CN107723014A - A kind of biomass fast pyrogenation upgrading purifier and technique - Google Patents
A kind of biomass fast pyrogenation upgrading purifier and technique Download PDFInfo
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- CN107723014A CN107723014A CN201711009596.1A CN201711009596A CN107723014A CN 107723014 A CN107723014 A CN 107723014A CN 201711009596 A CN201711009596 A CN 201711009596A CN 107723014 A CN107723014 A CN 107723014A
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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
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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
- C10G2300/706—Catalytic metal recovery
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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 pyrogenation upgrading purifier and technique, its device includes multifunctional reactor, pyrolysis catalysts classification piece-rate system, upgrading catalyst classification piece-rate system, pyrolysis catalysts regenerator, upgrading catalyst regenerator and product condensation separator.The device enables biomass in a reactor while realizes pyrolysis, the function of upgrading and purification.
Description
Technical field
The invention belongs to field of energy utilization, and in particular to a kind of biomass fast pyrogenation upgrading purifier and technique.
Background technology
Solving energy problem has great strategic importance for world economic growth.Coal, oil and natural gas etc. are changed
The long-term use of stone fuel, cause 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 not present product scale and disappeared
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 focus of domestic and international biomass liquefying research and development.
However, the pyrolysis oil inferior quality of rapidly pyrolysing and liquefying biomass in the prior art, lacks high added value, big dosage
Utilization ways.Due to biological furol viscosity is high, oxygen content is high, polarity is strong, calorific value is low, acidity is high, corrosion is strong, easily polymerize,
The defects of stability difference, it is necessary to carry out refined modification.In addition, containing fine ash in the liquid fuel of generation, biomass is also constrained
The use of fuel oil.
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 pyrogenation upgrading purification dress
Put so that biomass can realize pyrolysis, the function of upgrading and purification simultaneously in a reactor.
The present invention is directed to the technical scheme that above-mentioned technical problem is provided：
A kind of biomass fast pyrogenation upgrading purifier, including multifunctional reactor, pyrolysis catalysts classification segregative line
System, upgrading catalyst classification piece-rate system, pyrolysis catalysts regenerator, upgrading catalyst regenerator and product condensation separator；
The multifunctional reactor includes mixing heating zone, is arranged on the pyrolysis reaction region and position of mixing heating zone lower end
Upgrading filtering area in pyrolysis reaction region side；The pyrolysis reaction region is separated with upgrading filtering area by the first grid；
Material inlet and the first catalyst inlet are provided with the top of the mixing heating zone；The pyrolysis reaction region bottom is provided with
Returning charge valve, and be connected by the first material returning device with pyrolysis catalysts regenerator；The second catalysis is provided with the top of the upgrading filtering area
Agent import, bottom are provided with regulating valve, and sidepiece exports provided with gas-phase product；The outlet of the upgrading filtering area and gas-phase product passes through the
Two grids are separated, and gas-phase product outlet is connected with product condensation separator, and regulating valve is connected with upgrading catalyst regenerator import；
First catalyst inlet is connected with pyrolysis catalysts classification piece-rate system, and second catalyst inlet is with carrying
The classification piece-rate system connection of matter catalyst；The pyrolysis catalysts regenerator outlet and pyrolysis catalysts classification piece-rate system import
Connection, the upgrading catalyst regenerator outlet are connected with the classification piece-rate system import of upgrading catalyst.
In above-mentioned technical scheme, biomass is entered by material inlet, and pyrolysis catalysts are entered by the first catalyst inlet
Enter, both realize quick mixing heating by mutually colliding in mixing heating zone, and quickly enter pyrolysis reaction region and start acutely
Reaction, the gas-phase product of pyrolysis reaction region generation pass through the upgrading that the first grid enters in upgrading filtering area, with upgrading filtering area
Catalyst contact carries out upgrading purification, and the wherein upgrading catalyst in upgrading filtering area is entered by the second catalyst inlet.
Meanwhile upgrading filtering area also plays the effect of dust in filtering gas-phase product, the dust that gas-phase product carries
Grain is by the upgrading catalyst filtration of upgrading filtering area and moves down discharge therewith.The width of upgrading filtering area and the grain of upgrading catalyst
Degree etc. determine by pyrolysis reaction region generation gas-phase product upgrading filtering area residence time.
After reaction terminates, pyrolysis catalysts and the semicoke not reacted completely enter pyrolysis catalysts again by the first material returning device
Regeneration treatment is carried out in raw device, is classified piece-rate system into pyrolysis catalysts afterwards, the pyrolysis catalysts after separation are according to difference
Particle diameter respectively enters multifunctional reactor, the second returning charge valve or outer row；And reacted upgrading catalyst then enters upgrading and is catalyzed
Regeneration treatment is carried out in agent regenerator, is classified piece-rate system into upgrading catalyst afterwards, the upgrading catalyst after separation according to
Different-grain diameter respectively enters multifunctional reactor or outer row；In addition, gas-phase product eventually enters into product by gas-phase product outlet
Condensation separator is separated, and finally gives biogas, pyrolkigneous liquid, biological light oil and biological heavy oil etc..
Preferably, first catalyst inlet is vertically arranged at the top of mixing heating zone；The material inlet includes two
It is individual, 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 pyrolysis catalysts classification piece-rate system is composed in series by three-stage cyclone separator, upper level whirlwind
The outlet of separator is connected with next stage cyclone inlet；
The ash bucket of the first order cyclone separator is connected with the first catalyst inlet at the top of mixing heating zone, and described the
The ash bucket of secondary cyclone is connected by the second material returning device with pyrolysis catalysts regenerator, the third-stage cyclone separator
Ash bucket and outlet is outer respectively arranges.
Piece-rate system is classified by pyrolysis catalysts, can be by the pyrolysis after pyrolysis catalysts regenerator regeneration treatment
Catalyst is divided into 3 sections by grain diameter and puts into different workshop sections, the respectively lower particle diameter of first order cyclone separator separation respectively
Pyrolysis catalysts more than 0.5mm are reacted for fast pyrogenation, and the pyrolysis that second level cyclone separator isolates 0.1-0.5mm is urged
Agent is used to maintain technique thermal cycle, and third-stage cyclone separator is isolated to be arranged outside the catalyst less than 0.1mm.
Preferably, the upgrading catalyst classification piece-rate system is composed in series by secondary cyclone, upper level whirlwind
The outlet of separator is connected with next stage cyclone inlet；
The ash bucket of the fourth stage cyclone separator is connected with the second catalyst inlet at the top of upgrading filtering area, and described
Arranged outside the ash bucket of five-stage whirlwind separator and outlet respectively.
Piece-rate system is classified by upgrading catalyst, can be by the upgrading after upgrading catalyst regenerator regeneration treatment
Catalyst is divided into 2 sections by grain diameter and puts into different workshop sections, the respectively lower particle diameter of fourth stage cyclone separator separation respectively
Upgrading catalyst more than 0.5mm is used for upgrading filtering reaction, and the upgrading that level V cyclone separator isolates less than 0.5mm is urged
Arranged outside agent.
Preferably, it is provided with heat collector in the pyrolysis catalysts regenerator.The setting can be effectively utilized by incomplete
The heat of the biomass semicoke generation of reaction, can provide heat for pyrolytic reaction.
Preferably, if the mixing heating zone is provided with dry material mixed plate；The material mixed plate is shaped as 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 drift angle scope is 45-120 °.
Preferably, the pyrolysis reaction region is fluid bed, catalyst Al2O3, reaction temperature is 600-800 DEG C, catalyst
By being gravitationally fallen to returning charge valve, returning charge valve should have self-sealing function.
Preferably, the upgrading filtering area is moving bed, and catalyst is Ni base catalyst, and upgrading filtering area temperature is 400-
600 DEG C, catalyst falling speed is controlled by adjusting the regulating valve of bottom.
Preferably, the pyrolysis catalysts regenerator is fluid bed, and temperature is 700-950 DEG C.
Preferably, the upgrading catalyst regenerator is fluid bed, and temperature is 400-650 DEG C.
Preferably, first grid is spaced by inverted v-shaped flase floor forms；The inverted v-shaped flase floor is not
Symmetrical structure, it is less than positioned at the angle of pyrolysis reaction region side edges of boards and vertical direction positioned at upgrading filtering area side edges of boards with erecting
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 upgrading
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 bottom position that the inverted v-shaped flase floor is located at upgrading filtering area side edges of boards is flush to
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 grain of pyrolysis catalysts in pyrolysis reaction region
Footpath.
Preferably, second grid is spaced by in-line flase floor forms；The in-line flase floor with it is vertical
The angular range in direction is 15-45 °.
Preferably, tip position of the bottom position of the in-line flase floor less than next layer of in-line flase floor.
Preferably, the spacing distance of the in-line flase floor is less than the particle diameter of upgrading catalyst in upgrading filtering area.
Preferably, the upgrading filtering area includes two, is respectively symmetrically arranged at pyrolysis reaction region both sides.
Preferably, the upgrading catalyst regenerator burns device and reductive jar including fluid bed.Flowed out from upgrading filtering area
Upgrading catalyst reaction inactivation after return upgrading catalyst regenerator in fluid bed burn device again after reductive jar reduces,
It is fed again into by upgrading catalyst classification piece-rate system in upgrading filtering area, so circulation.
The present invention also provides a kind of biomass fast pyrogenation upgrading purification technique using such as above-mentioned device, including following step
Suddenly：
1) biomass and pyrolysis catalysts are entered by material inlet and the first catalyst inlet respectively, real in mixing heating zone
Now mixing heating, and start to react into pyrolysis reaction region；
Reacted pyrolysis catalysts and the semicoke not reacted completely are regenerated by the first material returning device into pyrolysis catalysts
In device, regeneration treatment is carried out；
2) gas-phase product of generation enters carrying in upgrading filtering area, with upgrading filtering area by the first grid in step 1)
The contact of matter catalyst is reacted；
Reacted upgrading catalyst then enters in upgrading catalyst regenerator, carries out regeneration treatment；
3) gas-phase product in step 2) after upgrading is filtered enters product condensation separator by the second grid, carries out
Product separating treatment；
4) pyrolysis catalysts in step 1) Jing Guo pyrolysis catalysts regenerator regeneration treatment, it is classified into pyrolysis catalysts
Piece-rate system, pyrolysis catalysts of the lower particle diameter more than 0.5mm are separated by first order cyclone separator and enter mixing heating zone, by the
The catalyst that secondary cyclone isolates 0.1-0.5mm enters pyrolysis catalysts regenerator by the second material returning device, by
The pyrolysis catalysts that three-stage cyclone separator isolates less than 0.1mm are then arranged outside；
5) the upgrading catalyst in step 2) Jing Guo upgrading catalyst regenerator regeneration treatment, it is classified into upgrading catalyst
Piece-rate system, upgrading catalyst of the lower particle diameter more than 0.5mm is separated by fourth stage cyclone separator and enters upgrading filtering area, by the
Five-stage whirlwind separator isolates upgrading catalyst of the particle diameter less than 0.5mm then outer row.
Compared with the existing technology, beneficial effects of the present invention are embodied in：
(1) biomass fast pyrogenation upgrading purifier provided by the present invention can realize the regeneration of catalyst and divide
Level separation, realizes recycling for catalyst.
(2) multifunctional reactor in biomass fast pyrogenation upgrading purifier provided by the present invention will by grid
Pyrolysis reaction region distinguishes with upgrading filtering, realizes biomass in a reactor while realizes pyrolysis, upgrading and purification
Function, the yield and quality of product liquid can be effectively improved, reduce product liquid contains grey rate.
(3) biomass fast pyrogenation upgrading purification technique provided by the present invention, can effectively improve product liquid
Yield and quality, reduce product liquid contains grey rate.
Brief description of the drawings
Fig. 1 is the structural representation of biomass fast pyrogenation upgrading purifier in embodiment；
Fig. 2 is the structural representation of multifunctional reactor in embodiment.
Wherein, 1, multifunctional reactor；101st, pyrolysis reaction region；102nd, upgrading filtering area；103rd, heating zone is mixed；104、
Gas-phase product exports；105th, the first grid；106th, the second grid；107th, the first catalyst inlet；108th, material inlet；109th,
Two catalyst inlets；110th, material mixed plate；111st, regulating valve；112nd, returning charge valve；2nd, pyrolysis catalysts regenerator；3rd, product is cold
Solidifying separator；4th, fluid bed burns device；5th, reductive jar；6th, the first material returning device；7th, the second material returning device；8th, first order cyclonic separation
Device；9th, fourth stage cyclone separator；10th, level V cyclone separator；11st, second level cyclone separator；12nd, third level whirlwind point
From device；13rd, heat collector.
Embodiment
With reference to specific embodiment, the invention will be further described.
Embodiment
As shown in figure 1, biomass fast pyrogenation upgrading purifier includes multifunctional reactor 1, pyrolysis catalysts are classified
Piece-rate system, upgrading catalyst classification piece-rate system, pyrolysis catalysts regenerator 2, upgrading catalyst regenerator and product condensation
Separator 3.
Wherein, pyrolysis catalysts classification piece-rate system is composed in series by three-stage cyclone separator, upper level cyclone separator
Outlet be connected with next stage cyclone inlet.The ash bucket of first order cyclone separator 8 is with mixing the top of heating zone 103
First catalyst inlet 107 is connected, and the ash bucket of second level cyclone separator 11 is regenerated by the second material returning device 7 with pyrolysis catalysts
Device 2 connects, and is arranged outside the ash bucket of third-stage cyclone separator 12 and outlet respectively.
And upgrading catalyst classification piece-rate system is then composed in series by secondary cyclone, upper level cyclone separator
Outlet is connected with next stage cyclone inlet.The of the ash bucket of fourth stage cyclone separator 9 and the top of upgrading filtering area 102
Two catalyst inlets 109 connect, and outer arrange then is distinguished in the ash bucket of level V cyclone separator 10 and outlet.
As shown in Fig. 2 multifunctional reactor 1 includes mixing heating zone 103, pyrolysis reaction region 101 and upgrading filtering area
102, three is in the enclosure interior of multifunctional reactor 1.
Mixing heating zone 103 is arranged on the top of pyrolysis reaction region 101, can be perpendicular in both global shape actual productions
Straight cuboid, and the bottom of pyrolysis reaction region 101 is provided with the returning charge valve 112 with self-sealing function, and by the first material returning device 6 with
Pyrolysis catalysts regenerator 2 connects.Upgrading filtering area 102 is two, is separately positioned on the both sides of pyrolysis reaction region 101.Pyrolysis is anti-
The upgrading filtering area 102 in area 101 and both sides is answered to be 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 the side edges of boards of pyrolysis reaction region 101 and vertical direction is less than and is located at the side edges of boards of upgrading filtering area 102 and vertical direction
Angle.It it is 30 ° positioned at the angular range of the side edges of boards of pyrolysis reaction region 101 and vertical direction, positioned at upgrading 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 the side edges of boards of pyrolysis reaction region 101
Position is less than the tip position of next layer of inverted v-shaped flase floor, and inverted v-shaped flase floor is located at the side edges of boards of upgrading filtering area 102
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 pyrolysis catalysts in pyrolysis reaction region 101.
The top of mixing heating zone 103 is provided with the catalyst inlet 107 of material inlet 108 and first.First catalyst inlet
107 are vertically arranged at the top of mixing heating zone 103, 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 the catalyst inlet 107 of material inlet 108 and first is 30 °,
First catalyst inlet 107 is connected with the ash bucket of first order cyclone separator 8.
If in addition, being provided with dry material mixed plate 110 in mixing heating zone 103, material mixed plate 110 is shaped as Mitsubishi
Post, 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.
Upgrading filtering area 102 due to the both sides of pyrolysis reaction region 101 only introduces the upgrading of side herein to be symmetrical arranged
Filter area 102.The shape of upgrading filtering area 102 can also be vertical cuboid, and top is provided with the second catalyst inlet 109, bottom
Provided with regulating valve 111, sidepiece is provided with gas-phase product outlet 104, and upgrading filtering area 102 and gas-phase product outlet 104 pass through the
Two grids 106 separate.
Gas-phase product outlet 104 is connected with product condensation separator 3, and gas-phase product separates by product condensation separator 3
Afterwards, biogas, pyrolkigneous liquid, biological light oil and biological heavy oil etc. are finally given.Second catalyst inlet 109 and fourth stage whirlwind
The ash bucket of separator 9 connects, and only provides side in Fig. 1, opposite side can equally connect the ash bucket of fourth stage cyclone separator 9.
Regulating valve 111 then connects upgrading catalyst regenerator, and upgrading catalyst regenerator burns device 4 and reductive jar including fluid bed successively
5, also only provide side herein, can be also connected with upgrading catalyst regenerator during opposite side practice.
Second grid 106 is spaced by in-line flase floor to be formed, the angle model of in-line flase floor and vertical direction
Enclose for 45 °, and it is relatively low positioned at the in-line flase floor edges of boards position of the side of upgrading filtering area 102.The bottom of in-line flase floor
Position is less than the tip position of next layer of in-line flase floor, while in-line flase floor spaces between distance and is less than and carries
The particle diameter of upgrading catalyst in matter filtering area 102.
The import of pyrolysis catalysts regenerator 2 is connected with the first material returning device 6 and the second material returning device 7 respectively, and pyrolysis catalysts
The import that regenerator 2 exports then with first order cyclone separator 8 is connected.
Fluid bed in upgrading catalyst regenerator burns the import of device 4 and the returning charge valve 111 of the bottom of upgrading filtering area 102
Connection, and import of the outlet of reductive jar 5 then with fourth stage cyclone separator 9 is connected.
In addition, being additionally provided with heat collector 13 in pyrolysis catalysts regenerator 2, heat collector 13 can be effectively utilized by incomplete
The heat of the biomass semicoke generation of reaction, can provide heat for pyrolytic reaction.
The course of work is as follows：
Biomass is passed into material inlet 108, and catalyst Al2O3The first catalyst inlet 107 is passed into, both enter
Heating zone 103 is mixed, realizes quick mixing heating by mutually colliding on material mixed plate 110, and it is anti-to quickly enter pyrolysis
Area 101 is answered to start vigorous reaction.
Reactiveness in pyrolysis reaction region 101 is fluid bed, and temperature is 600-800 DEG C, and solid particle leans on gravity fall
To returning charge valve 112, entered afterwards by the first material returning device 6 in pyrolysis catalysts regenerator 2.And what pyrolysis reaction region 101 generated
Gas-phase product then enters upgrading filtering area 102, the catalyst n i base catalyst with upgrading filtering area 102 by the first grid 105
Contact carries out upgrading filtering reaction, while Ni base catalyst also plays the effect of dust in filtering gas-phase product.
Reactiveness in upgrading filtering area 102 is moving bed, and temperature is 400-600 DEG C, and solid particle falling speed is led to
The regulating valve 111 of bottom is overregulated to control, and upgrading is returned after the upgrading catalyst reaction inactivation flowed out from upgrading filtering area 102
Fluid bed in catalyst regenerator burns device 4 again after the reduction of reductive jar 5, into upgrading catalyst classification piece-rate system.
The width of upgrading filtering area 102 and the granularity of upgrading catalyst etc. determine that the gas-phase product generated by pyrolysis reaction region 101 exists
The residence time of upgrading filtering area 102.
Gaseous phase materials after upgrading is filtered then enter product condensation separator 3 by gas-phase product outlet 104, pass through
After the separation of product condensation separator 3, biogas, pyrolkigneous liquid, biological light oil and biological heavy oil etc. are obtained.
Pyrolysis catalysts after the regeneration treatment of pyrolysis catalysts regenerator 2 then enter pyrolysis catalysts classification separation
System, pyrolysis catalysts are divided into 3 sections by grain diameter and put into different workshop sections respectively, be respectively：First order cyclonic separation
Lower pyrolysis catalysts of the particle diameter more than 0.5mm of the separation of device 8 are reacted for fast pyrogenation, and second level cyclone separator 11 is isolated
0.1-0.5mm pyrolysis catalysts are used to maintain technique thermal cycle, and third-stage cyclone separator 12 isolates urging less than 0.1mm
Arranged outside agent.
Upgrading catalyst after the regeneration treatment of upgrading catalyst regenerator 2 then enters the classification separation of upgrading catalyst
System, upgrading catalyst is divided into 2 sections by grain diameter and puts into different workshop sections respectively, be respectively：Fourth stage cyclonic separation
Lower upgrading catalyst of the particle diameter more than 0.5mm of the separation of device 9 is used for upgrading filtering reaction, and level V cyclone separator 10 is isolated small
In row outside 0.5mm upgrading catalyst.
Claims (10)
1. a kind of biomass fast pyrogenation upgrading purifier, it is characterised in that including multifunctional reactor, pyrolysis catalysts point
Level piece-rate system, upgrading catalyst classification piece-rate system, pyrolysis catalysts regenerator, upgrading catalyst regenerator and product condensation
Separator；
The multifunctional reactor includes mixing heating zone, is arranged on the pyrolysis reaction region of mixing heating zone lower end and positioned at heat
Solve the upgrading filtering area of reaction zone side；The pyrolysis reaction region is separated with upgrading filtering area by the first grid；
Material inlet and the first catalyst inlet are provided with the top of the mixing heating zone；The pyrolysis reaction region bottom is provided with returning charge
Valve, and be connected by the first material returning device with pyrolysis catalysts regenerator；Enter at the top of the upgrading filtering area provided with the second catalyst
Mouthful, bottom is provided with regulating valve, and sidepiece exports provided with gas-phase product；The upgrading filtering area passes through the second lattice with gas-phase product outlet
Grid are separated, and gas-phase product outlet is connected with product condensation separator, and regulating valve is connected with upgrading catalyst regenerator import；
First catalyst inlet is connected with pyrolysis catalysts classification piece-rate system, and second catalyst inlet is urged with upgrading
Agent classification piece-rate system connection；The pyrolysis catalysts regenerator outlet connects with pyrolysis catalysts classification piece-rate system import
Connect, the upgrading catalyst regenerator outlet is connected with the classification piece-rate system import of upgrading catalyst.
2. biomass fast pyrogenation upgrading purifier according to claim 1, it is characterised in that the pyrolysis catalysts
Classification piece-rate system is composed in series by three-stage cyclone separator, outlet and the next stage cyclone separator of upper level cyclone separator
Import connects；
The ash bucket of the first order cyclone separator is connected with the first catalyst inlet at the top of mixing heating zone, the second level
The ash bucket of cyclone separator is connected by the second material returning device with pyrolysis catalysts regenerator, the ash of the third-stage cyclone separator
Arranged outside bucket and outlet respectively.
3. biomass fast pyrogenation upgrading purifier according to claim 1, it is characterised in that the upgrading catalyst
Classification piece-rate system is composed in series by secondary cyclone, outlet and the next stage cyclone separator of upper level cyclone separator
Import connects；
The ash bucket of the fourth stage cyclone separator is connected with the second catalyst inlet at the top of upgrading filtering area, the level V
Arranged outside the ash bucket of cyclone separator and outlet respectively.
4. biomass fast pyrogenation upgrading purifier according to claim 1, it is characterised in that the mixing heating zone
If provided with dry material mixed plate；The material mixed plate is shaped as triangular prism, be arranged in parallel between each other and is layered dislocation and arranges
Row.
5. biomass fast pyrogenation upgrading purifier according to claim 1, it is characterised in that first grid by
Inverted v-shaped flase floor is spaced composition；The inverted v-shaped flase floor is dissymmetrical structure, positioned at pyrolysis reaction region side plate
The angle of side and vertical direction is less than the angle positioned at upgrading filtering area side edges of boards and vertical direction.
6. biomass fast pyrogenation upgrading purifier according to claim 5, it is characterised in that the inverted v-shaped lattice
Screen is located at tip position of the bottom position less than next layer of inverted v-shaped flase floor of pyrolysis reaction region side edges of boards；The V
The bottom position that font flase floor is located at upgrading filtering area side edges of boards is flush to the top position of next layer of inverted v-shaped flase floor
Put.
7. biomass fast pyrogenation upgrading purifier according to claim 1, it is characterised in that second grid by
In-line flase floor is spaced composition；The angular range of the in-line flase floor and vertical direction is 15-45 °.
8. biomass fast pyrogenation upgrading purifier according to claim 1, it is characterised in that the upgrading filtering area
Including two, pyrolysis reaction region both sides are respectively symmetrically arranged at.
9. biomass fast pyrogenation upgrading purifier according to claim 1, it is characterised in that the upgrading catalyst
Regenerator burns device and reductive jar including fluid bed.
10. a kind of biomass fast pyrogenation upgrading purification technique using such as any described device of claim 1~9, its feature
It is, comprises the following steps：
1) biomass and pyrolysis catalysts 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；
Reacted pyrolysis catalysts and the semicoke not reacted completely are entered in pyrolysis catalysts regenerator by the first material returning device,
Carry out regeneration treatment；
2) upgrading that the gas-phase product of generation enters in upgrading filtering area, with upgrading filtering area by the first grid in step 1) is urged
Agent contact is reacted；
Reacted upgrading catalyst then enters in upgrading catalyst regenerator, carries out regeneration treatment；
3) gas-phase product in step 2) after upgrading is filtered enters product condensation separator by the second grid, carries out product
Separating treatment；
4) pyrolysis catalysts in step 1) Jing Guo pyrolysis catalysts regenerator regeneration treatment, it is classified and separates into pyrolysis catalysts
System, lower pyrolysis catalysts of the particle diameter more than 0.5mm are separated by first order cyclone separator and enter mixing heating zone, by the second level
The catalyst that cyclone separator isolates 0.1-0.5mm enters pyrolysis catalysts regenerator by the second material returning device, by the third level
The pyrolysis catalysts that cyclone separator isolates less than 0.1mm are then arranged outside；
5) the upgrading catalyst in step 2) Jing Guo upgrading catalyst regenerator regeneration treatment, it is classified and separates into upgrading catalyst
System, lower upgrading catalyst of the particle diameter more than 0.5mm is separated by fourth stage cyclone separator and enters upgrading filtering area, by level V
Cyclone separator isolates upgrading catalyst of the particle diameter less than 0.5mm then outer row.
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| CN112779034A (en) * | 2019-11-28 | 2021-05-11 | 浙江科技学院 | Device and method for preparing light aromatic hydrocarbon from biomass |
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