CN105694925A - Organic waste pyrolysis system and application thereof - Google Patents
Organic waste pyrolysis system and application thereof Download PDFInfo
- Publication number
- CN105694925A CN105694925A CN201610118525.4A CN201610118525A CN105694925A CN 105694925 A CN105694925 A CN 105694925A CN 201610118525 A CN201610118525 A CN 201610118525A CN 105694925 A CN105694925 A CN 105694925A
- Authority
- CN
- China
- Prior art keywords
- gas
- pyrolysis
- outlet
- oil gas
- organic waste
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Granted
Links
- 238000000197 pyrolysis Methods 0.000 title claims abstract description 192
- 239000010815 organic waste Substances 0.000 title claims abstract description 65
- 238000000034 method Methods 0.000 claims abstract description 85
- 238000001035 drying Methods 0.000 claims abstract description 25
- 238000012216 screening Methods 0.000 claims abstract description 24
- 239000007787 solid Substances 0.000 claims abstract description 22
- 239000007789 gas Substances 0.000 claims description 189
- 239000000463 material Substances 0.000 claims description 65
- 239000010813 municipal solid waste Substances 0.000 claims description 59
- 238000002309 gasification Methods 0.000 claims description 50
- 230000008569 process Effects 0.000 claims description 38
- 238000002844 melting Methods 0.000 claims description 26
- 230000008018 melting Effects 0.000 claims description 26
- 235000019738 Limestone Nutrition 0.000 claims description 24
- 239000006028 limestone Substances 0.000 claims description 24
- 238000009825 accumulation Methods 0.000 claims description 21
- 238000012545 processing Methods 0.000 claims description 20
- 239000002245 particle Substances 0.000 claims description 19
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims description 18
- 239000003546 flue gas Substances 0.000 claims description 18
- 238000007599 discharging Methods 0.000 claims description 16
- 239000000203 mixture Substances 0.000 claims description 16
- 239000000567 combustion gas Substances 0.000 claims description 15
- 239000000446 fuel Substances 0.000 claims description 15
- 239000007921 spray Substances 0.000 claims description 15
- 239000002817 coal dust Substances 0.000 claims description 14
- 239000002737 fuel gas Substances 0.000 claims description 13
- 238000000746 purification Methods 0.000 claims description 12
- 238000010309 melting process Methods 0.000 claims description 11
- 239000003245 coal Substances 0.000 claims description 10
- 238000003860 storage Methods 0.000 claims description 9
- 239000000843 powder Substances 0.000 claims description 8
- 238000010791 quenching Methods 0.000 claims description 6
- 230000000171 quenching effect Effects 0.000 claims description 6
- 238000009795 derivation Methods 0.000 claims description 5
- 210000004127 vitreous body Anatomy 0.000 claims description 5
- 239000000779 smoke Substances 0.000 claims description 4
- 238000010298 pulverizing process Methods 0.000 claims description 3
- 238000010438 heat treatment Methods 0.000 abstract description 4
- 239000002699 waste material Substances 0.000 abstract description 4
- 238000005338 heat storage Methods 0.000 abstract description 2
- 239000000969 carrier Substances 0.000 abstract 1
- 238000010517 secondary reaction Methods 0.000 abstract 1
- 239000011269 tar Substances 0.000 description 31
- 239000002956 ash Substances 0.000 description 21
- 238000006243 chemical reaction Methods 0.000 description 13
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 9
- 230000004044 response Effects 0.000 description 8
- 238000002386 leaching Methods 0.000 description 7
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 6
- 239000007788 liquid Substances 0.000 description 6
- 238000000926 separation method Methods 0.000 description 6
- 239000011593 sulfur Substances 0.000 description 6
- 229910052717 sulfur Inorganic materials 0.000 description 6
- 239000000047 product Substances 0.000 description 4
- 239000002994 raw material Substances 0.000 description 4
- 238000012546 transfer Methods 0.000 description 4
- 238000004458 analytical method Methods 0.000 description 3
- 230000008901 benefit Effects 0.000 description 3
- 229910052799 carbon Inorganic materials 0.000 description 3
- 239000003795 chemical substances by application Substances 0.000 description 3
- 238000005336 cracking Methods 0.000 description 3
- 238000006477 desulfuration reaction Methods 0.000 description 3
- 230000023556 desulfurization Effects 0.000 description 3
- 239000010791 domestic waste Substances 0.000 description 3
- 238000005516 engineering process Methods 0.000 description 3
- 230000004927 fusion Effects 0.000 description 3
- 238000002156 mixing Methods 0.000 description 3
- 230000003213 activating effect Effects 0.000 description 2
- RHZUVFJBSILHOK-UHFFFAOYSA-N anthracen-1-ylmethanolate Chemical compound C1=CC=C2C=C3C(C[O-])=CC=CC3=CC2=C1 RHZUVFJBSILHOK-UHFFFAOYSA-N 0.000 description 2
- 239000003830 anthracite Substances 0.000 description 2
- 239000004568 cement Substances 0.000 description 2
- 239000000919 ceramic Substances 0.000 description 2
- 230000008859 change Effects 0.000 description 2
- 239000003610 charcoal Substances 0.000 description 2
- 239000002864 coal component Substances 0.000 description 2
- 238000002485 combustion reaction Methods 0.000 description 2
- 239000002361 compost Substances 0.000 description 2
- 150000001875 compounds Chemical class 0.000 description 2
- 230000006835 compression Effects 0.000 description 2
- 238000007906 compression Methods 0.000 description 2
- 239000004035 construction material Substances 0.000 description 2
- 230000018044 dehydration Effects 0.000 description 2
- 238000006297 dehydration reaction Methods 0.000 description 2
- 239000000428 dust Substances 0.000 description 2
- 238000001704 evaporation Methods 0.000 description 2
- 230000008020 evaporation Effects 0.000 description 2
- 238000000605 extraction Methods 0.000 description 2
- 239000003337 fertilizer Substances 0.000 description 2
- 239000011521 glass Substances 0.000 description 2
- 239000002920 hazardous waste Substances 0.000 description 2
- 229910001385 heavy metal Inorganic materials 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- 229910052751 metal Inorganic materials 0.000 description 2
- 239000002184 metal Substances 0.000 description 2
- 239000011812 mixed powder Substances 0.000 description 2
- 229910000510 noble metal Inorganic materials 0.000 description 2
- 238000006068 polycondensation reaction Methods 0.000 description 2
- 239000002244 precipitate Substances 0.000 description 2
- 239000002510 pyrogen Substances 0.000 description 2
- 230000000630 rising effect Effects 0.000 description 2
- 239000004576 sand Substances 0.000 description 2
- 239000002893 slag Substances 0.000 description 2
- 230000001988 toxicity Effects 0.000 description 2
- 231100000419 toxicity Toxicity 0.000 description 2
- 206010002660 Anoxia Diseases 0.000 description 1
- 241000976983 Anoxia Species 0.000 description 1
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- ZAMOUSCENKQFHK-UHFFFAOYSA-N Chlorine atom Chemical compound [Cl] ZAMOUSCENKQFHK-UHFFFAOYSA-N 0.000 description 1
- 206010021143 Hypoxia Diseases 0.000 description 1
- UCKMPCXJQFINFW-UHFFFAOYSA-N Sulphide Chemical compound [S-2] UCKMPCXJQFINFW-UHFFFAOYSA-N 0.000 description 1
- 238000010521 absorption reaction Methods 0.000 description 1
- 230000001133 acceleration Effects 0.000 description 1
- 238000004220 aggregation Methods 0.000 description 1
- 230000002776 aggregation Effects 0.000 description 1
- 150000001299 aldehydes Chemical class 0.000 description 1
- -1 and wherein Substances 0.000 description 1
- 230000007953 anoxia Effects 0.000 description 1
- 238000003763 carbonization Methods 0.000 description 1
- 239000000460 chlorine Substances 0.000 description 1
- 229910052801 chlorine Inorganic materials 0.000 description 1
- 238000003776 cleavage reaction Methods 0.000 description 1
- 239000010883 coal ash Substances 0.000 description 1
- 239000011285 coke tar Substances 0.000 description 1
- 230000006378 damage Effects 0.000 description 1
- 230000007423 decrease Effects 0.000 description 1
- 230000003247 decreasing effect Effects 0.000 description 1
- 238000006356 dehydrogenation reaction Methods 0.000 description 1
- 230000003111 delayed effect Effects 0.000 description 1
- 238000009826 distribution Methods 0.000 description 1
- 230000002708 enhancing effect Effects 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- DNJIEGIFACGWOD-UHFFFAOYSA-N ethanethiol Chemical compound CCS DNJIEGIFACGWOD-UHFFFAOYSA-N 0.000 description 1
- 239000005431 greenhouse gas Substances 0.000 description 1
- 238000005984 hydrogenation reaction Methods 0.000 description 1
- 239000004615 ingredient Substances 0.000 description 1
- 239000013067 intermediate product Substances 0.000 description 1
- 150000002500 ions Chemical class 0.000 description 1
- 150000002576 ketones Chemical class 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 150000007524 organic acids Chemical class 0.000 description 1
- 150000002989 phenols Chemical class 0.000 description 1
- 239000004033 plastic Substances 0.000 description 1
- 229920003023 plastic Polymers 0.000 description 1
- 235000019353 potassium silicate Nutrition 0.000 description 1
- 238000001556 precipitation Methods 0.000 description 1
- 239000002296 pyrolytic carbon Substances 0.000 description 1
- 230000007017 scission Effects 0.000 description 1
- 150000003384 small molecules Chemical class 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 230000026676 system process Effects 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
- C10B53/00—Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
- 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
Landscapes
- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Organic Chemistry (AREA)
- Materials Engineering (AREA)
- Life Sciences & Earth Sciences (AREA)
- Wood Science & Technology (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Combustion & Propulsion (AREA)
- Processing Of Solid Wastes (AREA)
Abstract
The invention discloses an organic waste pyrolysis system and a method for treating organic waste through the organic waste pyrolysis system. The organic waste pyrolysis system comprises a screening machine, a spiral feeder, a drying hoist tower, a first cyclone separator and a pyrolysis reactor, wherein the screening machine, the spiral feeder, the drying hoist tower, the first cyclone separator and the pyrolysis reactor are communicated in sequence. The system can effectively restrain a secondary reaction of oil gas and increase the yield of tar, heat-storage non-heat-carrier radiant tubes are adopted for heating by the utilization of dividing wall heat exchanging, gas and solid heat carriers are not needed, the heat value of pyrolysis gas is increased, and meanwhile the organic waste pyrolysis system can be combined in a modularized mode, and is suitable for different amount of waste to be treated and easy to industrialize.
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, domestic waste has become as the key factor that restriction green city is fast-developing。At present, treatment of urban garbage mode in countries in the world mainly includes sanitary landfills, burning, compost, pyrolysis and comprehensive garbage disposal etc.。And the relevant refuse classification of China, rubbish comprehensive utilization technique are delayed, the main processing ways of current rubbish is sanitary landfills is main, and the mode such as burning, compost is auxiliary。Further, along with the enhancing of scientific and technological progress and environmental consciousness, destruction that " burning method " and " landfill method " brings to environment and threaten the healthy more and more recognized of the mankind to arrive。A kind ofNovelTechnology to substitute " burning method " and " landfill method ", with reduce greenhouse gas emission and eliminate two English pollution problems, just by the urgent need to
Refuse pyrolysis treatment technology refer to by rubbish when anaerobic or heating when anoxia, so as to decompose。In pyrolytic process, its intermediate product trends towards the change that polarises: a kind of is be micromolecular cracking process, another kind be little molecule aggregation from macromolecular cleavage be the polycondensation process of macromole。Along with the rising of pyrolysis temperature, refuse pyrolysis mainly experiences dry (room temperature～200 DEG C), dry distilling (～500 DEG C) and gas and generates (～1200 DEG C) three phases。In the cold drying stage, the moisture of outer water contained in rubbish and capillary structure absorption is initially heated evaporation, secondly the constitution water decomposes in material。Along with the rising of the evaporation of moisture and pyrogenation and carbonization temperature, refuse pyrolysis enters the dry distilling stage。As long as there is internal water and CO in the dry distilling stage2Precipitation, deoxidation, the reaction such as desulfurization。Along with the continuation of temperature raises, the small-molecule substance generation second pyrolysis that the dry distilling stage produces, refuse pyrolysis enters gas generation phase, generates 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、CH4With CO etc.。
Due to China's Waste sorting method imperfection, cause the composition complex of rubbish own, often containing kitchen excess, plastics, old and useless battery, circuit board etc.。Find the tar ingredients also complex that refuse pyrolysis produces simultaneously, component analysis finds in tar containing material in hundreds of, including various organic acid, phenols, ketone, aldehydes, PAHs etc., wherein chlorine element and heavy metal element are generally higher, water content about 20%, calorific value is 13～18MJ/Kg about, causes stench because sulfide content is high simultaneously, and comprehensive utilization difficulty is big。Factors causes China's refuse pyrolysis, rubbish comprehensive utilization technique to be difficult to obtain important breakthrough。
Summary of the invention
It is contemplated that at least solve one of technical problem of existence in prior art。For this, it is an object of the present invention to propose a kind of organic waste pyrolysis system, this organic waste pyrolysis system can effectively suppress the secondary response of oil gas, improve tar yield, and have employed heat accumulating type without heat carrier radial canal heating technique, it is not necessary to gas, solid heat carrier, improve the calorific value of pyrolysis gas, simultaneously this organic waste pyrolysis system can modular combination, be suitable for different garbage treatment quantities, it is easy to industrialization。
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: screening machine, feeding screw, dry lifting tower, first cyclone separator, and pyrolysis reactor, wherein, described screening machine, described feeding screw, described dry lifting tower, described first cyclone separator and described pyrolysis reactor are sequentially connected logical, and wherein, described pyrolysis reactor includes: pyrolysis garbage inlet and semicoke outlet；Described pyrolysis garbage inlet is positioned at the top of described pyrolysis reactor, and is connected with the outlet of described solid refuse；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 the short transverse multi-tier arrangement of described pyrolysis reactor, every layer has many heat accumulation type radiant tubes parallel to each other in the horizontal direction, and the exhanst gas outlet on described heat accumulation type radiant tube is connected with the smoke inlet of described dry lifting tower；Oil gas derives pipeline, and described oil gas is derived and is provided with through hole on the tube wall of pipeline；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 the sidewall of described pyrolysis reactor and extend in described pyrolysis reactor and be connected with described oil gas derivation pipeline。
Organic waste pyrolysis system according to embodiments of the present invention can effectively suppress the secondary response of oil gas, improve tar yield, and have employed heat accumulating type utilizes septate heat transfer to heat without heat carrier radial canal, without gas, solid heat carrier, improve the calorific value of pyrolysis gas, this organic waste pyrolysis system can modular combination simultaneously, it is adaptable to different garbage treatment quantities, it is easy to industrialization。
It addition, organic waste pyrolysis system according to the above embodiment of the present invention can also have following additional technical characteristic:
According to embodiments of the invention, described gas-collecting branch pipe is multiple, and arranged parallel to each other along the length direction of described gas gathering manifold。
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 reactor, and every layer has many oil gas parallel to each other in the horizontal direction and derives 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 the respective left and right sides of described heat accumulation type radiant tube is symmetrically arranged with two oil gas and derives pipeline。
According to embodiments of the invention, described oil gas derives 1/2-3 times that spacing is described oil gas derivation pipe diameter d of pipeline and the tube wall of contiguous described heat accumulation type radiant tube。
According to embodiments of the invention, 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 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: the second cyclone separator, described second cyclone separator has pyrolysis oil gas mixture entrance, purifies oil gas vent and solid particle outlet, and described pyrolysis oil gas mixture entrance is connected with described gas gathering manifold。
According to embodiments of the invention, described system farther includes: spiral discharging device, and described spiral discharging device has semicoke entrance and semicoke mixture outlet, and described semicoke entrance is connected with the outlet of described semicoke。
According to embodiments of the invention, described system farther includes: spray column, and described spray column has purification oil gas entrance, tar outlet and combustible gas outlet, and described purification oil gas entrance is connected with described purification oil gas vent。
According to embodiments of the invention, described system farther includes: combustion gas air-introduced machine, and described combustion gas air-introduced machine has fuel gas inlet and gas outlet, and described fuel gas inlet is connected with the outlet of described combustible gas；Fuel cartridge, described fuel cartridge has storage tank fuel gas inlet and storage tank gas outlet, and described storage tank fuel gas inlet is connected with described gas outlet。
According to embodiments of the invention, this system farther includes: combination drying machine, and described combination drying facility have semicoke entrance, coal entrance, limestone entrance and mixed material outlet, and described semicoke entrance is connected with described semicoke mixture outlet；Disintegrating machine, described disintegrating machine has mixed material entrance and broken material outlet, and described mixed material entrance is connected with the outlet of described mixed material；And melting furnace, described melting furnace has gasification and melting material inlet, gasifying medium entrance, gasification gas outlet and slag-drip opening, described gasification and melting material inlet is connected with the outlet of described broken material, and described gasifying medium entrance is connected with the outlet of described percolate。
According to a further aspect in the invention, the invention provides a kind of method utilizing aforesaid organic waste pyrolysis system to process organic waste。According to embodiments of the invention, the method includes: to described screening machine, organic waste supply is carried out Screening Treatment, in order to obtain the organic waste after percolate and screening；By the organic waste after described screening in described feeding screw supply to described dry lifting tower, in order to adopt flue gas that described organic waste is dried lifting and process, in order to obtain the dry mixed material containing flue gas and garbage drying；The supply of the described dry mixed material containing flue gas and garbage drying is easily separated process to described first cyclone separator, in order to separate and obtain flue gas and solid refuse；And the supply of described solid refuse is carried out pyrolysis processing to described pyrolysis reactor, in order to obtain pyrolysis oil gas and semicoke, and the flue gas supply described pyrolysis processing produced is to described dry riser。
The method processing organic waste according to embodiments of the present invention, utilize pyrolysis reactor that rubbish is carried out pyrolysis, can effectively suppress the secondary response of oil gas, improve tar yield, and have employed heat accumulating type and utilize septate heat transfer heat without heat carrier radial canal, it is not necessary to gas, consolidate heat carrier, improve the calorific value of pyrolysis gas, simultaneously because organic waste pyrolysis system can modular combination, the method is applicable to different garbage treatment quantities, it is easy to industrialization promotion。
According to embodiments of the invention, the method farther includes: to the second cyclone separator, the supply of described pyrolysis oil gas is carried out purified treatment, in order to be purified oil gas and solid particle。
According to embodiments of the invention, described method farther includes: to spray column, the supply of described purification oil gas is carried out spray process, in order to obtain tar and combustible gas。
According to embodiments of the invention, described method farther includes: stored to fuel cartridge through the supply of combustion gas air-introduced machine by described combustible gas。
According to embodiments of the invention, the method farther includes: utilizes spiral discharging device to supply described semicoke to combination drying machine, and carries out combination drying with coal dust and limestone, in order to obtains the mixed material dried；Described dry mixed material supply is carried out pulverization process to disintegrating machine, in order to obtain material powders, be crushed to 200～500um；And the supply of described material powders is carried out gasification and melting process to melting furnace, in order to obtaining gasification gas and molten ash, wherein, the gasifying medium that described gasification and melting processes is described percolate and air。
According to embodiments of the invention, described method farther includes: described molten ash is carried out quenching, obtains vitreous body lime-ash。
Mass ratio according to embodiments of the invention, described semicoke and described coal dust gross mass Yu described limestone is (5-200): 1。
The additional aspect of the present invention and advantage will part provide in the following description, and part will become apparent from the description below, or is recognized by the practice of the present invention。
Accompanying drawing explanation
Above-mentioned and/or the additional aspect of the present invention and advantage are from conjunction with followingAccompanying drawingTo the description of embodiment will be apparent from easy to understand, wherein:
Fig. 1Show the structural representation of organic waste pyrolysis system according to an embodiment of the inventionFigure；
Fig. 2Show the structural representation of organic waste pyrolysis system according to an embodiment of the inventionFigure；
Fig. 3Show the structural representation of organic waste pyrolysis system according to an embodiment of the inventionFigure；
Fig. 4Show the structural representation of organic waste pyrolysis system according to an embodiment of the inventionFigure；
Fig. 5Show the structural representation of organic waste pyrolysis system according to an embodiment of the inventionFigure；
Fig. 6Show the structural representation of organic waste pyrolysis system according to an embodiment of the inventionFigure；
Fig. 7Show the flow process signal of the method utilizing organic waste pyrolysis system to process organic waste according to an embodiment of the inventionFigure；
Fig. 8Show the flow process signal of the method utilizing organic waste pyrolysis system to process organic waste according to an embodiment of the inventionFigure；
Fig. 9Show the flow process signal of the method utilizing organic waste pyrolysis system to process organic waste according to an embodiment of the inventionFigure。
Detailed description of the invention
Being described below in detail embodiments of the invention, the example of described embodiment existsIn accompanying drawingIllustrating, wherein same or similar label represents same or similar element or has the element of same or like function from start to finish。Below with reference toAccompanying drawingThe embodiment described is illustrative of, and is only used for explaining the present invention, and is not considered as limiting the invention。
In describing the invention, term " longitudinal direction ", " transverse direction ", " on ", D score, "front", "rear", "left", "right", " vertically ", " level ", " top ", the orientation of the instruction such as " end " or position relationship be based onAccompanying drawing instituteThe orientation shown or position relationship, be for only for ease of the description present invention rather than require that the present invention with specific azimuth configuration and operation, therefore must be not considered as limiting the invention。
It should be noted that term " first ", " second " are only for descriptive purposes, and it is not intended that indicate or imply relative importance or the implicit quantity indicating indicated technical characteristic。Thus, define " first ", the feature of " second " can express or implicitly include one or more these features。Further, in describing the invention, except as otherwise noted, " multiple " are meant that two or more。
According to an aspect of the present invention, the invention provides a kind of organic waste pyrolysis system。ReferenceFig. 1According to embodiments of the invention, this system is explained, this system includes screening machine 100, feeding screw 200, dry lifting tower 300, first cyclone separator 400, and pyrolysis reactor 500, wherein, screening machine 100 has garbage inlet, percolate outlet, organic waste outlet and inorganic refuse outlet；Feeding screw 200 has charging aperture and discharging opening, and wherein, charging aperture exports with the organic waste of screening machine 100 and is connected；The dry tower 300 that promotes has smoke inlet, organic waste entrance and the outlet of dry mixed material, and wherein, organic waste entrance is connected with the discharging opening of feeding screw 200；First cyclone separator 400 has dry mixed material entrance, exhanst gas outlet and solid refuse outlet, and wherein, dry mixed material entrance exports with the dry mixed material of dry lifting tower 300 and is connected；Pyrolysis reactor 500 has pyrolysis garbage inlet 512 and semicoke outlet 511, and wherein, pyrolysis garbage inlet 512 exports with the solid refuse of the first cyclone separator 400 and is connected。
Further, for the ease of understanding the structure of pyrolysis reactor, according to embodiments of the invention, the structure of pyrolysis reactor being explained, this pyrolysis reactor 500 may include that
Pyrolysis garbage inlet 512 and semicoke outlet 511, wherein, pyrolysis garbage inlet 512 is positioned at the top of pyrolysis reactor, and is connected with solid refuse outlet, and semicoke outlet 511 is positioned at the bottom of pyrolysis reactor。In some embodiments of the invention, it is understood that, this pyrolysis reactor 500 has housing 510, pyrolytic reaction space is limited in this housing 510, pyrolysis garbage inlet 512 and semicoke outlet 511 are arranged on housing 510, and wherein, pyrolysis garbage inlet 512 is positioned at the top of housing 510, and be connected with solid refuse outlet, semicoke outlet 511 is positioned at the bottom of housing 510。Thus, pyrolysis garbage inlet is positioned at the top of pyrolysis reactor, it is simple to rubbish enters from the one end in pyrolytic reaction space, and the other end is discharged, sufficiently conducted pyrolysis, and semicoke outlet is positioned at the bottom of housing, it is simple to semicoke is discharged。According to some embodiments of the present invention, housing 510 is additionally provided with fuel gas entrance 513 and air intake 514。
Heat accumulation type radiant tube 520, in this article also referred to as " radial canal ", this heat accumulation type radiant tube 520 in the inside of pyrolysis reactor along the short transverse multi-tier arrangement of described pyrolysis reactor, it can be appreciated that heat accumulation type radiant tube 520 is in the inside of housing 510 or pyrolytic reaction space, and along the short transverse multi-tier arrangement in housing 510 or pyrolytic reaction space, every layer has many heat accumulation type radiant tubes 510 parallel to each other in the horizontal direction, and the exhanst gas outlet 515 on this heat accumulation type radiant tube 510 is connected with the smoke inlet of dry lifting tower 300。Thus, adopting radial canal to have heat storage, will enter fuel and the air preheat of combustor, and reduce exhaust gas temperature, the thermal efficiency is high, and, adopt septate heat transfer technique, the component of rubbish is changed insensitive, makes this pyrolysis reactor be suitable to the pyrolysis of various garbage。
Oil gas derives pipeline 530, and oil gas is derived and is provided with through hole on the tube wall of pipeline 530。Thus, it is simple to oil gas is derived。
Discharge 540, discharge 540 includes gas gathering manifold 541 and the gas-collecting branch pipe 542 being connected with gas gathering manifold 541, wherein, it is outside that gas gathering manifold 541 is vertically situated at pyrolysis reactor 500, it is understood that outside for being vertically situated at housing 510, gas-collecting branch pipe 542 extends through the sidewall of pyrolysis reactor 500, the i.e. sidewall of housing 510, it extend in the pyrolytic reaction space of pyrolysis reactor 500, it is understood that in housing 510, and derive pipeline 530 with oil gas and be connected。Thus, utilize discharge quickly to be derived by pyrolysis oil gas, can effectively suppress the secondary response of oil gas, improve tar yield。
According to a particular embodiment of the invention, to include multiple parallel and equally distributed radial canal and each radial canal parallel with each radial canal in adjacent upper and lower two-layer radial canal and be in staggered distribution along reactor body short transverse for every layer of radial canal。Thus, it is possible to significantly improve the pyrolysis efficiency of material, and then improve pyrolysis oil productivity。
According to a particular embodiment of the invention, oil gas derives the pipeline 530 short transverse multi-tier arrangement along pyrolysis reactor, and every layer has many oil gas parallel to each other in the horizontal direction and derives pipeline, and oil gas is derived and is provided with through hole on the surface of pipeline；Oil gas is derived pipeline 530 and is connected with discharge 540, and discharge 540 is connected with oil gas vent。Thus, by arranging that in radial canal lower end oil gas is derived pipeline 530 and reduced the tar time of staying in burner hearth, it is to avoid the second pyrolysis of tar, tar yield is improved。According to a particular embodiment of the invention, oil gas is derived pipeline 530 and is arranged in parallel with radial canal 520, and the left and right sides of radial canal 520 is symmetrically arranged with two oil gas and derives pipeline 530。Thus, by arranging that in the both sides of radial canal oil gas is derived pipeline 530 and decreased the tar time of staying in burner hearth, it is to avoid the second pyrolysis of tar, tar yield is improved。
According to embodiments of the invention, oil gas delivery line 530 is symmetrical set the lower section at each heat accumulation type radiant tube 520。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, tar yield is improved。
According to embodiments of the invention, the connected mode of oil gas delivery line 530 and pyrolysis oil gas vent 516 is not particularly limited, and according to a particular embodiment of the invention, the oil gas delivery line 530 of same layer is connected to same pyrolysis oil gas vent 516。Some specific embodiments according to the present invention, adjacent two layers or more multi-layered oil gas delivery line 530 are connected to same pyrolysis oil gas vent 516。Thus, it is possible to collected by oil gas, Simplified flowsheet also improves tar yield, simultaneously can so that oil gas is derived。
According to a particular embodiment of the invention, oil gas derives 1/2-3 times that spacing is oil gas derivation pipeline 530 caliber d of pipeline 530 and the tube wall of contiguous radial canal 520。Thus, it is possible to the tar that generation will be derived at once, it is to avoid coke tar cracking, improves tar yield。
According to embodiments of the invention, discharge 540 includes: gas-collecting branch pipe 542 and gas gathering manifold 541, and wherein, gas gathering manifold 541 is derived pipeline 530 by multiple gas-collecting branch pipes 542 with multilamellar oil gas and is connected。Thus, the pyrolysis oil gas that pyrolysis produces is derived through discharge and gas gathering manifold, can effectively suppress the secondary response of oil gas, improves tar yield。
According to embodiments of the invention, described heat accumulation type radiant tube is made up of heat accumulating type honeycomb ceramics and radial canal。Thus, utilizing heat accumulating type honeycomb ceramics will enter fuel and the air preheat of combustor, reduce exhaust gas temperature, the thermal efficiency is high。
ReferenceFig. 2, according to embodiments of the invention, described system farther includes: spiral discharging device 600, and this spiral discharging device 600 has semicoke entrance and semicoke mixture outlet, and wherein, semicoke entrance exports with the semicoke of pyrolysis reactor 500 and is connected。Thus, the demand according to follow-up treating capacity, the rotating speed of adjustable screw discharger, control the discharging speed of semicoke etc.。
ReferenceFig. 3According to embodiments of the invention, this system farther includes: the second cyclone separator 700, and this second cyclone separator 700 has pyrolysis oil gas mixture entrance, purifies oil gas vent and solid particle outlet, and pyrolysis oil gas mixture entrance is connected with gas gathering manifold 541。Thus, utilize the second cyclone separator that pyrolysis oil gas is carried out purified treatment, immobilized particles and the dusts such as the semicoke being mixed in removal pyrolysis oil gas, prevent immobilized particles and dust block system, the safety and stability of raising system, and the purity of the pyrolysis oil that later separation obtains and combustion gas is high, and quality is good。Further, purified treatment separates the semicoke obtained and enters feeding screw, feeding screw conveying carry out subsequent treatment, efficiently reduce semicoke loss in production procedure, improve the utilization rate of semicoke。
ReferenceFig. 4, according to embodiments of the invention, this system farther includes: spray column 800, and this spray column 800 has purification oil gas entrance, tar outlet and combustible gas outlet, wherein, purifies oil gas entrance and is connected with purifying oil gas vent。Thus, utilize spray to process, reduce the temperature of pyrolysis oil gas, make the tar etc. in pyrolysis oil gas liquefy, and then, by gas-liquid separation, obtain tar and combustible gas。
ReferenceFig. 5, according to embodiments of the invention, this system farther includes: combustion gas air-introduced machine 1300, and this combustion gas air-introduced machine 1300 has fuel gas inlet and gas outlet, and wherein, fuel gas inlet is connected with combustible gas outlet；Fuel cartridge 1400, this fuel cartridge 1400 has storage tank fuel gas inlet and storage tank gas outlet, and wherein, storage tank fuel gas inlet is connected with described gas outlet。Thus, utilize combustion gas air-introduced machine that combustible gas is delivered to fuel cartridge to store。
ReferenceFig. 6According to embodiments of the invention, this system farther includes: combination drying machine 900, disintegrating machine 1100 and melting furnace 1200, this combination drying machine 900 has semicoke entrance, coal entrance, limestone entrance and mixed material outlet, wherein, semicoke entrance is connected with the semicoke mixture outlet of spiral discharging device 600, semicoke is delivered to combination drying machine by spiral discharging device 600, mix with coal dust and limestone in combination drying machine 900, obtain mixed material, in mixed process, coal dust and semicoke heat exchange, the moisture of coal self precipitates out dry。Limestone then can consolidate sulfur when gasification, reducing the sulfur content in gasification gas, addition limestone is lower than the cost of high-temperature gas desulfurization in the feed, adds limestone when gasification simultaneously and can reduce ash fusion point, reduce gasification temperature, improve the energy efficiency of gasification system。Disintegrating machine 1100 has mixed material entrance and broken material outlet, wherein, mixed material entrance is connected with mixed material outlet, for mixed material is carried out break process, obtain material powders, the particle diameter of mixed material reduces, it is simple to follow-up gasification and melting processes, and reduces the temperature and time that gasification and melting processes；Melting furnace 1200 has gasification and melting material inlet, gasifying medium entrance, gasification gas outlet and slag-drip opening, wherein, gasification and melting material inlet is connected with broken material outlet, gasifying medium entrance is connected with percolate outlet, utilize garbage filter concentrated solution and partial air as gasifying medium, with above-mentioned mixed material for 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。
According to a further aspect in the invention, the invention provides a kind of method utilizing aforesaid organic waste pyrolysis system to process organic waste。ReferenceFig. 7, according to embodiments of the invention, the method processing organic waste being explained, the method includes:
S100 Screening Treatment
According to embodiments of the invention, organic waste supply is carried out Screening Treatment to described screening machine, obtain the organic waste after percolate and screening。Thus, the water content of organic waste is reduced by Screening Treatment, it is simple to the follow-up pyrolysis processing that carries out, and, the gasifying medium that the percolate that screening obtains can process as gasification and melting, it is achieved making full use of of rubbish。
S200 dries lifting and processes
According to embodiments of the invention, the organic waste after screening is promoted in tower through feeding screw supply to dry, adopt the flue gas that pyrolysis processing obtains that described organic waste is dried lifting and process, obtain the dry mixed material containing flue gas and garbage drying。Thus, utilize the flue gas that pyrolysis processing obtains that described organic waste is dried lifting and process, reduce the water content of organic waste further, promote the carrying out of pyrolysis processing。
S300 separating treatment
According to embodiments of the invention, the dry mixed material containing flue gas and garbage drying is supplied to described first cyclone separator, is easily separated process, separate and obtain flue gas and solid refuse。Thus, the flue gas in dry mixed material is removed, it is to avoid flue gas affects pyrolytic reaction。
S400 pyrolysis processing
According to embodiments of the invention, the supply of described solid refuse is carried out pyrolysis processing to described pyrolysis reactor, in order to obtain pyrolysis oil gas and semicoke, and the flue gas supply described pyrolysis processing produced is to described dry riser。The pyrolysis reactor utilizing the embodiment of the present invention can effectively suppress the secondary response of oil gas, improve tar yield, and have employed heat accumulating type without heat carrier radial canal heating technique, without gas, solid heat carrier, improve the calorific value of pyrolysis gas, the advantages such as simultaneously to have taken into account equipment few for pyrolysis reactor, easily operates, failure rate is low。
The method processing organic waste according to embodiments of the present invention, utilize pyrolysis reactor that rubbish is carried out pyrolysis, can effectively suppress the secondary response of oil gas, improve tar yield, and have employed heat accumulating type and utilize septate heat transfer heat without heat carrier radial canal, it is not necessary to gas, consolidate heat carrier, improve the calorific value of pyrolysis gas, simultaneously because organic waste pyrolysis system can modular combination, the method is applicable to different garbage treatment quantities, it is easy to industrialization promotion。
ReferenceFig. 8, according to embodiments of the invention, the method farther includes:
S500 purified treatment
According to embodiments of the invention, the supply of described pyrolysis oil gas is carried out purified treatment to the second cyclone separator, in order to be purified oil gas and solid particle。Thus, utilize the second cyclone separator that pyrolysis oil gas is carried out purified treatment, immobilized particles and the dusts such as the semicoke being mixed in removal pyrolysis oil gas, prevent immobilized particles and dust block system, the safety and stability of raising system, and the purity of the pyrolysis oil that later separation obtains and combustion gas is high, and quality is good。Further, purified treatment separates the semicoke obtained and enters feeding screw, feeding screw conveying carry out subsequent treatment, efficiently reduce semicoke loss in production procedure, improve the utilization rate of semicoke。
ReferenceFig. 8, according to embodiments of the invention, the method farther includes:
S600 spray processes
According to embodiments of the invention, the supply of described purification oil gas is carried out spray process to spray column, in order to obtain tar and combustible gas。Thus, utilize spray to process, reduce the temperature of pyrolysis oil gas, make the tar etc. in pyrolysis oil gas liquefy, and then, by gas-liquid separation, obtain tar and combustible gas。
ReferenceFig. 8, according to embodiments of the invention, described method farther includes:
S700 combustible gas stores
Described combustible gas is stored to fuel cartridge through the supply of combustion gas air-introduced machine。Thus, utilize combustion gas air-introduced machine that combustible gas is delivered to fuel cartridge to store。According to some embodiments of the present invention, combustible gas can be delivered to pyrolysis reactor and provide the energy for pyrolysis processing, reduces the pyrolysis dependence to extra power, it is achieved the abundant comprehensive utilization of the energy。
According to embodiments of the invention, the method farther includes:
S800 combination drying crushes
Utilize spiral discharging device to supply described semicoke to combination drying machine, and carry out combination drying with coal dust and limestone, obtain the mixed material dried；Described dry mixed material supply is carried out pulverization process to disintegrating machine, obtains material powders, be crushed to 200～500 μm。Thus, mixing with coal dust and limestone, obtain mixed material in combination drying machine 900, in mixed process, coal dust and semicoke heat exchange, the moisture of coal self precipitates out dry, and mixed material is cooled to 80～200 degree。Limestone then can consolidate sulfur when gasification, reducing the sulfur content in gasification gas, addition limestone is lower than the cost of high-temperature gas desulfurization in the feed, adds limestone when gasification simultaneously and can reduce ash fusion point, reduce gasification temperature, improve the energy efficiency of gasification system, then, mixed material is carried out break process, the particle diameter of the material powders obtained is 200～500 μm, 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。
Mass ratio according to embodiments of the invention, semicoke and coal dust gross mass Yu limestone is (5-200): 1。The mass ratio of semicoke and coal dust gross mass and limestone can be adjusted according to the sulfur content of semicoke and coal dust and ash fusion point。According to embodiments of the invention, in gasification gas, sulfur content is low, and more preferably, meanwhile, ash melting point is low, and service life and energy efficiency to gasification furnace are all useful for the quality of gasification gas。
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 is 10mm。Thus, it is simple to Homogeneous phase mixing。
According to embodiments of the invention, the particle diameter of limestone is 8-12mm。According to a preferred embodiment of the invention, the particle diameter of limestone is 10mm。Thus, it is simple to Homogeneous phase mixing。
S900 gasification and melting processes
To melting furnace, the supply of described material powders being carried out gasification and melting process, obtains gasification gas and molten ash, wherein, the gasifying medium that described gasification and melting processes is described percolate and air。Thus, utilize garbage filter concentrated solution and partial air as gasifying medium, with above-mentioned mixed material for raw material, carry out gasification and melting reaction, produce gasification gas and molten ash。Hereby it is achieved that making full use of of refuse, it is prevented effectively from the generation producing garbage。According to embodiments of the invention, the liquid lime-ash that gasification produces is discharged by bottom melting furnace, becomes to produce after vitreous body the products such as fertilizer, cement, construction material through quenching。
According to embodiments of the invention, the method farther includes:
S1000 quenching
Described molten ash is carried out quenching, obtains vitreous body lime-ash。Thus, by quenching molten ash, in lime-ash, heavy metal ion content is few, and two English content are low, and vitreous body lime-ash can be used for preparing the products such as fertilizer, cement, construction material。
Below with reference to specific embodiment, the present invention will be described, it is necessary to explanation, and these embodiments are merely illustrative, and are not considered as limiting the invention。
Embodiment 1
Utilize the organic waste pyrolysis system of the embodiment of the present invention, with municipal refuse, Sichuan Hibisci Mutabilis coal and limestone for raw material, carry out garbage disposal, wherein, the structure of organic waste pyrolysis systemSuch as Fig. 6Shown in, garbage disposal flow processSuch as Fig. 9Described, wherein, domestic waste and Sichuan Hibisci Mutabilis coal component analysis asFollowing table instituteShowing, rubbish water content is 43%, and concrete waste disposal method is as follows:
1, municipal refuse is marched into the arena, and carries out rubbish pretreatment, by the not easily pyrolysis such as big particle diameter dregs, glass and metal contained in rubbish or can not the material of pyrolysis reject in advance。
2, deliver to the dry tower that promotes after the rubbish after rejecting not easily pyrogen being fed directly to sanitary fill compression dehydration and be dried process, obtain dried rubbish；
3, dried rubbish is delivered to pyrolysis reactor and carries out pyrolysis processing, obtain semicoke and pyrolysis oil gas, control to enter the combustion gas of radial canal and air stoichiometry and amount, control the temperature of pyrolysis oven, ensure that pyrolysis indoor temperature is about 680 DEG C, and controlling the rotating speed of spiral discharging device bottom pyrolysis reactor so that rubbish mean residence time is about 1.5h, then discharges pyrolysis reactor through bottom discharge spiral。
4, with the ratio of ratio 36.76:52.33:10.91, semicoke, Sichuan Hibisci Mutabilis coal coal and limestone being mixed powder process, prepared compound mean diameter is about 300 μm。
5, melting furnace gasification is fed the mixture into, gasifying agent adopts percolate and partial air, gasification and melting furnace temperature 1300 DEG C, in melting furnace, rubbish charcoal, coal react with gasifying agent generating gasification, produce gasification gas and liquid glass body lime-ash, building sand after the recovered noble metal of liquid lime-ash。
6, the pyrolysis oil gas that pyrolysis oven pyrolysis produces is after Oil-gas Separation, obtain high-quality pyrolytic tar, wherein, the pyrolysis gas of about 75% enters pyrolysis reactor burning provides fuel for pyrolysis processing, the blended gas turbine combustion generating laggard with preliminary purification of the gentle activating QI of pyrolysis gas of about 25%。
Lime-ash is analyzed: two English content in chilling slag are 1.3ng-TEQ/kg, Pb Leaching value is 0.2013mg/L, Cr Leaching value be 0.387mg/L, Cd Leaching value is 0.147mg/L, all the other do not detect, and meet about Extraction Toxicity Identification Standard of Hazardous Waste。
Embodiment 2
Utilize the organic waste pyrolysis system of the embodiment of the present invention, with municipal refuse, Huainan, Anhui anthracite and limestone for raw material, carry out garbage disposal, wherein, the structure of organic waste pyrolysis systemSuch as Fig. 6Shown in, garbage disposal flow processSuch as Fig. 9Described, wherein, domestic waste and Sichuan Hibisci Mutabilis coal component analysis asFollowing table instituteShowing, rubbish water content is 51%, and concrete waste disposal method is as follows:
1, municipal refuse is marched into the arena, and carries out rubbish pretreatment, by the not easily pyrolysis such as big particle diameter dregs, glass and metal contained in rubbish or can not the material of pyrolysis reject in advance。
2, deliver to the dry tower that promotes after the rubbish after rejecting not easily pyrogen being fed directly to sanitary fill compression dehydration and be dried process, obtain dried rubbish；
3, dried rubbish is delivered to pyrolysis reactor and carries out pyrolysis processing, obtain semicoke and pyrolysis oil gas, control to enter the combustion gas of radial canal and air stoichiometry and amount, control the temperature of pyrolysis oven, ensure that pyrolysis indoor temperature is about 700 DEG C, and controlling the rotating speed of spiral discharging device bottom pyrolysis reactor so that rubbish mean residence time is about 1.0h, then discharges pyrolysis reactor through bottom discharge spiral。
4, with the ratio of ratio 47.3:42.1:10.6, pyrolytic carbon, Huainan, Anhui anthracite, limestone being mixed powder process, prepared compound mean diameter is about 400um。
5, feeding the mixture into melting furnace gasification, gasifying agent adopts percolate and partial air, gasification and melting furnace temperature 1420 DEG C, in melting furnace, rubbish charcoal and the reaction of coal generating gasification, produce gasification gas and liquid lime-ash, building sand after the recovered noble metal of liquid lime-ash。
6, the pyrolysis oil gas that pyrolysis oven pyrolysis produces is after Oil-gas Separation, obtain high-quality pyrolytic tar, wherein, the pyrolysis gas of about 80% enters pyrolysis reactor burning provides fuel for pyrolysis processing, the blended gas turbine combustion generating laggard with preliminary purification of the gentle activating QI of pyrolysis gas of about 20%。
Lime-ash is analyzed: two English content in chilling slag are 1.1ng-TEQ/kg, Pb Leaching value is 0.2375mg/L, Cr Leaching value is 0.409mg/L, Cd Leaching value is 0.185mg/L, Hg Leaching value is 0.024mg/L, all the other do not detect, and meet about Extraction Toxicity Identification Standard of Hazardous Waste。
In the description of this specification, specific features, structure, material or feature that the description of reference term " embodiment ", " some embodiments ", " example ", " concrete example " or " some examples " etc. means in conjunction with this embodiment or example describe are 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 referring to identical embodiment or example。And, the specific features of description, structure, material or feature can combine in an appropriate manner in any one or more embodiments or example。
Although an embodiment of the present invention has been shown and described, it will be understood by those skilled in the art that: when without departing from principles of the invention and objective, these embodiments can be carried out multiple change, amendment, replacement and modification, the scope of the present invention byClaimAnd equivalent limits。
Claims (10)
1. an organic waste pyrolysis system, it is characterised in that including:
Screening machine, feeding screw, dry lifting tower, the first cyclone separator, and pyrolysis reactor, wherein, described screening machine, described feeding screw, described dry lifting tower, described first cyclone separator and described pyrolysis reactor are sequentially connected logical,
Wherein, described pyrolysis reactor includes:
Pyrolysis garbage inlet and semicoke outlet；
Described pyrolysis garbage inlet is positioned at the top of described pyrolysis reactor, and is connected with the outlet of described solid refuse；
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 the short transverse multi-tier arrangement of described pyrolysis reactor, every layer has many heat accumulation type radiant tubes parallel to each other in the horizontal direction, and the exhanst gas outlet on described heat accumulation type radiant tube is connected with the smoke inlet of described dry lifting tower；
Oil gas derives pipeline, and described oil gas is derived and is provided with through hole on the tube wall of pipeline；
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,
Described gas-collecting branch pipe extends through the sidewall of described pyrolysis reactor and extend in described pyrolysis reactor and be connected with described oil gas derivation pipeline。
2. system according to claim 1, it is characterised in that described gas-collecting branch pipe is multiple, and arranged parallel to each other along the length direction of described gas gathering manifold,
Optional, described gas-collecting branch pipe is perpendicular to described gas gathering manifold。
3. system according to claim 1 and 2, it is characterised in that described oil gas derives the pipeline short transverse multi-tier arrangement along described reactor, every layer has many oil gas parallel to each other in the horizontal direction and derives pipeline,
Optional, described oil gas is derived pipeline and is arranged in parallel with described heat accumulation type radiant tube, and the respective left and right sides of described heat accumulation type radiant tube is symmetrically arranged with two oil gas and derives pipeline。
4. the system according to any one of claim 1-3, it is characterised in that described oil gas derives 1/2-3 times that the distance between the tube wall of pipeline and contiguous described heat accumulation type radiant tube is described oil gas derivation 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 derived at described oil gas and is 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. the system according to any one of claim 1-4, it is characterised in that farther include:
Second cyclone separator, described second cyclone separator has pyrolysis oil gas mixture entrance, purifies oil gas vent and solid particle outlet, and described pyrolysis oil gas mixture entrance is connected with described gas gathering manifold,
Optional, described system farther includes:
Spiral discharging device, described spiral discharging device has semicoke entrance and semicoke mixture outlet, and described semicoke entrance is connected with the outlet of described semicoke,
Optional, described system farther includes:
Spray column, described spray column has purification oil gas entrance, tar outlet and combustible gas outlet, and described purification oil gas entrance is connected with described purification oil gas vent,
Optional, described system farther includes:
Combustion gas air-introduced machine, described combustion gas air-introduced machine has fuel gas inlet and gas outlet, and described fuel gas inlet is connected with the outlet of described combustible gas；And
Fuel cartridge, described fuel cartridge has storage tank fuel gas inlet and storage tank gas outlet, and described storage tank fuel gas inlet is connected with described gas outlet。
6. the system according to any one of claim 1-5, it is characterised in that farther include:
Combination drying machine, described combination drying facility have semicoke entrance, coal entrance, limestone entrance and mixed material outlet, and described semicoke entrance is connected with described semicoke mixture outlet；
Disintegrating machine, described disintegrating machine has mixed material entrance and broken material outlet, and described mixed material entrance is connected with the outlet of described mixed material；And
Melting furnace, described melting furnace has gasification and melting material inlet, gasifying medium entrance, gasification gas outlet and slag-drip opening, described gasification and melting material inlet is connected with the outlet of described broken material, and described gasifying medium entrance is connected with the outlet of described percolate。
7. the organic waste pyrolysis system that a kind utilizes described in any one of claim 1-6 processes the method for organic waste, it is characterised in that including:
Organic waste supply is carried out Screening Treatment to described screening machine, in order to obtain the organic waste after percolate and screening；
By the organic waste after described screening in described feeding screw supply to described dry lifting tower, adopt flue gas that described organic waste is dried lifting and process, in order to obtain the dry mixed material containing flue gas and garbage drying；
The supply of the described dry mixed material containing flue gas and garbage drying is easily separated process to described first cyclone separator, in order to separate and obtain flue gas and solid refuse；And
The supply of described solid refuse is carried out pyrolysis processing to described pyrolysis reactor, in order to obtain pyrolysis oil gas and semicoke, and the flue gas supply described pyrolysis processing produced is to described dry riser。
8. method according to claim 7, it is characterised in that farther include:
The supply of described pyrolysis oil gas is carried out purified treatment to the second cyclone separator, in order to be purified oil gas and solid particle,
Optionally, described method farther includes:
The supply of described purification oil gas is carried out spray process to spray column, in order to obtain tar and combustible gas,
Optionally, described method farther includes:
Described combustible gas is stored to fuel cartridge through the supply of combustion gas air-introduced machine。
9. the method according to claim 7 or 8, it is characterised in that farther include:
Utilize spiral discharging device to supply described semicoke to combination drying machine, and carry out combination drying with coal dust and limestone, in order to obtain the mixed material dried；
Described dry mixed material supply is carried out pulverization process to disintegrating machine, in order to obtain material powders, be crushed to 200～500 μm；And
To melting furnace, the supply of described material powders being carried out gasification and melting process, in order to obtain gasification gas and molten ash, wherein, the gasifying medium that described gasification and melting processes is described percolate and air,
Optionally, described method farther includes:
Described molten ash is carried out quenching, obtains vitreous body lime-ash。
10. the method according to any one of claim 7-9, it is characterised in that the mass ratio of described semicoke and described coal dust gross mass and described limestone is (5-200): 1。
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201610118525.4A CN105694925B (en) | 2016-03-02 | 2016-03-02 | Organic waste pyrolysis system and its application |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201610118525.4A CN105694925B (en) | 2016-03-02 | 2016-03-02 | Organic waste pyrolysis system and its application |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN105694925A true CN105694925A (en) | 2016-06-22 |
| CN105694925B CN105694925B (en) | 2018-02-27 |
Family
ID=56223817
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201610118525.4A Active CN105694925B (en) | 2016-03-02 | 2016-03-02 | Organic waste pyrolysis system and its application |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN105694925B (en) |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108328898A (en) * | 2017-01-18 | 2018-07-27 | 中国石油化工股份有限公司 | A kind of recycling processing method and device of oily sludge |
| CN114515524A (en) * | 2021-12-27 | 2022-05-20 | 重庆中天海智生态环境科技有限公司 | Soil remediation thermal desorption equipment and process thereof |
| CN114728861A (en) * | 2019-07-04 | 2022-07-08 | 盈思培肥料有限公司 | improved fertilizer |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2013064864A1 (en) * | 2011-11-03 | 2013-05-10 | Sorefor S.A. | Mobile modular system for exploiting the energy from forest residues |
| CN203683470U (en) * | 2014-01-08 | 2014-07-02 | 北京神雾环境能源科技集团股份有限公司 | System for collecting oil and gas generated in pyrolysis of coal in heat-accumulating-type radiant tube rotary furnace |
| CN204039347U (en) * | 2014-08-14 | 2014-12-24 | 北京神雾环境能源科技集团股份有限公司 | One way of life refuse pyrolysis comprehensive resource treatment system |
| CN204529748U (en) * | 2015-04-01 | 2015-08-05 | 曲靖众一精细化工股份有限公司 | A kind of fine particle four sections of moving-bed retorting furnaces |
| CN205635472U (en) * | 2016-03-02 | 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
- 2016-03-02 CN CN201610118525.4A patent/CN105694925B/en active Active
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2013064864A1 (en) * | 2011-11-03 | 2013-05-10 | Sorefor S.A. | Mobile modular system for exploiting the energy from forest residues |
| CN203683470U (en) * | 2014-01-08 | 2014-07-02 | 北京神雾环境能源科技集团股份有限公司 | System for collecting oil and gas generated in pyrolysis of coal in heat-accumulating-type radiant tube rotary furnace |
| CN204039347U (en) * | 2014-08-14 | 2014-12-24 | 北京神雾环境能源科技集团股份有限公司 | One way of life refuse pyrolysis comprehensive resource treatment system |
| CN204529748U (en) * | 2015-04-01 | 2015-08-05 | 曲靖众一精细化工股份有限公司 | A kind of fine particle four sections of moving-bed retorting furnaces |
| CN205635472U (en) * | 2016-03-02 | 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 |
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108328898A (en) * | 2017-01-18 | 2018-07-27 | 中国石油化工股份有限公司 | A kind of recycling processing method and device of oily sludge |
| CN108328898B (en) * | 2017-01-18 | 2021-04-06 | 中国石油化工股份有限公司 | Resourceful treatment method and device for oily sludge |
| CN114728861A (en) * | 2019-07-04 | 2022-07-08 | 盈思培肥料有限公司 | improved fertilizer |
| CN114728861B (en) * | 2019-07-04 | 2024-03-29 | 盈思培肥料营运有限公司 | improved fertilizer |
| CN114515524A (en) * | 2021-12-27 | 2022-05-20 | 重庆中天海智生态环境科技有限公司 | Soil remediation thermal desorption equipment and process thereof |
Also Published As
| Publication number | Publication date |
|---|---|
| CN105694925B (en) | 2018-02-27 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN102329653A (en) | Plasma garbage gasification device and process | |
| CN103204642A (en) | Novel dry-process cement kiln household garbage incineration method | |
| CN105219417A (en) | Biomass pyrolysis system and biomass are carried out to the method for pyrolysis | |
| CN106500107A (en) | A kind of system and method for refuse pyrolysis gasification and melting | |
| CN102260537A (en) | Device for preparing combustible gas by virtue of plasma pyrolysis and oxygen-enriched combustion-supporting material | |
| CN105694925A (en) | Organic waste pyrolysis system and application thereof | |
| CN205635475U (en) | Organic garbage pyrolytic system | |
| CN102329654B (en) | Biomass gasification device and process | |
| CN106513423A (en) | Waste circuit board recycling system and method | |
| CN109824271A (en) | It handles the method for house refuse and implements its system | |
| CN205635472U (en) | Organic garbage pyrolytic system | |
| CN105754622A (en) | Organic garbage pyrolysis system and application thereof | |
| CN102786951B (en) | Crude gas guiding device for coal pyrolyzing furnace | |
| CN105885884A (en) | Organic waste pyrolysis system and application thereof | |
| CN205635474U (en) | Organic garbage pyrolytic system | |
| CN105885885A (en) | Organic waste pyrolysis system and application thereof | |
| CN205933743U (en) | Organic garbage pyrolytic system | |
| CN206661886U (en) | The system for handling house refuse | |
| CN106047382A (en) | Automatic-dust-removal refuse pyrolysis and cracking system | |
| CN205501187U (en) | Pyrolysis reactor | |
| CN206519427U (en) | The system for handling house refuse | |
| CN102786952B (en) | Crude gas condensing device for coal pyrolyzing furnace | |
| CN206316118U (en) | The system for handling house refuse | |
| CN105157033A (en) | System and method for pyrolyzing and treating garbage | |
| CN206280976U (en) | The system for the treatment of house refuse and percolate |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| CB02 | Change of applicant information | ||
| CB02 | Change of applicant information |
Address after: 102200 Beijing city Changping District Machi Town cow Road No. 18 Applicant after: Shenwu Technology Group Co.,Ltd. Address before: 102200 Beijing city Changping District Machi Town cow Road No. 18 Applicant before: BEIJING SHENWU ENVIRONMENT AND ENERGY TECHNOLOGY Co.,Ltd. |
|
| GR01 | Patent grant | ||
| GR01 | Patent grant | ||
| PP01 | Preservation of patent right | ||
| PP01 | Preservation of patent right |
Effective date of registration: 20190121 Granted publication date: 20180227 |
|
| PD01 | Discharge of preservation of patent | ||
| PD01 | Discharge of preservation of patent |
Date of cancellation: 20220921 Granted publication date: 20180227 |
|
| PP01 | Preservation of patent right | ||
| PP01 | Preservation of patent right |
Effective date of registration: 20220921 Granted publication date: 20180227 |