CN205838913U - The system of pyrolysis biomass - Google Patents

The system of pyrolysis biomass Download PDF

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Publication number
CN205838913U
CN205838913U CN201620600605.9U CN201620600605U CN205838913U CN 205838913 U CN205838913 U CN 205838913U CN 201620600605 U CN201620600605 U CN 201620600605U CN 205838913 U CN205838913 U CN 205838913U
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China
Prior art keywords
pyrolysis
oil gas
reactor
pipeline
heat accumulation
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CN201620600605.9U
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Inventor
张宏伟
赵延兵
陈水渺
肖磊
吴道洪
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Shenwu Technology Group Corp Co Ltd
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Beijing Shenwu Environmental and Energy Technology Co Ltd
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    • 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
    • Y02P20/50Improvements relating to the production of bulk chemicals
    • Y02P20/584Recycling of catalysts

Abstract

The utility model discloses the system of pyrolysis biomass, this system includes: including: moving bed pyrolysis reactor and condenser, and wherein, described moving bed pyrolysis reactor includes: pyrolysis feed mouth, pyrolysis oil gas vent, semicoke outlet and catalyst inlet;Heat accumulation type radiant tube, described heat accumulation type radiant tube in the inside of described moving bed pyrolysis reactor along the short transverse multi-tier arrangement of described reactor;Oil gas derives pipeline, and described oil gas is derived and is provided with through hole on the tube wall of pipeline;Distributing device, described distributing device is arranged at above described heat accumulation type radiant tube;And dust arrester, described dust arrester is partially embedded in reactor, and dust arrester is derived pipeline with oil gas and connected by discharge, and dust arrester includes dust chamber, riser and collection chamber.This system can effectively suppress oil gas second pyrolysis, improves bio-oil yield, and improves the thermal efficiency of system and simplify system process.

Description

The system of pyrolysis biomass
Technical field
This utility model belongs to chemical field, and specifically, this utility model relates to a kind of system being pyrolyzed biomass.
Background technology
Biomass energy is a kind of form of energy that solar energy is contained in biomass with chemical energy form, and it is direct or indirect Come from the photosynthesis of plant, be the energy with biomass as carrier.At present countries in the world can in order to realize national economy Sustainable development, is all being devoted to develop the biomass energy utilization technologies of efficient pollution-free, with the fossil energy resource of protection this country. Biomass pyrolytic refers to that biomass are not having oxidant (air, oxygen, steam etc.) or providing only the condition of limited oxygen Under, be heated to exceed 500 DEG C, by thermal chemical reaction biomass macromolecular substances resolved into less combustible substance (solid-state charcoal, Combustible gas, bio oil) thermochemical study technical method.
In biomass pyrolytic course of reaction, it may occur that chemical change and the physical change of complexity.Divide from reaction process The pyrolytic process of analysis biomass substantially can be divided into three phases: the most pre-pyrolysis phase: when temperature rises to 120~200 DEG C, i.e. Making heating for a long time, raw material weight is also the most a small amount of to be reduced, mainly H2O, CO and CO are heated caused by release, and outward appearance is without substantially Change, but material internal structure generation rearrangement reaction, as dehydration, scission of link, free radical appearance, carbon back, carboxyl generate and peroxidating Hydrogen group formation etc.;2. the solid decomposition stage: temperature is 300~600 DEG C, and the physics of various complexity, chemical reaction are in this stage Occurring, cellulose, lignin and the hemicellulose in biomass first passes through depolymerisation in this process and resolves into monomer or monomer Derivant, is then degraded into various product further by various radical reactions and rearrangement reaction;3. coke catabolic phase: burnt C-H in charcoal, C-O key ruptures further, and coke quality declines with speed slowly and tends towards stability, and causes carbon in residual solids The enrichment of element.
From to the rate of heat addition of biomass with from the point of view of completing to react the time used, biomass pyrolytic technique substantially can be divided For two types: one is slow pyrolysis, one is fast pyrogenation.Slow pyrolysis process has the history of thousand of years, is a kind of To generate the carbonization process for the purpose of Linesless charcoal, the heating-up temperature of low temperature pyrogenation is 500~580 DEG C, middle temperature pyrolysis temperature be 660~ 750 DEG C, the temperature of high temperature pyrolysis is 900~1100 DEG C.Timber is placed in kiln, heats in the case of isolation air, permissible Obtain accounting for the char yield of raw materials quality 30%~35%.Fast pyrogenation is that levigate biomass material is placed on fast pyrogenation dress In putting, strictly control the rate of heat addition (typically generally 10~200 DEG C/s) and reaction temperature (controlling at about 500 DEG C), biological Raw material, in the case of anoxia, is rapidly heated to higher temperature, thus causes the decomposition of macromole, creates little molecule gas Body and coercibility volatile matter and a small amount of coke produced.Coercibility volatile matter is cooled rapidly into flowable liquid, and one-tenth is made a living Thing oil or tar, its ratio typically can reach the 40%~60% of raw materials quality.Compared with slow pyrolysis, the heat transfer of fast pyrogenation Course of reaction occurred within the extremely short time, and strong heat effect directly produces thermal decomposition product, then cools down rapidly, to greatest extent Add liquid product oil.
But, current biomass pyrolytic technology still haves much room for improvement.
Utility model content
One of technical problem that this utility model is intended to solve in correlation technique the most to a certain extent.To this end, this reality Being to propose a kind of system being pyrolyzed biomass by a novel purpose, this system can effectively suppress oil gas second pyrolysis, Improve bio-oil yield, and the thermal efficiency the simplified system technique of system can be improved.
At an aspect of the present utility model, the utility model proposes a kind of system being pyrolyzed biomass.According to this reality By novel embodiment, this system includes: moving bed pyrolysis reactor and condenser,
Wherein, described moving bed pyrolysis reactor includes:
The outlet of pyrolysis feed mouth, semicoke and catalyst inlet;
Described pyrolysis feed mouth is positioned on the roof of described reactor;
The outlet of described semicoke is positioned at the bottom of described reactor;
Described catalyst inlet is positioned on roof and/or the sidewall of described reactor;
Heat accumulation type radiant tube, described heat accumulation type radiant tube in the inside of described moving bed pyrolysis reactor along described reaction The short transverse multi-tier arrangement of device, every layer has many heat accumulation type radiant tubes the most parallel to each other;
Oil gas derives pipeline, and described oil gas is derived and is provided with through hole on the tube wall of pipeline;
Distributing device, described distributing device is arranged at above described heat accumulation type radiant tube and is delivered to described pyrolysis reactor for making Interior material is dispersed before contacting described heat accumulation type radiant tube;And
Dust arrester, described dust arrester is partially embedded in described reactor, and described dust arrester is led with described oil gas Go out pipeline to be connected by discharge, and described dust arrester includes dust chamber, riser and collection chamber, wherein, riser Top connects with the top of dust chamber, and the bottom of riser connects with the bottom of dust chamber, and dust chamber is connected with riser structure Circularize loop;Dust chamber is positioned at described reactor, riser and collection chamber and is positioned at outside described reactor;Dust chamber stretches into institute The sidewall stating inside reactor is provided with the pyrolysis oil gas entrance for connecting with described discharge, and dust chamber is adjacent with collection chamber And the sidewall that dust chamber and collection chamber share is provided with duct, collection chamber relative with the sidewall that dust chamber and collection chamber share Sidewall is provided with pyrolysis oil gas vent, and described pyrolysis oil gas vent is connected with described condenser;The top of riser is arranged Having ash-laden gas to export, the bottom of riser is provided with blast cap.
Thus, can effectively suppress oil gas second pyrolysis according to the system of the pyrolysis biomass of this utility model embodiment, Improve bio-oil yield, and by using heat accumulation type radiant tube heating technique, improve the thermal efficiency of system and simplify System process.
Optional, described oil gas derives the pipeline short transverse multi-tier arrangement along described pyrolysis reactor, and every layer has many The oil gas derivation pipeline that root is the most parallel to each other.Thus, it is possible to the oil gas significantly improved in reactor derives efficiency.
Optional, described oil gas is derived pipeline and is arranged in parallel with described heat accumulation type radiant tube, and described heat accumulation type radiant tube The respective left and right sides is symmetrically arranged with two oil gas and derives pipeline.Thus, it is possible to the oil gas improved in reactor further is led Go out efficiency.
Optional, the spacing of the tube wall that described oil gas derives pipeline and neighbouring described heat accumulation type radiant tube is described oil 1/2-3 times of gas delivery line road caliber d.Thus, it is possible to the oil gas improved further in reactor derives efficiency.
Optional, described oil gas is derived and is provided with multiple through hole on the tube wall of pipeline.Thus, it is possible to improve reaction further Oil gas in device derives efficiency.
Optional, described through hole is derived at described oil gas and is uniformly distributed on the length direction of pipeline.Thus, it is possible to further Improve the oil gas in reactor and derive efficiency.
Optional, the both sides tube wall of described heat accumulation type radiant tube is respectively arranged with baffle plate, described baffle plate is positioned at described oil The top in gas delivery line road, and cover the whole vertical projection of described oil gas derivation pipeline.Thus, it is possible not only to effectively prevent oil The blocking in gas delivery line road, and the biomass of whereabouts can be broken up, thus improve biomass pyrolytic efficiency.
Optional, described baffle plate is starting point from the phase tangent line of the vertical tangent plane of the tube wall of described heat accumulation type radiant tube, in one Determine angle and extend downward the vertical tangent plane of described oil gas derivation pipeline.
Optional, the angle ranging from 40-90 degree, without 90 degree.
Optional, oil gas described in same layer is derived pipeline and is communicated to same dust arrester.
Optional, the oil gas of adjacent two layers or more layers is derived pipeline and is connected to a dust arrester.
Optional, oil gas described in same layer is derived pipeline and is communicated to same dedusting dress by same described discharge Put.
Optional, the oil gas of adjacent two layers or more layers is derived pipeline and is communicated to by two or more described discharges Same dust arrester, and the number of plies of described oil gas delivery line is identical with the radical of described discharge.
Optional, heat accumulation type radiant tube the most parallel to each other is uniformly distributed.
Optional, the heat accumulation type radiant tube along the short transverse layout of described reactor is parallel to each other and is staggeredly arranged.
Optional, described dust arrester also includes dividing plate, and dividing plate is arranged on the bottom of connection dust chamber and the end of riser In the pipeline in portion.Described dividing plate, for regulating the inlet-outlet flow balance of filter medium, simultaneously facilitates mistake when starting pyrolysis reactor The loading of filter medium.
Optional, described dividing plate is push-pull valve or butterfly valve.
Optional, dust chamber accommodates filter medium, the particle diameter of described filter medium is 5-20mm.
Optional, a diameter of 2-10mm in described duct, preferably 3mm.
Optional, described duct is evenly distributed on the sidewall of dust chamber.It should be noted that by embedding for dust arrester part Enter inside pyrolysis reactor, it is not necessary to adding external heat source, dust arrester temperature is slightly below pyrolysis reactor fire box temperature, can have Effect avoids second pyrolysis or the condensation of tar, and the filter medium of dust arrester can be recycled, and efficiency of dust collection is high, simple to operate.
Optional, the system of described pyrolysis biomass farther includes: feed hopper, drying riser, pyrolysis hopper and spiral shell Precession glassware;Described feed hopper is connected with described pyrolysis hopper by described drying riser;Described pyrolysis hopper has treats heat Solve material inlet and material outlet to be pyrolyzed, described in material inlet to be pyrolyzed be connected with the outlet of described drying riser;Described Feeding screw has charging aperture and discharging opening, and described charging aperture is connected with described material outlet to be pyrolyzed, described discharging opening with The pyrolysis feed mouth of described moving bed pyrolysis reactor is connected.Thus so that when biomass enter stove, moisture is little, and heat dissipation is few, thus The pyrolysis efficiency of biomass can be improved further.
Optional, the system of described pyrolysis biomass farther includes: spiral discharging device, and described spiral discharging device is with described The semicoke outlet of moving bed pyrolysis reactor is connected.Thus, it is possible to cooled down by the thermal decomposition product semicoke that internal system is obtained Discharge, it is simple to later use.
Optional, the system of described pyrolysis biomass farther includes: many group cyclone separators and one shared half Burnt catcher, wherein, described many group cyclone separators are arranged between described moving bed pyrolysis reactor and described condenser, Often group cyclone separator includes one cyclonic cleaner unit and is arranged on two grades of whirlwind below described one cyclonic cleaner unit and divides From device, it is provided with between described one cyclonic cleaner unit and described secondary cyclone for connecting or cutting off the rotation of described one-level Wind cleaner unit and the valve of described secondary cyclone, the oil gas entrance of the one cyclonic cleaner unit of later group cyclone separator Being connected with the oil gas vent of the one cyclonic cleaner unit of previous group cyclone separator, described semicoke catcher divides with often group whirlwind Outlet from the described secondary cyclone of device is connected.Purer pyrolysis gas is obtained thus, it is possible to efficiently separate, it is simple to The carrying out of subsequent step, the bio oil purity obtained is high.
Optional, the system of described pyrolysis biomass farther includes: purifying column, and the entrance of described purifying column is cold with described The gas outlet of condenser is connected.Thus, it is simple to remove further the oil vapour from condenser combustion gas out.
Optional, every layer of described heat accumulation type radiant tube includes multiple parallel and equally distributed heat accumulation type radiant tube and every Individual described heat accumulation type radiant tube is parallel with each heat accumulation type radiant tube in adjacent upper and lower two-layer heat accumulation type radiant tube.Thus, Biomass enter reactor and can carry out uniform by radial canal, have ensured the biomass uniform heating at reactor, thus have entered One step improves the pyrolysis efficiency of biomass.
Optional, the height of described reactor is 3~20m, and width is 2-6m, and the caliber of described heat accumulation type radiant tube is 200~300mm, the horizontal range between adjacent described heat accumulation type radiant tube outer wall is 200~500mm, adjacent described heat accumulating type spoke Penetrating the vertical distance between pipe outer wall is 200~700mm.Thus, it is possible to ensure the biomass pyrolytic time of staying, thus carry further The pyrolysis efficiency of high biomass.
Additional aspect of the present utility model and advantage will part be given in the following description, and part will be from explained below In become obvious, or recognized by practice of the present utility model.
Accompanying drawing explanation
Above-mentioned and/or additional aspect of the present utility model and advantage are from combining general the accompanying drawings below description to embodiment Become obvious and easy to understand, wherein:
Fig. 1 is the system structure schematic diagram of the pyrolysis biomass according to one embodiment of this utility model;
Fig. 2 and Fig. 3 is that the moving bed pyrolysis in the system of the pyrolysis biomass according to one embodiment of this utility model is anti- Answer the part-structure schematic diagram of device;
Fig. 4 is the system structure schematic diagram of the pyrolysis biomass according to this utility model further embodiment;
Fig. 5 is the method flow schematic diagram of the pyrolysis biomass according to one embodiment of this utility model;
Fig. 6 is the method flow schematic diagram of the pyrolysis biomass according to this utility model further embodiment;
Fig. 7 is the method flow schematic diagram of the pyrolysis biomass according to another embodiment of this utility model;
Fig. 8 is the method flow schematic diagram of the pyrolysis biomass according to another embodiment of this utility model;
Fig. 9 is the method flow schematic diagram of the pyrolysis biomass according to another embodiment of this utility model.
Detailed description of the invention
Of the present utility model embodiment is described below in detail, and the example of described embodiment is shown in the drawings, the most ad initio Represent same or similar element to same or similar label eventually or there is the element of same or like function.Below by ginseng It is exemplary for examining the embodiment that accompanying drawing describes, it is intended to be used for explaining this utility model, and it is not intended that to this utility model Restriction.
In description of the present utility model, it is to be understood that term " " center ", " longitudinally ", " laterally ", " length ", " width Degree ", " thickness ", " on ", D score, "front", "rear", "left", "right", " vertically ", " level ", " top ", " end ", " interior ", " outward ", Orientation or the position relationship of the instruction such as " clockwise ", " counterclockwise ", " axially ", " radially ", " circumferential " are based on shown in the drawings Orientation or position relationship, be for only for ease of and describe this utility model and simplify description rather than instruction or the dress of hint indication Put or element must have specific orientation, with specific azimuth configuration and operation, therefore it is not intended that to this utility model Restriction.
Additionally, term " first ", " second " are only used for describing purpose, and it is not intended that instruction or hint relative importance Or the implicit quantity indicating indicated technical characteristic.Thus, define " first ", the feature of " second " can express or Implicitly include at least one this feature.In description of the present utility model, " multiple " are meant that at least two, such as two Individual, three etc., unless otherwise expressly limited specifically.
In this utility model, unless otherwise clearly defined and limited, term " install ", " being connected ", " connection ", " Gu Fixed " etc. term should be interpreted broadly, connect for example, it may be fixing, it is also possible to be to removably connect, or integral;Can be It is mechanically connected, it is also possible to be electrical connection;Can be to be joined directly together, it is also possible to be indirectly connected to by intermediary, can be two The connection of element internal or the interaction relationship of two elements, unless otherwise clear and definite restriction.Common skill for this area For art personnel, above-mentioned term concrete meaning in this utility model can be understood as the case may be.
In this utility model, unless otherwise clearly defined and limited, fisrt feature second feature " on " or D score Can be that the first and second features directly contact, or the first and second features are by intermediary mediate contact.And, first is special Levy second feature " on ", " top " and " above " but fisrt feature directly over second feature or oblique upper, or only Represent that fisrt feature level height is higher than second feature.Fisrt feature second feature " under ", " lower section " and " below " permissible Be fisrt feature immediately below second feature or obliquely downward, or be merely representative of fisrt feature level height less than second feature.
At an aspect of the present utility model, the utility model proposes a kind of system being pyrolyzed biomass.Below with reference to The system that Fig. 1-4 is pyrolyzed biomass to this utility model embodiment is described in detail.According to embodiment of the present utility model, This system includes: moving bed pyrolysis reactor 100 and condenser 200.
According to embodiment of the present utility model, moving bed pyrolysis reactor 100 includes: pyrolysis feed mouth 101, semicoke export 102, catalyst inlet 103, heat accumulation type radiant tube 11, oil gas derive pipeline 12, dust arrester 15 and distributing device 16.
According to embodiment of the present utility model, pyrolysis feed mouth 101 is positioned on the roof of reactor, and is suitable to biomass Raw material supplies to reactor.
According to embodiment of the present utility model, semicoke outlet 102 can be arranged on the bottom of reactor, and be suitable to be pyrolyzed The semicoke generated discharges reactor.
According to embodiment of the present utility model, heat accumulation type radiant tube 11 in the inside of moving bed pyrolysis reactor 100 along The short transverse multi-tier arrangement of reactor, every layer has many heat accumulation type radiant tubes the most parallel to each other.According to Specific embodiment of the utility model, heat accumulation type radiant tube the most parallel to each other is uniformly distributed, it is preferable that along anti- The heat accumulation type radiant tube answering the short transverse of device to arrange is parallel to each other and is staggeredly arranged.Specifically show according to of the present utility model Example, the caliber of heat accumulation type radiant tube can be 200~300mm.Thus, it is possible to significantly improve the pyrolysis efficiency of biomass, and then Improve pyrolysis oil yield.
According to embodiment of the present utility model, the horizontal range between adjacent heat accumulation type radiant tube outer wall is 200~500mm, Vertical distance between adjacent heat accumulation type radiant tube outer wall is 200~700mm.It is to be understood that outside adjacent heat accumulation type radiant tube Horizontal range between wall can be understood as the distance on same layer between heat accumulation type radiant tube outer wall, and outside adjacent heat accumulation type radiant tube Vertical distance between wall can be understood as the distance between the adjacent heat accumulation type radiant tube outer wall of adjacent upper and lower two interlayers.
According to embodiment of the present utility model, the number of plies of multilamellar heat accumulation type radiant tube can be 10-25 layer.Invention Crinis Carbonisatus Existing, this kind of structure is arranged so that reactor temperature field distribution is uniform, such that it is able to significantly improve the pyrolysis effect of biomass Rate, and then improve the yield of pyrolysis oil.
According to embodiment of the present utility model, heat accumulation type radiant tube can be unidirectional regenerative gas heat accumulation type radiant tube, The heat i.e. produced by combustion gas by heat accumulation type radiant tube body is to carry out heat supply by the way of radiation.According to this utility model Specific embodiment, heat accumulation type radiant tube can be provided with gas control valve (not shown).Thus, it is possible to by adjusting combustion gas The flow of the combustion gas that regulation valve regulation is passed through heat accumulation type radiant tube waits the accurate temperature controlling realized pyrolytic process, such that it is able to aobvious Write the pyrolysis efficiency improving biomass, and then improve the yield of pyrolysis oil.
Concrete, heat accumulation type radiant tube extend into reactor from the side of sidewall of reactor in the horizontal direction and runs through anti- Answer device, i.e. heat accumulation type radiant tube stretches into reactor from the side of sidewall of reactor in the horizontal direction and passes another of reactor Sidewall, and the two ends of heat accumulation type radiant tube all stretch out sidewall of reactor, and wherein, the fuel inlet on heat accumulation type radiant tube is positioned at Stretching out one end of reactor on heat accumulation type radiant tube, the exhanst gas outlet on heat accumulation type radiant tube is positioned on heat accumulation type radiant tube and stretches out The other end of reactor, or fuel inlet on heat accumulation type radiant tube and exhanst gas outlet be positioned on heat accumulation type radiant tube same End.The flow etc. being passed through the combustion gas of heat accumulation type radiant tube by adjustment realizes the accurate temperature controlling to pyrolytic process, and heat accumulating type Radial canal uses the combustion system of periodically commutation so that the temperature field of single heat accumulation type radiant tube is more or less the same in 30 DEG C, thus Ensureing the uniformity of reactor temperature field, the flow of the combustion gas being such as passed through heat accumulation type radiant tube by adjustment makes reactor The regulation temperature range of the heat accumulation type radiant tube in interior epimere region is 500~800 DEG C, it is ensured that the abundant pyrolysis of biomass, passes through Adjust the flow of combustion gas being passed through heat accumulation type radiant tube and make the regulation temperature of the heat accumulation type radiant tube in hypomere region in reactor Scope is 450~650 DEG C, thus the biomass that a heating part further is pyrolyzed the most completely.
According to embodiment of the present utility model, oil gas is derived and is provided with through hole on the tube wall of pipeline 12.Thus, by arranging Oil gas derives pipeline so that the pyrolysis oil gas produced in pyrolytic process is quickly derived, thus effectively suppression oil gas second pyrolysis, carry High pyrolysis oil yield.
According to specific embodiment of the utility model, oil gas derives the pipeline 12 short transverse multi-tier arrangement along reactor, Every layer has many oil gas the most parallel to each other and derives pipeline.Thus, it is possible to the oil significantly improved in reactor Conductance goes out efficiency.
According to specific embodiment of the utility model, oil gas is derived pipeline 12 and is arranged in parallel with heat accumulation type radiant tube 11, and The left and right sides of heat accumulation type radiant tube 11 is symmetrically arranged with two oil gas and derives pipeline 12.Inventor finds, by every storage Hot type radial canal both sides are installed oil gas and are derived pipeline, and the oil gas that pyrolysis produces is derived rapidly by deriving pipeline, thus effectively Inhibit the second pyrolysis of oil gas, and then (yield of pyrolysis oil has reached aluminum rice steamer oil content to improve the yield of pyrolysis oil 94%), good in economic efficiency.
According to concrete example of the present utility model, it can be 30~80mm that oil gas derives the caliber of pipeline.
According to specific embodiment of the utility model, as in figure 2 it is shown, oil gas derives pipeline and neighbouring heat accumulation type radiant tube The spacing of tube wall be that oil gas derives pipe diameter d 1/2-3 times.Thus, it is possible to derive the pyrolysis oil of generation at once, it is to avoid Pyrolysis oil cracks such that it is able to improve pyrolysis oil productivity further.
According to specific embodiment of the utility model, oil gas is derived and is provided with multiple through hole, preferably on the tube wall of pipeline 12 Ground, multiple through holes are derived at oil gas and are uniformly distributed on the length direction of pipeline 12.Thus, it is simple to pyrolysis oil quickly derives, permissible The oil gas improved further in reactor derives efficiency.
According to specific embodiment of the utility model, as in figure 2 it is shown, set respectively on the both sides tube wall of heat accumulation type radiant tube 11 Being equipped with baffle plate 13, baffle plate 13 is positioned at oil gas derives the top of pipeline 12, and covers the whole vertical projection of oil gas derivation pipeline 12. By arranging baffle plate 13 on the both sides tube wall of heat accumulation type radiant tube 12, rubbing oil conductance during being possible to prevent biomass to decline Go out pipeline, and then extend the life-span of oil gas derivation pipeline;And baffle plate 13 can also play the drainage to biomass, prevent raw Material is stuck in heat accumulation type radiant tube and oil gas is derived between pipeline, causes biomass to block.
According to specific embodiment of the utility model, as in figure 2 it is shown, baffle plate 13 erecting from the tube wall of heat accumulation type radiant tube 11 The phase tangent line in vertical cut face A (A1) is starting point, and α extends downward oil gas and derives the vertical tangent plane B (B1) of pipeline 12 at an angle, Angle [alpha] is 40-90 degree, without 90 degree.So that the shortest length of baffle plate is can to block oil gas to derive pipeline.
According to embodiment of the present utility model, as it is shown in figure 1, dust arrester 15 is partially embedded in reactor 100, dedusting Device 15 is derived pipeline 12 with oil gas and is connected by discharge 14.Make the pyrolysis oil gas in reactor be derived pipeline by oil gas to receive Supplying to dust arrester 15 through discharge after collection, i.e. discharge 14 derives pipeline 12 with oil gas respectively and dust arrester 15 is connected.
According to specific embodiment of the utility model, as it is shown on figure 3, dust arrester 15 includes dust chamber 151, riser 152 and collection chamber 153.
Specifically, with reference to Fig. 3, the top of riser 152 connects with the top of dust chamber 151, the bottom of riser 152 and The bottom connection of dust chamber 151, dust chamber 151 is connected with riser 152 composition loop checking installation;Dust chamber 151 is positioned at described In reactor, riser 152 and collection chamber 153 are positioned at outside described reactor;Dust chamber 151 stretches into the side within reactor 100 Wall is provided with the pyrolysis oil gas entrance 154 for connecting with discharge 14, and dust chamber 151 is adjacent with collection chamber 153 and dust chamber 151 are provided with duct 159 with the shared sidewall of collection chamber 153, the sidewall phase shared with dust chamber and collection chamber of collection chamber 153 To sidewall be provided with pyrolysis oil gas vent 155, and be pyrolyzed oil gas vent 155 and be connected with condenser 200;Riser 152 Top is provided with ash-laden gas outlet 156, and the bottom of riser 152 is provided with blast cap 157 (for blowing in described riser 152 Enter gas).
Wherein, it is internal that dust chamber 151 is positioned at pyrolysis reactor 100, and this is designed with the temperature helping utilize pyrolysis reactor 100 Degree.
Specifically, the work process of dust arrester 15 includes:
The pyrolysis oil gas pyrolysis oil gas entrance 154 stretching on sidewall reactor 100 within setting by dust chamber 151 Enter dust chamber, and flow through filter medium, dust can be removed by the collision of filter medium, thus remove in pyrolysis oil gas Dust, then by the opposite side sidewall of dust chamber 151, (i.e. dust chamber 151 shares the pyrolysis oil gas of removing dust with collection chamber 153 Sidewall) on duct enter collection chamber 153, and then relative with the sidewall that dust chamber and collection chamber share from collection chamber 153 Sidewall on arrange pyrolysis oil gas vent 155 discharge.
According to concrete examples more of the present utility model, after one-time dedusting terminates, by the blast cap bottom riser 152 157 to the internal gas that is blown into of riser 152, and one side purges the dust on the filter medium being adsorbed with dust, on the other hand Filter medium through purge is blown and cycles back to dust chamber 151, to recycle.
In embodiments more of the present utility model, dust arrester 15 also includes that dividing plate 158, dividing plate 158 are arranged on connection In the pipeline of the bottom of the bottom of dust chamber 151 and riser 152.Dividing plate 158 is put down for the turnover flow regulating filter medium Weighing apparatus, simultaneously facilitates the loading of filter medium when starting pyrolysis reactor.Preferably, described dividing plate is push-pull valve or butterfly valve.
In embodiments more of the present utility model, dust chamber 151 accommodates filter medium, the grain of described filter medium Footpath is 5-20mm.
In embodiments more of the present utility model, the duct that the sidewall that dust chamber 151 and collection chamber 153 share is arranged A diameter of 2-10mm of 159, preferably 3mm.
In embodiments more of the present utility model, described duct 159 is evenly distributed on the sidewall of dust chamber 151.
It should be noted that it is internal that dust arrester 15 is partially embedded into pyrolysis reactor 100, it is not necessary to add external heat Source, dust arrester 15 temperature is slightly below pyrolysis reactor 100 fire box temperature, can be prevented effectively from second pyrolysis or the condensation of tar, The filter medium of dust arrester 15 can be recycled, and efficiency of dust collection is high, simple to operate.
Specifically, dust arrester 15 can be multiple.Thus, it is possible to significantly reduce the dust content of pyrolysis oil gas.
According to specific embodiment of the utility model, same layer oil gas is derived pipeline 12 and is communicated to same dust arrester 15.Thus oil gas can be collected and dedusting, Simplified flowsheet.
Oil gas according to specific embodiment of the utility model, adjacent two layers or more layers is derived pipeline and is connected to one Dust arrester 15.Thus, it is possible to further Simplified flowsheet.
According to specific embodiment of the utility model, same layer oil gas derives pipeline 12 can pass through same discharge 14 It is communicated to same dust arrester 15, i.e. same layer oil gas derivation pipeline 12 and same dust arrester 15 and connects same respectively Discharge 14.Thus oil gas can be collected and dedusting, Simplified flowsheet.
Oil gas according to specific embodiment of the utility model, adjacent two layers or more layers derives pipeline 12 can be by two The discharge 14 of root or more is communicated to same dust arrester 15, i.e. oil gas and derives the number of plies of pipeline and the radical of discharge Identical, the oil gas of same layer is derived pipeline and is connected with same dust arrester 15 by a discharge, and many discharges Finally it is collected to same dust arrester 15, such as it is shown in figure 1, the oil gas of middle adjacent two layers derives pipeline 12 by two Discharge 14 is communicated to same dust arrester 15.
According to embodiment of the present utility model, reactor head region can spherically type or taper.
According to embodiment of the present utility model, the bottom of reactor can be in inverted cone.Thus, it is possible to make pyrolysis generate Semicoke discharge reactor smoothly.
According to embodiment of the present utility model, the height of reactor can be 3~20m, and width is 2-6m.Thus, it is possible to Realize the pyrolysis completely to biomass.
According to embodiment of the present utility model, distributing device 16 is arranged at above heat accumulation type radiant tube 11 and is delivered to heat for making Solve the material in reactor 100 dispersed before contact heat accumulation type radiant tube 11.Thereby, it is possible to effectively make material in contact Before heat accumulation type radiant tube dispersed, and then pyrolysis effect and bio oil yield can be effectively improved.
According to embodiment of the present utility model, catalyst inlet 103 be positioned at moving bed pyrolysis reactor 100 roof and/ Or on sidewall.Catalyst becomes scattered about storeroom uniformly by catalyst inlet 103, by the catalysis pyrolysis more biology of output Oil, thus, is pyrolyzed effective, and oil yield is high.
According to concrete example of the present utility model, can be on the roof of moving bed pyrolysis reactor 100 and two sidewalls Being respectively provided with catalyst inlet 103, thus, catalyst can spray into reactor uniformly by each catalyst inlet, and is scattered In storeroom, so that the biomass solid material pulverized and catalyst can uniformly be mixed in pyrolysis reactor.
According to other concrete examples of the present utility model, catalyst uses the solid ceramic acid of preheating, thus, in pyrolysis Temperature be 450 DEG C~550 DEG C and solid ceramic acid catalyst effect under can make biomass solid material quickly and fully It is pyrolyzed.
According to embodiment of the present utility model, condenser 200 is suitable to receive what thermal storage type moving bed pyrolysis reactor obtained Pyrolysis oil gas, and it is carried out condensation process, in order to respectively obtain bio oil and combustible gas.It should be noted that such as Fig. 1 institute Showing, condenser 200 completes circulating cooling by recirculated cooling water.
In embodiments more of the present utility model, with reference to Fig. 4, the system of described pyrolysis biomass farther includes: storage Oil device 1200.According to embodiment of the present utility model, Fuel Tanking Unit 1200 is connected with condenser 200, is used for collecting condenser 200 bio oil obtained.
The system of the pyrolysis biomass according to this utility model embodiment is pyrolysis by using many group heat accumulation type radiant tubes Process provides thermal source, can realize the accurate control to pyrolytic process by the flow of the combustion gas that adjustment is passed through heat accumulation type radiant tube Temperature, and heat accumulation type radiant tube passes through heat storage type combustion, it is ensured that the uniformity in temperature field, such that it is able to significantly improve biomass Pyrolysis efficiency, and then improve the yield of pyrolysis oil, make relative to traditional use gas heat carrier or solid thermal carriers simultaneously Pyrolytic reaction device for pyrolysis thermal source is compared, moving bed pyrolysis reactor of the present utility model need not to arrange preheating unit and Carrier separative element, such that it is able to greatly simplify pyrolytic reaction technological process, and then significantly reduces fault rate and the gained of device In pyrolysis oil, dust content is relatively low, and exhaust gas temperature is low, and secondly this utility model is by layout around heat accumulation type radiant tube Oil gas derives pipeline, can be derived rapidly by the oil gas that pyrolysis produces, thus restrained effectively the second pyrolysis of oil gas, and then Improve pyrolysis oil yield, additionally by oil gas derive pipeline be provided above baffle plate, be possible not only to effectively prevent oil gas from leading Go out the blocking of pipeline, and the biomass of whereabouts can be broken up so that biomass are the most dispersed, thus improve Biomass pyrolytic efficiency, and by using condenser that pyrolysis oil gas is carried out condensation process, can with isolated bio oil and Combustible gas, thus increase economic efficiency.
Concrete, by adjusting the flow that the regulation valve regulation on gas pipeline is passed through the combustion gas of unidirectional heat accumulation type radiant tube Deng the accurate temperature controlling realized pyrolytic process so that heat accumulation type radiant tube temperature is 500~700 DEG C, and biomass are through pyrolysis feed Mouthfuls 101 enter in reactors, in biomass are uniformly scattered in reactor and be heated to 500~600 DEG C pyrolytic reactions occur, raw The configured oil gas around heat accumulation type radiant tube of the pyrolysis oil gas become is derived pipeline and is collected to dust arrester (every layer 2-3 oil Gas delivery line road is one group, and the oil gas that pyrolysis produces is derived pipeline by oil gas and pooled together in 2 seconds for unit with group), And the baffle plate that biomass are arranged on oil gas in dropping process and derive above pipeline is broken up the most dispersed, thing Expect that the time of staying is the 1-10 second in the reactor, and be pyrolyzed oil gas vent through it after the pyrolysis oil gas removing dust device dedusting obtained Supply carries out condensation process to condenser, obtains bio oil and combustible gas.
With reference to Fig. 4, farther include according to the system of the pyrolysis biomass of this utility model embodiment: feed hopper 300, baking Dry riser 400, pyrolysis hopper 500 and feeding screw 600.
According to embodiment of the present utility model, feed hopper 300 connects with pyrolysis hopper 500 by drying riser 400;Heat Solving hopper 500 and have material inlet 501 to be pyrolyzed and material outlet 502 to be pyrolyzed, material inlet 501 to be pyrolyzed promotes with drying The outlet of pipe is connected;Feeding screw 600 has charging aperture 601 and discharging opening 602, charging aperture 601 and material outlet to be pyrolyzed 502 are connected, and discharging opening 602 is connected with the pyrolysis feed mouth 101 of moving bed pyrolysis reactor 100.
According to specific embodiment of the utility model, sent from feed hopper 300 less than the biomass of 2mm particle diameter through being crushed to Enter to dry riser 400, fill into the hot-air of 200-250 DEG C from the bottom drying riser 400 and biomass material is carried Rising and dry, biomass material is delivered to be pyrolyzed in hopper 500 after drying, and then sends into pyrolysis through feeding screw 600 Reactor 100 is pyrolyzed.Thus so that when biomass enter stove, moisture is little, and heat dissipation is few, such that it is able to improve biology further The pyrolysis efficiency of matter.
According to embodiment of the present utility model, feed hopper 300 is suitable to store biomass material.It should be noted that it is " biological Matter " kind be not particularly limited, any biomass (such as corn straw, Testa Tritici etc.) are suitable for system of the present utility model System, and " feed hopper " herein can be any device that may be used for storage biomass material present in prior art.
According to embodiment of the present utility model, the bottom drying riser can be gone out with the flue gas on heat accumulation type radiant tube Mouth (not shown) is connected, thus, it is possible to use the heat smoke in heat accumulation type radiant tube biomass material is dried and promotes, Obtain containing the biomass being dried and the mixed material of tail gas.As it was previously stated, the temperature of the heat smoke obtained in heat accumulation type radiant tube Degree can be 200~250 DEG C.Thus, it is possible not only to make full use of the waste heat of flue gas so that system energy consumption significantly reduces, and The too high fire safety hidden danger brought of biomass temperature can be prevented effectively from.
With reference to Fig. 4, farther include according to the system of the pyrolysis biomass of this utility model embodiment: spiral discharging device 700.According to embodiment of the present utility model, spiral discharging device 700 exports 102 phases with the semicoke of moving bed pyrolysis reactor 100 Even.Thus, it is possible to the thermal decomposition product semicoke cooling effectively internal system settled down is discharged, it is simple to later use.
According to specific embodiment of the utility model, can further the semicoke of discharge be gasified by gasification furnace etc. Process, to produce fuel gas and lime-ash, and this fuel gas is delivered to heat accumulation type radiant tube uses as fuel.Thus, pass through Thermal decomposition product semicoke internal system obtained gasifies, and fuel gas supply gasification obtained is made to heat accumulation type radiant tube Use for fuel, the dependence that outside is refueled can be significantly reduced.
With reference to Fig. 4, farther include according to the system of the pyrolysis biomass of this utility model embodiment: organize cyclonic separation more Device 800 and a shared semicoke catcher 900, wherein, many group cyclone separators 800 are arranged on moving bed pyrolysis reaction Between device 100 and condenser 200, often group cyclone separator 800 includes one cyclonic cleaner unit 81 and is arranged on one cyclonic Secondary cyclone 82 below cleaner unit 81, is provided with use between one cyclonic cleaner unit 81 and secondary cyclone 82 In connection or cut off the valve of described one cyclonic cleaner unit and described secondary cyclone, the one of later group cyclone separator The level oil gas entrance of cyclone dust extractor 81 is connected with the oil gas vent of the one cyclonic cleaner unit 81 of previous group cyclone separator, Semicoke catcher 900 is connected with the outlet of the secondary cyclone 82 often organizing cyclone separator 800.
Thus, it is possible to before the pyrolysis oil gas obtained by moving bed pyrolysis reactor 100 is delivered to condenser 200, right Pyrolysis oil gas carries out further dedusting and purified treatment, in order to make through one cyclonic cleaner unit 81 and secondary cyclone The thin semicoke got off after 82 enters semicoke catcher 900, and the purer pyrolysis gas obtained after dedusting and separation then may be used Send in condenser with conveying and quickly cool down, thus, it is possible to improve the efficiency of follow-up cooling, and in condenser gained oil product and The quality of combustible gas, the bio oil purity obtained is high.
In embodiments more of the present utility model, with reference to Fig. 4, the system of described pyrolysis biomass farther includes: clean Change tower 1000.According to embodiment of the present utility model, the entrance of purifying column 1000 is connected with the gas outlet of condenser 200.By This, it is possible to remove further oil vapour and collect from condenser clean combustion gas out, it is simple to pyrolysis product is carried out comprehensive utilization With.
In embodiments more of the present utility model, with reference to Fig. 4, the system of described pyrolysis biomass farther includes: collection Gas tank 1100.According to embodiment of the present utility model, air collector 1100 is connected with purifying column 1000, for collecting through purifying column 1000 purify the pure combustion gas obtained.
Understanding for convenience, the method that the system utilizing above-mentioned pyrolysis biomass is pyrolyzed biomass below is carried out in detail Describe.
As it is shown in figure 5, according to embodiment of the present utility model, the method includes:
S100: biomass are delivered in moving bed pyrolysis reactor carry out pyrolysis processing
According to embodiment of the present utility model, biomass are delivered to moving bed pyrolysis reactor from pyrolysis feed mouth, Fuel and air are respectively fed in heat accumulation type radiant tube so that fuel burns generation heat to life in heat accumulation type radiant tube Matter-radiation heating carries out pyrolysis processing, such that it is able to obtain being pyrolyzed oil gas and semicoke.
According to an embodiment of the present utility model, the granularity of biomass is not particularly restricted, those skilled in the art Can select according to actual needs, according to specific embodiment of the utility model, the granularity of biomass is less than 2mm.Thus, Pyrolysis efficiency can be improved.
According to concrete examples more of the present utility model, the pyrolytic reaction time of biomass is the 1-10 second, pyrolytic reaction temperature Degree is for 450-550 degree Celsius.Thus, pyrolysis efficiency is high, biological quality better.Specifically, heat accumulating type spoke can be passed through by adjustment The flow etc. penetrating the combustion gas of pipe realizes the accurate temperature controlling to pyrolytic process, and heat accumulation type radiant tube uses the burning of periodically commutation Mode so that the temperature field of single heat accumulation type radiant tube is more or less the same in 30 DEG C, thus ensures the uniform of reactor temperature field Property, the flow of the combustion gas being such as passed through heat accumulation type radiant tube by adjustment makes the heat accumulation type radiant tube in epimere region in reactor Regulation temperature range be 500~800 DEG C, it is ensured that the abundant pyrolysis of biomass, be passed through the combustion of heat accumulation type radiant tube by adjustment The flow of gas makes the regulation temperature range of the heat accumulation type radiant tube in hypomere region in reactor be 450~650 DEG C, thus enters one The biomass that a step heating part is pyrolyzed the most completely.
S200: be delivered in condenser carry out condensation process by pyrolysis oil gas
According to embodiment of the present utility model, by the pyrolysis oil gas removing dust device that obtains in moving bed pyrolysis reactor Pyrolysis oil gas vent is delivered in condenser carry out condensation process, (is otherwise referred to as " burnt herein such that it is able to obtain bio oil Oil ") and combustible gas.It should be noted that those skilled in the art can be according to actual needs to condensation process in condenser Condition selects.
The method of the pyrolysis biomass according to this utility model embodiment is pyrolysis by using many group heat accumulation type radiant tubes Process provides thermal source, can realize the accurate control to pyrolytic process by the flow of the combustion gas that adjustment is passed through heat accumulation type radiant tube Temperature, and heat accumulation type radiant tube passes through heat storage type combustion, it is ensured that the uniformity in temperature field, such that it is able to significantly improve biomass Pyrolysis efficiency, and then improve the yield of pyrolysis oil, simultaneously the most traditional use gas heat carrier or solid thermal carriers are as warm The pyrolytic reaction device solving thermal source is compared, and moving bed pyrolysis reactor of the present utility model need not arrange preheating unit and carrier Separative element, such that it is able to greatly simplify pyrolytic reaction technological process, and then significantly reduces fault rate and the gained pyrolysis of device In oil, dust content is relatively low, and exhaust gas temperature is low, and secondly this utility model is by layout oil gas around heat accumulation type radiant tube Derive pipeline, the oil gas that pyrolysis produces can be derived rapidly, thus restrained effectively the second pyrolysis of oil gas, and then improve The yield of pyrolysis oil, additionally by oil gas derive pipeline be provided above baffle plate, be possible not only to effectively prevent oil gas delivery line The blocking in road, and the biomass of whereabouts can be broken up so that biomass are the most dispersed, thus improve biology Matter pyrolysis efficiency, and by using condenser that pyrolysis oil gas is carried out condensation process, can be with isolated bio oil and flammable Gas, thus increase economic efficiency.
Specifically, by adjusting the flow that the regulation valve regulation on gas pipeline is passed through the combustion gas of unidirectional heat accumulation type radiant tube Deng the accurate temperature controlling realized pyrolytic process so that in reactor, the regulation temperature range of the heat accumulation type radiant tube in epimere region is 500~800 DEG C, it is ensured that the abundant pyrolysis of biomass, the flow of the combustion gas being passed through heat accumulation type radiant tube by adjustment makes reaction In device, the regulation temperature range of the heat accumulation type radiant tube in hypomere region is 450~650 DEG C, thus a heating part does not has further The biomass being pyrolyzed completely.The configured oil gas around heat accumulation type radiant tube of pyrolysis oil gas generated is derived pipeline and is collected to remove (it is one group that every layer 2-3 oil gas derives pipeline to dirt device, and the oil gas that pyrolysis produces derives pipeline with group for unit 2 by oil gas Pool together in Miao), and the baffle plate that biomass are arranged on oil gas in dropping process and derive above pipeline breaks up instead Answering in device dispersed, the material time of staying in the reactor is the 1-10 second, and the heat of the pyrolysis oil gas removing dust device obtained Solve oil gas vent supply and carry out condensation process to condenser, obtain bio oil and combustible gas.
In embodiments more of the present utility model, before carrying out described condensation process, farther include: by described heat Solve oil-gas transportation and carry out separation and purification treatment to described many group cyclone separators.Specifically, as shown in Figure 6, according to this practicality The method of the pyrolysis biomass of new embodiment farther includes:
S300: pyrolysis oil gas is delivered to organizes cyclone separator more and carries out separation and purification treatment
Thus, it is possible to before the pyrolysis oil gas obtained by moving bed pyrolysis reactor 100 is delivered to condenser 200, right Pyrolysis oil gas carries out further dedusting and purified treatment, in order to make through one cyclonic cleaner unit 81 and secondary cyclone The thin semicoke that gets off after 82 enters semicoke catcher 900, the most defeated through dedusting and the purer pyrolysis gas obtained after separating Quickly cool down in delivering to condenser, thus, it is possible to improve the efficiency of follow-up cooling, and gained oil product and combustible gas in condenser Quality, the bio oil purity obtained is high.
In embodiments more of the present utility model, the method for described pyrolysis biomass farther includes: by described combustion gas It is delivered to described purifying column and carries out purified treatment.According to concrete example of the present utility model, as it is shown in fig. 7, new according to this practicality The method of the pyrolysis biomass of type embodiment farther includes:
S400: fuel gas transmission to purifying column is carried out purified treatment
Thereby, it is possible to remove further oil vapour and collect from condenser clean combustion gas out, it is simple to pyrolysis product Comprehensively utilize.Such as the purer fuel gas obtained can be directly fed to heat accumulation type radiant tube make as fuel With, the dependence that outside is refueled can be significantly reduced.
As shown in Figure 8, farther include according to the method for the pyrolysis biomass of this utility model embodiment:
S500: biomass are carried out pretreatment and is delivered to moving bed pyrolysis reactor
In embodiments more of the present utility model, S500 includes: make described biomass pass sequentially through feed hopper and drying Riser carries out pretreatment, then makes pretreatment product pass sequentially through pyrolysis hopper and feeding screw is delivered to described moving bed Pyrolysis reactor.
According to specific embodiment of the utility model, sent from feed hopper 300 less than the biomass of 2mm particle diameter through being crushed to Enter to dry riser 400, fill into the hot-air of 200-250 DEG C from the bottom drying riser 400 and biomass material is carried Rising and dry, biomass material is delivered to be pyrolyzed in hopper 500 after drying, and then sends into pyrolysis through feeding screw 600 Reactor 100 is pyrolyzed.Thus so that when biomass enter stove, moisture is little, and heat dissipation is few, such that it is able to improve biology further The pyrolysis efficiency of matter.
According to embodiments more of the present utility model, the method for pyrolysis biomass of the present utility model can be wrapped further Include: thermal decomposition product semicoke internal system settled down is by being connected with the semicoke of moving bed pyrolysis reactor 100 outlet 102 Spiral discharging device 700 cooling discharge.
Additionally, with reference to Fig. 9, according to a concrete example of the present utility model, the side of pyrolysis biomass of the present utility model Method includes:
S500: biomass are carried out pretreatment and is delivered to moving bed pyrolysis reactor;
S100: biomass are delivered in moving bed pyrolysis reactor carry out pyrolysis processing;
S300: pyrolysis oil gas is delivered to organizes cyclone separator more and carries out separation and purification treatment;
S200: be delivered in condenser carry out condensation process by pyrolysis oil gas;
S400: fuel gas transmission to purifying column is carried out purified treatment.
That is, according to concrete example of the present utility model, the method for pyrolysis biomass of the present utility model may include that
First, by through be crushed to less than 2mm particle diameter biomass from feed hopper 300 be admitted to dry riser 400, from baking The bottom of dry riser 400 fills into the hot-air of 200-250 DEG C and promotes biomass material and dry, biomass material warp It is delivered to after crossing drying be pyrolyzed in hopper 500, then in feeding screw 600 sends into pyrolysis reactor 100.
Then, make biomass material stop 1-10s in pyrolysis reactor, and be warming up to 450-550 DEG C, wherein pulverize Biomass solid material and catalyst are mixed in pyrolysis reactor, are 450 DEG C~550 DEG C and solid ceramic acid in pyrolysis temperature Make biomass solid material be pyrolyzed under the effect of catalyst, obtain being pyrolyzed oil gas and hot semicoke, and, this pyrolysis oil gas (500 DEG C) are crossed via dust arrester 15 dust removal process;
It follows that hot semicoke is cooled down discharge by spiral discharging device 700;The high-temperature hot that will obtain in pyrolysis reactor Solve oil-gas transportation and at most organize cyclone separator 800, and make through one cyclonic cleaner unit 81 and be arranged on one cyclonic dedusting The thin semicoke that gets off after secondary cyclone 82 below device 81 enters semicoke collection device 900, then will through dedusting and The purer pyrolysis oil gas obtained after separation is delivered in condenser 200.
Then, utilize condenser 200 that pure pyrolysis oil gas is carried out condensation process, obtain biomass pyrolysis oil and combustion Gas;Bio oil after supercooling is transported to Fuel Tanking Unit 1200.
Then, by from condenser 200 fuel gas transmission out to purifying column 1000, in order to remove the oil steaming in combustion gas Vapour, then collects pure combustion gas by air collector 1100.
It addition, according to specific embodiments more of the present utility model, the method for pyrolysis biomass of the present utility model is permissible Farther include: the semicoke of discharge is carried out gasification process, to produce fuel gas and lime-ash, and by this fuel by gasification furnace etc. Gas is delivered to heat accumulation type radiant tube and uses as fuel.Thus, the thermal decomposition product semicoke by internal system being obtained carries out gas Change, and fuel gas supply gasification obtained uses as fuel to heat accumulation type radiant tube, can significantly reduce and feed outside The dependence of fuel.
As it was previously stated, can have selected from following according to the system and method for the pyrolysis biomass of this utility model embodiment At least one advantage:
1) moving bed pyrolysis reactor employing heat accumulation type radiant tube heat supply, response system simple in construction, easy to operate, temperature Being evenly distributed, heats is good.
2) in moving bed pyrolysis reactor, the top of heat accumulation type radiant tube autoreactor to bottom multi-tier arrangement, will reaction Device region is divided into two sections, and upper-lower section conversion zone can carry out accurate temperature controlling, freely regulates a control part and is pyrolyzed the most completely Material.The combustion system that radial canal periodically commutates, can not only improve the thermal efficiency of system, and ensure that the equal of temperature field Even property;
3) oil gas is installed around every heat accumulation type radiant tube and derives pipeline, such as, join on every heat accumulation type radiant tube both sides There are two oil gas to derive pipeline, are provided with multiple pyrolysis oil gas vent at reactor sidepiece and top, can promote that oil gas is timely and effective Ground is discharged, and the second pyrolysis of suppression oil gas improves bio oil productivity, good in economic efficiency.
4) derive the baffle plate installed above of pipeline at oil gas, can prevent being pyrolyzed oil gas and quickly derive line clogging, have again It is beneficial to breaing up of material such that it is able to advantageously promote pyrolysis.
5) catalyst is injected into become scattered about uniformly storeroom by catalyst inlet, more by catalysis pyrolysis output Bio oil;
6) whole technique does not has heat carrier, technological process to obtain great simplification, and the fault-free that can extend system is continuous The operation time, it is suitable for industrialization promotion.
7) material is entered in pyrolysis reactor by distributing device, and continues to fall and be uniformly scattered by baffle plate and radial canal Enter in moving-burden bed reactor, thus, make material can remain even in reacting furnace and be all distributed such that it is able to improve pyrolysis effect Rate.
8) the hot semicoke in thermal decomposition product is discharged by moving bed pyrolysis reactor bottom, cools down through deslagging cooling spiral It is directly entered semicoke collection device to cold conditions semicoke, further, hot tar and pyrolysis gas cooling and purifying respectively is processed, it is possible to Greatly pyrolysis product is comprehensively utilized.
9) 2mm particles below biomass can be processed according to the system of the pyrolysis biomass of this utility model embodiment, Biomass economy rate is high, and technique is simple, is suitable to promote.
10) being partially embedded into inside pyrolysis reactor by dust arrester, it is not necessary to add external heat source, dust arrester temperature is slightly Less than pyrolysis reactor fire box temperature, can be prevented effectively from second pyrolysis or the condensation of tar, the filter medium of dust arrester can follow Ring uses, and efficiency of dust collection is high, simple to operate.
Below with reference to specific embodiment, this utility model is described, it should be noted that these embodiments are only Illustrative, and limit this utility model never in any form.Unreceipted concrete technology or condition in embodiment, according to ability The technology described by document or condition in territory or carry out according to product description.Material therefor or the unreceipted factory of instrument Shang Zhe, be can by city available from conventional products.
Embodiment
Corn straw is processed by the system using the pyrolysis biomass of Fig. 1-4, and corn straw analytical data, technique are grasped Make parameter and material balance is shown in Table 1-table 3.
Table 1 corn straw analytical data
Table 2 process operation parameter
Table 3 material balance table
From table 3 it can be seen that the tar yield that corn straw pyrolysis obtains is 58%, oil yield is higher.And combustion gas is pure, Recycle value is high.
In the description of this specification, reference term " embodiment ", " some embodiments ", " example ", " specifically show Example " or the description of " some examples " etc. means to combine this embodiment or example describes specific features, structure, material or spy Point is contained at least one embodiment of the present utility model or example.In this manual, the schematic table to above-mentioned term State and be necessarily directed to identical embodiment or example.And, the specific features of description, structure, material or feature are permissible One or more embodiment in office or example combine in an appropriate manner.Additionally, in the case of the most conflicting, this area Technical staff the feature of the different embodiments described in this specification or example and different embodiment or example can be entered Row combines and combination.
Although above it has been shown and described that embodiment of the present utility model, it is to be understood that above-described embodiment is Exemplary, it is impossible to it is interpreted as that those of ordinary skill in the art is in scope of the present utility model to restriction of the present utility model In above-described embodiment can be changed, revise, replace and modification.

Claims (10)

1. the system being pyrolyzed biomass, it is characterised in that including: moving bed pyrolysis reactor and condenser,
Wherein, described moving bed pyrolysis reactor includes:
The outlet of pyrolysis feed mouth, semicoke and catalyst inlet;
Described pyrolysis feed mouth is positioned on the roof of described reactor;
The outlet of described semicoke is positioned at the bottom of described reactor;
Described catalyst inlet is positioned on roof and/or the sidewall of described reactor;
Heat accumulation type radiant tube, described heat accumulation type radiant tube in the inside of described moving bed pyrolysis reactor along described reactor Short transverse multi-tier arrangement, every layer has many heat accumulation type radiant tubes the most parallel to each other;
Oil gas derives pipeline, and described oil gas is derived and is provided with through hole on the tube wall of pipeline;
Distributing device, described distributing device is arranged at above described heat accumulation type radiant tube and is delivered in described pyrolysis reactor for making Material is dispersed before contacting described heat accumulation type radiant tube;And
Dust arrester, described dust arrester is partially embedded in described reactor, described dust arrester and described oil gas delivery line Road is connected by discharge, and described dust arrester includes dust chamber, riser and collection chamber, wherein, the top of riser Connecting with the top of dust chamber, the bottom of riser connects with the bottom of dust chamber, and dust chamber is connected with riser composition ring Shape loop;Dust chamber is positioned at described reactor, riser and collection chamber and is positioned at outside described reactor;Dust chamber stretch into described instead Answering the sidewall within device to be provided with the pyrolysis oil gas entrance for connecting with described discharge, dust chamber is adjacent with collection chamber and filters The sidewall that dirt room shares with collection chamber is provided with duct, the sidewall relative with the sidewall that dust chamber and collection chamber share of collection chamber It is provided with pyrolysis oil gas vent, and described pyrolysis oil gas vent is connected with described condenser;The top of riser is provided with and contains Dust and gas exports, and the bottom of riser is provided with blast cap.
System the most according to claim 1, it is characterised in that described oil gas derives the pipeline height along described pyrolysis reactor Degree direction multi-tier arrangement, every layer has many oil gas the most parallel to each other and derives pipeline,
Optional, described oil gas is derived pipeline and is arranged in parallel with described heat accumulation type radiant tube, and described heat accumulation type radiant tube is each The left and right sides be symmetrically arranged with two oil gas and derive pipelines,
Optional, described oil gas derivation pipeline is that described oil gas is led with the spacing of the tube wall of neighbouring described heat accumulation type radiant tube Go out 1/2-3 times of pipe diameter d.
System the most according to claim 1 and 2, it is characterised in that be provided with many on the tube wall of described oil gas derivation pipeline Individual through hole,
Optional, described through hole is derived at described oil gas and is uniformly distributed on the length direction of pipeline.
System the most according to claim 1, it is characterised in that be respectively provided with on the both sides tube wall of described heat accumulation type radiant tube There are baffle plate, described baffle plate to be positioned at described oil gas and derive the top of pipeline, and cover the whole vertical throwing of described oil gas derivation pipeline Shadow,
Optional, described baffle plate is starting point from the phase tangent line of the vertical tangent plane of the tube wall of described heat accumulation type radiant tube, in certain angle Degree extends downward described oil gas and derives the vertical tangent plane of pipeline,
Optional, the angle ranging from 40-90 degree, without 90 degree.
System the most according to claim 2, it is characterised in that oil gas described in same layer is derived pipeline and is communicated to same removing Dirt device,
Optional, the oil gas of adjacent two layers or more layers is derived pipeline and is connected to a dust arrester,
Optional, oil gas described in same layer is derived pipeline and is communicated to same dust arrester by same described discharge,
Optional, the oil gas of adjacent two layers or more layers is derived pipeline and is communicated to same by two or more described discharges Individual dust arrester.
System the most according to claim 1, it is characterised in that heat accumulation type radiant tube the most parallel to each other is equal Even distribution,
Optional, the heat accumulation type radiant tube along the short transverse layout of described reactor is parallel to each other and is staggeredly arranged.
System the most according to claim 1, it is characterised in that described dust arrester also includes dividing plate, dividing plate is arranged on even In the pipeline of the bottom of logical dust chamber and the bottom of riser,
Optional, described dividing plate is push-pull valve or butterfly valve,
Optional, dust chamber accommodates filter medium, the particle diameter of described filter medium is 5-20mm,
Optional, a diameter of 2-10mm in described duct,
Optional, a diameter of 3mm in described duct,
Optional, described duct is evenly distributed on the sidewall of dust chamber.
System the most according to claim 1, it is characterised in that farther include: feed hopper, drying riser, pyrolysis material Bucket and feeding screw;
Described feed hopper is connected with described pyrolysis hopper by described drying riser;
Described pyrolysis hopper has material inlet to be pyrolyzed and material outlet be pyrolyzed, described in material inlet to be pyrolyzed and described baking The outlet of dry riser is connected;
Described feeding screw has charging aperture and discharging opening, and described charging aperture is connected with described material outlet to be pyrolyzed, described Discharging opening is connected with the pyrolysis feed mouth of described moving bed pyrolysis reactor,
Optional, farther including: spiral discharging device, described spiral discharging device goes out with the semicoke of described moving bed pyrolysis reactor Mouth is connected.
System the most according to claim 8, it is characterised in that farther include: many group cyclone separators and one are altogether Semicoke catcher,
Wherein,
Described many group cyclone separators are arranged between described moving bed pyrolysis reactor and described condenser, and often group whirlwind divides Include one cyclonic cleaner unit from device and be arranged on the secondary cyclone below described one cyclonic cleaner unit, described one Level cyclone dust extractor and described secondary cyclone between be provided with for connect or cut off described one cyclonic cleaner unit with The valve of described secondary cyclone, the oil gas entrance of the one cyclonic cleaner unit of later group cyclone separator revolves with previous group The oil gas vent of the one cyclonic cleaner unit of wind segregation apparatus is connected,
Described semicoke catcher is connected with the outlet of the described secondary cyclone often organizing cyclone separator.
System the most according to claim 9, it is characterised in that farther include: purifying column, the entrance of described purifying column It is connected with the gas outlet of described condenser.
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Publication number Priority date Publication date Assignee Title
CN105907407A (en) * 2016-06-17 2016-08-31 北京神雾环境能源科技集团股份有限公司 Biomass pyrolysis system and method

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN105907407A (en) * 2016-06-17 2016-08-31 北京神雾环境能源科技集团股份有限公司 Biomass pyrolysis system and method

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