CN202610180U - Device for extracting biological oil from biomass - Google Patents
Device for extracting biological oil from biomass Download PDFInfo
- Publication number
- CN202610180U CN202610180U CN2012202449524U CN201220244952U CN202610180U CN 202610180 U CN202610180 U CN 202610180U CN 2012202449524 U CN2012202449524 U CN 2012202449524U CN 201220244952 U CN201220244952 U CN 201220244952U CN 202610180 U CN202610180 U CN 202610180U
- Authority
- CN
- China
- Prior art keywords
- reactor
- outlet
- biomass
- import
- pyrolysis
- 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.)
- Expired - Fee Related
Links
Images
Classifications
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E50/00—Technologies for the production of fuel of non-fossil origin
- Y02E50/10—Biofuels, e.g. bio-diesel
Abstract
The utility model discloses a device for extracting biological oil from biomass. The device comprises a pyrolysis reactor (1), a gasification reactor (2), a burning reactor (3) and a quench cooler (4). A method comprises the following steps that step 1, crushed and naturally-dried biomass enters a biomass dryer (6) firstly, and the moisture content of the biomass is dried by under 3 percent; step 2, the dried biomass passes through a storage bin (12) as a middle storage tank, a downcomer (13) and a feeder (14) to be sent to the pyrolysis reactor (1), the biomass is quickly pyrolyzed at the reaction temperature of 400-600 DEG C and under the reducing atmosphere, and the biomass is transformed and generated into pyrolysis gas and pyrolysis semicoke; and step 3, the pyrolysis semicoke from the semicoke outlet (1D) of the pyrolysis reactor (1) enters the gasification reactor (2) through a feed delivery pipe (9). The device effectively carries out deoxygenation in the pyrolysis process, the quality of biological oil is increased, and the energy efficiency of a system is high.
Description
Technical field
The utility model discloses a kind of biomass and produce the device of bio oil, relate to the biomass resource utilization field.
Background technology
Along with the fast development of human society, the world energy sources increasing demand increases, and the human long-term fossil energy that relies on is not only exhausted day by day, and in the extensive utilization of fossil energy, has caused the serious environmental pollution.Biomass (comprising agricultural stalk, forestry waste and all kinds of organic wastes etc.) are a kind of reproducible clean energies, and are unique renewable resourcess that is converted into liquid fuel.Utilize biomass to produce liquid fuel, not only can alleviate dependence, and can reduce the discharging of topsoil and greenhouse gases significantly oil.
Biomass pyrolysis liquefaction is one of major technique of producing the liquid fuel bio oil, is meant biomass through rapid heating, and the direct pyrolysis of biomass generates gaseous product and solid coke under 400-600 ℃ of condition; Pyrolysis gas is cooled off fast, and the liquid product that condensation obtains is bio oil, but uncooled non-condensable gases and solid-state coke form biomass pyrolysis provide thermal source or export as sub product.In order to improve the bio oil productive rate, improve the bio oil quality, satisfy industrialized demand, multiple pyrolysis reactor has been developed in countries in the world, comprises fluidized-bed reactor, rotation awl reactor drum, vacuum moving-burden bed reactor, microwave heating reactor drum etc.Utilize present pyrolysis liquefaction technology, the bio oil productive rate can be 40%～80%, still because the biomass material oxygen level is high; Moisture is big, causes that the oxygen amount contains height (35-40wt%) in the bio oil, water ratio big (15-30 wt %); Cause bio oil acid strong, physico-chemical property is unstable, and quality is low.In order to improve the pyrolysis product quality; The technological line that present investigator comparatively pays close attention to mainly comprises catalyse pyrolysis and two aspects of shortening: have the investigator to propose in pyrolytic process, to add catalyzer and carry out catalyse pyrolysis; Catalyzer is generally [Xiao Rui such as sieve catalyst, alkaline earth metal oxide; Zhang Huiyan, the online catalyse pyrolysis of a kind of biomass is produced the method for low oxygen content liquid fuel, 2011100003772.7; ], but the greatest problem that catalyse pyrolysis the faces easy coking and deactivation that is catalyzer cause life of catalyst shorter, and the deoxidation rate is limited.Shortening is under condition of high voltage, to add hydrogen and the deoxidation of catalyzer realization bio oil in the bio oil; Thereby obtain high-quality bio oil, but present major obstacle is to need to consume a large amount of hydrogen sources, and reaction pressure is high; Generally more than 10MPa; Energy consumption is big, and is less economical, and noble metal catalyst is not suitable in biomass pyrolysis process, adding.Have the investigator to propose to carry out under the condition that precious metals pt catalyzer and intermediate pore molecular sieve catalyst combine catalyse pyrolysis and shortening improving the quality of oil recently, but it is high to face the catalyzer cost, is prone to the problem of inactivation.Therefore it is significant to develop efficient, economic biomass pyrolytic oil-producing technique.
Summary of the invention
Technical problem:Certificate is in the limitation of prior art; The purpose of the utility model provides the device that a kind of biomass are produced bio oil; Produce big, the high problem of system's energy consumption of bio oil oxygen level height, moisture of liquid fuel to solve existing biomass pyrolytic, propose a kind of bio oil devices and methods therefor of producing low oxygen content, low-water-content through biomass graded thermal transition.
Technical scheme:For solving the problems of the technologies described above; The device that the utility model provides a kind of biomass to produce bio oil, this device comprises pyrolysis reactor, gasifying reactor, combustion reactor; Quencher; Feedwater heating apparatus and biomass moisture eliminator, first tornado dust collector and second tornado dust collector, carrier pipe, revert pipe, feed bin, downtake and material feeder, and connecting pipeline; Wherein,
Pyrolysis reactor comprises biomass feed inlet and gas feed, and pyrolysis gas outlet and semicoke outlet; Gasifying reactor comprises semicoke import, water vapour import, gaseous product outlet, the outlet of circulation bed material and slag-drip opening; Combustion reactor comprises fuel gas inlet, air/oxygen import, the import of circulation bed material, flue gas/circulation bed material outlet; Quencher comprises the pyrolysis gas import, cooling medium inlet, the bio oil outlet of condensation, non-condensable gases outlet; Feedwater heating apparatus is a recuperative heat exchanger, comprises high-temperature flue gas import, exhanst gas outlet, feed-water inlet and steam outlet; The biomass moisture eliminator is the contact interchanger, comprises gas approach, exhanst gas outlet, biomass inlet and dried biomass outlet; Wherein,
Carrier pipe is connected the semicoke outlet of pyrolysis reactor with the semicoke import of gasifying reactor, the pyrolysis gas outlet of pyrolysis reactor is connected with the first tornado dust collector inlet mouth, and the pyrolysis gas after the dedusting feeds the import of quencher pyrolysis gas; The gaseous product outlet of gasifying reactor is connected with the gas feed of pyrolysis reactor;
Revert pipe links to each other the circulation bed material outlet of gasifying reactor with the circulation bed material import of combustion reactor; Flue gas/circulation bed material outlet is connected with the second tornado dust collector import, and the dipleg of second tornado dust collector directly stretches in the combustion reactor; The non-condensable gases outlet of quencher links to each other with the fuel gas inlet of combustion reactor;
The second tornado dust collector pneumatic outlet is connected with the high-temperature flue gas import of feedwater heating apparatus, and the exhanst gas outlet of feedwater heating apparatus is connected with biomass moisture eliminator gas approach; The steam outlet of feedwater heating apparatus directly is connected with the water vapour import of gasifying reactor; The biomass dryer export connects feed bin, and import links to each other bin outlet with material feeder through downtake, and the material feeder outlet directly is connected with the pyrolysis reactor import.
Preferably, pyrolysis reactor is spouted fluidized bed or bubbling fluidized bed, and pyrolysis reactor gas feed and biomass feed inlet lay respectively at the bottom of pyrolysis reactor;
Gasifying reactor is spouted fluidized bed or bubbling fluidized bed, and the water vapour import of gasifying reactor is positioned at the bottom of gasifying reactor;
Combustion reactor is a circulating fluidized bed, and combustion reactor fuel gas inlet and air/oxygen import lay respectively at the bottom of combustion reactor
The semicoke outlet of pyrolysis reactor; The circulation bed material import of the import of gasifying reactor semicoke and outlet of circulation bed material and combustion reactor all is positioned at the bottom of each autoreactor; And the position of semicoke outlet is higher than the semicoke import, and the position of circulation bed material outlet is higher than the import of circulation bed material.
Beneficial effect:The method of the utility model realizes that to biomass the classification thermal transition utilizes; Biomass fast pyrogenation obtains bio oil, non-condensable gases and semicoke; Wherein pyrogenous origin non-condensable gases provides heat through burning form biomass pyrolysis process and semicoke gasification; Utilize semicoke and water vapour to carry out gasification reaction and hydrogen-rich gas is provided, and the combustion processes of the gasification of semicoke and non-condensable gases separately, under the condition that guarantees confession hot gasization for pyrolytic process; Avoid rare gas element and oxygen to sneak in the gasification product gas, thereby the hydrogen of high density is provided for pyrolysis reactor.
The hydrogen of required adding is directly from the inside of biomass pyrolytic system oil system in the technology biomass pyrolysis process of the utility model; Avoided the dependence of external hydrogen supply gas; Both reduce the Financial cost and the energy consumption of biomass-making oil, reduced the oxygen level in the bio oil again, improved the quality of bio oil.
The technological process of the utility model is through the setting of each stage reactor; Make full use of the energy of biomass; The burning, high-temperature flue gas heated feed water and the dried biomass that comprise non-condensable gases; Improve the Energy efficiency of Wood Adhesives from Biomass bio oil system, and carried out dry pre-treatment before the biomass pyrolytic and help reducing the bio oil water ratio, improved the quality of bio oil.
Description of drawings
Fig. 1 is the technological process and the system and device synoptic diagram of the utility model.
Embodiment
Below in conjunction with accompanying drawing the utility model is further specified.
The device of a kind of biomass of the utility model being produced bio oil below in conjunction with accompanying drawing 1 and specific examples is elaborated.
The biomass of the utility model are produced the device of bio oil through biomass graded thermal transition; Biomass fast pyrogenation under the hydrogen-rich reducing atmosphere of pyrolysis reactor is obtained bio oil; Non-condensable gases and semicoke; Wherein pyrogenous origin non-condensable gases provides heat through burning form biomass pyrolysis process and semicoke gasification, utilize semicoke and water vapour to carry out gasification reaction and for pyrolytic process hydrogen-rich gas is provided, and the high-temperature flue gas of combustion reactor is used for heated feed water and dried biomass; Make device realize biomass pyrolytic system oil under the hydrogen source with confessing from supplying heat source; The utility model improves the bio oil quality not only in the effective deoxidation of pyrolytic process, and system's Energy efficiency is high.
The device that the biomass that the utility model provides are produced bio oil comprises pyrolysis reactor 1; Gasifying reactor 2, combustion reactor 3; Quencher 4; Feedwater heating apparatus 5 and biomass moisture eliminator 6, the first tornado dust collector 7 and second tornado dust collector 8, carrier pipe 9, revert pipe 11, feed bin 12, downtake 13 and material feeder 14, and connecting pipeline; Wherein,
Pyrolysis reactor 1 comprises biomass feed inlet 1A and gas feed 1B, and pyrolysis gas outlet 1C and semicoke outlet 1D; Gasifying reactor 2 comprises semicoke import 2A, water vapour import 2B, gaseous product outlet 2C, circulation bed material outlet 2D and slag-drip opening 2E; Combustion reactor 3 comprises fuel gas inlet 3A, air/oxygen import 3B, circulation bed material import 3C, flue gas/circulation bed material outlet 3D; Quencher 4 comprises pyrolysis gas import 4A, cooling medium inlet 4D, the bio oil outlet 4B of condensation, non-condensable gases outlet 4C; Feedwater heating apparatus 5 is a recuperative heat exchanger, comprises high-temperature flue gas import 5A, exhanst gas outlet 5C, feed-water inlet 5B and steam outlet 5D; Biomass moisture eliminator 6 is the contact interchanger, comprises gas approach 6A, exhanst gas outlet 6C, biomass inlet 6B and dried biomass outlet 6D; Wherein,
Carrier pipe 9 is connected the semicoke outlet 1D of pyrolysis reactor 1 and the semicoke import 2A of gasifying reactor 2; The pyrolysis gas outlet 1C of pyrolysis reactor 1 is connected with first tornado dust collector, 7 inlet mouths, and the pyrolysis gas after the dedusting feeds quencher 4 pyrolysis gas import 4A; The gaseous product outlet 2C of gasifying reactor 2 is connected with the gas feed 1B of pyrolysis reactor 1;
Revert pipe 11 links to each other the circulation bed material outlet 2D of gasifying reactor 2 with the circulation bed material import 3C of combustion reactor 3; Flue gas/circulation bed material outlet 3D is connected with 8 imports of second tornado dust collector, and the dipleg 10 of second tornado dust collector 8 directly stretches in the combustion reactor 3; The non-condensable gases outlet 4C of quencher 4 links to each other with the fuel gas inlet 3A of combustion reactor 3;
Second tornado dust collector, 8 pneumatic outlet 8B are connected with the high-temperature flue gas import 5A of feedwater heating apparatus 5, and the exhanst gas outlet 5C of feedwater heating apparatus 5 is connected with biomass moisture eliminator 6 gas approach 6A; The steam outlet 5D of feedwater heating apparatus 5 directly is connected with the water vapour import 2B of gasifying reactor 2; Biomass moisture eliminator 6 outlet 6D connect feed bin 12, and 14 imports link to each other bin outlet 12B with material feeder through downtake 13, and material feeder 14 outlets directly are connected with pyrolysis reactor 1 import 1A.
Pyrolysis reactor 1 is spouted fluidized bed or bubbling fluidized bed, and pyrolysis reactor 1 gas feed 1B and biomass feed inlet 1A lay respectively at the bottom of pyrolysis reactor 1;
Gasifying reactor 2 is spouted fluidized bed or bubbling fluidized bed, and the water vapour import 2B of gasifying reactor 2 is positioned at the bottom of gasifying reactor 2;
Combustion reactor 3 is a circulating fluidized bed, and the fuel gas inlet 3A of combustion reactor 3 and air/oxygen import 3B lay respectively at the bottom of combustion reactor 3.
The semicoke outlet 1D of pyrolysis reactor 1; The circulation bed material import 3C of the semicoke import 2A of gasifying reactor 2 and circulation bed material outlet 2D and combustion reactor 3 all is positioned at the bottom of each autoreactor; And the position of semicoke outlet 1D is higher than semicoke import 2A, and the position of circulation bed material outlet 2D is higher than circulation bed material import 3C.
The method that the biomass of the utility model are produced bio oil comprises the steps:
Step 1: at first get into biomass moisture eliminator 6 through biomass broken, seasoning, the water cut of biomass is dried to below 3%;
Step 2: dried biomass are sent into pyrolysis reactor 1 through downtake 13 by material feeder 14 through the feed bin 12 as relay tank, 400 ~ 600 ℃ of temperature of reaction, under the reducing atmosphere fast pyrogenation take place, and Wood Adhesives from Biomass generates pyrolysis gas and pyrolysis char;
Step 3: the pyrolysis char by pyrolysis reactor 1 semicoke outlet 1D gets into gasifying reactor 2 through carrier pipe 9, reacts 750～900 ℃ of generating gasification with gasifying medium water vapour, and gasification product is H
2, CO and CO
2Gasification product is admitted to pyrolysis reactor 1, and biomass pyrolytic is carried out under hydrogen-rich reducing atmosphere, and provides pyrolysis needed heat simultaneously;
Step 4: get into quencher 4 coolings after removing the tiny semicoke particle that carries with air-flow by the pyrolysis gas of pyrolysis reactor 1 pyrolysis gas outlet 1C through first tornado dust collector 7; Be separated into bio oil and non-condensable gases two portions after the pyrolysis gas cooling; Wherein a bio oil part is as the product take-off equipment, and another part is sent into the heat-eliminating medium of quencher 4 as bio oil by quencher 4 cooling medium inlet 4D;
Step 5: the non-condensable gases of quencher 4 non-condensable gasess outlet 4C is sent into combustion reactor 3 and air/oxygen gas firing; In the heating flame reactor drum as the circulation bed material of thermal barrier; Combustion reactor 3 service temperatures are controlled at 850 ~ 1000 ℃; The circulation bed material is carried through the dipleg 10 of second tornado dust collector 8 by combustion product gases and sends into gasifying reactor 2, for the semicoke gasification provides heat; The high-temperature flue gas of second tornado dust collector, 8 pneumatic outlet 8B feeds feedwater heating apparatus 5 earlier, sends into biomass moisture eliminator 6 back dischargers again.
Described semicoke gasification product is a hydrogen-rich gas, wherein composition H
2: 50%～70%, CO 5%～15% and CO
215%～30%, the gas inlet temperature of pyrolysis reactor 1 is at 700 ℃～850 ℃.
Described feedwater heating apparatus 5 outlet steam temperatures are at 450 ℃ ~ 600 ℃.
Described quencher 4 heat-eliminating mediums are the round-robin bio oil; The bio oil temperature of quencher 4 heat-eliminating mediums inlet 4D is controlled at below 25 ℃.
Service temperature in the described biomass moisture eliminator 6 is at 80～200 ℃, and the funnel temperature of exhanst gas outlet 6C is below 150 ℃.
Described biomass are for through any or its arbitrary combination in the agricultural wastes after the seasoning, the forestry waste etc., and the biomass particle diameter after the fragmentation is at 0.5～5mm.
Described circulation bed material is the inert thermal barrier, comprises lime-ash, Al
2O
3, SiO
2In any.
The device of the utility model comprises: pyrolysis reactor 1; Gasifying reactor 2, combustion reactor 3; Quencher 4, feedwater heating apparatus 5 and biomass moisture eliminator 6, tornado dust collector 7 and 8, carrier pipe 9, revert pipe 11, feed bin 12, downtake 13 and material feeder 14 and connecting pipeline are formed.Wherein pyrolysis reactor 1 comprises two import: biomass feed inlet 1A and gas feed 1B, and two outlets: pyrolysis gas outlet 1C and semicoke outlet 1D; Gasifying reactor 2 comprises a semicoke import 2A, a water vapour import 2B, a gasification product outlet 2C, a circulation bed material outlet 2D and a slag-drip opening 2E; Combustion reactor 3 includes 3 imports and 1 outlet: fuel gas inlet 3A, air/oxygen import 3B, circulation bed material import 3C, flue gas/circulation bed material outlet 3D; Quencher comprises pyrolysis gas import 4A, cooling medium inlet 4D, the bio oil outlet 4B of condensation, non-condensable gases outlet 4C.Wherein carrier pipe 9 is connected the semicoke outlet 1D of pyrolysis reactor 1 and the semicoke import 2A of gasifying reactor 2, and the gas feed 1B of gaseous product outlet 2C and pyrolysis reactor 1 passes through pipe connection; Revert pipe 11 links to each other the circulation bed material outlet 2D of gasifying reactor 2 with the circulation bed material import 3C of combustion reactor 3; The flue gas of combustion reactor 3/circulation bed material outlet 3D is connected with tornado dust collector 8 gas feed 8A, and the dipleg 10 of tornado dust collector 8 directly stretches in the combustion reactor 3; The pyrolysis gas outlet 1C of pyrolysis reactor 1 is connected with tornado dust collector 7 inlet mouth 7A, and pneumatic outlet 7B is connected to quencher 4 inlet 4A, and the non-condensable gases outlet 4C of quencher 4 links to each other with the fuel gas inlet 3A of combustion reactor 3; Feedwater heating apparatus 5 is a recuperative heat exchanger, comprises high-temperature flue gas import 5A and middle temperature exhanst gas outlet 5C, feed-water inlet 5B and steam outlet 5D; Biomass moisture eliminator 6 is the contact interchanger; Comprise gas approach 6A and exhanst gas outlet 6C; Biomass inlet 6B and dried biomass outlet 6D; Wherein tornado dust collector 8 pneumatic outlet 8B are connected with feedwater heating apparatus 5 high-temperature flue gas import 5A, and exhanst gas outlet 5C is connected with biomass moisture eliminator 6 gas approach 6A; Feedwater heating apparatus 5 steam outlet 5D directly are connected with the water vapour import 2B of gasifying reactor 2; The dried biomass outlet 6D of biomass moisture eliminator 6 is connected with feed bin 12 through transport pipe; Feed bin 12 outlet 12B are connected with downtake 13 upper ends; Downtake 13 lower ends connect material feeder 14 import 14A, and material feeder 14 outlet 14B directly are connected with the biomass inlet 1A of pyrolysis reactor 1.
In addition, pyrolysis reactor 1 is spouted fluidized bed or bubbling fluidized bed, and gas feed 1B is positioned at the bottom under the reactor drum air distribution plate, and biomass feed inlet 1A is positioned on the reactor lower part air distribution plate; Gasifying reactor 2 is spouted fluidized bed or bubbling fluidized bed, and water vapour import 2B is positioned at the bottom under gasifying reactor 2 air distribution plates; Combustion reactor 3 is a circulating fluidized bed, and fuel gas inlet 3A and air/oxygen import 3B are positioned at the bottom of reactor drum; The semicoke outlet 1D of pyrolysis reactor 1; The circulation bed material import 3C of the semicoke import 2A of gasifying reactor 2 and circulation bed material outlet 2D and combustion reactor 3 all is positioned at the bottom of each autoreactor; And the position of outlet 1D is higher than import 2A, and the position of outlet 2D is higher than import 3C.
In above-mentioned device; The technological process of biomass pyrolytic system oil is following: through seasoning, the biomass that are crushed to 0.5-2mm such as biomass straw, forestry wood chip etc.; At first get into biomass moisture eliminator 6; Utilize system's fume afterheat under 80～200 ℃, to carry out drying, obtain water ratio and be lower than 3% dried biomass.Dried then biomass get into the feed bin 12 as relay tank; Send into pyrolysis reactor 1 through tremie pipe 13 through material feeder 14; Raw material in feed bin 12 and the tremie pipe 13 plays the effect of isolating biomass moisture eliminator 6 and pyrolysis reactor 1 gas; It is mixed to avoid gas to scurry, in addition through regulating the rotating speed of material feeder 14, adjustable apparatus biomass pyrolytic system oil handling amount.
In pyrolysis reactor 1, feed gasification product gas H simultaneously from gasifying reactor 2
2, CO and CO
2, biomass are under hydrogen-rich reducing atmosphere, and fast pyrogenation in 400 ~ 550 ℃ of scopes is converted into pyrolysis gas and semicoke.
Outlet 1C gets into tornado dust collector 7 to pyrolysis gas through pyrolysis reactor 1 top; Get into quencher 4 behind the tiny semicoke particle that removal is carried; The tiny semicoke particle discharger of tornado dust collector 7 dust outlet 7C is perhaps sent into gasifying reactor 2; Pyrolysis gas is separated into condensability product bio oil and non-condensable gases in quencher 4; Bio oil is by quencher 4 lower part outlet 4B output, and wherein a bio oil part is as the product take-off equipment, and another part is sent into quencher 4 as the heat-eliminating medium of bio oil by quencher 4 inlet 4D; Non-condensable gases is outlet 4C output through quencher 4 tops, sends into combustion reactor 3 through gas piping.
In addition, the pyrolysis char of pyrolysis reactor 1 outlet gets into gasifying reactor 2 through carrier pipe 9, reacts 800～900 ℃ of generating gasification with gasifying medium water vapour, and gasification product is a hydrogen-rich gas, wherein contains H
2: 50%～70%, CO 5%～15% and CO
215%～30%; 750～850 ℃ gasification product gas is admitted to pyrolysis reactor 1; Biomass pyrolytic is carried out under hydrogen-rich reducing atmosphere, and provide pyrolysis needed heat simultaneously, and semicoke gasification institute heat requirement is provided by the circulation bed material between gasifying reactor 2 and the combustion reactor 3; Be that gasifying reactor 2 directly links to each other with combustion reactor 3; At combustion reactor 3 and air/oxygen gas firing, combustion reactor 3 service temperatures are controlled at 850 ~ 1000 ℃, the circulation bed material in the heating flame reactor drum from the non-condensable gases of quencher 4; High temperature circulation bed material is carried through the dipleg 10 of tornado dust collector 8 by combustion product gases and sends into gasifying reactor 2; The circulation bed material is that the semicoke gasification provides heat as thermal barrier, and circulation between combustion reactor 3 and gasifying reactor 2, and described circulation bed material is lime-ash, Al
2O
3Or SiO
2Deng inert material, realize the biomass half coke gasification from heat supply, and combustion processes and gasification separated, avoided rare gas element and oxygen to sneak in the gasification product gas, thereby hydrogeneous hydrogen-rich gas more than 50% be provided for pyrolysis reactor.Gasifying reactor 2 bottoms are provided with slag-drip opening 2E; Device can be from slag-drip opening 2E discharge section lime-ash and bed material after for some time operation; Bed height is stable in the maintenance reactor drum, and the lime-ash of discharging is sent into pyrolysis reactor 1 together with the gasification product gas that a material also can be sneaked into gasifying reactor 2 outlets.
The above is merely the preferred embodiments of the utility model; The protection domain of the utility model does not exceed with above-mentioned embodiment; As long as the equivalence that those of ordinary skills do according to the utility model institute disclosure is modified or changed, all should include in the protection domain of putting down in writing in claims.
Claims (2)
1. biomass are produced the device of bio oil; It is characterized in that: this device comprises pyrolysis reactor (1); Gasifying reactor (2), combustion reactor (3), quencher (4), feedwater heating apparatus (5) and biomass moisture eliminator (6); First tornado dust collector (7) and second tornado dust collector (8), carrier pipe (9), revert pipe (11), feed bin (12), downtake (13) and material feeder (14), and connecting pipeline; Wherein,
Pyrolysis reactor (1) comprises biomass feed inlet (1A) and gas feed (1B), and pyrolysis gas outlet (1C) and semicoke outlet (1D); Gasifying reactor (2) comprises semicoke import (2A), water vapour import (2B), gaseous product outlet (2C), the outlet of circulation bed material (2D) and slag-drip opening (2E); Combustion reactor (3) comprises fuel gas inlet (3A), air/oxygen import (3B), circulation bed material import (3C), flue gas/circulation bed material outlet (3D); Quencher (4) comprises pyrolysis gas import (4A), cooling medium inlet (4D), the bio oil outlet (4B) of condensation, non-condensable gases outlet (4C); Feedwater heating apparatus (5) is a recuperative heat exchanger, comprises high-temperature flue gas import (5A), exhanst gas outlet (5C), feed-water inlet (5B) and steam outlet (5D); Biomass moisture eliminator (6) is the contact interchanger, comprises gas approach (6A), exhanst gas outlet (6C), biomass inlet (6B) and dried biomass outlet (6D); Wherein,
Carrier pipe (9) is connected the semicoke outlet (1D) of pyrolysis reactor (1) and the semicoke import (2A) of gasifying reactor (2); The pyrolysis gas outlet (1C) of pyrolysis reactor (1) is connected with first tornado dust collector (7) inlet mouth, and the pyrolysis gas after the dedusting feeds quencher (4) pyrolysis gas import (4A); The gaseous product outlet (2C) of gasifying reactor (2) is connected with the gas feed (1B) of pyrolysis reactor (1);
Revert pipe (11) links to each other the circulation bed material outlet (2D) of gasifying reactor (2) with the circulation bed material import (3C) of combustion reactor (3); Flue gas/circulation bed material outlet (3D) is connected with second tornado dust collector (8) import, and the dipleg (10) of second tornado dust collector (8) directly stretches in the combustion reactor (3); The non-condensable gases outlet (4C) of quencher (4) links to each other with the fuel gas inlet (3A) of combustion reactor (3);
Second tornado dust collector (8) pneumatic outlets (8B) are connected with the high-temperature flue gas import (5A) of feedwater heating apparatus (5), and the exhanst gas outlet (5C) of feedwater heating apparatus (5) is connected with biomass moisture eliminator (6) gas approach (6A); The steam outlet (5D) of feedwater heating apparatus (5) directly is connected with the water vapour import (2B) of gasifying reactor (2); Biomass moisture eliminator (6) outlet (6D) connects feed bin (12), and import links to each other bin outlet (12B) with material feeder (14) through downtake (13), and material feeder (14) outlet directly is connected with pyrolysis reactor (1) import (1A).
2. biomass according to claim 1 are produced the device of bio oil; It is characterized in that: pyrolysis reactor (1) is spouted fluidized bed or bubbling fluidized bed, and pyrolysis reactor (1) gas feed (1B) and biomass feed inlet (1A) lay respectively at the bottom of pyrolysis reactor (1);
Gasifying reactor (2) is spouted fluidized bed or bubbling fluidized bed, and the water vapour import (2B) of gasifying reactor (2) is positioned at the bottom of gasifying reactor (2);
Combustion reactor (3) is a circulating fluidized bed, and the fuel gas inlet (3A) of combustion reactor (3) and air/oxygen import (3B) lay respectively at the bottom of combustion reactor (3)
The semicoke outlet (1D) of pyrolysis reactor (1); The circulation bed material import (3C) of the semicoke import (2A) of gasifying reactor (2) and circulation bed material outlet (2D) and combustion reactor (3) all is positioned at the bottom of each autoreactor; And the position of semicoke outlet (1D) is higher than semicoke import (2A), and the position of circulation bed material outlet (2D) is higher than circulation bed material import (3C).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2012202449524U CN202610180U (en) | 2012-05-29 | 2012-05-29 | Device for extracting biological oil from biomass |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2012202449524U CN202610180U (en) | 2012-05-29 | 2012-05-29 | Device for extracting biological oil from biomass |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN202610180U true CN202610180U (en) | 2012-12-19 |
Family
ID=47343895
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN2012202449524U Expired - Fee Related CN202610180U (en) | 2012-05-29 | 2012-05-29 | Device for extracting biological oil from biomass |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN202610180U (en) |
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102703098A (en) * | 2012-05-29 | 2012-10-03 | 东南大学 | Device and method for preparing biological oil from biomass |
| CN104212495A (en) * | 2014-04-02 | 2014-12-17 | 刘国海 | Integrated device and method for preparing oil product and synthetic gas from fine coal |
| CN105505477A (en) * | 2015-12-07 | 2016-04-20 | 浙江大学 | Multi-graded pyrolysis and gasification device of solid fuel and application method of multi-graded pyrolysis and gasification device |
| CN108070405A (en) * | 2017-12-20 | 2018-05-25 | 武汉凯迪工程技术研究总院有限公司 | Biomass multi-production method and its system based on low temperature fluidized bed in three |
| CN109963927A (en) * | 2016-10-12 | 2019-07-02 | Ws-热处理技术有限责任公司 | Method and apparatus for gasified bio-matter amount |
-
2012
- 2012-05-29 CN CN2012202449524U patent/CN202610180U/en not_active Expired - Fee Related
Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102703098A (en) * | 2012-05-29 | 2012-10-03 | 东南大学 | Device and method for preparing biological oil from biomass |
| CN102703098B (en) * | 2012-05-29 | 2013-12-11 | 东南大学 | Device and method for preparing biological oil from biomass |
| CN104212495A (en) * | 2014-04-02 | 2014-12-17 | 刘国海 | Integrated device and method for preparing oil product and synthetic gas from fine coal |
| CN105505477A (en) * | 2015-12-07 | 2016-04-20 | 浙江大学 | Multi-graded pyrolysis and gasification device of solid fuel and application method of multi-graded pyrolysis and gasification device |
| CN109963927A (en) * | 2016-10-12 | 2019-07-02 | Ws-热处理技术有限责任公司 | Method and apparatus for gasified bio-matter amount |
| CN109963927B (en) * | 2016-10-12 | 2021-10-29 | Ws-热处理技术有限责任公司 | Method and device for gasifying biomass |
| US11236278B2 (en) | 2016-10-12 | 2022-02-01 | WS-Wärmeprozeßtechnik GmbH | Process for gasifying biomass with tar adsorption |
| CN108070405A (en) * | 2017-12-20 | 2018-05-25 | 武汉凯迪工程技术研究总院有限公司 | Biomass multi-production method and its system based on low temperature fluidized bed in three |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN102703098B (en) | Device and method for preparing biological oil from biomass | |
| CN103305285B (en) | Device and method for preparing low-tar high-heat-value combustible gas by three-section-type gasification of biomass | |
| CN103740389B (en) | The multi-production process of low-rank coal cascade utilization | |
| CN101245264B (en) | Single-bed self-heating type thermal decomposition gasification combustion reactor and thermal decomposition gasification combustion method | |
| CN104789245B (en) | A kind of pyrolysis gasifying device and technique | |
| CN202610180U (en) | Device for extracting biological oil from biomass | |
| CN103146432B (en) | Biomass pyrolysis gasification and tar catalytic cracking device and method | |
| CN102977927A (en) | Apparatus for preparing synthesis gas based on dual fluidized bed biomass gasification and preparation method thereof | |
| CN101747918B (en) | Method for preparing natural gas by dry quenching co-production coal | |
| CN203128183U (en) | System for producing active carbon and hydrogen by biomass steam low-temperature pyrolysis | |
| CN103011157A (en) | System and method for producing activated carbon and hydrogen through low-temperature pyrolysis of biomass steam | |
| CN106629715A (en) | System and method for preparing active carbon by biomass | |
| CN102226107A (en) | Technology and equipment for preparation of synthetic gas by two-stage high temperature biomass gasification | |
| CN105542806A (en) | Device and method for producing clean fuel gas and biomass charcoal through continuous biomass carbonization | |
| CN101531910A (en) | System for rapidly pyrolysing and liquefying biomass | |
| CN105132021A (en) | Distributed multi-source complementary miniature biomass power generation system | |
| CN106221817A (en) | The device and method of high heating value gas is prepared based on double-fluidized-bed biomass pyrolytic | |
| CN203999499U (en) | A kind of integrated form two-step approach biomass and coal copyrolysis device | |
| CN101665704A (en) | Rapid and large-scale method for producing biofuel | |
| CN203307297U (en) | Device for preparing low-tar and higher-calorific-value combustible gas by biomass three-phase type gasification | |
| CN211227042U (en) | Device for catalytic hydrogen production and power generation of biomass | |
| CN201198470Y (en) | Biomass rapid pyrolysis liquefaction system | |
| CN107586567A (en) | A kind of reformed based on continuous carbonization, gasification cleans joint production process with the pyrolysis gas of biomass charcoal for bakeing coupling processing | |
| CN109161405B (en) | Device and method for co-producing carbon by biomass fluidized bed-fixed bed gasification coupling coal-fired boiler | |
| CN101974351B (en) | Scale fixed bed biomass gasification power generation production technology and suite of equipment |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| C17 | Cessation of patent right | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20121219 Termination date: 20140529 |