CN105885884A - Organic waste pyrolysis system and application thereof - Google Patents
Organic waste pyrolysis system and application thereof Download PDFInfo
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- CN105885884A CN105885884A CN201610252359.7A CN201610252359A CN105885884A CN 105885884 A CN105885884 A CN 105885884A CN 201610252359 A CN201610252359 A CN 201610252359A CN 105885884 A CN105885884 A CN 105885884A
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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
- 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
- C10G1/002—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal in combination with oil conversion- or refining processes
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
- C10J3/58—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels combined with pre-distillation of the fuel
- C10J3/60—Processes
- C10J3/64—Processes with decomposition of the distillation products
- C10J3/66—Processes with decomposition of the distillation products by introducing them into the gasification zone
-
- 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
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J2300/00—Details of gasification processes
- C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
- C10J2300/0913—Carbonaceous raw material
- C10J2300/093—Coal
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J2300/00—Details of gasification processes
- C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
- C10J2300/0913—Carbonaceous raw material
- C10J2300/0943—Coke
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 gas and liquid separating tower, a purifier and a gas turbine. 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; besides, the pyrolysis reactor adopts a regenerative radiant tube as a heating source, and is free of heat carrier. Further, pyrolytic oil gas is separated by the gas and liquid separating tower to produce tar and fuel gas; the fuel gas supplies fuel for power generation for the gas turbine; thus, effectively comprehensive utilization of energy is achieved.
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 pyrolysis oil gas that pyrolysis can be made to produce discharges faster, can effectively suppress to be pyrolyzed oil gas
Second pyrolysis, improves pyrolytic tar productivity.Further, this pyrolysis reactor utilizes heat accumulation type radiant tube as heating source, does not has heat
Carrier.And it being pyrolyzed the pyrolysis oil gas of generation through gas-liquid separation tower isolated tar and combustion gas, combustion gas is for providing for gas turbine
Fuel generates electricity, it is achieved the comprehensive utilization of the energy.
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: pyrolysis garbage inlet, exhanst gas outlet and semicoke outlet；Institute
State pyrolysis garbage inlet 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；Gas-liquid separation tower, described gas-liquid separation tower has oil gas entrance, pyrolysis oil outlet
And gas outlet, described oil gas entrance is connected with described discharge；Depurator, described alembic have gas access to be clean and
Purified gas outlet, described gas access to be clean is connected with described gas outlet；And gas turbine, described gas turbine has
Fuel inlet, described fuel inlet is had to be connected with the described purified gas outlet of described depurator.
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 pyrolysis oil gas that pyrolysis produces separates through gas-liquid separation tower
Obtaining tar and combustion gas, wherein, combustion gas is for providing fuel to generate electricity for gas turbine, it is achieved effective comprehensive utilization of the energy.
It addition, organic waste pyrolysis system according to the above embodiment of the present invention can also 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: mixing arrangement, and described mixing arrangement has semicoke entrance, coal
Exporting with limestone entrance and mixed material, described semicoke entrance exports with the described semicoke of described pyrolysis reactor and is connected；Powder process
Machine, described in there is mixed material entrance and comminuting matter outlet, wherein, the outlet of mixed material entrance and mixed material is connected；With
And melting furnace, described melting furnace has gasification and melting material inlet, gasifying medium entrance, gasification gas outlet and deslagging
Mouthful, described gasification and melting material inlet is connected with comminuting matter outlet.
According to embodiments of the invention, this system farther includes: spiral discharging device, and described spiral discharging device has discharger and enters
Mouth and discharger export, and described discharger entrance exports with the semicoke of described pyrolysis reactor and is connected, the outlet of described discharger and institute
The described semicoke entrance stating mixing arrangement is connected.
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 and break up coal and limestone outlet, described break up coal and limestone outlet are described with described mixing arrangement
Coal is connected with limestone entrance.
According to embodiments of the invention, this system farther includes: oil storage tank, and described oil storage tank has pyrolysis oil entrance, described
Pyrolysis oil entrance is connected with the outlet of described pyrolysis oil.
According to embodiments of the invention, this system farther includes: gas mixer, and described gas mixer has combustion gas
Entrance, gasification gas entrance and mixed gas outlet, described fuel gas inlet is connected with the gas outlet of described gas-liquid separation tower, described
Gasification gas entrance exports with the described gasification gas of melting furnace and is connected, described mixed gas outlet and described gas access to be clean
It is connected.
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；Described pyrolysis oil gas is delivered to gas-liquid separation tower and carries out Oil-gas Separation process, in order to obtain
Pyrolysis oil and combustion gas, wherein, a part for described combustion gas is transported to the heat accumulation type radiant tube in described pyrolysis reactor as combustion
Material, for described pyrolysis processing；Described for part fuel gas transmission is carried out purified treatment to depurator, in order to after being purified
Combustion gas；And by described fuel gas transmission to gas turbine, described gas turbine generates electricity with described combustion gas for fuel.
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, the pyrolysis oil gas that pyrolysis produces is through gas
Liquid knockout tower isolated tar and combustion gas, wherein, combustion gas is for providing fuel to generate electricity for gas turbine, it is achieved the energy
Effectively comprehensive utilization.
According to embodiments of the invention, the method farther includes: utilize spiral discharging device 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；Described dry mixed material is supplied extremely
Flour mill carries out pulverization process, in order to obtain material powders, and the particle diameter of described material powders is 200～500 μm；And by described
Material powders supply carries out gasification and melting process to melting furnace, in order to obtain gasify gas and molten ash.
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.
According to embodiments of the invention, the method farther includes: before described purified treatment, and described gasification gas is delivered to gas
Body mixing arrangement mixes with described combustion gas, in order to obtain mixed gas.
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.
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 structural representation of the most organic pyrolytic reaction system；
Fig. 6 shows the structural representation of the most organic pyrolytic reaction system；
Fig. 7 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. 8 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. 9 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, gas-liquid separation tower 600, depurator 800 and gas turbine 900.
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 at pyrolysis reactor
The internal short transverse multi-tier arrangement along pyrolysis reactor, every layer has many heat accumulating type the most parallel to each other radiation
Pipe 120.Thus, use radial canal to have heat storage, fuel and the air preheat of combustor will be entered, and reduce exhaust gas 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 multiple
The pyrolysis of rubbish.
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 is permissible
Rotate under the driving of motor.According to a particular embodiment of the invention, shaft 132 rotatably stretches into from semicoke outlet 112
In the reaction compartment of pyrolysis reactor 100.Thus, by arranging mixing component in pyrolysis reactor, puddler is back and forth
During rotation so that stacking material is loosened, increase the voidage between stacking material, reduce pyrolysis oil gas and pass 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.
With reference to Fig. 5, according to embodiments of the invention, this system includes gas-liquid separation tower 600, and this gas-liquid separation tower 600 has
Oil gas entrance 601, pyrolysis oil outlet 603 and gas outlet 602, wherein, oil gas entrance 601 and pyrolysis reactor 100
The oil gas vent of discharge is connected, and this gas-liquid separation tower 600 is used for the combustion gas in separation pyrolyzing oil gas and pyrolysis oil, wherein, divides
Return pyrolysis reactor 100 from the Some gases obtained, provide fuel for pyrolysis processing, cost-effective, reduce this system external
The dependence of portion's fuel.
According to embodiments of the invention, this system includes depurator 800.This depurator 800 has gas access 801 to be clean
With purified gas outlet 802, wherein, gas access 801 to be clean is connected with gas outlet, and depurator 800 is used for treating only
Activating QI body carries out purified treatment, the mixed gas after being purified.Thus, by purified treatment, remove the impurity in gas,
Prevent impurity blocking device, affect stability and the safety of device.
According to embodiments of the invention, this system includes gas turbine 900, and this gas turbine 900 has fuel inlet 901,
Wherein, fuel inlet 901 is connected with the purified gas outlet 802 of depurator 800.Gas turbine 900 is with the combustion after this purification
Gas is fuel, is operated operating, it is achieved effective comprehensive utilization of the energy.
With reference to Fig. 4, according to embodiments of the invention, this system farther includes: oil storage tank 1300, and this oil storage tank 1300 has
Having pyrolysis oil entrance, this pyrolysis oil entrance exports 603 with the pyrolysis oil of gas-liquid separation tower 600 and is connected, and is used for storing isolated
Pyrolysis oil.
With reference to Fig. 5, according to some embodiments of the present invention, this system farther includes spiral discharging device 1000, this spiral discharging
Device 1000 has discharger entrance and discharger outlet, and wherein, discharger entrance exports 113 with the semicoke of pyrolysis reactor 100
It is connected.Thus, the semicoke utilizing spiral discharging device pyrolysis to be produced is discharged.
With reference to Fig. 5, according to some embodiments of the present invention, this system farther includes: gas mixer 700, this gas
Mixing arrangement 700 has fuel gas inlet 701, gasification gas entrance 703 and mixed gas outlet 702, wherein, fuel gas inlet 701
Being connected with the gas outlet 602 of gas-liquid separation tower 600, gasification gas entrance 703 exports with the gasification gas of melting furnace 400
404 are connected, and mixed gas outlet 702 is connected with the gas access to be clean 801 of depurator 800, for by combustion gas and gasification
Gas mixes, and supplies gas turbine as fuel, and not only the combustion efficiency of fuel is good, and the comprehensive high-efficiency achieving the energy utilizes.
With reference to Fig. 5, according to embodiments of the invention, this system farther includes: mixing arrangement 200, flour mill 300 are gentle
Change melting furnace 400.Specifically, 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 spiral discharging device 600 will be partly
Jiao is delivered to mixing arrangement 200, mixes with coal dust and limestone, obtain mixed material in mixing arrangement 200, is mixing
Cheng Zhong, coal dust and semicoke heat exchange, the moisture of coal self separates out and is dried.Limestone then can solid sulfur, reduction gasification when gasification
Sulfur content in gas, adds the limestone low cost than high-temperature gas desulfurization in the feed, and add limestone when gasification can simultaneously
To reduce ash fusion point, reduce gasification temperature, improve the energy efficiency of gasification system.Flour mill 300 has mixed material entrance
301 and broken material outlet 302, wherein, mixed material entrance 301 exports 202 phases with the mixed material of mixing arrangement 200
Even, for mixed material is carried out break process, obtaining material powders, the particle diameter of mixed material reduces, it is simple to follow-up gasification
Melt process, reduces the temperature and time that gasification and melting processes；Melting furnace 400 have gasification and melting material inlet 403,
Gasifying medium entrance 401, oxidant inlet 402, gasification gas outlet 404, wherein, gasification and melting material inlet 403 and system
Powder machine 300 broken material outlet 302 be connected, utilize garbage filter concentrated solution and partial air as gasifying medium, with above-mentioned
Mixed material is raw material, carries out gasification and melting reaction, produces gasification gas and molten ash.Hereby it is achieved that the making full use of of refuse.
With reference to Fig. 6, according to embodiments of the invention, this system farther includes: disintegrating machine 500, and this disintegrating machine 500 has
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
Limestone outlet 503 is connected with coal and the limestone entrance 203 of mixing arrangement 200.For the coal of bulk and limestone are carried out
Break 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.
With reference to Fig. 6, according to a particular embodiment of the invention, this system farther includes: hopper 1100 and feeding screw 1200.
Hopper 1100 has charging aperture and discharging opening, and hopper 1100 is used for depositing organic waste；Feeding screw 1200 has charging
Device entrance and feeder outlets, wherein, feeder entrance is connected with discharging opening, feeder entrance and the heat of pyrolysis reactor 100
Solving garbage inlet 111 to be connected, feeding screw 900 is for being delivered to pyrolysis reactor by the rubbish in hopper.
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. 7, according to embodiments of the invention, the method for this process organic waste is explained, the method
Including:
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 pyrolysis
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 Oil-gas Separation processes
According to embodiments of the invention, pyrolysis oil gas is delivered to gas-liquid separation tower and carries out Oil-gas Separation process, in order to be pyrolyzed
Oil and combustion gas, wherein, the heat accumulation type radiant tube that a part for this combustion gas is transported in pyrolysis reactor as fuel, for
Pyrolysis processing, cost-effective, reduce the dependence of this system external portion fuel.
S300 purified treatment
According to embodiments of the invention, Some gases is delivered to depurator and carries out purified treatment, in order to the combustion gas after being purified.
Thus, by purified treatment, remove the impurity in gas, prevent impurity blocking device, affect stability and the safety of device.
According to embodiments of the invention, the method farther includes: before purified treatment, and gasification gas is delivered to gas mixing dress
Mix with combustion gas in putting, obtain mixed gas.Thus, gentle for combustion gas activating QI is mixed, supplies gas turbine as fuel,
Not only the combustion efficiency of fuel is good, and the comprehensive high-efficiency achieving the energy utilizes.
S400 supplies gas turbine
According to embodiments of the invention, by fuel gas transmission to gas turbine, gas turbine generates electricity with combustion gas for fuel.Thus,
Fuel is provided for gas turbine, it is achieved the comprehensive of the energy effectively utilizes with the combustion gas that pyrolysis obtains.
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, the pyrolysis oil gas that pyrolysis produces is through gas
Liquid knockout tower isolated tar and combustion gas, wherein, combustion gas is for providing fuel to generate electricity for gas turbine, it is achieved the energy
Effectively comprehensive utilization.
With reference to Fig. 8, according to embodiments of the invention, the method farther includes:
S500 combination drying
According to embodiments of the invention, utilize spiral discharging device to supply semicoke to mixing arrangement, and carry out with coal dust and limestone
Combination drying, in order to obtain the mixed material being dried, effectively utilizes semicoke heat simultaneously.Thus, in mixing arrangement and coal dust
Mix with limestone, obtain mixed material, in mixed process, coal dust and semicoke heat exchange, the moisture of coal self separates out and is dried,
Mixed material is lowered the temperature.Limestone then can consolidate sulfur when gasification, reduces the sulfur content in gasification gas, adds 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, 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.
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, and
Calorific value is not less than 15GJ/Kg, beneficially provides enough energy for follow-up gasification and melting.
S600 pulverization process
According to embodiments of the invention, dry mixed material supply is carried out pulverization process to flour mill, obtains material powders,
The particle diameter of this material powders is 200～500 μm.Thus, mixed material being carried out break process, the particle diameter of material reduces, it is simple to
Follow-up gasification and melting processes, and reduces the temperature and time that gasification and melting processes.
S700 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 gasification and melting processes is 1100～1500 degrees Celsius.Thus, gas fusion processes
Temperature low, the energy-conservation energy.
With reference to Fig. 9, according to embodiments of the invention, the method farther includes:
S800 break process
According to embodiments of the invention, before combination drying, disintegrating machine is utilized by coal dust and to state limestone and carry out break process, with
Just the coal dust after being crushed and broken after limestone.According to some embodiments of the present invention, broken after coal dust 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:
Pyrolysis garbage inlet, exhanst gas outlet and semicoke outlet；
Described pyrolysis garbage inlet is positioned at the top of described pyrolysis reactor；The outlet of described semicoke is positioned at described pyrolysis reactor
Bottom；
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；
Gas-liquid separation tower, described gas-liquid separation tower have oil gas entrance, pyrolysis oil outlet and gas outlet, described oil gas entrance with
Described discharge is connected；
Depurator, described alembic has gas access to be clean and purified gas outlet, and described gas access to be clean is with described
Gas outlet is connected；And
Gas turbine, described gas turbine has fuel inlet, and described fuel inlet goes out with the described purification gas of described depurator
Mouth 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:
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 semicoke of described pyrolysis reactor and is connected；
Flour mill, described in there is mixed material entrance and comminuting matter outlet, wherein, mixed material entrance and mixed material export
It is connected；And
Melting furnace, described melting furnace has gasification and melting material inlet, gasifying medium entrance, gasification gas outlet and row
Cinder notch, described gasification and melting material inlet is connected with comminuting matter outlet.
6. according to the system according to any one of claim 1-5, it is characterised in that farther include:
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, and the outlet of described discharger is connected with the described semicoke entrance of described mixing arrangement,
Optionally, described system farther includes:
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,
Optionally, described system farther includes:
Oil storage tank, described oil storage tank has the described pyrolysis oil of pyrolysis oil entrance, described pyrolysis oil entrance and described gas-liquid separation tower
Outlet is connected.
7. according to the system according to any one of claim 1-6, it is characterised in that farther include:
Gas mixer, described gas mixer has fuel gas inlet, gasification gas entrance and mixed gas outlet, described combustion
Gas entrance is connected with the gas outlet of described gas-liquid separation tower, and described gasification gas entrance exports with the described gasification gas of melting furnace
Being connected, described mixed gas outlet is connected with described gas access to be clean.
8. utilizing the method that the organic waste pyrolysis system described in any one of claim 1-7 processes organic waste, it is special
Levy and be, including:
Organic waste supply is carried out pyrolysis processing to pyrolysis reactor, obtains being pyrolyzed oil gas and semicoke；
Described pyrolysis oil gas is delivered to gas-liquid separation tower and carries out Oil-gas Separation process, obtain pyrolysis oil and combustion gas, wherein, described
The heat accumulation type radiant tube that a part for combustion gas is transported in described pyrolysis reactor, as fuel, provides for pyrolysis oven refuse pyrolysis
Heat；
Described for part fuel gas transmission is carried out purified treatment to depurator, the combustion gas after being purified；And
By described fuel gas transmission to gas turbine, described gas turbine generates electricity with described combustion gas for fuel.
Method the most according to claim 8, it is characterised in that farther include:
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；
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,
Optionally, described method farther includes:
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,
Optionally, described method farther includes:
Before described purified treatment, it is delivered in gas mixer mix with described combustion gas by described gasification gas, in order to
To mixed gas.
Method the most according to claim 8 or claim 9, it is characterised in that described semicoke and described coal dust gross mass are with described
The mass ratio of limestone is (5-200): 1,
Optionally, the temperature of described dry mixed material is not higher than 150 DEG C, and heat is not less than 15GJ/Kg,
Optionally, the temperature that described gasification and melting processes is 1100～1500 degrees Celsius.
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106391673A (en) * | 2016-11-30 | 2017-02-15 | 北京神雾环境能源科技集团股份有限公司 | System and method for treating household garbage |
| CN106642081A (en) * | 2016-12-12 | 2017-05-10 | 大连理工大学 | Organic matter self-energized pyrolysis-combustion time-sharing reaction device and method |
| CN107629809A (en) * | 2017-11-03 | 2018-01-26 | 北京神雾电力科技有限公司 | A kind of wall-hanging rapid pyrolysis apparatus |
Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2005120210A (en) * | 2003-10-16 | 2005-05-12 | Kubota Corp | Waste disposal by gasification and system therefor |
| CN103765102A (en) * | 2011-05-23 | 2014-04-30 | 杰富意工程株式会社 | Waste-melting method |
| CN104094059A (en) * | 2012-02-28 | 2014-10-08 | 新日铁住金工程技术株式会社 | Waste gasification and melting furnace |
| CN105462615A (en) * | 2015-12-14 | 2016-04-06 | 大连理工大学 | Device utilizing waste plastics to thermally convert and prepare hydrogen-rich syngas and process |
| CN105505412A (en) * | 2016-01-27 | 2016-04-20 | 北京神雾环境能源科技集团股份有限公司 | Moving bed pyrolysis reactor |
| CN205635475U (en) * | 2016-04-21 | 2016-10-12 | 北京神雾环境能源科技集团股份有限公司 | Organic garbage pyrolytic system |
-
2016
- 2016-04-21 CN CN201610252359.7A patent/CN105885884A/en active Pending
Patent Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2005120210A (en) * | 2003-10-16 | 2005-05-12 | Kubota Corp | Waste disposal by gasification and system therefor |
| CN103765102A (en) * | 2011-05-23 | 2014-04-30 | 杰富意工程株式会社 | Waste-melting method |
| CN104094059A (en) * | 2012-02-28 | 2014-10-08 | 新日铁住金工程技术株式会社 | Waste gasification and melting furnace |
| CN105462615A (en) * | 2015-12-14 | 2016-04-06 | 大连理工大学 | Device utilizing waste plastics to thermally convert and prepare hydrogen-rich syngas and process |
| CN105505412A (en) * | 2016-01-27 | 2016-04-20 | 北京神雾环境能源科技集团股份有限公司 | Moving bed pyrolysis reactor |
| CN205635475U (en) * | 2016-04-21 | 2016-10-12 | 北京神雾环境能源科技集团股份有限公司 | Organic garbage pyrolytic system |
Non-Patent Citations (2)
| Title |
|---|
| 李文秀等: "《2005中国钢铁年会论文集》", 31 October 2005, 冶金工业出版社 * |
| 钱家麟等: "《油页岩干馏炼油工艺》", 31 March 2014, 中国石化出版社 * |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106391673A (en) * | 2016-11-30 | 2017-02-15 | 北京神雾环境能源科技集团股份有限公司 | System and method for treating household garbage |
| CN106642081A (en) * | 2016-12-12 | 2017-05-10 | 大连理工大学 | Organic matter self-energized pyrolysis-combustion time-sharing reaction device and method |
| CN106642081B (en) * | 2016-12-12 | 2018-08-07 | 大连理工大学 | A kind of organic matter self energizing pyrolysis and combustion timesharing reaction unit and method |
| CN107629809A (en) * | 2017-11-03 | 2018-01-26 | 北京神雾电力科技有限公司 | A kind of wall-hanging rapid pyrolysis apparatus |
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