supply pass through
Multiple oil gas vents draw revolving beds at the top of revolving bed, and temperature is 660 DEG C after the high-temperature oil gas of generation is mixed with fixed gas, is passed through
Oil gas manifold converges each oil gas vent oil gas into cooling and purifying unit.
Beijing area autumn house refuse moisture content is low, and tolerance after cooling is higher, and fixed gas is with 1 as the case may be：
(1~2.4) is divided into two parts, and first as band denitration heat accumulating type rotating commutator burning source of the gas；It is de- that second portion is used for band
The fixed gas heat exchange of nitre heat accumulating type rotating commutator is used, and heat exchange Posterior circle to revolving bed is pyrolyzed heat source gas as rubbish.And
Periodically outwards transport portion fixed gas supply waste heat boiler uses, it is ensured that revolving bed heat uses balance.
Process of the present invention can long-term smooth operation, the yield and main character of obtained thermal decomposition product are shown in Table
2。
Table 1 house refuse raw material (butt) analysis result
Embodiment 2
The somewhere autumn house refuse of granularity 5mm~120mm, is continuously introduced into revolving bed with 1.3t/h, is with temperature
800 DEG C or so of fixed gas direct contact heat transfer is simultaneously pyrolyzed at 660 DEG C, generation hot solids object containing charcoal, tar steam and can
Combustion gas, obtained hot solids object containing charcoal temperature carries out cooling recycling heat for 640 DEG C or so into cooling system, after cooling solid
Body object containing charcoal is sent into storage bin.The oil gas of generation and the fixed gas mixture of heat supply pass through multiple oil gas vents at the top of revolving bed
Revolving bed is drawn, temperature is 650 DEG C after the high-temperature oil gas of generation mix with fixed gas, by oil gas manifold that each oil gas vent is oily
Gas converges into cooling and cleaning system.
Hubei province autumn house refuse moisture content is slightly higher, and tolerance after cooling is relatively low, as the case may be fixed gas with
1：(1~1.8) is divided into two parts, and first portion is used as band denitration heat accumulating type rotating commutator burning source of the gas；Second portion is used for
Fixed gas heat exchange with denitration heat accumulating type rotating commutator is used, and heat exchange Posterior circle to revolving bed is pyrolyzed heat source gas as rubbish.
And periodically outwards transport portion fixed gas supply waste heat boiler uses, it is ensured that revolving bed heat uses balance.
Process of the present invention can long-term smooth operation, the yield and main character of obtained thermal decomposition product are shown in Table
2。
2 data result of table
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 of the present invention or example.In the present specification, schematic expression of the above terms is not
It must be directed to identical embodiment or example.Moreover, particular features, structures, materials, or characteristics described can be any
It is combined in an appropriate manner in a or multiple embodiments or example.In addition, without conflicting with each other, the technology of this field
Different embodiments described in this specification or example and different embodiments or exemplary feature can be combined by personnel
And combination.
Although the embodiment of the present invention has 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, those of ordinary skill in the art within the scope of the invention can be to above-mentioned
Embodiment is changed, changes, replacing and modification.
Claims (9)
1. a kind of thermal decomposition of organic wastes system, which is characterized in that including：
Breaker, the breaker are suitable for the organic waste carrying out break process, and it is former to obtain granular pyrolysis
Material；
Drier, the drier are connected with the breaker and suitable for being carried out to the pyrolysis feed Jing Guo the break process
Drying and processing；
Revolving bed pyrolysis oven, the revolving bed pyrolysis oven are connected with the drier and suitable for being pyrolyzed to the pyrolysis feed
Processing, and there is cloth tray rotatable, for holding the pyrolysis feed, the cloth tray in the revolving bed pyrolysis oven
By the pyrolysis chamber being separated into the revolving bed pyrolysis oven above the cloth tray, the confession below the cloth tray
Hot chamber,
Wherein, there is the through hole of multiple connections pyrolysis chamber and heat supply chamber in the cloth tray,
The heat supply chamber has hot air intake,
The pyrolysis chamber has feed inlet and gas outlet, and the feed inlet is connected with the drier；
Solids treatment device is pyrolyzed, the solid product processing unit is connected with the solid outlet；
Cooling and purifier, the cooling and purifier are connected with the gas outlet, to be produced in the pyrolysis chamber
Raw oil gas product carries out Oil-gas Separation and obtains oil and fixed gas；
Oil storage tank, the oil storage tank are connected with the cooling and purifier；
Heat accumulating type rotary heat exchanger, the heat accumulating type rotary heat exchanger respectively with the cooling and purifier and the revolving bed
The hot air intake of pyrolysis oven is connected, for after the fixed gas is heated for the pyrolysis processing,
The heat accumulating type rotary heat exchanger includes：
Insulation shell, defines chamber in the housing, and the housing has first entrance, first outlet, second entrance and the
Two outlets；
Partition plate, the partition plate are located in the chamber and divide the chamber into accumulation of heat chamber and heat release chamber；
Heat storage, the heat storage are located at the middle part of the heat release chamber and the middle part of accumulation of heat chamber, the heat release chamber it is upper
Portion forms the second outlet, and the second entrance is formed at the lower part of the heat release chamber, and the top of the accumulation of heat chamber is formed
Combustion chamber, combustion chamber are turned on first entrance, and first outlet is formed at the lower part of the accumulation of heat chamber,
Wherein, the first entrance is connected to enter with fixed gas described in receiving portion, described second with the cooling and purifier
Mouth is connected to receive fixed gas described in another part, the second outlet and the hot air intake phase with cooling and purifier
Even.
2. thermal decomposition of organic wastes system according to claim 1, which is characterized in that the heat accumulating type rotary heat exchanger bag
Include denitration catalyst reative cell.
3. thermal decomposition of organic wastes system according to claim 2, which is characterized in that the denitration catalyst reative cell bag
It includes：Ammonia-spraying grid or spray urea grid, ammonia or urea and SCR catalytic reaction chambers.
4. thermal decomposition of organic wastes system according to claim 1, which is characterized in that further comprise：
Smoke eliminator, the smoke eliminator are connected with the drier.
5. thermal decomposition of organic wastes system according to claim 1, which is characterized in that the through hole in the cloth tray is circle
Hole and/or fin square hole, wherein, a diameter of 2~6 millimeters of the circular hole, the long side of the fin square hole is 10~15
Millimeter, broadside are 3~5 millimeters.
6. utilize the method for claim 1-5 any one of them system pyrolysis organic waste, which is characterized in that including：
The organic waste is subjected to break process using the breaker, obtains granular pyrolysis feed；
Drying and processing is carried out to the pyrolysis feed Jing Guo the break process using drier；
By the feed inlet by the pyrolysis feed particle of drying and processing from the pyrolysis chamber of the revolving bed pyrolysis oven
Cloth is carried out in the cloth tray, and hot gas is passed through into the heat supply chamber from the hot air intake, makes the pyrolysis former
Material particle is pyrolyzed, and obtains solid product and oil gas product；
The solid product is handled and collected in the pyrolysis solids treatment device；
The oil gas product is subjected to Oil-gas Separation processing in the cooling and purifier, to obtain oil and fixed gas,
And the oil is stored in the oil storage tank；
In fixed gas described in the combustion chamber Indoor Combustion part of the heat accumulating type rotary heat exchanger or the outer heat released for combustible gas
Amount heats fixed gas described in another part, and the fixed gas after heating is used for the pyrolysis.
7. the method for organic waste is pyrolyzed according to claim 6, which is characterized in that the heat accumulating type rotary heat exchanger
The temperature for being used to heat the high-temperature flue gas of fixed gas after combustion chamber Indoor Combustion is 600~950 degrees Celsius.
8. the method for organic waste is pyrolyzed according to claim 6, which is characterized in that the temperature of the fixed gas after heating
It spends for 550~850 degrees Celsius.
9. the method for organic waste is pyrolyzed according to claim 6, which is characterized in that the pyrolysis is taken the photograph 550~800
When progress 1~3 is small under family name's degree.
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| CN103666491B (en) * | 2013-12-04 | 2015-09-02 | 北京神雾环境能源科技集团股份有限公司 | Rotating bed gas retort |
| CN103756697B (en) * | 2014-01-07 | 2017-01-18 | 北京神雾环境能源科技集团股份有限公司 | Method and system for processing waste and sludge |
| CN104178186B (en) * | 2014-09-09 | 2016-11-02 | 北京神雾环境能源科技集团股份有限公司 | A kind of coal low-temperature carbonization system and method |
| CN204434544U (en) * | 2014-12-26 | 2015-07-01 | 北京神雾环境能源科技集团股份有限公司 | Rotating bed pyrolysis oven and pyrolysis system |
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2014
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