CN107937011A - A kind of biomass fast thermal decomposition device and technique - Google Patents
A kind of biomass fast thermal decomposition device and technique Download PDFInfo
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- CN107937011A CN107937011A CN201711014989.1A CN201711014989A CN107937011A CN 107937011 A CN107937011 A CN 107937011A CN 201711014989 A CN201711014989 A CN 201711014989A CN 107937011 A CN107937011 A CN 107937011A
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G1/00—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal
- C10G1/08—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal with moving catalysts
- C10G1/086—Characterised by the catalyst used
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
- C10B49/00—Destructive distillation of solid carbonaceous materials by direct heating with heat-carrying agents including the partial combustion of the solid material to be treated
- C10B49/16—Destructive distillation of solid carbonaceous materials by direct heating with heat-carrying agents including the partial combustion of the solid material to be treated with moving solid heat-carriers in divided form
- C10B49/20—Destructive distillation of solid carbonaceous materials by direct heating with heat-carrying agents including the partial combustion of the solid material to be treated with moving solid heat-carriers in divided form in dispersed form
- C10B49/22—Destructive distillation of solid carbonaceous materials by direct heating with heat-carrying agents including the partial combustion of the solid material to be treated with moving solid heat-carriers in divided form in dispersed form according to the "fluidised bed" technique
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- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
- C10B53/00—Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/10—Feedstock materials
- C10G2300/1011—Biomass
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/70—Catalyst aspects
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/70—Catalyst aspects
- C10G2300/703—Activation
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- 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
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Abstract
The present invention relates to a kind of biomass fast thermal decomposition device and technique, its device includes pyrolysis reactor, catalyst classification piece-rate system, catalyst regenerator and product condensation separator；Pyrolysis reactor includes mixing heating zone, pyrolysis reaction region and pyrolysis filtering area；Pyrolysis reaction region is separated with pyrolysis filtering area by the first grid；Material inlet and the first catalyst inlet are equipped with the top of mixing heating zone；Pyrolysis reaction region lower part is connected equipped with returning charge valve by the first material returning device with catalyst regenerator；The second catalyst inlet is equipped with the top of pyrolysis filtering area, lower part is equipped with regulating valve, and sidepiece is exported equipped with gas-phase product；Pyrolysis filtering area is exported with gas-phase product and separated by the second grid, and gas-phase product outlet is connected with product condensation separator, and regulating valve is connected by the second material returning device with catalyst regenerator import.The device enables biomass in pyrolysis reactor while completes two level pyrolysis and filtering, reduces the rate containing ash of product liquid.
Description
Technical field
The present invention relates to field of energy utilization, and in particular to a kind of biomass fast thermal decomposition device and technique.
Background technology
Solve energy problem has great strategic importance for world economic growth.Coal, oil and natural gas etc. are changed
The long-time service of stone fuel, causes serious environmental pollution and greenhouse effects.In addition, fossil fuel is non-renewable energy resources,
Liquid fuel shortage in the long term is by as the big problem of puzzlement human development.
Biomass energy is can be uniquely converted into a kind of regenerative resource of liquid fuel.In view of biomass distribution is scattered, shape
The reason for state is different, and energy density is low and is subject to seasonal restrictions, in the prior art using biomass Thermochemical Liquefaction, by biomass
Partly or entirely it is converted into the liquid fuel that energy density is big, is easy to store and transports.This method is there is no product scale and disappears
Take territory restriction, be environment friendly, most promising oil substitutes.Therefore, biomass fast pyrogenation technology will be this generation
Recording most has the technology of industrialization development potentiality, is the emphasis and hot spot of domestic and international biomass liquefying research and development.
When biomass is pyrolyzed under different reaction conditions, gas, liquid and solid three-phase product can be all generated.Mesh
Preceding existing reaction system is also easy to produce a large amount of dust, the gas for causing reaction to generate since raw material rubs seriously during the reaction
Contain a large amount of dust in state product, be present in after condensation in liquid fuel, have impact on the later use of liquid fuel.On the other hand,
Fast pyrolysis process needs pyrogenous origin gaseous products to want rapid condensation just to can guarantee that liquid yield into liquid fuel, and
Heavy constituent content is more in obtained product liquid, also limit the later use approach of liquid fuel.
The content of the invention
In view of the above-mentioned deficiencies in the prior art, it is an object of the present invention to provide a kind of biomass fast thermal decomposition device so that raw
Material can complete two level pyrolysis in a pyrolysis reactor, and realize gas-phase product fast filtering, effectively reduce liquid production
The rate containing ash of thing, improves the yield and quality of product liquid.
The present invention is directed to the technical solution that above-mentioned technical problem is provided：
A kind of biomass fast thermal decomposition device, including pyrolysis reactor, catalyst classification piece-rate system, catalyst regenerator
With product condensation separator；
The pyrolysis reactor includes mixing heating zone, is arranged on the pyrolysis reaction region of mixing heating zone lower end and is located at
The pyrolysis filtering area of pyrolysis reaction region side；The pyrolysis reaction region is separated with pyrolysis filtering area by the first grid；
Material inlet and the first catalyst inlet are equipped with the top of the mixing heating zone；The pyrolysis reaction region lower part is equipped with
Returning charge valve, and be connected by the first material returning device with catalyst regenerator；Be equipped with the top of the pyrolysis filtering area the second catalyst into
Mouthful, lower part is equipped with regulating valve, and sidepiece is exported equipped with gas-phase product；The pyrolysis filtering area passes through the second lattice with gas-phase product outlet
Grid separate, and gas-phase product outlet is connected with product condensation separator, regulating valve by the second material returning device and catalyst regenerator into
Mouth connection；
First catalyst inlet and the second catalyst inlet are connected with catalyst classification piece-rate system respectively, described to urge
Agent regenerator outlet is connected with catalyst classification piece-rate system import.
In above-mentioned technical solution, biomass is entered by material inlet, and catalyst is entered by the first catalyst inlet, and two
Person realizes quick mixing heating by mutually colliding in mixing heating zone, and quickly enters pyrolysis reaction region and start vigorous reaction,
The gas-phase product of pyrolysis reaction region generation enters pyrolysis filtering area by the first grid, is contacted with the catalyst in pyrolysis filtering area
Pyrolytic reaction is carried out again, product heavy constituent content is reduced, significantly improves product liquid quality, and is pyrolyzed in filtering area
Catalyst is entered by the second catalyst inlet.
Meanwhile it is pyrolyzed the effect that filtering area also plays dust in filtering gas-phase product, the dust that gas-phase product carries
Grain is pyrolyzed the catalyst filtration of filtering area and moves down discharge therewith.The width of filtering area and the granularity of catalyst etc. is pyrolyzed to determine
By pyrolysis reaction region generation gas-phase product pyrolysis filtering area residence time.
After reaction, solid material is regenerated by the first returning charge valve and the second material returning device into catalyst regenerator
Processing, is classified piece-rate system into catalyst afterwards, catalyst after separation according to different-grain diameter respectively enter pyrolysis reactor,
Second returning charge valve or outer row, and gas-phase product eventually enters into product condensation separator by gas-phase product outlet and is separated, most
Biogas, wood vinegar, biological light oil and biological heavy oil etc. are obtained eventually.
Preferably, first catalyst inlet is vertically arranged at the top of mixing heating zone；The material inlet includes two
It is a, it is obliquely installed respectively at the top of mixing heating zone.Further preferably, two material inlets are symmetricly set on mixing heating
At the top of area, and the angle of material inlet and the first catalyst inlet is 15-75 °.
Preferably, the catalyst classification piece-rate system is composed in series by tetra-cyclone, upper level cyclonic separation
The outlet of device is connected with next stage cyclone inlet；
The ash bucket of the first order cyclone separator is connected with the second catalyst inlet at the top of pyrolysis filtering area, and described the
The ash bucket of secondary cyclone is connected with the first catalyst inlet at the top of mixing heating zone, the third-stage cyclone separator
Ash bucket be connected with the second material returning device, the ash bucket of the fourth stage cyclone separator and outlet outer row respectively.
Piece-rate system is classified by catalyst, the catalyst after catalyst regenerator regeneration treatment can be pressed particle
Particle diameter is divided into 4 sections and puts into different workshop sections respectively, is respectively that lower catalyst of the particle diameter more than 2mm of first order separator separation is used
In the secondary pyrolysis filtering of high-temperature oil gas, the catalyst that second level separator isolates 0.5-2mm is reacted for fast pyrogenation, and the 3rd
The catalyst that level separator isolates 0.1-0.5mm is used to maintain technique thermal cycle, and fourth stage separator is isolated less than 0.1mm
Catalyst outside arrange.
Preferably, it is equipped with heat collector in the catalyst regenerator.The setting can be effectively utilized by biomass semicoke
The heat of generation.
Preferably, if the mixing heating zone is equipped with dry material mixed plate；The shape of the material mixed plate is triangular prism,
It is arranged in parallel between each other and is layered Heterogeneous Permutation.Further preferably, the number of plies of the material mixed plate is 2-8 layers.
Preferably, the cross section of the material mixed plate is isosceles triangle, and apex angle scope is 45-120 °.
Preferably, the pyrolysis reaction region is fluid bed, and catalyst is Ni/Al2O3, reaction temperature is 600-900 DEG C, is urged
Agent should have self-sealing function by being gravitationally fallen to returning charge valve, returning charge valve.
Preferably, the pyrolysis filtering area is moving bed, and catalyst is Ni/Al2O3, pyrolysis filtering area temperature is 600-900
DEG C, catalyst falling speed is controlled by adjusting the regulating valve of lower part.
Preferably, first grid is spaced by inverted v-shaped flase floor forms；The inverted v-shaped flase floor is not
Symmetrical structure, is less than positioned at pyrolysis filtering area side edges of boards with erecting positioned at the angle of pyrolysis reaction region side edges of boards and vertical direction
Nogata to angle.
Preferably, it is 15-45 ° positioned at the angular range of pyrolysis reaction region side edges of boards and vertical direction；Positioned at being pyrolyzed
The angular range for filtering area side edges of boards and vertical direction is 15-75 °.
Preferably, the inverted v-shaped flase floor is located at the bottom positions of pyrolysis reaction region side edges of boards and falls V less than next layer
The tip position of font flase floor；The inverted v-shaped flase floor is flush to positioned at the bottom position of pyrolysis filtering area side edges of boards
The tip position of next layer of inverted v-shaped flase floor.
Preferably, the spacing distance between the inverted v-shaped flase floor is less than the particle diameter of catalyst in pyrolysis reaction region.
Preferably, second grid is spaced by linear type flase floor forms；The linear type flase floor with it is vertical
The angular range in direction is 15-45 °.
Preferably, tip position of the bottom position of the linear type flase floor less than next layer of linear type flase floor.
Preferably, the spacing distance of the linear type flase floor is less than the particle diameter of catalyst in pyrolysis filtering area.
Preferably, the pyrolysis filtering area includes two, is symmetrically arranged in pyrolysis reaction region both sides.
The present invention also provides a kind of biomass fast pyrogenation technique using above device, include the following steps：
1) biomass and catalyst are entered by material inlet and the first catalyst inlet respectively, are realized in mixing heating zone mixed
Heating is closed, and starts to react into pyrolysis reaction region；
Catalyst after reaction and the semicoke not reacted completely are entered in catalyst regenerator by the first material returning device, are carried out
Regeneration treatment；
2) gas-phase product of generation enters pyrolysis filtering area by the first grid in step 1), with urging in pyrolysis filtering area
Agent contact is reacted, and filters dust in gas-phase product；
Catalyst after reaction is then entered in catalyst regenerator by the second material returning device, carries out regeneration treatment；
3) gas-phase product in step 2) after pyrolysis is filtered enters product condensation separator by the second grid, carries out
Product separating treatment；
4) step 1) and the middle catalyst Jing Guo catalyst regenerator regeneration treatment of step 2), are classified into catalyst and separate
System, separates lower catalyst of the particle diameter more than 2mm by first order separator and enters pyrolysis filtering area, separated by second level separator
The catalyst for going out 0.5-2mm enters mixing heating zone, and the catalyst that 0.1-0.5mm is isolated by third level separator is sent into second
Material returning device, is used to maintain technique thermal cycle afterwards into catalyst regenerator, is isolated by fourth stage separator less than 0.1mm's
Catalyst is then outer to be arranged.
Compared with the existing technology, beneficial effects of the present invention are embodied in：
(1) biomass fast thermal decomposition device provided by the present invention can realize the regeneration and classification separation of catalyst,
Realize recycling for catalyst.
(2) pyrolysis reactor in biomass fast thermal decomposition device provided by the present invention by grid by pyrolysis reaction region
Distinguished with pyrolysis filtering, realize biomass two level pyrolysis and filtration, purification in a reactor, liquid can be effectively improved
The yield of body product, reduces the rate containing ash of product liquid.
(3) biomass fast pyrogenation technique provided by the present invention, can effectively improve the yield of product liquid, reduce
The rate containing ash of product liquid.
Brief description of the drawings
Fig. 1 is the structure diagram of biomass fast thermal decomposition device in embodiment；
Fig. 2 is the structure diagram of pyrolysis reactor in embodiment.
Wherein, 1, pyrolysis reactor；101st, pyrolysis reaction region；102nd, it is pyrolyzed filtering area；103rd, heating zone is mixed；104th, gas
Phase product exit；105th, the first grid；106th, the second grid；107th, the first catalyst inlet；108th, material inlet；109th, second
Catalyst inlet；110th, material mixed plate；111st, regulating valve；112nd, returning charge valve；2nd, catalyst regenerator；3rd, product condensation separation
Device；4th, first order cyclone separator；5th, second level cyclone separator；6th, third-stage cyclone separator；7th, fourth stage cyclonic separation
Device；8th, the first material returning device；9th, the second material returning device；10th, heat collector.
Embodiment
With reference to specific embodiment, the invention will be further described.
Embodiment
Include pyrolysis reactor 1 as shown in Figure 1 for biomass fast thermal decomposition device, catalyst is classified piece-rate system, catalysis
Agent regenerator 2 and product condensation separator 3.
Wherein, catalyst classification piece-rate system is composed in series by tetra-cyclone, and upper level cyclone separator goes out
Mouth is connected with next stage cyclone inlet.The ash bucket of first order cyclone separator 4 and the second of 102 top of pyrolysis filtering area
Catalyst inlet 109 connects, the ash bucket of second level cyclone separator 5 and the first catalyst inlet for mixing the top of heating zone 103
107 connections, the ash bucket of third-stage cyclone separator 6 is connected with the second material returning device 9, the ash bucket of fourth stage cyclone separator 7 with go out
Mouth is outer respectively to be arranged.
As shown in Fig. 2, pyrolysis reactor 1 includes mixing heating zone 103, pyrolysis reaction region 101 and pyrolysis filtering area 102,
Three is in 1 enclosure interior of pyrolysis reactor.
Mixing heating zone 103 is arranged on 101 top of pyrolysis reaction region, can be perpendicular in both global shape actual productions
Straight cuboid, and 101 lower part of pyrolysis reaction region is equipped with returning charge valve 112, and connected by the first material returning device 8 with catalyst regenerator 2
Connect.It is two to be pyrolyzed filtering area 102, is separately positioned on 101 both sides of pyrolysis reaction region.The pyrolysis of pyrolysis reaction region 101 and both sides
Filtering area 102 is separated by the first grid 105.
First grid 105 is spaced by inverted v-shaped flase floor to be formed, and inverted v-shaped flase floor is dissymmetrical structure, is located at
The angle of 101 side edges of boards of pyrolysis reaction region and vertical direction is less than positioned at pyrolysis 102 side edges of boards of filtering area and vertical direction
Angle.It it is 30 ° positioned at the angular range of 101 side edges of boards of pyrolysis reaction region and vertical direction, positioned at pyrolysis filtering area 102 1
The angular range of side plate side and vertical direction is 45 °.Inverted v-shaped flase floor is located at the bottom of 101 side edges of boards of pyrolysis reaction region
Position is less than the tip position of next layer of inverted v-shaped flase floor, and inverted v-shaped flase floor is positioned at pyrolysis 102 side edges of boards of filtering area
Bottom position be flush to the tip position of next layer of inverted v-shaped flase floor.In addition, the spacer between inverted v-shaped flase floor
From the particle diameter less than catalyst in pyrolysis reaction region 101.
The top of mixing heating zone 103 is equipped with 108 and first catalyst inlet 107 of material inlet.First catalyst inlet
107 are vertically arranged at 103 top of mixing heating zone, and material inlet 108 includes two, is obliquely installed respectively in mixing heating zone
103 tops.Two material inlets 108 are symmetrical arranged, and the angle of 108 and first catalyst inlet 107 of material inlet is 30 °,
First catalyst inlet 107 is connected with the ash bucket of second level cyclone separator 5.
If in addition, being equipped with dry material mixed plate 110 in mixing heating zone 103, the shape of material mixed plate 110 is Mitsubishi
Column, both ends are individually fixed in the wall of mixing heating zone 103, and cross section is isosceles triangle, and corner angle is 120 °, mutually it
Between be arranged in parallel and be layered Heterogeneous Permutation.The number of plies of material mixed plate 110 is 3 layers.
Pyrolysis filtering area 102 due to 101 both sides of pyrolysis reaction region only introduces the pyrolysis of side herein to be symmetrical arranged
Filter area 102.The shape for being pyrolyzed filtering area 102 can also be vertical cuboid, and top is equipped with the second catalyst inlet 109, lower part
Equipped with regulating valve 111, sidepiece is equipped with gas-phase product outlet 104, and is pyrolyzed filtering area 102 and gas-phase product outlet 104 by the
Two grids 106 separate.
Gas-phase product outlet 104 is connected with product condensation separator 3, and gas-phase product is separated by product condensation separator 3
Afterwards, biogas, wood vinegar, biological light oil and biological heavy oil etc. are finally obtained.Second catalyst inlet 109 and first order whirlwind
The ash bucket of separator 4 connects, and only provides side in Fig. 2, opposite side can equally connect the ash bucket of first order cyclone separator 4.
Regulating valve 111 then connects the second material returning device 9, and the second material returning device 9 connects catalyst regenerator 2, also only provides side herein, separately
It can be also connected during the practice of side by the second material returning device 9 with catalyst regenerator 2.
Second grid 106 is spaced by linear type flase floor to be formed, the angle model of linear type flase floor and vertical direction
Enclose for 45 °, and it is relatively low positioned at the linear type flase floor edges of boards position of 102 side of pyrolysis filtering area.The bottom of linear type flase floor
Position is less than the tip position of next layer of linear type flase floor, while linear type flase floor spaces between distance and is less than heat
Solve the particle diameter of catalyst in filtering area 102.
2 import of catalyst regenerator is connected with the first material returning device 8 and the second material returning device 9 respectively, and catalyst regenerator 2 goes out
Import of the mouth then with first order cyclone separator 4 is connected.In addition, heat collector 10 is additionally provided with catalyst regenerator 2, heat collector 10
The heat generated by biomass semicoke can be effectively utilized.
The course of work is as follows：
Biomass is passed into material inlet 108, and catalyst n i/Al2O3It is passed into the first catalyst inlet 107, Liang Zhejin
Enter to mix heating zone 103, realize quick mixing heating by mutually colliding on material mixed plate 110, and quickly enter pyrolysis
Reaction zone 101 starts vigorous reaction.
Reactiveness in pyrolysis reaction region 101 is fluid bed, and temperature is 600-900 DEG C, and solid particle leans on gravity fall
To returning charge valve 112, entered afterwards by the first material returning device 8 in catalyst regenerator 2.And the gas phase that pyrolysis reaction region 101 generates
Product then enters pyrolysis filtering area 102 by the first grid 105, the catalyst n i/Al with being pyrolyzed filtering area 1022O3Contact carries out
Reaction, while catalyst n i/Al2O3Also play the effect of dust in filtering gas-phase product.
Reactiveness in pyrolysis filtering area 102 is moving bed, and temperature is 600-900 DEG C, and solid particle falling speed is led to
The regulating valve 111 of lower part is overregulated to control, and solid particle is then entered in catalyst regenerator 2 by the second material returning device 9.Pyrolysis
Filtering area 102 primarily serves filtering dust and reduces the effect of product heavy constituent content, can significantly improve product liquid quality.
The width of pyrolysis filtering area 102 and the granularity of catalyst etc. are determined to be pyrolyzed by the gas-phase product that pyrolysis reaction region 101 generates
The residence time of filtering area 102.After reaction, solid material enters catalyst again by 112 and first material returning device 8 of returning charge valve
In raw device 2, and gaseous phase materials enter product condensation separator 3 by gas-phase product outlet 104, by product condensation separator 3
Separation after, obtain biogas, wood vinegar, biological light oil and biological heavy oil etc..
Catalyst after 2 regeneration treatment of catalyst regenerator then enters catalyst classification piece-rate system, will be catalyzed
Agent is divided into 4 sections by grain diameter and puts into different workshop sections respectively, is respectively：The lower particle diameter of the separation of first order separator 4 is more than 2mm
Catalyst be used for high-temperature oil gas it is secondary pyrolysis filtering；The catalyst that second level separator 5 isolates 0.5-2mm is used for fast speed heat
Solution reaction；The catalyst that third level separator 6 isolates 0.1-0.5mm is sent into the second material returning device 9, afterwards into catalyst regeneration
Device 2 is used to maintain technique thermal cycle；Fourth stage separator 7 is isolated to be arranged outside the catalyst less than 0.1mm.
Claims (10)
1. a kind of biomass fast thermal decomposition device, it is characterised in that including pyrolysis reactor, catalyst classification piece-rate system, urge
Agent regenerator and product condensation separator；
The pyrolysis reactor includes mixing heating zone, is arranged on the pyrolysis reaction region of mixing heating zone lower end and positioned at pyrolysis
The pyrolysis filtering area of reaction zone side；The pyrolysis reaction region is separated with pyrolysis filtering area by the first grid；
Material inlet and the first catalyst inlet are equipped with the top of the mixing heating zone；The pyrolysis reaction region lower part is equipped with returning charge
Valve, and be connected by the first material returning device with catalyst regenerator；The second catalyst inlet is equipped with the top of the pyrolysis filtering area, under
Portion is equipped with regulating valve, and sidepiece is exported equipped with gas-phase product；The pyrolysis filtering area passes through the second grid point with gas-phase product outlet
Open, gas-phase product outlet is connected with product condensation separator, and regulating valve is connected by the second material returning device and catalyst regenerator import
Connect；
First catalyst inlet and the second catalyst inlet are connected with catalyst classification piece-rate system respectively, the catalyst
Regenerator outlet is connected with catalyst classification piece-rate system import.
2. biomass fast thermal decomposition device according to claim 1, it is characterised in that the catalyst is classified piece-rate system
It is composed in series by tetra-cyclone, the outlet of upper level cyclone separator is connected with next stage cyclone inlet；
The ash bucket of the first order cyclone separator is connected with the second catalyst inlet at the top of pyrolysis filtering area, the second level
The ash bucket of cyclone separator is connected with the first catalyst inlet at the top of mixing heating zone, the ash of the third-stage cyclone separator
Bucket is connected with the second material returning device, row outside the ash bucket of the fourth stage cyclone separator and outlet respectively.
3. biomass fast thermal decomposition device according to claim 1, it is characterised in that the mixing heating zone is equipped with some
Material mixed plate；The shape of the material mixed plate is triangular prism, is arranged in parallel between each other and is layered Heterogeneous Permutation.
4. biomass fast thermal decomposition device according to claim 1, it is characterised in that first grid is by inverted v-shaped
Flase floor is spaced composition；The inverted v-shaped flase floor is dissymmetrical structure, positioned at pyrolysis reaction region side edges of boards and vertically
The angle in direction is less than the angle positioned at pyrolysis filtering area side edges of boards and vertical direction.
5. biomass fast thermal decomposition device according to claim 4, it is characterised in that the inverted v-shaped flase floor is located at
Tip position of the bottom position of pyrolysis reaction region side edges of boards less than next layer of inverted v-shaped flase floor；The inverted v-shaped grid
Plate is flush to the tip position of next layer of inverted v-shaped flase floor positioned at the bottom position of pyrolysis filtering area side edges of boards.
6. biomass fast thermal decomposition device according to claim 4, it is characterised in that between the inverted v-shaped flase floor
Spacing distance be less than pyrolysis reaction region in catalyst particle diameter.
7. biomass fast thermal decomposition device according to claim 1, it is characterised in that second grid is by linear type lattice
Screen is spaced composition；The angular range of the linear type flase floor and vertical direction is 15-45 °.
8. biomass fast thermal decomposition device according to claim 7, it is characterised in that the bottom of the linear type flase floor
Tip position of the position less than next layer of linear type flase floor.
9. biomass fast thermal decomposition device according to claim 1, it is characterised in that the pyrolysis filtering area includes two
It is a, it is symmetrically arranged in pyrolysis reaction region both sides.
A kind of 10. biomass fast pyrogenation technique using such as any described device of claim 1~9, it is characterised in that including
Following steps：
1) biomass and catalyst are entered by material inlet and the first catalyst inlet respectively, realize that mixing rises in mixing heating zone
Temperature, and start to react into pyrolysis reaction region；
Catalyst after reaction and the semicoke not reacted completely are entered in catalyst regenerator by the first material returning device, are regenerated
Processing；
2) gas-phase product of generation enters pyrolysis filtering area by the first grid in step 1), with the catalyst in pyrolysis filtering area
Contact is reacted, and filters dust in gas-phase product；
Catalyst after reaction is then entered in catalyst regenerator by the second material returning device, carries out regeneration treatment；
3) gas-phase product in step 2) after pyrolysis is filtered enters product condensation separator by the second grid, carries out product
Separating treatment；
4) step 1) and the middle catalyst Jing Guo catalyst regenerator regeneration treatment of step 2), segregative line is classified into catalyst
System, separates lower catalyst of the particle diameter more than 2mm by first order separator and enters pyrolysis filtering area, isolated by second level separator
The catalyst of 0.5-2mm enters mixing heating zone, and the catalyst feeding second that 0.1-0.5mm is isolated by third level separator is returned
Glassware, is used to maintain technique thermal cycle afterwards into catalyst regenerator, urging less than 0.1mm is isolated by fourth stage separator
Agent is then outer to arrange.
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110699102A (en) * | 2019-11-05 | 2020-01-17 | 西安热工研究院有限公司 | Drying and pyrolyzing furnace and drying and pyrolyzing method for municipal domestic garbage |
Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN2465382Y (en) * | 2001-02-21 | 2001-12-12 | 永济电机厂工业公司 | Sand filter |
| RU2240869C1 (en) * | 2003-10-21 | 2004-11-27 | Государственное образовательное учреждение высшего профессионального образования "Волгоградский государственный архитектурно-строительный университет" | Filter-cyclone |
| CN101021334A (en) * | 2007-03-16 | 2007-08-22 | 合肥工业大学 | Internal-combustion heating type biomass gasification furnace |
| CN103396824A (en) * | 2013-08-13 | 2013-11-20 | 山东泰然新能源有限公司 | High-efficiency production technique for preparing fuel oil by pyrolyzing biomass |
| CN106675595A (en) * | 2015-11-05 | 2017-05-17 | 中国石油化工股份有限公司大连石油化工研究院 | Biomass pyrolysis gasification method and biomass pyrolysis gasification system |
| CN207987111U (en) * | 2017-10-25 | 2018-10-19 | 浙江科技学院 | A kind of biomass fast thermal decomposition device |
-
2017
- 2017-10-25 CN CN201711014989.1A patent/CN107937011B/en active Active
Patent Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN2465382Y (en) * | 2001-02-21 | 2001-12-12 | 永济电机厂工业公司 | Sand filter |
| RU2240869C1 (en) * | 2003-10-21 | 2004-11-27 | Государственное образовательное учреждение высшего профессионального образования "Волгоградский государственный архитектурно-строительный университет" | Filter-cyclone |
| CN101021334A (en) * | 2007-03-16 | 2007-08-22 | 合肥工业大学 | Internal-combustion heating type biomass gasification furnace |
| CN103396824A (en) * | 2013-08-13 | 2013-11-20 | 山东泰然新能源有限公司 | High-efficiency production technique for preparing fuel oil by pyrolyzing biomass |
| CN106675595A (en) * | 2015-11-05 | 2017-05-17 | 中国石油化工股份有限公司大连石油化工研究院 | Biomass pyrolysis gasification method and biomass pyrolysis gasification system |
| CN207987111U (en) * | 2017-10-25 | 2018-10-19 | 浙江科技学院 | A kind of biomass fast thermal decomposition device |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110699102A (en) * | 2019-11-05 | 2020-01-17 | 西安热工研究院有限公司 | Drying and pyrolyzing furnace and drying and pyrolyzing method for municipal domestic garbage |
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