CN107937007A - A kind of three-stage coal dust and biomass pyrolytic processing system - Google Patents
A kind of three-stage coal dust and biomass pyrolytic processing system Download PDFInfo
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- CN107937007A CN107937007A CN201711405141.1A CN201711405141A CN107937007A CN 107937007 A CN107937007 A CN 107937007A CN 201711405141 A CN201711405141 A CN 201711405141A CN 107937007 A CN107937007 A CN 107937007A
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- 239000002028 Biomass Substances 0.000 title claims abstract description 69
- 239000002817 coal dust Substances 0.000 title claims abstract description 26
- 238000000197 pyrolysis Methods 0.000 claims abstract description 111
- 239000000463 material Substances 0.000 claims abstract description 39
- 238000011084 recovery Methods 0.000 claims abstract description 36
- 239000002918 waste heat Substances 0.000 claims abstract description 36
- 239000003077 lignite Substances 0.000 claims abstract description 35
- 239000002994 raw material Substances 0.000 claims abstract description 31
- 238000001035 drying Methods 0.000 claims abstract description 26
- 238000006243 chemical reaction Methods 0.000 claims abstract description 16
- 238000010791 quenching Methods 0.000 claims abstract description 16
- 239000003245 coal Substances 0.000 claims abstract description 15
- 239000007789 gas Substances 0.000 claims description 49
- 238000010438 heat treatment Methods 0.000 claims description 36
- 239000004744 fabric Substances 0.000 claims description 25
- 239000000571 coke Substances 0.000 claims description 21
- 238000002156 mixing Methods 0.000 claims description 20
- 239000002737 fuel gas Substances 0.000 claims description 13
- 238000010792 warming Methods 0.000 claims description 9
- 230000000171 quenching effect Effects 0.000 claims description 6
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims description 5
- 239000002826 coolant Substances 0.000 claims description 5
- 239000003546 flue gas Substances 0.000 claims description 5
- 230000005540 biological transmission Effects 0.000 claims description 3
- 239000003921 oil Substances 0.000 abstract description 22
- 238000000034 method Methods 0.000 abstract description 8
- 239000000567 combustion gas Substances 0.000 abstract description 7
- 239000012075 bio-oil Substances 0.000 abstract description 6
- 230000011218 segmentation Effects 0.000 abstract description 3
- 238000009825 accumulation Methods 0.000 description 6
- 238000005516 engineering process Methods 0.000 description 4
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 2
- 238000000605 extraction Methods 0.000 description 2
- 239000005416 organic matter Substances 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- 229910052717 sulfur Inorganic materials 0.000 description 2
- 239000011593 sulfur Substances 0.000 description 2
- 229910000831 Steel Inorganic materials 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 239000000919 ceramic Substances 0.000 description 1
- 239000003610 charcoal Substances 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 238000009826 distribution Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 230000005484 gravity Effects 0.000 description 1
- 239000004615 ingredient Substances 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 239000011368 organic material Substances 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 239000010959 steel Substances 0.000 description 1
- 238000003860 storage Methods 0.000 description 1
- 230000002195 synergetic effect Effects 0.000 description 1
- 238000005979 thermal decomposition reaction Methods 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
- C10B57/00—Other carbonising or coking processes; Features of destructive distillation processes in general
- C10B57/02—Multi-step carbonising or coking processes
-
- 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
- C10B53/02—Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form of cellulose-containing material
-
- 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
- C10B53/04—Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form of powdered 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
- C10G1/00—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E50/00—Technologies for the production of fuel of non-fossil origin
- Y02E50/10—Biofuels, e.g. bio-diesel
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
- Y02P20/129—Energy recovery, e.g. by cogeneration, H2recovery or pressure recovery turbines
Abstract
The present invention relates to a kind of three-stage coal dust and biomass pyrolytic reaction system, mainly include：Riser arrangement, raw material bucket, pyrolysis reactor, waste-heat recovery device, oil wash Quench tower apparatus and air accumulator are dried, wherein：The pyrolysis reactor is divided into high temperature pyrolysis section, middle low temperature pyrogenation section and waste heat recovery section, the drying riser arrangement is by the raw material bucket by biomass, lignite enters the high temperature pyrolysis section and middle low temperature pyrogenation section carries out segmentation pyrolysis processing, the arrangement achieves the integrated treatment to coal dust and biomass, the bio oil resource for the clean environment firendly being fully extracted in combustion gas resource and the biomass resource in coal resources, realize that system organically combines, and play the pyrolysis advantage of different material, the heat of product in pyrolytic process is fully recycled at the same time, improve system thermal efficiency.
Description
Technical field
The invention belongs to the pyrolysis processing of the Organic Ingredients in chemical industry, and in particular to a kind of three-stage coal dust and biomass thermal
Solve processing system.
Background technology
Coal resources in China and biomass resource are all very abundant, and low-order coal such as jet coal and lignite in coal are biologies
Matter transformed next primary coal after many years, therefore biomass and low-order coal have many similitudes from structure.Coal
Charcoal and biomass pyrolytic technology can fully extract the organic matter in raw material, become valuable oil gas.Currently for two
Kind raw material all develops many reaction systems, and the two kinds of raw materials blending of Ye You research institutions primary study are pyrolyzed, to play
The synergistic effect of two kinds of raw materials.But biomass material sulfur content is low, and sulfur content of coal is generally high, two kinds of raw material blending carry out again
Many problems are brought during the product later use that pyrolysis processing obtains, do not play the excellent of this clean renewable resources of biomass
Gesture.
The content of the invention
The present invention in view of the deficiencies of the prior art, with reference to the characteristics of pulverized coal pyrolysis and biomass pyrolytic, develops one kind three
Segmentation coal dust and biomass pyrolytic processing system, take single reaction process, simply and easily realize to coal dust and life very much
The integrated treatment of material, the bio oil for the clean environment firendly being fully extracted in combustion gas resource and the biomass resource in coal resources
Resource, realizes that system organically combines, and plays the pyrolysis advantage of different material, while the heat of product in pyrolytic process is carried out
Fully recycling, improves system thermal efficiency.
In order to solve the above technical problems, the technical solution that the present invention takes is：
The present invention proposes a kind of three-stage coal dust and biomass pyrolytic reaction system, including：Dry riser arrangement, raw material
Bucket, pyrolysis reactor, waste-heat recovery device, oil wash Quench tower apparatus and air accumulator, wherein：
The pyrolysis reactor is divided into high temperature pyrolysis section, middle low temperature pyrogenation section and waste heat recovery section from top to bottom, wherein, institute
State high temperature pyrolysis section and be equipped with material collecting device and Multi-layer warming device, wherein, the material collecting device is arranged at the Multi-layer warming dress
The lower section put, the high-temperature semi-coke produced for collecting pyrolysis；The cloth of Multi-layer staggered arrangement is equipped with the middle low temperature pyrogenation section
Cone, every layer of cloth cone is multiple；The waste heat recovery section is equipped with heat-exchanger rig；
The drying riser arrangement respectively send lignite, biomass to the raw material bucket respectively, will be brown by the raw material bucket
Coal, biomass respectively enter the high temperature pyrolysis section and middle low temperature pyrogenation section；
The waste-heat recovery device is connected with the air accumulator, the oil wash Quench tower apparatus respectively with the middle low temperature pyrogenation section
And heating unit connection；The waste-heat recovery device is by the pyrolysis pneumatic transmission that the high temperature pyrolysis section produces to the air accumulator；Institute
The circulation that oil wash quenching column realizes oil using oil circulating pump is stated, and is exported in oil circulating pump and sets what heat exchanger produced quenching column
Heat exchanges heat.
Further, the pyrolysis reactor includes furnace body, and the furnace body includes：Epimere pyrolysis gas outlet and hypomere pyrolysis
Gas exports, and the inner cavity of the furnace body is divided into epimere high temperature pyrolysis area, stage casing more than low temperature pyrogenation section and hypomere from top to bottom
Heat-recovery section, the ratio of the vertical length of low temperature pyrogenation section and hypomere waste heat recovery section in the epimere high temperature pyrolysis area, stage casing
Scope is 3:2:1-5:3:1.
Further, the furnace body further includes：First charging aperture and cold burnt discharge port, the first charging aperture are arranged at institute
The top of furnace body is stated, the epimere pyrolysis gas outlet is arranged at the sidepiece of the furnace body and under the high temperature pyrolysis section
Side, the hypomere pyrolysis gas outlet is arranged at the sidepiece of the furnace body and positioned at the downside of the middle low temperature pyrogenation section, described cold
Burnt discharge port is arranged at the bottom of the furnace body.
Further, the three-stage coal dust and biomass pyrolytic reaction system further include coke bin, the coke bin with it is described
Cold Jiao's discharge port connection.
Further, the heating unit includes fuel gas inlet, air intlet and exhanst gas outlet, and the heat-exchanger rig includes
Hot air outlet and inlet of cold air, wherein, the air intlet of the hot air outlet of the heat-exchanger rig and the heating unit
It is connected, enters the heating unit using the cooling medium after heat exchange as combustion-supporting gas foldback.
Further, the material collecting device is broach hopper, its bottom is exported equipped with batch mixing, and sidepiece, which is equipped with, runs through the stove
The second charging aperture of body, biomass material are mixed by the second charging aperture into the broach hopper with the high-temperature semi-coke
Close, under drop down onto and carry out being sufficiently mixed contact pyrolysis on cloth cone, obtain mixing semicoke, the mixing semicoke enters described remaining
Heat-recovery section.
Further, the drying riser arrangement includes biomass drying riser, lignite drying riser, the original
Hopper includes biomass material bucket, lignite raw material bucket, the exhanst gas outlet and the lignite drying riser, lignite raw material bucket according to
It is secondary to be linked in sequence；The lignite raw material bucket is connected with the first charging aperture；Described biomass material bucket one end and described second
Feed inlet connects, and the other end is connected with biomass drying riser, and the biomass drying riser is dried with the lignite
Dry riser connects, and entering biomass from lignite drying riser again after flue gas drying lignite dries riser to biomass
Dried.
Further, the number of plies of the heating unit is 10-30 layers, and every layer of heating unit includes multiple heating and fill
Put；The heating unit is heat accumulation type radiant tube, and more than 1000 DEG C of flue gas is produced in the heating unit.
Further, the number of plies of cloth cone is 8-20 layer, and often the spacing of adjacent two layers is 100-400mm, in every layer
The spacing of two neighboring cloth cone is 50-300mm；The positive triangular pyramid for a length of 50-200mm of rib of the cloth cone.
Further, the waste heat recovery section is equipped with heat exchanger tube, and the cooling medium is cold air, the cold air heat exchange
Be warming up to afterwards 300-400 DEG C by the external connecting tube enter the high temperature pyrolysis section heating unit in fuel gas buring,
Mixing semicoke temperature after heat exchange is arranged outside after being down to 60 DEG C by belt feeder.
Beneficial effects of the present invention include at least：
1）Three-stage coal dust and biomass pyrolytic reaction system of the present invention are simple in structure, take three-stage pyrolytic reaction,
Different products is obtained, realizes the at utmost utilization to material；
2）Single reaction process is taken, simply and easily realizes very much the integrated treatment to coal dust and biomass, fully extraction
The bio oil resource of combustion gas resource in coal resources and the clean environment firendly in biomass resource, realizes that system organically combines,
And the pyrolysis advantage of different material is played, while the heat of product in pyrolytic process is fully recycled, improve system thermal effect
Rate.
Brief description of the drawings
Fig. 1 is schematic structural view of the invention.
Wherein, furnace body 1, first charging aperture 101, epimere pyrolysis gas outlet 102, hypomere pyrolysis gas outlet 103, cold burnt discharging
Mouthfuls 104, heating unit 2, air intlet 201, fuel gas inlet 202, exhanst gas outlet 203, material collecting device 3, batch mixing outlet 301, the
Two feed inlets 302, cloth cone 4, heat-exchanger rig 5, external connecting tube 6, high temperature pyrolysis section 7, middle low temperature pyrogenation section 8, waste heat recovery
Section 9, lignite raw material bucket 10, biomass material bucket 11, lignite drying riser 12, biomass drying riser 13, waste heat recovery
Device 14, oil wash Quench tower apparatus 15, coke bin 16, air accumulator 17, heat exchanger 18, oil circulating pump 19.
Embodiment
In order to make those skilled in the art more fully understand technical scheme, below in conjunction with specific embodiment pair
The present invention is described in further detail.The embodiments described below is exemplary, and is only used for explaining the present invention, and cannot be managed
Solve as limitation of the present invention.Particular technique or condition are not specified in embodiment, it is described according to document in the art
Technology or condition are carried out according to product description.
According to an embodiment of the invention, Fig. 1 is schematic structural view of the invention, with reference to shown in Fig. 1, three-stage of the present invention
Coal dust and biomass pyrolytic reaction system, including：Dry riser arrangement, biomass material bucket 11, lignite raw material bucket 10, pyrolysis
Reactor, waste-heat recovery device 14, oil wash Quench tower apparatus 15 and air accumulator 17, wherein：
The pyrolysis reactor includes furnace body 1, and the furnace body includes：Epimere pyrolysis gas outlet 102 and hypomere pyrolysis gas outlet
103, the inner cavity of the furnace body is divided into high temperature pyrolysis section 7, middle low temperature pyrogenation section 8 and waste heat recovery section 9 from top to bottom, its
In, the high temperature pyrolysis section 7 is equipped with material collecting device and 3 Multi-layer warming devices 2, wherein, the material collecting device 3 is arranged at described more
The lower section of layer heating unit 2, the high-temperature semi-coke produced for collecting pyrolysis；Multi-layer staggered is equipped with the middle low temperature pyrogenation section 8
The cloth cone 4 of arrangement, every layer of cloth cone include multiple cloth cones 4；The waste heat recovery section 9 is equipped with heat-exchanger rig 5；
The drying riser arrangement includes biomass drying riser 13 and lignite drying riser 12, the biomass drying
Riser 13 and lignite drying riser respectively send biomass, lignite to the biomass material bucket 11, lignite raw material respectively
Bucket 10, the middle low temperature pyrogenation section 8, high temperature pyrolysis section are respectively enterd by the biomass material bucket 11, lignite raw material bucket 10
7；
Described 14 one end of waste-heat recovery device is exported with the epimere pyrolysis gas 102, and the other end is connected with the air accumulator 17, institute
State 15 input end of oil wash Quench tower apparatus with the hypomere pyrolysis gas outlet 103 to be connected, gas outlet and the high temperature pyrolysis section 7
The fuel gas inlet connection of heating unit；The waste-heat recovery device 14 is by the pyrolysis pneumatic transmission that the high temperature pyrolysis section 7 produces to institute
State air accumulator 17；The oil wash quenching column realizes the circulation of oil using oil circulating pump 19, and exports setting in oil circulating pump 19 and change
The heat that hot device 18 produces quenching column exchanges heat.
According to an embodiment of the invention, with reference to shown in Fig. 1, the inner cavity of furnace body of the present invention is divided into along short transverse
High temperature pyrolysis section 7, middle low temperature pyrogenation section 8 and waste heat recovery section 9, wherein, the high temperature pyrolysis section 7, middle low temperature pyrogenation section 8 and remaining
The vertical length ratio of heat-recovery section 9 is 3:2:1-5:3:1.
According to an embodiment of the invention, with reference to shown in Fig. 1, furnace body 1 of the present invention includes：First charging aperture 101, epimere
Pyrolysis gas outlet 102, hypomere pyrolysis gas outlet 103 and cold burnt discharge port 104, wherein, the first charging aperture 101 is arranged at institute
The top of furnace body 1 is stated, the epimere pyrolysis gas outlet 102 is arranged at the sidepiece of the furnace body 1 and is located at the high temperature pyrolysis section 7
Downside, the hypomere pyrolysis gas outlet 103 is arranged at the sidepiece of the furnace body 1 and under the middle low temperature pyrogenation section 8
Side, the cold burnt discharge port 104 are arranged at the bottom of the furnace body 1.
According to an embodiment of the invention, with reference to shown in Fig. 1, heating unit described in multilayer of the present invention is arranged at the high warm
Section is solved, every layer of heating unit includes multiple heating units, it is preferred that the number of plies of heating unit of the present invention is 10-30
Layer.
According to some embodiments of the present invention, heating unit of the present invention is heat accumulation type radiant tube, with reference to shown in Fig. 1,
Including：Air intlet, fuel gas inlet and exhanst gas outlet through the furnace body, through the air intlet and fuel gas inlet to described
Heat accumulation type radiant tube each leads into air and fuel gas buring, produces more than 1000 DEG C of flue gas, passes through the heat accumulation type radiant tube
Indirectly heat is carried out to the material in the high temperature pyrolysis section.
According to an embodiment of the invention, with reference to shown in Fig. 1, material collecting device of the present invention is arranged at the high temperature pyrolysis section
And positioned at the lower section of the heat accumulation type radiant tube, the material collecting device is preferably broach hopper, its bottom is exported equipped with batch mixing, side
Portion is equipped with the second charging aperture through the furnace body, first charging aperture of the material through the furnace body be sent into the high temperature pyrolysis section into
Row pyrolysis, the high-temperature semi-coke of generation are fallen into the broach hopper, then by the second charging aperture into the broach hopper
It is sent into room temperature material to mix with the high-temperature semi-coke, carries out being sufficiently mixed contact on the cloth cone by dropping down onto under self gravitation
And be pyrolyzed, obtain mixing semicoke.
According to an embodiment of the invention, with reference to shown in Fig. 1, cloth cone shifts to install low in described described in multilayer of the present invention
Warm pyrolysis section, every layer of cloth cone include multiple cloth cones.
According to some embodiments of the present invention, the number of plies of the cloth cone is 8-20 layers, and the spacing per adjacent two layers is
100-400mm, the spacing of two neighboring cloth cone is 50-300mm in every layer；Cloth cone for a length of 50-200mm's of rib
Positive triangular pyramid, material are ceramics or heat resisting steel.
According to an embodiment of the invention, with reference to shown in Fig. 1, heat-exchanger rig of the present invention is arranged at the waste heat recovery
Section, the heat-exchanger rig include inlet of cold air and hot air outlet, and the hot air outlet of the heat-exchanger rig passes through outside described
The air intake that connecting tube is put with the heating unit is connected；According to some embodiments of the present invention, heat exchange dress of the present invention
Preferably heat exchanger tube is put, the cooling medium is cold air.
According to an embodiment of the invention, with reference to shown in Fig. 1, external connecting tube of the present invention is arranged at outside the furnace body,
And the both ends of the external connecting tube respectively with the air intake of the heating unit and the hot air outlet of the heat-exchanger rig
It is connected, be warming up to 300-400 DEG C after the cold air heat exchange enters adding for the high temperature pyrolysis section by the external connecting tube
By being arranged outside belt feeder after 60 DEG C being down in thermal with fuel gas buring, mixing semicoke temperature after heat exchange.
In a specific embodiment of the present invention, the lignite raw material bucket, the lignite in biomass material bucket and biomass are former
Material enters the high temperature pyrolysis section, middle low temperature pyrogenation section by the first charging aperture, second charging aperture respectively, and lignite is described
In high temperature pyrolysis section, contacted with the radiant tube that surface temperature is more than 1000 DEG C and rely on gravity fall, produced in dropping process
Raw a large amount of pyrolysis gas and high-temperature semi-coke, and tar fully cracks at high temperature, wherein the temperature of pyrolysis gas is 650-850 DEG C, heat
The temperature for solving semicoke is 500-750 DEG C；
High temperature pyrolysis gas are discharged into the waste-heat recovery device from the epimere pyrolysis gas outlet, in the waste-heat recovery device
In, pyrolysis gas temperature is reduced to less than 120 DEG C, into the air accumulator, is supplied as outside unstripped gas；
Life of the low temperature pyrogenation section with entering the middle low temperature pyrogenation section by the second charging aperture during the pyrolysis char enters
Raw material of substance is tentatively mixed, and realizes sufficiently heating by the distribution of gusset cone, makes biomass in heat
The middle low temperature pyrogenation temperature range for solving 500-600 DEG C of temperature produces substantial amounts of oil gas, and is sent into through the hypomere pyrolysis gas outlet
The oil wash Quench tower apparatus, recycles substantial amounts of bio oil, and the pyrolysis gas of generation is then directly entered the spoke of the high temperature pyrolysis section
Pipe is penetrated to burn；
After lignite semi-coke and biomass semicoke are sufficiently mixed, mixing semicoke is obtained, temperature is 400-450 DEG C, passes through the waste heat
Exhausting section, is preheated to normal temperature air and is sent after 300-400 DEG C to the heating tube of high temperature pyrolysis section, and after semicoke is down to less than 60 DEG C
Directly sent by the cold burnt discharge port to the coke bin.
According to some embodiments of the present invention, the work of three-stage coal dust and biomass pyrolytic reaction system of the present invention
Principle is：Lignite through the lignite drying riser drying lifting after enters the lignite hopper, its at this time, from high temperature pyrolysis
The flue-gas temperature of section is 200-250 DEG C after heat exchange；The raw material of the lignite hopper is sent lignite by the first charging aperture
Enter the high temperature pyrolysis section, by heat accumulation type radiant tube indirectly heat, pyrolysis temperature control is 800-1100 DEG C, and material is described
High temperature pyrolysis section is fallen by self gravitation, concurrently raw pyrolytic reaction, and the organic matter in material largely discharges generation temperature
The pyrolysis gas and high-temperature semi-coke for 650-850 DEG C are spent, the pyrolysis gas is discharged into described remaining from the epimere pyrolysis gas outlet
Heat reclamation device, the temperature of pyrolysis gas is down to less than 120 DEG C described in the waste-heat recovery device, and eventually enters into the storage
Gas tank, supplies as outside unstripped gas；And the high-temperature semi-coke that the temperature produced is 500-750 DEG C is converged by the broach hopper
Collection, at this time, is passed through biomass material to the broach hopper again by the second charging aperture and is mixed with the high-temperature semi-coke, leads to
Cross under self gravitation and drop down onto the middle low temperature pyrogenation section, bored by the cloth, the high-temperature semi-coke and the room temperature biomass
Material is sufficiently mixed contact, and realizes fully heating by triangle cloth cone, makes biomass in 500-600 DEG C of pyrolysis temperature
Middle low temperature pyrogenation temperature range produce substantial amounts of oil gas, pyrolysis gas and mixing semicoke, the oil gas is through the hypomere pyrolysis gas
The oil wash Quench tower apparatus is sent into outlet, recycles substantial amounts of bio oil, the pyrolysis gas of generation is sent directly into high temperature pyrolysis section
Heating tube is burnt, and is dropped down onto the waste heat recovery section under the mixing semicoke, is exchanged heat by the heat exchanger tube, to described
Mixing semicoke further carries out waste heat recovery, and more specifically, the entrance through the heat exchanger tube is passed through cold air and exchanges heat, described
Cold air heat exchange after be warming up to 300-400 DEG C by the external connecting tube enter the high temperature pyrolysis section heating unit in
Fuel gas buring, makes full use of heat, saves the consumption of high temperature pyrolysis section combustion gas, and mixing semicoke temperature after heat exchange is down to
Through cold burnt discharge port by being arranged outside belt feeder after 60 DEG C.
According to some embodiments of the present invention, the present invention takes the pyrolysis of high temperature pyrolysis section to be obtained to the volatile matter in raw material
To maximum extraction, and by Pintsch process, the oil vapour produced in raw material is cracked into combustion gas, can produce a large amount of high-quality
Fuel gas or unstripped gas, and the thermal decomposition product of oily yield very high temperature can be obtained by the pyrolysis of middle low temperature pyrogenation section, realization pair
Raw material and heat make full use of, and the heat for mixing semicoke is fully recycled using waste heat recovery section, by waste heat recovery section
Hot-air after mixed heat, is entered in the heating unit of the high temperature pyrolysis section with fuel gas buring by the external connecting tube, filled
Divide and utilize heat, save the consumption of high temperature pyrolysis section combustion gas, so as to improve energy utilization efficiency, reduce production cost.
Inventor has found that three-stage coal dust and biomass pyrolytic reaction system according to the present invention are simple in structure, adopt
Three-stage pyrolytic reaction is taken, obtains different products, realizes the at utmost utilization to material；Meanwhile the present invention utilizes high temperature
The heat carrier for pyrolysis high-temperature semi-coke low temperature pyrogenation section as in that pyrolysis section produces, realizes the segmentation pyrolysis to carbonaceous organic material
Utilize, and the waste heat of high-temperature semi-coke is fully recycled, making full use of for energy is realized, so as to reduce the energy in pyrolytic process
Consumption, and realize the simplification of technique, moreover, it is achieved that the integrated treatment to coal dust and biomass, is fully extracted coal resources
In combustion gas resource and the clean environment firendly in biomass resource bio oil resource, realize that system organically combines, and play difference
The pyrolysis advantage of raw material.
In the description of the present invention, it is to be understood that the orientation or position relationship of the instruction such as term " on ", " under " are base
In orientation shown in the drawings or position relationship, description description of the invention and simplified, rather than instruction or hint are for only for ease of
Signified device or element must have specific orientation, with specific azimuth configuration and operation, therefore it is not intended that to this
The limitation of invention.
In the description of this specification, reference term " one embodiment ", " some embodiments ", " example ", " specifically show
The description of example " or " some examples " etc. means specific features, structure, material or the spy for combining the embodiment or example description
Point is contained at least one embodiment of the present invention or example.In the present specification, schematic expression of the above terms is not
It must be directed to identical embodiment or example.Moreover, particular features, structures, materials, or characteristics described can be any
Combined in an appropriate manner in a or multiple embodiments or example.In addition, without conflicting with each other, the technology of this area
Different embodiments or example described in this specification and different embodiments or exemplary feature can be combined by personnel
And combination.
Although the embodiment of the present invention has been shown and described above, it is to be understood that above-described embodiment is example
Property, it is impossible to limitation of the present invention is interpreted as, those of ordinary skill in the art within the scope of the invention can be to above-mentioned
Embodiment is changed, changes, replacing and modification, meanwhile, for those of ordinary skill in the art, the think of according to the application
Think, in specific embodiments and applications there will be changes.
Claims (10)
1. a kind of three-stage coal dust and biomass pyrolytic processing system, including：Dry riser arrangement, raw material bucket, pyrolytic reaction
Device, waste-heat recovery device, oil wash Quench tower apparatus and air accumulator, wherein：
The pyrolysis reactor is divided into high temperature pyrolysis section, middle low temperature pyrogenation section and waste heat recovery section from top to bottom, wherein, institute
State high temperature pyrolysis section and be equipped with material collecting device and Multi-layer warming device, wherein, the material collecting device is arranged at the Multi-layer warming dress
The lower section put, the high-temperature semi-coke produced for collecting pyrolysis；The cloth of Multi-layer staggered arrangement is equipped with the middle low temperature pyrogenation section
Cone, every layer of cloth cone is multiple；The waste heat recovery section is equipped with heat-exchanger rig；
The drying riser arrangement respectively send lignite, biomass to the raw material bucket respectively, will be brown by the raw material bucket
Coal, biomass respectively enter the high temperature pyrolysis section and middle low temperature pyrogenation section；
The waste-heat recovery device is connected with the air accumulator, the oil wash Quench tower apparatus respectively with the middle low temperature pyrogenation section
And heating unit connection；The waste-heat recovery device is by the pyrolysis pneumatic transmission that the high temperature pyrolysis section produces to the air accumulator；Institute
The circulation that oil wash quenching column realizes oil using oil circulating pump is stated, and is exported in oil circulating pump and sets what heat exchanger produced quenching column
Heat exchanges heat.
2. three-stage coal dust according to claim 1 and biomass pyrolytic processing system, it is characterised in that the pyrolysis is anti-
Device is answered to include furnace body, the furnace body includes：Epimere pyrolysis gas outlet and hypomere pyrolysis gas outlet, the inner cavity of the furnace body on to
Under be divided into low temperature pyrogenation section and hypomere waste heat recovery section in epimere high temperature pyrolysis area, stage casing, the epimere high temperature pyrolysis area,
The proportion of the vertical length of low temperature pyrogenation section and hypomere waste heat recovery section is 3 in stage casing:2:1-5:3:1.
3. three-stage coal dust according to claim 1 and biomass pyrolytic processing system, it is characterised in that the furnace body is also
Including：First charging aperture and cold burnt discharge port, the first charging aperture are arranged at the top of the furnace body, the epimere pyrolysis gas
Outlet is arranged at the sidepiece of the furnace body and is arranged at institute positioned at the downside of the high temperature pyrolysis section, the hypomere pyrolysis gas outlet
State the sidepiece of furnace body and be arranged at the bottom of the furnace body positioned at the downside of the middle low temperature pyrogenation section, the cold burnt discharge port.
4. three-stage coal dust according to claim 1 and biomass pyrolytic processing system, it is characterised in that the three-stage
Coal dust and biomass pyrolytic reaction system further include coke bin, and the coke bin is connected with the cold burnt discharge port.
5. three-stage coal dust according to claim 1 and biomass pyrolytic processing system, it is characterised in that the heating dress
Put includes hot air outlet and inlet of cold air including fuel gas inlet, air intlet and exhanst gas outlet, the heat-exchanger rig, its
In, the hot air outlet of the heat-exchanger rig is connected with the air intlet of the heating unit, and the cooling medium after heat exchange is made
Enter the heating unit for combustion-supporting gas foldback.
6. three-stage coal dust according to claim 1 and biomass pyrolytic processing system, it is characterised in that the rewinding dress
Broach hopper is set to, its bottom is exported equipped with batch mixing, and sidepiece is equipped with the second charging aperture through the furnace body, and biomass material leads to
The second charging aperture is crossed to mix with the high-temperature semi-coke into the broach hopper, under drop down onto carried out on cloth cone it is abundant
Pyrolysis is mixed, obtains mixing semicoke, the mixing semicoke enters the waste heat recovery section.
7. three-stage coal dust according to claim 6 and biomass pyrolytic processing system, it is characterised in that the drying lifting
Pipe device includes biomass drying riser, lignite drying riser, and the raw material bucket includes biomass material bucket, lignite raw material
Bucket, the exhanst gas outlet are linked in sequence successively with lignite drying riser, lignite raw material bucket；The lignite raw material bucket and institute
State first charging aperture connection；Described biomass material bucket one end is connected with the second charging aperture, the other end and the biomass
Riser connection is dried, the biomass drying riser is connected with lignite drying riser.
8. three-stage coal dust according to claim 1 and biomass pyrolytic processing system, it is characterised in that the heating dress
The number of plies put is 10-30 layers, and every layer of heating unit includes multiple heating units；The heating unit radiates for heat accumulating type
Pipe, produces more than 1000 DEG C of flue gas in the heating unit.
9. three-stage coal dust according to claim 1 and biomass pyrolytic processing system, it is characterised in that the cloth cone
The number of plies be 8-20 layer, the spacing per adjacent two layers is 100-400mm, and the spacing that two neighboring cloth is bored in every layer is 50-
300mm；The positive triangular pyramid for a length of 50-200mm of rib of the cloth cone.
10. three-stage coal dust according to claim 1 and biomass pyrolytic reaction system, it is characterised in that the waste heat
Exhausting section is equipped with heat exchanger tube, and the cooling medium is cold air, and 300-400 DEG C is warming up to by described after the cold air heat exchange
External connecting tube enter the high temperature pyrolysis section heating unit in fuel gas buring, it is described mixing semicoke temperature after heat exchange
By being arranged outside belt feeder after being down to 60 DEG C.
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109355070A (en) * | 2018-11-02 | 2019-02-19 | 武汉博立达农业科技发展有限公司 | Biomass and coal copyrolysis reactor |
| CN110713843A (en) * | 2019-10-14 | 2020-01-21 | 江苏海洋大学 | Coal and biomass co-pyrolysis reaction device and method |
Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104710997A (en) * | 2015-04-01 | 2015-06-17 | 曲靖众一精细化工股份有限公司 | Destructive distillation device and destructive distillation method of solid heat carrier |
| CN204550473U (en) * | 2015-03-31 | 2015-08-12 | 长安大学 | A kind of pulverized coal pyrolysis stove |
| CN105176563A (en) * | 2015-09-25 | 2015-12-23 | 北京神雾环境能源科技集团股份有限公司 | Rapid biomass pyrogenation system and method |
| CN107189799A (en) * | 2017-06-26 | 2017-09-22 | 北京神雾电力科技有限公司 | Material copyrolysis reaction system and method for pyrolysis |
| CN107345166A (en) * | 2017-08-31 | 2017-11-14 | 北京神雾电力科技有限公司 | Pyrolytic gasification reactor |
| CN208104298U (en) * | 2017-12-22 | 2018-11-16 | 北京神雾电力科技有限公司 | A kind of three-stage coal dust and biomass pyrolytic processing system |
-
2017
- 2017-12-22 CN CN201711405141.1A patent/CN107937007A/en active Pending
Patent Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN204550473U (en) * | 2015-03-31 | 2015-08-12 | 长安大学 | A kind of pulverized coal pyrolysis stove |
| CN104710997A (en) * | 2015-04-01 | 2015-06-17 | 曲靖众一精细化工股份有限公司 | Destructive distillation device and destructive distillation method of solid heat carrier |
| CN105176563A (en) * | 2015-09-25 | 2015-12-23 | 北京神雾环境能源科技集团股份有限公司 | Rapid biomass pyrogenation system and method |
| CN107189799A (en) * | 2017-06-26 | 2017-09-22 | 北京神雾电力科技有限公司 | Material copyrolysis reaction system and method for pyrolysis |
| CN107345166A (en) * | 2017-08-31 | 2017-11-14 | 北京神雾电力科技有限公司 | Pyrolytic gasification reactor |
| CN208104298U (en) * | 2017-12-22 | 2018-11-16 | 北京神雾电力科技有限公司 | A kind of three-stage coal dust and biomass pyrolytic processing system |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109355070A (en) * | 2018-11-02 | 2019-02-19 | 武汉博立达农业科技发展有限公司 | Biomass and coal copyrolysis reactor |
| CN109355070B (en) * | 2018-11-02 | 2023-12-01 | 武汉兰多生物科技有限公司 | Biomass and coal co-pyrolysis reactor |
| CN110713843A (en) * | 2019-10-14 | 2020-01-21 | 江苏海洋大学 | Coal and biomass co-pyrolysis reaction device and method |
| CN110713843B (en) * | 2019-10-14 | 2021-05-11 | 江苏海洋大学 | Coal and biomass co-pyrolysis reaction device and method |
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