CN105885885A - Organic waste pyrolysis system and application thereof - Google Patents
Organic waste pyrolysis system and application thereof Download PDFInfo
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- CN105885885A CN105885885A CN201610252360.XA CN201610252360A CN105885885A CN 105885885 A CN105885885 A CN 105885885A CN 201610252360 A CN201610252360 A CN 201610252360A CN 105885885 A CN105885885 A CN 105885885A
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- Prior art keywords
- pyrolysis
- gas
- oil gas
- entrance
- semicoke
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Classifications
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- 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
- C10B47/00—Destructive distillation of solid carbonaceous materials with indirect heating, e.g. by external combustion
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G1/00—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/10—Feedstock materials
- C10G2300/1003—Waste materials
Abstract
The invention discloses an organic waste pyrolysis system and a method for disposing organic wastes by the same. The organic waste pyrolysis system comprises a pyrolysis reactor, a screw discharger, a mixing device, a pulverizer and a gasifying and melting furnace. According to the organic waste pyrolysis system, the pyrolysis reactor is used for pyrolysis of organic wastes; the organic wastes are distributed uniformly in the pyrolysis reactor by means of a stirring assembly in the pyrolysis reactor, thus, more sufficient pyrolysis is achieved, oil gas generated in pyrolysis can be released within a shorter time, secondary pyrolysis of the oil gas is suppressed effectively, and yield of pyrolytic tar is increased. Further, semi-coke generated during pyrolysis is mixed with coal and limestone and then subjected to gasifying and melting treatment so that gasified gas with high economic value is obtained.
Description
Technical field
The present invention relates to organic waste pyrolysis system, and the method utilizing this organic waste pyrolysis system process organic waste.
Background technology
Along with the acceleration of China's modernization, it is important that domestic waste has become as fast-developing one of restriction green city
Factor.At present, treatment of urban garbage mode in countries in the world mainly includes that sanitary landfills, burning, compost, pyrolysis and rubbish are combined
Conjunction process etc..And the relevant refuse classification of China, rubbish comprehensive utilization technique are delayed, the main processing ways of current rubbish is for defending
Raw landfill is main, and the mode such as burning, compost is auxiliary.Further, along with scientific and technological progress and the enhancing of environmental consciousness, " burning method "
Destruction and threat the healthy more and more recognized of the mankind that " landfill method " brings to environment arrive.A kind of new
The technology of type is to substitute " burning method " and " landfill method ", to reduce greenhouse gas emission and to eliminate two English pollution problems, just
By in the urgent need to
Refuse pyrolysis treatment technology refer to by rubbish when anaerobic or heating when anoxia, be allowed to decompose.In pyrolytic process,
Its intermediate product trends towards the change that polarises: a kind of be from macromolecular cleavage be the cracking process of little molecule, another kind be little molecule
It is polymerized to the polycondensation process of macromole.Along with the rising of pyrolysis temperature, refuse pyrolysis mainly experience dry (room temperature～200 DEG C),
Dry distilling (～500 DEG C) and gas generate (～1200 DEG C) three phases.In the cold drying stage, outer water contained in rubbish and
The moisture of capillary structure absorption is initially heated evaporation, secondly the constitution water decomposes in material.Evaporation and heat along with moisture
Solving the rising of pyrolysis temperature, refuse pyrolysis enters the dry distilling stage.As long as there is internal water and CO in the dry distilling stage2Precipitation, deoxidation,
Desulfurization etc. are reacted.Along with the continuation of temperature raises, the small-molecule substance generation second pyrolysis that the dry distilling stage produces, refuse pyrolysis enters
Enter gas generation phase, generate second pyrolysis product.Secondary response mainly has cracking, dehydrogenation, polycondensation, hydrogenation, bridged bond
Reaction, water carbon reaction etc..Second pyrolysis reaction primary product includes: H2、CH4, CO etc..
Due to China's Waste sorting method imperfection, cause rubbish composition complex own, often contain kitchen excess, plastics, give up
Used batteries, circuit board etc..Finding the tar ingredients also complex that refuse pyrolysis produces, component analysis finds in tar simultaneously
Containing material in hundreds of, including various organic acid, phenols, ketone, aldehydes, PAHs etc., wherein chlorine element and heavy metal
Element is the most higher, water content about 20%, calorific value about 13～18MJ/Kg, causes stench because sulfide content is high simultaneously,
Comprehensive utilization difficulty is big.Factors causes China's refuse pyrolysis to be difficult to obtain important breakthrough.
Thus, existing refuse pyrolysis equipment haves much room for improvement.
Summary of the invention
It is contemplated that at least solve one of technical problem present in prior art.To this end, it is an object of the present invention to carry
Go out a kind of organic waste pyrolytic reaction system, wherein, pyrolysis reactor has mixing component, make material be distributed in reactor
Uniformly, it is pyrolyzed more fully, and the oil gas that pyrolysis can be made to produce discharges faster, can effectively suppress the second pyrolysis of oil gas,
Improve pyrolytic tar productivity.Further, this pyrolysis reactor utilizes heat accumulation type radiant tube as heating source, does not has heat carrier.And it is hot
Solve the semicoke produced and be mixed into circulation of qi promoting body melt process with coal and limestone, obtain the gasification gas of high economic worth, it is achieved that refuse
Make full use of.
According to an aspect of the present invention, the invention provides a kind of organic waste pyrolysis system.According to embodiments of the invention,
This system includes: pyrolysis reactor, and described pyrolysis reactor includes: organic waste entrance, exhanst gas outlet and semicoke outlet；Institute
State organic waste entrance and be positioned at the top of described pyrolysis reactor；The outlet of described semicoke is positioned at the bottom of described pyrolysis reactor；Store
Hot type radial canal, described heat accumulation type radiant tube is many along the short transverse of described pyrolysis reactor in the inside of described pyrolysis reactor
Layer is arranged, every layer has many heat accumulation type radiant tubes the most parallel to each other；Oil gas derives pipeline, and described oil gas is led
Go out and on the tube wall of pipeline, be provided with through hole；Mixing component, described mixing component includes: rotatable shaft, described shaft
The inside of described pyrolysis reactor it is extend into by the outlet of described semicoke；Multiple puddlers, described puddler is along the length of described shaft
Degree is connected on described shaft, and described puddler is positioned at the interlayer of described heat accumulation type radiant tube；Discharge, described gas collection
Pipe includes gas gathering manifold and the gas-collecting branch pipe being connected with described gas gathering manifold, and wherein, described gas gathering manifold is vertically situated at
Outside described pyrolysis reactor, described gas-collecting branch pipe extends through the sidewall of described pyrolysis reactor and extend into described pyrolysis reactor
In and with described oil gas derive pipeline be connected；Spiral discharging device, described spiral discharging device has discharger entrance and discharger goes out
Mouthful, described discharger entrance exports with the semicoke of described pyrolysis reactor and is connected；Mixing arrangement, described mixing arrangement has semicoke
Entrance, coal entrance, limestone entrance and mixed material outlet, described semicoke entrance and the described discharger of described spiral discharging device
Outlet is connected；Flour mill, described flour mill have mixed material entrance and broken material outlet, wherein, mixed material entrance with
The mixed material outlet of described mixing arrangement is connected；And melting furnace, described melting furnace has gasification and melting material and enters
Mouth, gasifying medium entrance, gasification gas outlet and oxidant inlet, described gasification and melting material inlet is broken with described flour mill
Material outlet is connected.
Organic waste pyrolysis system according to embodiments of the present invention, utilizes this pyrolysis reactor to be pyrolyzed organic waste, pyrolysis
Reactor has mixing component, makes material be evenly distributed in reactor, be pyrolyzed more fully, and pyrolysis can be made to produce
Oil gas discharges faster, can effectively suppress the second pyrolysis of oil gas, improves pyrolytic tar productivity.Further, this pyrolysis reactor
Utilize heat accumulation type radiant tube as heating source, there is no heat carrier.Meanwhile, the semicoke that pyrolysis produces mixes with coal and limestone and carries out
Gasification and melting processes, and obtains the gasification gas of high economic worth, wherein, coal dust and semicoke heat exchange, and the moisture of coal self separates out and is dried,
Limestone then can when gasification solid sulfur, reduce the sulfur content in gasification gas, add limestone in the feed and take off than high-temperature gas
The low cost of sulfur, adds limestone when gasification simultaneously and can reduce ash fusion point, reduce gasification temperature, improve the energy of gasification system
Amount efficiency.
It addition, organic waste pyrolysis system according to the above embodiment of the present invention, it is also possible to have a following additional technical characteristic:
According to embodiments of the invention, described puddler is perpendicular to described shaft, and divides along the length separation of described shaft
Cloth.
According to embodiments of the invention, described puddler adjacent projections on the same cross section of described shaft is certain angle
Degree.
According to embodiments of the invention, described puddler is between the interlayer of described heat accumulation type radiant tube.
According to embodiments of the invention, the angle ranging from 0～90 degree, without end value.
According to embodiments of the invention, the angle ranging from 30～90 degree, without 90 degree.
According to embodiments of the invention, described gas-collecting branch pipe is multiple, and parallel to each other along the length direction of described gas gathering manifold
Arrange.
According to embodiments of the invention, described gas-collecting branch pipe is perpendicular to described gas gathering manifold.
According to embodiments of the invention, described oil gas derives the pipeline short transverse multi-tier arrangement along described pyrolysis reactor, every layer
There are many oil gas the most parallel to each other and derive pipeline.
According to embodiments of the invention, described oil gas is derived pipeline and is arranged in parallel with described heat accumulation type radiant tube, and described heat accumulating type
The respective left and right sides of radial canal is symmetrically arranged with two oil gas and derives pipeline.
According to embodiments of the invention, described oil gas derivation pipeline with the spacing of the tube wall of neighbouring described heat accumulation type radiant tube is
Described oil gas derives 1/2-3 times of pipe diameter d.
According to embodiments of the invention, described oil gas is derived and is provided with multiple through hole on the tube wall of pipeline.Preferred according to the present invention
Embodiment, described through hole is derived at described oil gas and is uniformly distributed on the length direction of pipeline.
According to embodiments of the invention, oil gas described in same layer is derived pipeline and is communicated to same described gas-collecting branch pipe.
According to embodiments of the invention, this system farther includes: disintegrating machine, and described disintegrating machine has broken machine-made egg-shaped or honey-comb coal briquets entrance, breaks
Broken machine limestone entrance, break up coal and limestone outlet, described break up coal is connected with described mixing arrangement with limestone outlet.
According to a further aspect in the invention, the invention provides one utilizes aforesaid organic waste pyrolysis system to process organic waste
Method.According to embodiments of the invention, the method includes: to pyrolysis reactor, organic waste supply is carried out pyrolysis processing,
To obtain being pyrolyzed oil gas and semicoke, wherein, a part for described pyrolysis gas is transported to the heat accumulating type in described pyrolysis reactor
Radial canal, as fuel, thinks that described pyrolysis provides heat；Spiral discharging device is utilized to supply described semicoke to mixing arrangement, and
Carry out combination drying with coal dust and limestone, in order to obtain the mixed material being dried, effectively utilize semicoke heat simultaneously；By described
The mixed material supply being dried carries out pulverization process to flour mill, in order to obtaining material powders, the particle diameter of described material powders is
200～500 μm；And the supply of described material powders is carried out gasification and melting process to melting furnace, in order to obtain gasifying gas and
Molten ash.
The method processing organic waste according to embodiments of the present invention, utilizes aforesaid pyrolysis reactor that organic waste is carried out heat
Solving, owing to having mixing component in pyrolysis reactor, material is more evenly distributed in reactor, and pyrolysis is more abundant, and pyrolysis produces
Oil gas discharge faster, can effectively suppress the second pyrolysis of oil gas, improve pyrolytic tar productivity.Further, this pyrolytic reaction
Device utilizes heat accumulation type radiant tube as heating source, does not has heat carrier, simple to operate.Meanwhile, it is pyrolyzed the semicoke produced and coal and stone
Lime stone is mixed into circulation of qi promoting melt process, obtains the gasification gas of high economic worth, wherein, coal dust and semicoke heat exchange, coal self
Moisture separates out and is dried, limestone then can when gasification solid sulfur, reduce the sulfur content in gasification gas, add Calx in the feed
Stone, than the low cost of high-temperature gas desulfurization, adds limestone when gasification simultaneously and can reduce ash fusion point, reduce gasification temperature, carry
The energy efficiency of high gasification system.
Mass ratio according to embodiments of the invention, described semicoke and described coal dust gross mass Yu described limestone is (5-200):
1。
According to embodiments of the invention, the temperature of described dry mixed material is not higher than 150 DEG C, and calorific value is not less than
15GJ/Kg。
According to embodiments of the invention, the temperature that described gasification and melting processes is 1100～1500 degrees Celsius.
According to embodiments of the invention, the method farther includes: before described combination drying, utilizes disintegrating machine by described coal dust
Carry out break process with described limestone, in order to the coal dust after being crushed and broken after limestone.
The additional aspect of the present invention and advantage will part be given in the following description, and part will become bright from the following description
Aobvious, or recognized by the practice of the present invention.
Accompanying drawing explanation
Above-mentioned and/or the additional aspect of the present invention and advantage the accompanying drawings below description to embodiment will be apparent from from combining and
Easy to understand, wherein:
Fig. 1 shows the structural representation of the most organic pyrolytic reaction system；
Fig. 2 shows the structural representation of pyrolysis reactor according to an embodiment of the invention；
Fig. 3 shows the structural representation of local pyrolysis reactor according to an embodiment of the invention；
Fig. 4 shows the structural representation of the most organic pyrolytic reaction system；
Fig. 5 shows the stream of the method utilizing organic waste pyrolysis system process organic waste according to an embodiment of the invention
Journey schematic diagram；
Fig. 6 shows the stream of the method utilizing organic waste pyrolysis system process organic waste according to an embodiment of the invention
Journey schematic diagram.
Detailed description of the invention
Embodiments of the invention are described below in detail, and the example of described embodiment is shown in the drawings, the most identical or
Similar label represents same or similar element or has the element of same or like function.Describe below with reference to accompanying drawing
Embodiment is exemplary, is only used for explaining the present invention, and is not considered as limiting the invention.
In describing the invention, term " longitudinally ", " laterally ", " on ", D score, "front", "rear", "left", "right",
The orientation of the instruction such as " vertically ", " level ", " top ", " end " or position relationship are to close based on orientation shown in the drawings or position
System, is for only for ease of the description present invention rather than requires that therefore the present invention can not must manage with specific azimuth configuration and operation
Solve as limitation of the present invention.
Organic waste pyrolysis system
According to an aspect of the present invention, the invention provides a kind of organic waste pyrolysis system.With reference to Fig. 1, according to the present invention
Embodiment, this organic waste pyrolysis system is explained, wherein, in figure, the direction of arrow represents the direction of Flow of Goods and Materials,
This system includes: pyrolysis reactor 100, spiral discharging device 600, mixing arrangement 200, flour mill 300 and melting furnace
400。
According to embodiments of the invention, pyrolysis reactor is also referred to as " reactor " in this article, with reference to Fig. 2, according to this
Bright embodiment, explains the structure of this reactor, and this reactor includes:
Organic waste entrance 111, exhanst gas outlet 114 and semicoke outlet 113, wherein, organic waste entrance 111 is positioned at pyrolysis
The top of reactor 100, semicoke outlet 113 is positioned at the bottom of pyrolysis reactor 100.In some embodiments of the invention,
It is to be understood that this pyrolysis reactor has housing 110, restriction pyrolytic reaction space in this housing, organic waste entrance 111,
Exhanst gas outlet 114 and semicoke outlet 113 are arranged on housing, and wherein, organic waste entrance 111 is positioned at the top of housing 110,
Semicoke outlet 113 is positioned at the bottom of housing 110.Thus, organic waste entrance is positioned at the top of pyrolysis reactor, it is simple to rubbish
Entering from the one end in pyrolytic reaction space, the other end is discharged, and is fully pyrolyzed, and semicoke outlet is positioned at the bottom of housing, just
Discharge in semicoke.According to embodiments of the invention, this pyrolysis reactor 100 can also have and helps fuel gas inlet 115 and fuel gas
Entrance 116, provides fuel for pyrolysis processing.
Heat accumulation type radiant tube 120, is also referred to as " radial canal " in this article, and this heat accumulation type radiant tube 120 is anti-in described pyrolysis
Answering the short transverse multi-tier arrangement along described pyrolysis reactor inside device, every layer has many storages the most parallel to each other
Hot type radial canal 120.Thus, use radial canal to have heat storage, fuel and the air preheat of combustor, the row of reducing will be entered
Cigarette temperature, the thermal efficiency is high, and, use septate heat transfer technique, the component of rubbish is changed insensitive, makes this pyrolysis reactor
Be suitable to the pyrolysis of various garbage.
Mixing component 130, this mixing component includes: rotatable shaft 132 and multiple puddler 131, wherein, stirring
Axle 132 is extend into the inside of pyrolysis reactor by semicoke outlet 113；Puddler 131 connects respectively along the length of shaft 132
On shaft 132, puddler 131 is positioned at the interlayer of heat accumulation type radiant tube 120.Thus, material enters through organic waste entrance
After entering in pyrolysis reactor, puddler is during carrying out back rotation so that stacking material is loosened, and increases stacking material
Between voidage, reduce pyrolysis oil gas through material bed pressure drop so that the pyrolysis oil gas of generation can pass rapidly through material bed row
Go out.
Oil gas derives pipeline 140, and this oil gas is derived and is provided with through hole on the tube wall of pipeline 140.Thus, it is simple to oil gas is derived.
Discharge 150, this discharge includes gas gathering manifold 152 and the gas-collecting branch pipe 151 being connected with gas gathering manifold 152,
Wherein, gas gathering manifold 152 is vertically situated at outside pyrolysis reactor, it is understood that for being vertically situated at outside housing 110
Portion, gas-collecting branch pipe 151 extends through the sidewall of pyrolysis reactor, the i.e. sidewall of housing 110, extend into the heat of pyrolysis reactor
In solution reaction compartment, it is understood that in housing 110, and derive pipeline 140 with oil gas and be connected.Thus, gas collection is utilized
Pyrolysis oil gas is quickly derived by pipe, can effectively suppress the secondary response of oil gas, improves tar yield.
According to a particular embodiment of the invention, every layer of radial canal 120 include multiple parallel and equally distributed radial canal 120 and
Each radial canal 120 is parallel with each radial canal 120 in adjacent upper and lower two-layer radial canal 120 and high along reactor body
Degree direction is in staggered distribution.Thus, it is possible to significantly improve the pyrolysis efficiency of material, and then improve pyrolysis oil productivity.
According to embodiments of the invention, heat accumulation type radiant tube 120 is made up of heat accumulating type honeycomb ceramics and radial canal.Thus, profit
To enter fuel and the air preheat of combustor with heat accumulating type honeycomb ceramics, and reduce exhaust gas temperature, the thermal efficiency is high.
According to a particular embodiment of the invention, oil gas derives pipeline 140 along the short transverse multi-tier arrangement of pyrolysis reactor, every layer
There are many oil gas the most parallel to each other and derive pipeline 140, the surface of oil gas derivation pipeline 140 is provided with logical
Hole；Oil gas is derived pipeline 140 and is connected with discharge 150, and discharge 150 is connected with oil gas vent.Thus, by spoke
Penetrate pipe lower end and arrange that oil gas is derived pipeline and reduced the tar time of staying in burner hearth, it is to avoid the second pyrolysis of tar, improve tar
Productivity.According to a particular embodiment of the invention, oil gas is derived pipeline 140 and is arranged in parallel with radial canal 120, and radial canal 120
The left and right sides be symmetrically arranged with two oil gas and derive pipelines 140.Thus, by arranging oil gas delivery line in the both sides of radial canal
Road decreases the tar time of staying in burner hearth, it is to avoid the second pyrolysis of tar, improves tar yield.
According to embodiments of the invention, oil gas is derived pipeline 140 and is symmetrical set in the lower section of each heat accumulation type radiant tube 120.
Thus, it is simple to oil gas is derived, and decreases the tar time of staying in burner hearth, it is to avoid the second pyrolysis of tar, improve tar to produce
Rate.
According to embodiments of the invention, oil gas derivation pipeline 140 is not particularly limited with the connected mode of oil gas vent 112,
According to a particular embodiment of the invention, the oil gas of same layer is derived pipeline 140 and is connected to same oil gas vent 112.According to this
Some specific embodiments of invention, the oil gas of adjacent two layers or more layers is derived pipeline 140 and is connected to same oil gas vent 112.
Thus, it is possible to collected by oil gas, Simplified flowsheet also improves tar yield, simultaneously can be so that oil gas is derived.
According to a particular embodiment of the invention, oil gas derives pipeline 140 with the spacing of the tube wall of neighbouring radial canal 120 is oily
1/2-3 times of gas delivery line road 120 caliber d.Thus, it is possible to the tar that generation will be derived at once, it is to avoid coke tar cracking, carry
High tar yield.
According to embodiments of the invention, discharge 150 includes: gas-collecting branch pipe 151 and gas gathering manifold 152, wherein, gas collection is total
Pipe 152 is derived pipeline 140 by multiple gas-collecting branch pipes 151 with multilamellar oil gas and is connected.Thus, the pyrolysis oil gas warp that pyrolysis produces
Discharge and gas gathering manifold are derived, and can effectively suppress the secondary response of oil gas, improve tar yield.
According to a particular embodiment of the invention, mixing component 130 include shaft 132 and be connected on shaft 132 multiple
Puddler 131, shaft 132 drives puddler 131 to rotate.According to a particular embodiment of the invention, shaft 132 can
To rotate under the driving of motor.According to a particular embodiment of the invention, shaft 132 rotatably exports 112 from semicoke
It extend in the reaction compartment of pyrolysis reactor 100.Thus, by arranging mixing component, puddler in pyrolysis reactor
During carrying out back rotation so that stacking material is loosened, increase the voidage between stacking material, reduce pyrolysis
Oil gas is through material bed pressure drop so that the pyrolysis oil gas of generation can pass rapidly through material bed discharge.
A specific embodiment according to the present invention, multiple puddlers 131 are perpendicular to shaft 132, and along shaft 132
Length separation distribution.Thus, it is possible to make puddler effectively loosen inside reactor material, such that it is able to significantly improve heat
Solve the derivation rate of oil gas.
According to another specific embodiment of the present invention, on the shaft section of shaft 132, being projected in of multiple puddler 131
The length separation of shaft 132 opens distribution.Thus, it is possible to make puddler effectively loosen inside reactor material, thus enter
One step improves the derivation rate of pyrolysis oil gas.
According to another specific embodiment of the present invention, as it is shown on figure 3, puddler 131 is at the same cross section of shaft 132
On projection at an angle, this angle is 0～90 degree (without end value), preferably 30～90 degree (without 90 degree).Thus,
So that puddler loosens inside reactor material effectively, thus improve the derivation rate of pyrolysis oil gas further.According to this
Another bright specific embodiment, on the shaft section of shaft 132, multiple puddlers 131 be projected in shaft 132
Distribution it is evenly spaced apart in circumference.According to the concrete example of the present invention, on the shaft section of shaft 132, multiple puddlers
In the projection of 131, the adjacent angle theta between two puddlers 131 can be 0～90 degree (without end value), preferably 30～90
Degree (without 90 degree).Thus, it is possible to make puddler effectively loosen inside reactor material, thus improve pyrolysis further
The derivation rate of oil gas.
According to some specific embodiments of the present invention, the length of shaft 132 can be 1-18m, and detachable puddler 131 is vertical
Spacing can be 0.4-1m, and the number of plies of puddler 131 can be 11-26 layer.
According to some embodiments of the present invention, puddler 131 is between the interlayer of heat accumulation type radiant tube 120.Thus, it is possible to effectively
Ground loosens inside reactor material, thus improves the derivation rate of pyrolysis oil gas further, avoids tying on heat accumulation type radiant tube simultaneously
Burnt, it is ensured that equipment is properly functioning.
According to some embodiments of the present invention, this system includes spiral discharging device 600, and this spiral discharging device 600 has discharger
Entrance and discharger outlet, wherein, discharger entrance exports 113 with the semicoke of pyrolysis reactor 100 and is connected.Thus, utilize
The semicoke that pyrolysis is produced by spiral discharging device is discharged.
With reference to Fig. 1, according to embodiments of the invention, this system also includes: mixing arrangement 200, flour mill 300 and gasification are molten
Melting stove 400, this mixing arrangement 200 has semicoke entrance 201, coal and limestone entrance 203 and mixed material outlet 202,
Wherein, semicoke entrance 201 exports with the discharger of spiral discharging device 600 and is connected, and semicoke is delivered to mix by spiral discharging device 600
Locking device 200, mixes with coal dust and limestone in mixing arrangement 200, obtains mixed material, in mixed process, and coal dust
With semicoke heat exchange, the moisture of coal self separates out and is dried.Limestone then can consolidate sulfur when gasification, and the sulfur reduced in gasification gas contains
Measure, add the limestone low cost than high-temperature gas desulfurization in the feed, add limestone simultaneously when gasification and can reduce grey molten
Point, reduces gasification temperature, improves the energy efficiency of gasification system.Flour mill 300 has mixed material entrance 301 and broken thing
Material outlet 302, wherein, mixed material entrance 301 exports 202 with the mixed material of mixing arrangement 200 and is connected, for mixed
Compound material carries out break process, obtains material powders, and the particle diameter of mixed material reduces, it is simple to follow-up gasification and melting processes, fall
The temperature and time that low gasification and melting processes；Melting furnace 400 has gasification and melting material inlet 403, gasifying medium entrance
401, oxidant inlet 402, gasification gas outlet 404, wherein, gasification and melting material inlet 403 is broken with flour mill 300
Material outlet 302 is connected, utilize garbage filter concentrated solution and partial air as gasifying medium, with above-mentioned mixed material as raw material,
Carry out gasification and melting reaction, produce gasification gas and molten ash.Hereby it is achieved that the making full use of of refuse.
With reference to Fig. 4 according to embodiments of the invention, this system farther includes: disintegrating machine 500, and this disintegrating machine 500 has broken
Broken machine-made egg-shaped or honey-comb coal briquets entrance 501, disintegrating machine limestone entrance 502 and break up coal and limestone outlet 503, wherein, break up coal and stone
Lime stone outlet 503 is connected with coal and the limestone entrance 203 of mixing arrangement 200.For the coal of bulk and limestone are broken
Broken process, obtains coal and limestone particle, and the average diameter of particles after crushing is 8-12mm, it is simple to follow-up powder process processes.
According to a particular embodiment of the invention, this system farther includes: hopper 800 and feeding screw 900.Hopper 800
Having charging aperture and discharging opening, hopper 800 is used for depositing organic waste；Feeding screw 900 has feeder entrance and charging
Device exports, and wherein, feeder entrance is connected with discharging opening, feeder entrance and the pyrolysis garbage inlet of pyrolysis reactor 100
111 are connected, and feeding screw 900 is for being delivered to pyrolysis reactor by the rubbish in hopper.
Organic waste pyrolysis system according to embodiments of the present invention, utilizes this pyrolysis reactor to be pyrolyzed organic waste, pyrolysis
Reactor has mixing component, makes material be evenly distributed in reactor, be pyrolyzed more fully, and pyrolysis can be made to produce
Oil gas discharges faster, can effectively suppress the second pyrolysis of oil gas, improves pyrolytic tar productivity.Further, this pyrolysis reactor
Utilize heat accumulation type radiant tube as heating source, there is no heat carrier.Meanwhile, the semicoke that pyrolysis produces mixes with coal and limestone, profit
Carrying out gasification and melting process with gas fusion stove, obtain the gasification gas of high economic worth, wherein, coal dust and semicoke heat exchange, coal is certainly
The moisture of body separates out and is dried, limestone then can when gasification solid sulfur, reduce the sulfur content in gasification gas, add in the feed
Limestone, than the low cost of high-temperature gas desulfurization, adds limestone when gasification simultaneously and can reduce ash fusion point, reduce gasification temperature,
Improve the energy efficiency of gasification system.
The method processing organic waste
According to a further aspect in the invention, the invention provides one utilizes aforesaid organic waste pyrolysis system to process organic waste
Method.With reference to Fig. 5, according to embodiments of the invention, the method includes:
S100 pyrolysis processing
According to embodiments of the invention, organic waste supply is carried out pyrolysis processing to pyrolysis reactor, obtain being pyrolyzed oil gas and
Semicoke, wherein, the heat accumulation type radiant tube that a part for pyrolysis gas is transported in pyrolysis reactor, as fuel, thinks described heat
Solve and heat is provided.Utilize aforesaid pyrolysis reactor that organic waste is pyrolyzed, owing to pyrolysis reactor having mixing component,
Material is more evenly distributed in reactor, and pyrolysis is more abundant, and the oil gas that pyrolysis produces discharges faster, can effectively suppress oil gas
Second pyrolysis, improve pyrolytic tar productivity.Further, this pyrolysis reactor utilizes heat accumulation type radiant tube as heating source, does not has
Heat carrier, simple to operate.
S200 combination drying
According to embodiments of the invention, utilize spiral discharging device by described semicoke supply to mixing arrangement, and with coal dust and limestone
Carry out combination drying, in order to obtain the mixed material being dried, effectively utilize semicoke heat simultaneously.Thus, in mixing arrangement with
Coal dust and limestone mixing, obtain mixed material, and in mixed process, coal dust and semicoke heat exchange, the moisture of coal self separates out dry
Dry, mixed material is lowered the temperature.Limestone then can consolidate sulfur when gasification, reduces the sulfur content in gasification gas, adds in the feed
Limestone, than the low cost of high-temperature gas desulfurization, adds limestone when gasification simultaneously and can reduce ash fusion point, reduce gasification temperature,
Improve the energy efficiency of gasification system.
Mass ratio according to embodiments of the invention, semicoke and coal dust gross mass with limestone can contain according to the sulfur of semicoke and coal dust
Amount and ash fusion point are adjusted.Mass ratio according to some embodiments of the present invention, semicoke and coal dust gross mass with limestone is
(5-200): 1.According to embodiments of the invention, add limestone and make ash melting point low, to service life of gasification furnace and
Energy efficiency is all useful, and meanwhile, in gasification gas, sulfur content is low, and the quality of gasification gas is more preferably.
According to embodiments of the invention, the particle diameter of coal dust is 8-12mm.According to a preferred embodiment of the invention, the particle diameter of coal dust
For 10mm.
According to embodiments of the invention, the particle diameter of limestone is 8-12mm.According to a preferred embodiment of the invention, limestone
Particle diameter is 10mm.
According to embodiments of the invention, the temperature of dry mixed material is not higher than 150 DEG C, and calorific value is not less than 15GJ/Kg.
Thus, the mixed material temperature being dried is not higher than 150 degrees Celsius, can be effectively prevented material and catch fire, it is ensured that the safety of production
Property, and calorific value is not less than 15GJ/Kg, beneficially provides enough energy for follow-up gasification and melting.
S300 pulverization process
According to embodiments of the invention, described dry mixed material supply is carried out pulverization process to flour mill, in order to obtain thing
Material powder, the particle diameter of described material powders is 200～500 μm.Thus, mixed material is carried out break process, the particle diameter of material
Reduce, it is simple to follow-up gasification and melting processes, reduce the temperature and time that gasification and melting processes.
S400 gasification and melting processes
According to embodiments of the invention, material powders supply is carried out gasification and melting process to melting furnace, obtain gasifying gas and
Molten ash.
According to embodiments of the invention, the temperature that described gasification and melting processes is 1100～1500 degrees Celsius.Thus, gas fusion
The temperature processed is low, the energy-conservation energy.
The method processing organic waste according to embodiments of the present invention, utilizes aforesaid pyrolysis reactor that organic waste is carried out heat
Solving, owing to having mixing component in pyrolysis reactor, material is more evenly distributed in reactor, and pyrolysis is more abundant, and pyrolysis produces
Oil gas discharge faster, can effectively suppress the second pyrolysis of oil gas, improve pyrolytic tar productivity.Further, this pyrolytic reaction
Device utilizes heat accumulation type radiant tube as heating source, does not has heat carrier, simple to operate.Meanwhile, it is pyrolyzed the semicoke produced and coal and stone
Lime stone is mixed into circulation of qi promoting melt process, obtains the gasification gas of high economic worth, wherein, coal dust and semicoke heat exchange, coal self
Moisture separates out and is dried, limestone then can when gasification solid sulfur, reduce the sulfur content in gasification gas, add Calx in the feed
Stone, than the low cost of high-temperature gas desulfurization, adds limestone when gasification simultaneously and can reduce ash fusion point, reduce gasification temperature, carry
The energy efficiency of high gasification system.
With reference to Fig. 6, according to embodiments of the invention, the method farther includes:
S500 break process
According to embodiments of the invention, before described combination drying, disintegrating machine is utilized described coal dust and described limestone to be broken
Broken process, in order to the coal dust after being crushed and broken after limestone.According to some embodiments of the present invention, the coal after crushing
Powder and broken after the average diameter of limestone be 8-12mm, it is simple to follow-up powder process processes.
Below with reference to specific embodiment, the present invention will be described, it should be noted that these embodiments are merely illustrative,
And be not considered as limiting the invention.
Embodiment 1
With certain domestic waste and Fujian Tian Hushan coal as raw material, this house refuse is processed, wherein, house refuse
Component analysis is as shown in table 1 below, and rubbish water content is 46%, and the component analysis of Fujian Tian Hushan coal is as shown in table 2 below, specifically
Processing method is as follows:
Table 1
Table 2
(1) marching into the arena rubbish pretreatment, big particle diameter dregs, glass and the metal etc. contained in the rubbish after marching into the arena are difficult to pyrolysis
Or the material that can not be pyrolyzed is rejected in advance；
(2) rubbish after rejecting being difficult to pyrogen delivers to garbage pyrolysis furnace after being fed directly to sanitary fill compression dehydration, enters
Row pyrolysis, controls the ignition temperature in pyrolysis oven combustor, it is ensured that pyrolysis indoor temperature is about 750 DEG C, controls refuse pyrolysis
Furnace bottom discharging revolution speed of screw so that rubbish mean residence time～1h, the refuse pyrolysis charcoal that pyrolysis obtains is through bottom discharge spiral
Discharge pyrolysis oven；
(3) refuse pyrolysis charcoal, Fujian Tian Hushan anthracite, limestone are mixed powder process with the ratio of ratio 59.1:32.4:8.5,
The compound mean diameter prepared～300 μm；
(4) feeding the mixture into melting furnace gasification, gasifying agent uses percolate and partial air, melting furnace
Temperature 1380 DEG C, in melting furnace, rubbish charcoal, coal react with gasifying agent generating gasification, generate gasification gas and liquid glass
Glass body lime-ash, wherein, building sand after the recovered noble metal of liquid lime-ash；
(5) the pyrolysis oil gas that pyrolysis oven pyrolysis produces is after Oil-gas Separation, obtains high-quality pyrolytic tar ,～the pyrolysis gas of 70% enters
Pyrolysis oven burning is pyrolysis offer ability ,～30% the gentle activating QI of pyrolysis gas is blended and the laggard gas turbine combustion of preliminary purification
Generating.
Lime-ash is analyzed: the two non-1.3ng-TEQ/kg of English content in chilling slag, Pb Leaching value is 0.2013mg/L, Cr
Leaching value be 0.387mg/L, Cd Leaching value be 0.147mg/L, remaining does not detects, meet about hazardous waste leach
Toxicity judging standard.
Embodiment 2
With certain domestic waste and Fujian Tian Hushan coal as raw material, this house refuse is processed, wherein, house refuse
Component analysis is as shown in table 3 below, and rubbish water content is 53%, and the component analysis of Fujian Tian Hushan coal is as shown in table 4 below, specifically
Processing method is as follows:
Table 3
| Project | Fabric | Plastics | Paper | Timber | More than kitchen | Dregs | Glass, metal | Amount to |
| House refuse | 4.11 | 26.21 | 15.78 | 3.98 | 20.21 | 14.22 | 15.49 | 100 |
Table 4
(1) marching into the arena rubbish pretreatment, big particle diameter dregs, glass and the metal etc. contained in the rubbish after marching into the arena are difficult to pyrolysis
Or the material that can not be pyrolyzed is rejected in advance；
(2) rubbish after rejecting being difficult to pyrogen delivers to garbage pyrolysis furnace after being fed directly to sanitary fill compression dehydration, enters
Row pyrolysis, controls the ignition temperature in pyrolysis oven combustor, it is ensured that pyrolysis indoor temperature is about 700 DEG C, controls refuse pyrolysis
Furnace bottom discharging revolution speed of screw so that rubbish mean residence time～1h, the refuse pyrolysis charcoal that pyrolysis obtains is through bottom discharge spiral
Discharge pyrolysis oven；
(3) pyrolytic carbon, Yangquan Shanxi anthracite, limestone are mixed powder process with the ratio of ratio 53.2:37.9:8.9, prepare
Compound mean diameter～400 μm；
(4) feeding the mixture into melting furnace gasification, gasifying agent uses percolate and partial air, melting furnace
Temperature 1420 DEG C, in melting furnace, rubbish charcoal and the reaction of coal generating gasification, generate gasification gas and liquid lime-ash, liquid
Building sand after the recovered noble metal of lime-ash；
(5) the pyrolysis oil gas that pyrolysis oven pyrolysis produces is after Oil-gas Separation, obtains high-quality pyrolytic tar ,～the pyrolysis gas of 80% enters
Pyrolysis oven burning is pyrolysis offer ability ,～20% the gentle activating QI of pyrolysis gas is blended and the laggard gas turbine combustion of preliminary purification
Generating.
Lime-ash is analyzed: the two non-1.1ng-TEQ/kg of English content in chilling slag, Pb Leaching value is 0.2375mg/L, Cr
Leaching value be 0.409mg/L, Cd Leaching value be 0.185mg/L, Hg Leaching value be 0.024mg/L, remaining is not
Detection, meets about Extraction Toxicity Identification Standard of Hazardous Waste.
In the description of this specification, reference term " embodiment ", " some embodiments ", " example ", " concrete example ",
Or specific features, structure, material or the feature bag that the description of " some examples " etc. means to combine this embodiment or example describes
It is contained at least one embodiment or the example of the present invention.In this manual, the schematic representation of above-mentioned term is not necessarily referred to
Be identical embodiment or example.And, the specific features of description, structure, material or feature can be at any one
Or multiple embodiment or example combine in an appropriate manner.
Although an embodiment of the present invention has been shown and described, it will be understood by those skilled in the art that: without departing from this
These embodiments can be carried out multiple change in the case of the principle of invention and objective, revise, replace and modification, the present invention's
Scope is limited by claim and equivalent thereof.
Claims (10)
1. an organic waste pyrolysis system, it is characterised in that including:
Pyrolysis reactor, described pyrolysis reactor includes:
Organic waste entrance, exhanst gas outlet and semicoke outlet；Described organic waste entrance is positioned at the top of described pyrolysis reactor
Portion；The outlet of described semicoke is positioned at the bottom of described pyrolysis reactor；
Heat accumulation type radiant tube, described heat accumulation type radiant tube in the inside of described pyrolysis reactor along described pyrolysis reactor
Short transverse multi-tier arrangement, every layer has many heat accumulation type radiant tubes the most parallel to each other；
Oil gas derives pipeline, and described oil gas is derived and is provided with through hole on the tube wall of pipeline；
Mixing component, described mixing component includes:
Rotatable shaft, described shaft is extend into the inside of described pyrolysis reactor by the outlet of described semicoke；
Multiple puddlers, described puddler is connected on described shaft along the length of described shaft, described
Puddler is positioned at the interlayer of described heat accumulation type radiant tube；
Discharge, described discharge includes gas gathering manifold and the gas-collecting branch pipe being connected with described gas gathering manifold, wherein,
Described gas gathering manifold is vertically situated at outside described pyrolysis reactor, and described gas-collecting branch pipe extends through described pyrolysis reactor
In sidewall extend into described pyrolysis reactor and derive pipeline with described oil gas to be connected；
Spiral discharging device, described spiral discharging device has discharger entrance and discharger outlet, described discharger entrance and described heat
The semicoke outlet solving reactor is connected；
Mixing arrangement, described mixing arrangement has semicoke entrance, coal and limestone entrance and mixed material outlet, and described semicoke enters
Mouth exports with the described discharger of described spiral discharging device and is connected；
Flour mill, described flour mill has mixed material entrance and broken material outlet, and described mixed material entrance mixes with described
The described mixed material outlet of device is connected；And
Melting furnace, described melting furnace has gasification and melting material inlet, gasifying medium entrance, gasification gas outlet and oxygen
Agent entrance, described gasification and melting material inlet exports with the broken material of described flour mill and is connected.
System the most according to claim 1, it is characterised in that described puddler is perpendicular to described shaft, and edge
The length separation distribution of described shaft,
Optionally, described puddler adjacent projections on the same cross section of described shaft at an angle,
Optionally, described puddler between the interlayer of described heat accumulation type radiant tube,
Optionally, the angle ranging from 0～90 degree, without end value,
Optionally, the angle ranging from 30～90 degree, without 90 degree.
System the most according to claim 1 and 2, it is characterised in that described gas-collecting branch pipe is multiple, and along described
The length direction of gas gathering manifold is arranged parallel to each other,
Optional, described gas-collecting branch pipe is perpendicular to described gas gathering manifold.
4. according to the system according to any one of claim 1-3, it is characterised in that described oil gas derives pipeline along described heat
Solving the short transverse multi-tier arrangement of reactor, every layer has many oil gas the most parallel to each other and derives pipeline,
Optional, described oil gas is derived pipeline and is arranged in parallel with described heat accumulation type radiant tube, and described heat accumulation type radiant tube is respective
The left and right sides is symmetrically arranged with two oil gas and derives pipeline,
Optionally, the spacing of the tube wall that described oil gas derives pipeline and neighbouring described heat accumulation type radiant tube is that described oil gas is derived
1/2-3 times of pipe diameter d,
Optional, described oil gas is derived and is provided with multiple through hole on the tube wall of pipeline, it is preferable that described through hole is led at described oil gas
Go out and be uniformly distributed on the length direction of pipeline,
Optional, oil gas described in same layer is derived pipeline and is communicated to same described gas-collecting branch pipe.
5. according to the system according to any one of claim 1-4, it is characterised in that farther include:
Disintegrating machine, described disintegrating machine has broken machine-made egg-shaped or honey-comb coal briquets entrance, disintegrating machine limestone entrance and break up coal and limestone outlet,
Described break up coal is connected with described coal and the limestone entrance of described mixing arrangement with limestone outlet.
6. utilizing the method that the organic waste pyrolysis system described in any one of claim 1-5 processes organic waste, it is special
Levy and be, including:
Organic waste supply is carried out pyrolysis processing to pyrolysis reactor, in order to obtain being pyrolyzed oil gas and semicoke, wherein, described
A part for pyrolysis gas is transported to the heat accumulation type radiant tube in described pyrolysis reactor as fuel, thinks that described pyrolysis processing carries
Heating load；
Utilize spiral discharging device to supply described semicoke to mixing arrangement, and carry out combination drying with coal dust and limestone, in order to
To the mixed material being dried, effectively utilize semicoke heat simultaneously；
Described dry mixed material supply is carried out pulverization process to flour mill, in order to obtain material powders, described material powders
Particle diameter be 200～500 μm；And
The supply of described material powders is carried out gasification and melting process to melting furnace, in order to obtain gasify gas and molten ash.
Method the most according to claim 6, it is characterised in that the gross mass of described semicoke and described coal dust and described stone
The mass ratio of lime stone is (5-200): 1.
8. according to the method described in claim 6 or 7, it is characterised in that the temperature of described dry mixed material is not higher than
150 DEG C, and calorific value is not less than 15GJ/Kg.
9. according to the method described in any one of claim 6-8, it is characterised in that the temperature that described gasification and melting processes is
1100～1500 degrees Celsius.
10. according to the method described in any one of claim 6-9, it is characterised in that farther include:
Before described combination drying, utilize disintegrating machine that described coal dust and described limestone are carried out break process, in order to be crushed
After coal dust and broken after limestone.
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