CN107400539A - Low order fuel low temperature gasification device based on spiral pyrolysis apparatus and fluidized-bed gasifier - Google Patents
Low order fuel low temperature gasification device based on spiral pyrolysis apparatus and fluidized-bed gasifier Download PDFInfo
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- CN107400539A CN107400539A CN201710813279.9A CN201710813279A CN107400539A CN 107400539 A CN107400539 A CN 107400539A CN 201710813279 A CN201710813279 A CN 201710813279A CN 107400539 A CN107400539 A CN 107400539A
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- 238000000197 pyrolysis Methods 0.000 title claims abstract description 152
- 238000002309 gasification Methods 0.000 title claims abstract description 92
- 239000000446 fuel Substances 0.000 title claims abstract description 74
- 239000000463 material Substances 0.000 claims abstract description 14
- 230000008878 coupling Effects 0.000 claims abstract description 12
- 238000010168 coupling process Methods 0.000 claims abstract description 12
- 238000005859 coupling reaction Methods 0.000 claims abstract description 12
- 230000015572 biosynthetic process Effects 0.000 claims description 29
- 238000003786 synthesis reaction Methods 0.000 claims description 29
- 238000000926 separation method Methods 0.000 claims description 14
- 238000005979 thermal decomposition reaction Methods 0.000 claims description 12
- 238000004891 communication Methods 0.000 claims description 9
- 230000008676 import Effects 0.000 claims description 4
- 238000003032 molecular docking Methods 0.000 claims description 3
- 238000005192 partition Methods 0.000 claims 1
- 239000011232 storage material Substances 0.000 claims 1
- 239000011269 tar Substances 0.000 abstract description 32
- 239000003513 alkali Substances 0.000 abstract description 11
- 229910001413 alkali metal ion Inorganic materials 0.000 abstract description 10
- 229910001420 alkaline earth metal ion Inorganic materials 0.000 abstract description 10
- 238000006555 catalytic reaction Methods 0.000 abstract description 4
- 239000011280 coal tar Substances 0.000 abstract description 2
- 239000007789 gas Substances 0.000 description 50
- 239000000571 coke Substances 0.000 description 35
- 238000000034 method Methods 0.000 description 17
- 238000006243 chemical reaction Methods 0.000 description 16
- 230000008569 process Effects 0.000 description 14
- 239000000047 product Substances 0.000 description 13
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 8
- 229910052760 oxygen Inorganic materials 0.000 description 8
- 239000001301 oxygen Substances 0.000 description 8
- 239000003245 coal Substances 0.000 description 7
- 239000002028 Biomass Substances 0.000 description 6
- 230000000694 effects Effects 0.000 description 6
- 230000003197 catalytic effect Effects 0.000 description 5
- 238000005516 engineering process Methods 0.000 description 5
- 238000010438 heat treatment Methods 0.000 description 5
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 5
- 239000012159 carrier gas Substances 0.000 description 4
- 238000011049 filling Methods 0.000 description 4
- 239000002245 particle Substances 0.000 description 4
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 3
- 229910052799 carbon Inorganic materials 0.000 description 3
- 239000003054 catalyst Substances 0.000 description 3
- 230000008859 change Effects 0.000 description 3
- 238000010411 cooking Methods 0.000 description 3
- 238000002156 mixing Methods 0.000 description 3
- 239000010813 municipal solid waste Substances 0.000 description 3
- 239000002994 raw material Substances 0.000 description 3
- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 description 2
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 2
- DGAQECJNVWCQMB-PUAWFVPOSA-M Ilexoside XXIX Chemical compound C[C@@H]1CC[C@@]2(CC[C@@]3(C(=CC[C@H]4[C@]3(CC[C@@H]5[C@@]4(CC[C@@H](C5(C)C)OS(=O)(=O)[O-])C)C)[C@@H]2[C@]1(C)O)C)C(=O)O[C@H]6[C@@H]([C@H]([C@@H]([C@H](O6)CO)O)O)O.[Na+] DGAQECJNVWCQMB-PUAWFVPOSA-M 0.000 description 2
- FYYHWMGAXLPEAU-UHFFFAOYSA-N Magnesium Chemical compound [Mg] FYYHWMGAXLPEAU-UHFFFAOYSA-N 0.000 description 2
- 238000010521 absorption reaction Methods 0.000 description 2
- 229910052784 alkaline earth metal Inorganic materials 0.000 description 2
- 150000001342 alkaline earth metals Chemical class 0.000 description 2
- 229910052791 calcium Inorganic materials 0.000 description 2
- 239000011575 calcium Substances 0.000 description 2
- 229910002092 carbon dioxide Inorganic materials 0.000 description 2
- 238000007233 catalytic pyrolysis Methods 0.000 description 2
- 238000001833 catalytic reforming Methods 0.000 description 2
- 239000003610 charcoal Substances 0.000 description 2
- 239000012530 fluid Substances 0.000 description 2
- 238000011065 in-situ storage Methods 0.000 description 2
- 229910052749 magnesium Inorganic materials 0.000 description 2
- 239000011777 magnesium Substances 0.000 description 2
- 239000000203 mixture Substances 0.000 description 2
- 238000012545 processing Methods 0.000 description 2
- 238000000746 purification Methods 0.000 description 2
- 230000009257 reactivity Effects 0.000 description 2
- 230000004044 response Effects 0.000 description 2
- 229910052708 sodium Inorganic materials 0.000 description 2
- 239000011734 sodium Substances 0.000 description 2
- 230000007480 spreading Effects 0.000 description 2
- 238000003892 spreading Methods 0.000 description 2
- 239000013589 supplement Substances 0.000 description 2
- MYMOFIZGZYHOMD-UHFFFAOYSA-N Dioxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 description 1
- ZLMJMSJWJFRBEC-UHFFFAOYSA-N Potassium Chemical compound [K] ZLMJMSJWJFRBEC-UHFFFAOYSA-N 0.000 description 1
- 230000009471 action Effects 0.000 description 1
- 229910052783 alkali metal Inorganic materials 0.000 description 1
- 150000001340 alkali metals Chemical class 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000004364 calculation method Methods 0.000 description 1
- 239000001569 carbon dioxide Substances 0.000 description 1
- 229910002091 carbon monoxide Inorganic materials 0.000 description 1
- 238000004523 catalytic cracking Methods 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 239000003034 coal gas Substances 0.000 description 1
- 238000002485 combustion reaction Methods 0.000 description 1
- 239000002131 composite material Substances 0.000 description 1
- 150000001875 compounds Chemical class 0.000 description 1
- 238000009833 condensation Methods 0.000 description 1
- 230000005494 condensation Effects 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 238000005336 cracking Methods 0.000 description 1
- 238000000354 decomposition reaction Methods 0.000 description 1
- 230000007423 decrease Effects 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000001035 drying Methods 0.000 description 1
- 238000005243 fluidization Methods 0.000 description 1
- 239000002737 fuel gas Substances 0.000 description 1
- PCHJSUWPFVWCPO-UHFFFAOYSA-N gold Chemical compound [Au] PCHJSUWPFVWCPO-UHFFFAOYSA-N 0.000 description 1
- 239000010931 gold Substances 0.000 description 1
- 229910052737 gold Inorganic materials 0.000 description 1
- 238000012946 outsourcing Methods 0.000 description 1
- 230000003647 oxidation Effects 0.000 description 1
- 238000007254 oxidation reaction Methods 0.000 description 1
- 230000036284 oxygen consumption Effects 0.000 description 1
- 229910052700 potassium Inorganic materials 0.000 description 1
- 239000011591 potassium Substances 0.000 description 1
- 238000004321 preservation Methods 0.000 description 1
- 230000000171 quenching effect Effects 0.000 description 1
- 239000012265 solid product Substances 0.000 description 1
- 239000004449 solid propellant Substances 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
- 238000004781 supercooling Methods 0.000 description 1
- 230000001629 suppression Effects 0.000 description 1
- 238000012546 transfer Methods 0.000 description 1
- -1 vapor Chemical compound 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
- C10J3/58—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels combined with pre-distillation of the fuel
- C10J3/60—Processes
- C10J3/64—Processes with decomposition of the distillation products
- C10J3/66—Processes with decomposition of the distillation products by introducing them into the gasification zone
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
- C10J3/46—Gasification of granular or pulverulent flues in suspension
- C10J3/54—Gasification of granular or pulverulent fuels by the Winkler technique, i.e. by fluidisation
- C10J3/56—Apparatus; Plants
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
- C10J3/72—Other features
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
- C10J3/72—Other features
- C10J3/82—Gas withdrawal means
- C10J3/84—Gas withdrawal means with means for removing dust or tar from the gas
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J2200/00—Details of gasification apparatus
- C10J2200/15—Details of feeding means
- C10J2200/154—Pushing devices, e.g. pistons
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J2300/00—Details of gasification processes
- C10J2300/18—Details of the gasification process, e.g. loops, autothermal operation
- C10J2300/1807—Recycle loops, e.g. gas, solids, heating medium, water
Landscapes
- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Combustion & Propulsion (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Organic Chemistry (AREA)
- Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
- Processing Of Solid Wastes (AREA)
Abstract
Low order fuel low temperature gasification device based on spiral pyrolysis apparatus and fluidized-bed gasifier, belong to the field of gasification of low order fuel.The power output shaft of motor one is connected with speed-changing gear box power input shaft, one-level spiral pyrolysis apparatus is intercoupled with airlock by speed-changing gear box, connected between I and II spiral pyrolysis apparatus helical axis by shaft coupling, deuterostrophies pyrolysis apparatus connects with fluidized-bed gasifier；Deuterostrophies pyrolysis apparatus top is provided with steam entry；Fluidized-bed gasifier connects with cyclone separator, and fluidized-bed gasifier connects with gas handling system, and scum pipe connects with fluidized-bed gasifier bottom；Cyclone separator connects with one-level feed back pipe, and one-level feed back pipe connects with spiral material returning device, and spiral material returning device connects with two level feed back pipe, and two level feed back pipe connects with deuterostrophies pyrolysis apparatus.The present invention realizes the high efficient cryogenic gasification of low order fuel using being pyrolyzed burnt In-stiu catalysis part tar and relapsing alkali and alkaline earth metal ions catalysis coal tar low temperature gasification.
Description
Technical field
The present invention relates to a kind of low order fuel low temperature gasification device based on spiral pyrolysis apparatus and fluidized-bed gasifier, belong to
The field of gasification of low order fuel.
Background technology
Gasification refers to carbon-containing fuel（Coal, coal tar or biomass etc.）For raw material, with oxygen（Air, oxygen-enriched or technical pure
Oxygen）, vapor, carbon dioxide etc. be used as gasifying agent, in specific equipment, a series ofization occur under certain temperature and pressure
Reaction is learned, is to contain CO, H by solid fuel conversion2、CH4Deng the process of fuel gas.
Low order fuel（Low-order coal, biomass and rubbish from cooking）Reserves and abundance, degree of metamorphism is low, and volatile matter is high,
Gasification reactivity is high.In addition, the alkali and alkaline earth metal ions being rich in inside low order fuel（Low-order coal is rich in sodium, calcium and magnesium, biomass
Rich in potassium, calcium and magnesium, and sodium is mainly contained in rubbish from cooking）There is good catalytic action to gasification, be also remarkably improved combustion
The gasification rate of material.To low order fuel（Low-order coal and biomass）Calculation of thermodynamics show, when reaction temperature be higher than 700 DEG C
When, there is provided energy be enough to ensure that being gasified totally for the fuel.
The gasification of low order fuel generally comprises two processes, the pyrolysis of raw material and the gasification of coke.Conventional gasification
In the presence of two key issues, first, tar content is high in synthesis gas, during low temperature（<200℃）Easily condensation, it is viscous with water, coke etc.
Knot together, blocks air duct, equipment for gasification operation occurs difficult, while energy contained in tar（5%~15%）
Cannot effectively it utilize, wherein tar is mainly derived from the pyrolytic process of low order fuel；Second, the gasification rate of coke is low, pyrolysis
During in low order fuel 20% ~ 70% alkali and alkaline earth metal ions will be discharged into the form of atom or compound in gas phase,
The content of catalyst in the coke of generation is caused to reduce, reactivity and gasification rate are greatly reduced, and are unfavorable for carrying for efficiency of carbon con version
High and equipment for gasification maximization.
Two-part pyrolytic gasification technology separates the gasification of the pyrolysis of fuel and coke, carries out Discrete control, to
Promote the decomposition of tar and improve the gasification rate of coke.Wherein, more typical is the outer heat of the joint that Denmark University of Science and Technology develops
The two stage gasification technology of formula spiral pyrolysis apparatus and downdraft fixed bed gasifiers.Biomass pyrolytic generation pyrolysis gas containing tar with
High-temperature semi-coke enters down-draft type gasifying furnace together, when pyrolysis gas is by removing tar therein during high-temperature semi-coke gasification layer, but by
The limitation of external-heat spiral pyrolysis apparatus, is not easy to amplify, and the resistance of downdraft fixed bed gasifiers is larger, gasification rate compared with
It is low.Chinese patent 94190559.4 discloses a kind of low-order coal two of coupling fluidized bed pyrolysis apparatus and updraft type fixed-bed gasification furnace
Section gasification process.Fluid bed heat solution preocess（400-700 DEG C, ＜ 50atm）The semicoke of middle generation is fed to updraft type fixed bed
Interior gasification（1200 DEG C of ＜, ＜ 50atm）, pyrolysis gas and gasification gas each discharge, be sent to the TRT of terminal after mixing,
But tar content is higher in mixed gas.Chinese patent CN101440307A discloses a kind of coupling updraft type fixed-bed gasification furnace and stream
Change the two stage gasification technique of bed gasification furnace, epimere fixed bed gasification is further cracked using the high temperature in hypomere fluidized-bed gasification furnace
Tar in stove generation coal gas.Chinese patent CN1916123 discloses a kind of coupling fluidized bed and downdraft fixed bed two sections
Gasification process, the technique significantly reduce tar content by the catalytic reforming effect of semicoke bed.Chinese patent
CN102703131 discloses a kind of combined fluidized bed pyrolysis apparatus and the two-stage furnace gasification process of entrained flow gasifiers, utilizes air-flow
The catalytic reforming of high temperature pyrolysis, partial oxidation and semicoke in bed is acted on to remove tar.Domestic patent uses in pyrolysis phase
Self-heating fluid bed or fixed bed, be advantageous to the enhanced processing of equipment.
But in terms of tar removing, catalytic pyrolysis of the existing patent in gasifying stage by high-temperature coke to tar
Or the Pintsch process of tar itself removes tar, gasification temperature is higher, and removing of the tar in pyrolysis phase is not examined
Consider；Higher gasification temperature inevitably results in relatively low vaporized efficiency（It is cold gas efficiency for coal）, work as gasification temperature
When being increased to 1600 DEG C from 900 DEG C, vaporized efficiency decreases by 20% or so.In terms of coke gasification, existing patent passes through raising
The measure of temperature or pressure improves gasification rate, underutilization to alkali and alkaline earth metal ions catalyst in low order fuel；
Higher gasification temperature and pressure also results in higher investment and operating cost.
Therefore, to the gasification of low order fuel, the tar content in synthesis gas is reduced while gasification temperature is reduced, and
The alkali and alkaline earth metal ions that pyrolytic process discharges are relapsed to coke, can effectively solve to exist during low order fuel gasification
Above mentioned problem.
The content of the invention
The invention aims to reduce the tar content in low order fuel synthesis gas, while improve the reaction of coke
Property, there is provided a kind of low order fuel low temperature gasification device based on spiral pyrolysis apparatus and fluidized-bed gasifier.
The present invention is solves problem present in low order fuel gasification, based on existing two-part gasification technology, in pyrolysis rank
The spiral pyrolysis apparatus that Duan Caiyong no carrier gas is passed through；Fluidized-bed reactor is used in gasifying stage, to recycle stock while gasification
（Heat carrier）Heating is with to spiral pyrolysis apparatus heat supply.
Stacking states, and no-load in two-stage screw pyrolysis apparatus is presented in low order fuel in two-stage screw pyrolysis apparatus in the present invention
Gas is passed through；Low order fuel is decomposed by mixing to be heated with heat carrier, and pyrolysis gas is by slowly spreading spilling fuel bed；Generation
Pyrolysis gas and coke be sent directly into fluidized-bed gasifier and gasifying medium and react heat release, while being converted into gasification gas pair
Heat carrier is heated.The present invention is flowed by suppressing the gas in fuel bed, on the one hand extends tar in fuel bed
The interior residence time, make tar that sufficient cracking can occur under the catalytic action of coke, the tar reduced in pyrolysis gas contains
Amount；On the other hand, the alkali and alkaline earth metal ions that pyrolysis discharges in particle, it is not easy to be carried out due to the suppression of gas flowing
Fuel bed, it will adsorbed again in the presence of adjacent particles, the low temperature gasification for catalytic coke.Under stacking states
Intergranular close contact enhances above-mentioned both sides action effect.
The purpose of the present invention is achieved through the following technical solutions：
Low order fuel low temperature gasification device based on spiral pyrolysis apparatus and fluidized-bed gasifier, its composition include aggregate-storing system, spiral shell
Revolve pyrolysis system, fluidized gasification system and cyclone separation system；
Described aggregate-storing system includes feed bin, airlock, speed-changing gear box and motor one, and described spiral pyrolysis system includes one
Level spiral pyrolysis apparatus, shaft coupling and deuterostrophies pyrolysis apparatus, described fluidized gasification system include fluidized-bed gasifier, air inlet
System and scum pipe, described cyclone separation system include spiral material returning device, two level feed back pipe, at least one cyclone separator and
At least one one-level feed back pipe；
Described airlock is arranged on the bottom in feed bin, the described power output shaft of motor one and the power of speed-changing gear box
Input shaft is connected, and described speed-changing gear box has two power output shafts, and a wherein power for speed-changing gear box is defeated
Shaft is connected with airlock, and another power output shaft of speed-changing gear box is driven with the helical axis of one-level spiral pyrolysis apparatus
Connection, the fuel outlet of described feed bin lower end connect with the fuel inlet of one-level spiral pyrolysis apparatus upper end；
Connected between the described helical axis of one-level spiral pyrolysis apparatus and the helical axis of deuterostrophies pyrolysis apparatus by shaft coupling, one
The level outside cylinder of spiral pyrolysis apparatus docks with the outside cylinder of deuterostrophies pyrolysis apparatus, the heat of described deuterostrophies pyrolysis apparatus
Solution product exit connects with fluidized-bed gasifier；Spiral pyrolysis system is obliquely installed, the fuel inlet one of one-level spiral pyrolysis apparatus
Less than the thermal decomposition product exit end of deuterostrophies pyrolysis apparatus, deuterostrophies pyrolysis apparatus top is provided with steam entry at end；
The top of described fluidized-bed gasifier connects with cyclone separator, and bottom and the gas handling system of fluidized-bed gasifier connect
Logical, described scum pipe one end connects with the bottom of fluidized-bed gasifier；
Described cyclone separator bottom is correspondingly communicated with an one-level feed back pipe, all described one-level feed back pipe bottoms and spiral shell
Cycle glassware top is connected, and described spiral material returning device bottom is connected with two level feed back pipe top, and described two level feed back pipe is set
Put in one-level spiral pyrolysis apparatus and deuterostrophies pyrolysis apparatus intersection, and two level feed back pipe bottom and deuterostrophies pyrolysis apparatus top
Circulation feed back inlet communication.
It is of the invention to be relative to the beneficial effect of prior art：
1st, tar content is low in synthesis gas, without purification（Or simple purification）It can be used.Device of the present invention divides two-stage
To reduce the content of tar, first, in spiral pyrolysis apparatus, because no carrier gas adds, volatile matter can only be by slowly diffusing into
Fluidized bed gasification system, and spreading is carried out in coke layer, is advantageous to the catalytic pyrolysis of pyrolysis generation tar；Secondly, exist
In fluidized-bed gasifier, remaining tar reacts with oxygen-containing vapor, realizes conversion completely.
2nd, higher efficiency of carbon con version and vaporized efficiency.Device of the present invention can by the alkali metal in low order fuel and
The catalyst such as alkaline-earth metal are enriched in coke, the gasification reaction for catalytic coke；The coke of high reaction activity is without cooling
It is directly entered in fluidized-bed gasifier and participates in gasification reaction, remains the high activity of Jiao in situ.So that overall gasification temperature compared with
It is low（1000 DEG C of ＜）, ensure that higher vaporized efficiency.
3rd, pyrolytic process is controllable, and thermal decomposition product uniformity is good.Device of the present invention, low order fuel is in spiral pyrolysis apparatus
In residence time and temperature it is adjustable, pyrolytic process is controllable, and the uniformity of thermal decomposition product component is good, be advantageous to the later stage gasification bar
The setting of part.
4th, raw material sources are wide, strong applicability, good economy performance.Low order fuel is the composite can be widely applied to, because low
Containing abundant alkali and alkaline earth metal ions in rank coal, biomass and rubbish from cooking, the gasification available for catalysis low order fuel
Reaction.Low order fuel price is cheap, and the moisture of its internal preservation can be utilized by original position, without drying in advance, effectively raise
The economy of low order fuel utilization.
5th, oxygen consumption is low.Relatively low gasification temperature effectively reduces the consumption of oxygen；Therefore gasifying medium or can adopt
With oxygen rich gas, so as to reduce N in synthesis gas2Concentration.
Brief description of the drawings
The low order fuel low temperature gasification apparatus structure based on spiral pyrolysis apparatus and fluidized-bed gasifier that Fig. 1 is the present invention shows
It is intended to one.
The low order fuel low temperature gasification apparatus structure based on spiral pyrolysis apparatus and fluidized-bed gasifier that Fig. 2 is the present invention shows
It is intended to two, wherein, synthesis gas is discharged after heat-exchange system heat release, and normal-temperature water is converted into vapor row from after heat-exchange system heat absorption
Go out；
Fig. 3 is the low order fuel low temperature gasification apparatus structure schematic diagram based on spiral pyrolysis apparatus and fluidized-bed gasifier of the present invention
Three, wherein, synthesis gas is discharged after dividing wall type heat exchanger and heat-exchange system heat release successively, and normal-temperature water is from after heat-exchange system heat absorption
It is converted into vapor discharge；
Fig. 4 is the structural representation of speed-changing gear box.
Each component names and label are as follows in Fig. 1 ~ Fig. 4：
It is aggregate-storing system 1, feed bin 11, airlock 12, speed-changing gear box 13, the 13-1 of driving gear one, the 13-2 of driving gear two, driven
The 13-3 of gear one, the 13-4 of driven gear two, power input shaft 13-5, power output shaft 13-6, motor 1, spiral pyrolysis system
2nd, one-level spiral pyrolysis apparatus 21, shaft coupling 22, deuterostrophies pyrolysis apparatus 23, steam entry 23-1, dividing wall type heat exchanger 24, stream
Change bed gasification system 3, fluidized-bed gasifier 31, gas handling system 32, scum pipe 33, cyclone separation system 4, cyclone separator 41,
One-level feed back pipe 42, spiral material returning device 43, two level feed back pipe 44, motor 2 45, heat-exchange system 5.
Wherein：Airlock 12, speed-changing gear box 13, motor 1, one-level spiral pyrolysis apparatus 21, shaft coupling 22, two level spiral shell
Rotation pyrolysis apparatus 23, dividing wall type heat exchanger 24, fluidized-bed gasifier 31, motor 2 45, spiral material returning device 43 and heat-exchange system 5 are
Prior art, it is outsourcing product.
Embodiment
Technical scheme is further described below in conjunction with the accompanying drawings, but is not limited thereto, it is every to this
Inventive technique scheme is modified or equivalent substitution, without departing from the spirit and scope of technical solution of the present invention, all should cover
In protection scope of the present invention.
Embodiment one：As Figure 1 and Figure 4, present embodiment discloses one kind and is based on spiral pyrolysis apparatus and fluidisation
The low order fuel low temperature gasification device of bed gasifier, its composition include aggregate-storing system 1, spiral pyrolysis system 2, fluidized gasification system
System 3 and cyclone separation system 4；
Described aggregate-storing system 1 includes feed bin 11, airlock 12, speed-changing gear box 13 and motor 14, described spiral pyrolysis system
System 2 includes one-level spiral pyrolysis apparatus 21, shaft coupling 22 and deuterostrophies pyrolysis apparatus 23, and described fluidized gasification system 3 includes
Fluidized-bed gasifier 31, gas handling system 32 and scum pipe 33, described cyclone separation system 4 include spiral material returning device 43, two level
Feed back pipe 44, at least one cyclone separator 41 and at least one one-level feed back pipe 42；
Described airlock 12 is arranged on the bottom in feed bin 11, the power output shaft and speed-changing gear box of described motor 1
13 power input shaft drive connection, described speed-changing gear box 13 have two power output shaft 13-6, speed-changing gear box 13
A wherein power output shaft 13-6 be connected with airlock 12, another power output shaft 13-6 of speed-changing gear box 13
It is connected with the helical axis of one-level spiral pyrolysis apparatus 21, fuel outlet and the one-level spiral pyrolysis apparatus of the described lower end of feed bin 11
The fuel inlet connection of 21 upper ends；
Pass through shaft coupling 22 between the described helical axis of one-level spiral pyrolysis apparatus 21 and the helical axis of deuterostrophies pyrolysis apparatus 23
Connection, the outside cylinder of one-level spiral pyrolysis apparatus 21 dock with the outside cylinder of deuterostrophies pyrolysis apparatus 23, described two level spiral shell
The thermal decomposition product outlet of rotation pyrolysis apparatus 23 connects with fluidized-bed gasifier 31；Spiral pyrolysis system 2 is obliquely installed, one-level spiral heat
The fuel inlet one end for solving device 21 is less than the thermal decomposition product exit end of deuterostrophies pyrolysis apparatus 23, on deuterostrophies pyrolysis apparatus 23
Portion is provided with steam entry 23-1；
The top of described fluidized-bed gasifier 31 connects with cyclone separator 41, bottom and the air inlet system of fluidized-bed gasifier 31
The connection of system 32, described one end of scum pipe 33 connects with the bottom of fluidized-bed gasifier 31；
The described bottom of cyclone separator 41 is correspondingly communicated with an one-level feed back pipe 42, under all described one-level feed back pipes 42
Portion connects with the top of spiral material returning device 43, and the described bottom of spiral material returning device 43 connects with the top of two level feed back pipe 44, described
Two level feed back pipe 44 is arranged on one-level spiral pyrolysis apparatus 21 and the intersection of deuterostrophies pyrolysis apparatus 22, and the bottom of two level feed back pipe 44
With the circulation feed back on the top of deuterostrophies pyrolysis apparatus 22（Heat carrier）Inlet communication.
In present embodiment, one-level spiral pyrolysis apparatus 21 is intercoupled to ensure with airlock 12 by speed-changing gear box 13
The continuous feed of low order fuel.
Speed-changing gear box 13 in present embodiment includes the 13-1 of driving gear one, the 13-2 of driving gear two, driven gear
One 13-3, the 13-4 of driven gear two, power input shaft 13-5 and two power output shaft 13-6；The described 13-1 of driving gear one
Nibbled with the shared power input shaft 13-5 of the 13-2 of driving gear two, the described 13-1 of driving gear one with the 13-3 of driven gear one
Close, the described 13-2 of driving gear two engages with the 13-4 of driven gear two, the 13-3 of driven gear one power installed therein
On output shaft 13-6, the 13-4 of driven gear two is arranged on another power output shaft 13-6.
The helical axis of spiral material returning device 43 in present embodiment is driven by motor 2 45 and rotated.
Embodiment two：As shown in figure 1, present embodiment is that embodiment one is made furtherly
Bright, the angle between the described bottom surface of spiral pyrolysis system 2 and horizontal plane is α, α=5 ° ~ 45 °.Ensure to be pyrolyzed in spiral pyrolysis apparatus
The degree of filling of product so that volatile matter can only be spread out by solid product layer, so as to which sufficiently reaction occur therewith.
Embodiment three：As shown in figure 1, present embodiment is that embodiment one is made furtherly
Bright, if the described length of spiral pyrolysis system 2 is L, the original position of the length of spiral pyrolysis system 2 is located at one-level spiral pyrolysis apparatus
21 fuel inlet one end, the outside cylinder of described one-level spiral pyrolysis apparatus 21 and the outside cylinder of deuterostrophies pyrolysis apparatus 23
Docking location is arranged in the 1/3L regions on the length direction of spiral pyrolysis system 2.Ensure that heat carrier exists with feeding low order fuel
Sufficiently contact and heat transfer occur in deuterostrophies pyrolysis apparatus 23.
Embodiment four：As shown in figure 1, present embodiment is that embodiment three is made furtherly
Bright, described steam entry 23-1 is set close to fuel inlet.
To supplement moisture in gas phase（Include the moisture dried with discharged in pyrolytic process）Deficiency, make burnt under the conditions of this
The gasification of charcoal and the reformation of tar maximize, and reduce the content of thermal decomposition product outlet tar, while reduce the particle diameter and matter of coke
Amount, is advantageous to the complete conversion of later stage tar and coke.
Embodiment five：As shown in figure 1, present embodiment be embodiment one or three is made it is further
Illustrate, the conveying amount of described deuterostrophies pyrolysis apparatus 23 is 2 ~ 5 times of the conveying amount of one-level spiral pyrolysis apparatus 21.
Embodiment six：As shown in Fig. 2 present embodiment is that embodiment one is made furtherly
Bright, the low order fuel low temperature gasification device based on spiral pyrolysis apparatus and fluidized-bed gasifier also includes heat exchanger system 5；
The synthesis gas import of described heat exchanger system 5 is connected by pipeline with the syngas outlet of cyclone separation system 4（Heat exchanger system
Vapor caused by system 5 is each led into deuterostrophies pyrolysis apparatus 23 and fluidized-bed gasifier 31 by a certain percentage）.
Embodiment seven：As shown in figure 3, present embodiment is that embodiment six is made furtherly
Bright, the low order fuel low temperature gasification device based on spiral pyrolysis apparatus and fluidized-bed gasifier also includes dividing wall type heat exchanger
24；Described dividing wall type heat exchanger 24 is arranged on the outside of spiral pyrolysis system 2, dividing wall type heat exchanger 24 both ends respectively with whirlwind
The syngas outlet of piece-rate system 4 and the synthesis gas inlet communication of heat-exchange system 5.
Residence time of the low order fuel in spiral pyrolysis system 2 is controlled by its inclination angle and rotating speed, and temperature is then carried by heat
The amount of body controls, and both of the above make it that the pyrolytic process of low order fuel is controllable, and the component of thermal decomposition product is consistent, be easy to later stage gas
The setting of change condition is to ensure the complete conversion of tar and coke.
Coke after pyrolysis and the pyrolysis gas containing a small amount of tar are directly entered fluidized-bed gasifier 31 and gasified, and gasification is situated between
Matter is oxygen-containing gas and vapor, passes through the temperature for adjusting the share of oxygen to control in fluidized-bed gasifier 31.Due to coke
Not through supercooling, the negative effect of cold quenching effect is avoided, remains the high response of Jiao in situ；Importantly, coke
In the alkali and alkaline earth metal ions that are largely enriched with can great catalytic coke gasification, both common guarantee coke
Low temperature gasification activity.Caused gas main component is H in fluidized-bed gasifier 312、CO、CO2And CH4。
800 DEG C ~ 1000 DEG C of the recycle stock that fluidized-bed gasifier 31 exports（Heat carrier）Separated through cyclone separation system 4
Enter afterwards in spiral pyrolysis system 2, then it is heated by being mixed with low order fuel.
The low temperature gasification device of the present invention, wherein, heat-exchange system 5 is provided with synthesis gas downstream, the heat-exchange system 5 produces
Raw vapor is each led into deuterostrophies pyrolysis apparatus 23 and fluidized-bed gasifier 31 by a certain percentage.Sensible heat in synthesis gas
The vapor needed for heat-exchange system 5 is used to, improves the overall gasification efficiency of heat-exchange system 5.
The low temperature gasification device of the present invention, is additionally provided with dividing wall type heat exchanger 24 outside spiral pyrolysis system 2, described
The both ends of dividing wall type heat exchanger 24 are respectively equipped with the import of one-level synthesis gas and two level syngas outlet, and the one of cyclone separation system 4
Level syngas outlet passes through pipeline and the one-level synthesis gas inlet communication of dividing wall type heat exchanger 24, the two level of dividing wall type heat exchanger 24
Syngas outlet and the two level synthesis gas inlet communication of heat-exchange system 5.Sensible heat in synthesis gas is respectively applied for pyrolytic reaction
Vapor needed for process heat supply and generation heat-exchange system 5, the cascade utilization of energy is realized, further increases heat exchange system
The overall gasification efficiency of system 5.
The present invention the course of work be：Airlock 12 is intercoupled with one-level spiral pyrolysis apparatus 21 by speed-changing gear box 13
Low order fuel is added continuously in spiral pyrolysis system 2.Low order fuel passes through the circulation feed back with 800 DEG C ~ 1000 DEG C（Heat carries
Body）Mixing carries out heating and dries and be pyrolyzed, and includes the gasification and reformation of part high response thermal decomposition product.Needed for gasification and reformation
Vapor a part from low order fuel dryer and pyrolysis caused by moisture, another part derive from by spiral pyrolysis system
The moisture of steam entry 23-1 supplements on system 2, low order fuel or coke pass through the inside spin axle of spiral pyrolysis system 2（Auger）'s
Rotational conveyance enters in fluidized-bed gasifier 31, and volatile matter is then by diffusing into fluidized-bed gasifier 31.Thermal decomposition product（It is surplus
Remaining tar and coke）Occur to reform and gasify inside fluidized-bed gasifier 31, controlled by adjusting the share of oxygen-containing gas
Temperature in fluidized-bed gasifier 31.The heat carrier and synthesis gas that fluidized-bed gasifier 31 exports are separated by cyclone separator 4,
Heat carrier enters spiral pyrolysis system 2, and synthesis gas then enters other processing equipments in downstream.
Fuel inlet one end of spiral pyrolysis system 2 is less than thermal decomposition product exit end, adds in spiral pyrolysis system 2
The degree of filling of coke（The big I of degree of filling is adjusted by changing the angle between the bottom surface of spiral pyrolysis system 2 and horizontal plane）, make
Obtaining volatile matter must be by the laggard fluidized bed gasifier 31 of coke beds, being advantageous to catalysis of the coke to tar in volatile matter and splitting
Solution；Simultaneously as no carrier gas is passed through, volatile matter must add volatile matter in Jiao by diffusing into fluidized-bed gasifier 31
Residence time in charcoal bed, which also promotes the catalytic cracking reaction of volatile matter.In addition, raising and the nothing of coke degree of filling
Being passed through for carrier gas is advantageous to relapsing for the alkali and alkaline earth metal ions that pyrolysis discharges, it is suppressed that alkali gold in coke in pyrolytic process
A large amount of volatilizations of category and alkaline-earth metal so that most of alkali and alkaline earth metal ions enrichment is on the coke particles.
The present invention is provided with heat-exchange system 5 in synthesis gas downstream, and vapor caused by described heat-exchange system 5 is by certain ratio
Example is each led into deuterostrophies pyrolysis apparatus 23 and fluidized-bed gasifier 31.The synthesis gas that cyclone separation system 4 is separated exists
Discharged in heat-exchange system 5 after heat release, and normal-temperature water is passed into heat-exchange system 5 and is used to cool to synthesis gas, the water after heating
Steam（400℃~600℃）Utilized by system itself.
Dividing wall type heat exchanger 24 is additionally provided with outside described spiral pyrolysis system 2, described dividing wall type heat exchanger 24 exists
Both ends are respectively equipped with the import of one-level synthesis gas and two level syngas outlet, and the one-level syngas outlet 41-1 of cyclone separator 41 leads to
The one-level synthesis gas inlet communication of pipeline and dividing wall type heat exchanger 24 is crossed, the two level syngas outlet of dividing wall type heat exchanger 24 is with changing
The two level synthesis gas inlet communication of hot systems 5.The one-level synthesis gas that cyclone separation system 4 is separated is successively through wall-type heat exchange
After the heat release of device 24, turn into two level synthesis gas into heat release again in heat-exchange system 5, turn into the discharge of three-level synthesis gas, after heating
Vapor（200℃~400℃）Utilized by system itself.
Claims (7)
- A kind of 1. low order fuel low temperature gasification device based on spiral pyrolysis apparatus and fluidized-bed gasifier, it is characterised in that：Its group Into including aggregate-storing system（1）, spiral pyrolysis system（2）, fluidized gasification system（3）And cyclone separation system（4）；Described storage Material system（1）Including feed bin（11）, airlock（12）, speed-changing gear box（13）With motor one（14）, described spiral, which is pyrolyzed, is System（2）Including one-level spiral pyrolysis apparatus（21）, shaft coupling（22）With deuterostrophies pyrolysis apparatus（23）, described fluidized gasification System（3）Including fluidized-bed gasifier（31）, gas handling system（32）And scum pipe（33）, described cyclone separation system（4）Bag Include spiral material returning device（43）, two level feed back pipe（44）, at least one cyclone separator（41）And at least one one-level feed back pipe （42）；Described airlock（12）It is arranged on feed bin（11）Interior bottom, described motor one（14）Power output shaft and gear Gearbox（13）Power input shaft drive connection, described speed-changing gear box（13）With two power output shafts（13-6）, Speed-changing gear box（13）A wherein power output shaft（13-6）With airlock（12）Drive connection, speed-changing gear box（13）'s Another power output shaft（13-6）With one-level spiral pyrolysis apparatus（21）Helical axis drive connection, described feed bin（11）Lower end Fuel outlet and one-level spiral pyrolysis apparatus（21）The fuel inlet connection of upper end；Described one-level spiral pyrolysis apparatus（21）Helical axis and deuterostrophies pyrolysis apparatus（23）Helical axis between pass through shaft coupling Device（22）Connection, one-level spiral pyrolysis apparatus（21）Outside cylinder and deuterostrophies pyrolysis apparatus（23）Outside cylinder docking, institute The deuterostrophies pyrolysis apparatus stated（23）Thermal decomposition product outlet and fluidized-bed gasifier（31）Connection；Spiral pyrolysis system（2）Incline Tiltedly set, one-level spiral pyrolysis apparatus（21）Fuel inlet one end be less than deuterostrophies pyrolysis apparatus（23）Thermal decomposition product outlet one End, deuterostrophies pyrolysis apparatus（23）Top is provided with steam entry（23-1）；Described fluidized-bed gasifier（31）Top and cyclone separator（41）Connection, fluidized-bed gasifier（31）Bottom with Gas handling system（32）Connection, described scum pipe（33）One end and fluidized-bed gasifier（31）Bottom connection；Described cyclone separator（41）Bottom is correspondingly communicated with an one-level feed back pipe（42）, all described one-level feed back pipes （42）Bottom and spiral material returning device（43）Top connects, described spiral material returning device（43）Bottom and two level feed back pipe（44）Top Connection, described two level feed back pipe（44）It is arranged on one-level spiral pyrolysis apparatus（21）With deuterostrophies pyrolysis apparatus（22）Intersection, And two level feed back pipe（44）Bottom and deuterostrophies pyrolysis apparatus（22）The circulation feed back inlet communication on top.
- 2. the low order fuel low temperature gasification device according to claim 1 based on spiral pyrolysis apparatus and fluidized-bed gasifier, It is characterized in that：Described spiral pyrolysis system（2）Angle between bottom surface and horizontal plane is α, α=5 ° ~ 45 °.
- 3. according to the claim 1 low order fuel according to claim 1 based on spiral pyrolysis apparatus and fluidized-bed gasifier Low temperature gasification device, it is characterised in that：Described spiral pyrolysis system（2）Angle between bottom surface and horizontal plane is α, α=5 ° ~ 45°.The described low order fuel low temperature gasification device based on spiral pyrolysis apparatus and fluidized-bed gasifier, it is characterised in that：If institute The spiral pyrolysis system stated（2）Length is L, spiral pyrolysis system（2）The original position of length is located at one-level spiral pyrolysis apparatus （21）Fuel inlet one end, described one-level spiral pyrolysis apparatus（21）Outside cylinder and deuterostrophies pyrolysis apparatus（23）It is outer Portion's cylinder docking location is arranged on spiral pyrolysis system（2）In 1/3L regions on length direction.
- 4. the low order fuel low temperature gasification device according to claim 3 based on spiral pyrolysis apparatus and fluidized-bed gasifier, It is characterized in that：Described steam entry（23-1）Set close to fuel inlet.
- 5. being filled based on the low order fuel low temperature gasification of spiral pyrolysis apparatus and fluidized-bed gasifier according to claim 1 or 3 Put, it is characterised in that：Described deuterostrophies pyrolysis apparatus（23）Conveying amount be one-level spiral pyrolysis apparatus（21）The 2 ~ 5 of conveying amount Times.
- 6. the low order fuel low temperature gasification device according to claim 1 based on spiral pyrolysis apparatus and fluidized-bed gasifier, It is characterized in that：The described low order fuel low temperature gasification device based on spiral pyrolysis apparatus and fluidized-bed gasifier also includes heat exchange Device system（5）；Described heat exchanger system（5）Synthesis gas import pass through pipeline and cyclone separation system（4）Synthesis gas go out Mouth connection.
- 7. the low order fuel low temperature gasification device according to claim 6 based on spiral pyrolysis apparatus and fluidized-bed gasifier, It is characterized in that：The described low order fuel low temperature gasification device based on spiral pyrolysis apparatus and fluidized-bed gasifier also includes partition Formula heat exchanger（24）；Described dividing wall type heat exchanger（24）It is arranged on spiral pyrolysis system（2）Outside, dividing wall type heat exchanger（24） Both ends respectively with cyclone separation system（4）Syngas outlet and heat-exchange system（5）Synthesis gas inlet communication.
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| CN108151024A (en) * | 2017-12-22 | 2018-06-12 | 广东天源环境科技有限公司 | A kind of solid waste substance treating method and processing system |
| CN115405918A (en) * | 2022-08-11 | 2022-11-29 | 湖北鑫星节能炉具有限公司 | Biomass particle combustion furnace with bottom ventilation structure |
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| CN103045307A (en) * | 2012-12-21 | 2013-04-17 | 中国科学院过程工程研究所 | Pyrolysis and gasification method and device for preparing tar-free hydrogen-rich gas |
| CN105602623A (en) * | 2015-12-16 | 2016-05-25 | 上海理工大学 | Two-stage down-suction biomass gasifier |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN103045307A (en) * | 2012-12-21 | 2013-04-17 | 中国科学院过程工程研究所 | Pyrolysis and gasification method and device for preparing tar-free hydrogen-rich gas |
| CN105602623A (en) * | 2015-12-16 | 2016-05-25 | 上海理工大学 | Two-stage down-suction biomass gasifier |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN108151024A (en) * | 2017-12-22 | 2018-06-12 | 广东天源环境科技有限公司 | A kind of solid waste substance treating method and processing system |
| CN115405918A (en) * | 2022-08-11 | 2022-11-29 | 湖北鑫星节能炉具有限公司 | Biomass particle combustion furnace with bottom ventilation structure |
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