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 PDF

Info

Publication number
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
Authority
CN
China
Prior art keywords
pyrolysis
biomass
temperature
heat
coal dust
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.)
Pending
Application number
CN201711405141.1A
Other languages
Chinese (zh)
Inventor
陈水渺
肖磊
汪勤亚
吴道洪
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Beijing Shenwu Power Technology Co Ltd
Beijing Shenwu Environmental and Energy Technology Co Ltd
Original Assignee
Beijing Shenwu Power Technology Co Ltd
Priority date (The priority date 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 date listed.)
Filing date
Publication date
Application filed by Beijing Shenwu Power Technology Co Ltd filed Critical Beijing Shenwu Power Technology Co Ltd
Priority to CN201711405141.1A priority Critical patent/CN107937007A/en
Publication of CN107937007A publication Critical patent/CN107937007A/en
Pending legal-status Critical Current

Links

Classifications

    • CCHEMISTRY; METALLURGY
    • C10PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10BDESTRUCTIVE DISTILLATION OF CARBONAGEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
    • C10B57/00Other processes not covered before; Features of destructive distillation processes in general
    • C10B57/02Multi-step carbonising or coking processes
    • CCHEMISTRY; METALLURGY
    • C10PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10BDESTRUCTIVE DISTILLATION OF CARBONAGEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
    • C10B53/00Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form
    • C10B53/02Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form of cellulose-containing material
    • CCHEMISTRY; METALLURGY
    • C10PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10BDESTRUCTIVE DISTILLATION OF CARBONAGEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
    • C10B53/00Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form
    • C10B53/04Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form of powdered coal
    • CCHEMISTRY; METALLURGY
    • C10PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10GCRACKING 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
    • C10G1/00Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal
    • YGENERAL 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
    • Y02TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02EREDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
    • Y02E50/00Technologies for the production of fuel of non-fossil origin
    • Y02E50/10Biofuels, e.g. bio-diesel
    • YGENERAL 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
    • Y02TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02PCLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P20/00Technologies relating to chemical industry
    • Y02P20/10Process efficiency
    • Y02P20/129Energy 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

A kind of three-stage coal dust and biomass pyrolytic processing system
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.
CN201711405141.1A 2017-12-22 2017-12-22 A kind of three-stage coal dust and biomass pyrolytic processing system Pending CN107937007A (en)

Priority Applications (1)

Application Number Priority Date Filing Date Title
CN201711405141.1A CN107937007A (en) 2017-12-22 2017-12-22 A kind of three-stage coal dust and biomass pyrolytic processing system

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
CN201711405141.1A CN107937007A (en) 2017-12-22 2017-12-22 A kind of three-stage coal dust and biomass pyrolytic processing system

Publications (1)

Publication Number Publication Date
CN107937007A true CN107937007A (en) 2018-04-20

Family

ID=61941810

Family Applications (1)

Application Number Title Priority Date Filing Date
CN201711405141.1A Pending CN107937007A (en) 2017-12-22 2017-12-22 A kind of three-stage coal dust and biomass pyrolytic processing system

Country Status (1)

Country Link
CN (1) CN107937007A (en)

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN110713843A (en) * 2019-10-14 2020-01-21 江苏海洋大学 Coal and biomass co-pyrolysis reaction device and method

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
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

Similar Documents

Publication Publication Date Title
CN102363730B (en) Oil shale dry-wet mixing method dry distillation technology and heat accumulating type external firing shale oven
CN104073263B (en) Heat accumulating type rotating bed low-temperature carbonization system and technique
CN103031139B (en) Device and method for preparing bio-oil through rapid biomass pyrolysis
CN101289622B (en) Process for upgrading of bovey coal by solid thermal-loading suspending pyrogenation device of bovey coal
CN103980920B (en) A kind of inferior fuel pyrolytic process
CN105861080B (en) The method of biomass down-flow fluidized bed using ECT quick catalysis pyrolysis system and pyrolysis biomass
CN102766476B (en) Multi-layer upright tower type duff dust and oil shale distillation plant with stirring function and process
CN102643703B (en) Novel external heating type lignite pyrolysis quality increasing system and process
CN107937007A (en) A kind of three-stage coal dust and biomass pyrolytic processing system
CN202186980U (en) Multi-level multitube revolving low temperature destructive distillation system for powdered coal
CN203048874U (en) All-in-one destructive distillation furnace
CN102827619B (en) Integrated gas retort
CN107858161A (en) A kind of two-part coal dust and biomass solution processing system
CN208104298U (en) A kind of three-stage coal dust and biomass pyrolytic processing system
CN105368472A (en) Pyrolysis apparatus and method
CN207738699U (en) A kind of gas complete alternation distillation system for the long flame dry distillation of coal
CN202849331U (en) Multi-layer vertical tower fine coal and oil shale destructive distillation production device with stirring
CN207811669U (en) A kind of efficient waste heat recycling pyrolysis reactor
CN202610207U (en) Novel external-heated type brown coal pyrolysis quality-improving system
CN206289212U (en) A kind of pyrolysis of coal system
CN207811671U (en) A kind of two-part coal dust and biomass solution processing system
CN207811674U (en) A kind of three-stage pulverized coal pyrolysis processing system
CN205328940U (en) System for pyrolysis coal
CN107937000A (en) A kind of three-stage pulverized coal pyrolysis processing system
CN203904256U (en) Low-temperature heat accumulating type revolving bed carbonization system

Legal Events

Date Code Title Description
PB01 Publication
PB01 Publication
SE01 Entry into force of request for substantive examination
SE01 Entry into force of request for substantive examination