CN110484284A - A kind of flammable solid pyrolysis of waste device and method for pyrolysis - Google Patents
A kind of flammable solid pyrolysis of waste device and method for pyrolysis Download PDFInfo
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- CN110484284A CN110484284A CN201910726577.3A CN201910726577A CN110484284A CN 110484284 A CN110484284 A CN 110484284A CN 201910726577 A CN201910726577 A CN 201910726577A CN 110484284 A CN110484284 A CN 110484284A
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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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- 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
- 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
- C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
- C10B57/00—Other carbonising or coking processes; Features of destructive distillation processes in general
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Abstract
The present invention discloses a kind of flammable solid pyrolysis of waste device and method for pyrolysis, which includes fluidized bed pyrolysis reactor and fluidized bed combustion reactor, and the two uses heat carrier bed material reciprocating cycle；Flammable solid refuse derived fuel is pyrolyzed in fluidized bed pyrolysis reactor, and the overflow of heat carrier bed material is sent by star material returning device to combustion reactor；Heat carrier bed material is heated again using combustion reactor combustion and pyrolysis oil gas heat release；Heat carrier bed material after heating is again introduced into pyrolysis reactor by material returning apparatus of fluidized bed.Using heat carrier bed material, reciprocating cycle, the heat transmission that burning is generated solve the problems, such as that inside reactor temperature caused by conventional reactor heat transfer is uneven to pyrolytic process between two reactors；It is pyrolyzed returning charge star material returning device, reaches good sealing effect, burn returning charge material returning apparatus of fluidized bed, avoids mechanical moving element high oxidation and deformation, while can control solid circulation flux.
Description
Technical field
The present invention relates to a kind of flammable solid pyrolysis of waste device and method for pyrolysis, belong to the heat of flammable solid waste
Handle reutilization technology.
Background technique
Considerable solid waste, including agriculture and forestry organic waste material, urban life can be generated in the annual production in China, life
Rubbish, municipal sludge etc., the processing of these solid waste and efficiently utilization, have great significance.
Solid waste processing is long-standing, because city size is small when early stage, small-scale solid waste is just
It buries or stacks nearby, with the development of society, the yield of solid waste is more and more, environmental requirement also becomes more tight
Lattice, solid waste treating technology continue to develop, and obtain significant achievement, mesh in minimizing, recycling and innoxious everyway
Preceding more representational processing technique has: sanitary landfill method, high temperature pyrolytic cracking (HTP), incineration method, composting method, producing methane method and fluidized bed
Combustible gas method processed.Pyrolytic technique in numerous options, due to its production technology be relatively easy to operation, industrialization amplification difficulty compared with
Gas that is low, being pyrolyzed generation simultaneously and solid energy product energy density are higher and easy to use and receive extensive attention and answer
With.
But the generation of solid waste has certain region and seasonality, and the wavelet of solid waste
Dynamic range is big, and causing the pyrolysis of flammable solid waste in practical application in industry to control, each of product forms simultaneously by certain difficulty
Component ratio variation is also more apparent.Dual fluidized bed system can preferably solve the problems, such as appeal, still, double-fluidized-bed for being pyrolyzed
When burning, the high temperature circulation Material control between two furnaces is key, and the prior art is defeated using pneumatic conveying or high temperature flood dragon machinery
A large amount of high temperature circulation material circulating between two furnaces will be realized, prevent again by methods, the system complex, poor reliability such as sending
It is only pyrolyzed oil gas and flue gas is ganged up between two furnaces, the prior art is difficult to solve.
Summary of the invention
Goal of the invention: existing solid waste pyrolytic technique there are aiming at the problem that, the present invention provides a kind of flammable solid
Body pyrolysis of waste device, and a kind of method for carrying out solid waste pyrolysis using the device is provided, the device and method is suitable
For various solid wastes such as agriculture and forestry organic waste material, domestic waste and municipal sludges.
Technical solution: a kind of flammable solid pyrolysis of waste device of the present invention, the pyrolysis installation are interactive double
Fluidized bed, including fluidized bed pyrolysis reactor and fluidized bed combustion reactor, the two use heat carrier bed material reciprocating cycle,
In, fluidized bed combustion reactor is connected to, by what is absorbed heat in combustion process by material returning apparatus of fluidized bed with fluidized bed pyrolysis reactor
Heat carrier bed material is sent into fluidized bed pyrolysis reactor, and fluidized bed pyrolysis reactor is reacted by star material returning device with fluidized bed combustion
Heat carrier bed material after heat release is sent into fluidized bed combustion reactor by device connection；The connection of fluidized bed pyrolysis reactor upper outlet
Pyrolysis reactor cyclone separator separates solid product char and pyrolysis oil gas, out the pyrolysis oil of pyrolysis reactor cyclone separator
Gas is connected to fluidized bed pyrolysis reactor and fluidized bed combustion reactor respectively by twice pipeline.
Wherein, the reaction temperature of fluidized bed pyrolysis reactor is 450~500 DEG C, the reaction temperature of fluidized bed combustion reactor
Degree is 800~900 DEG C.
The fluidized wind of fluidized bed combustion reactor is hot-air.Specifically, fluidized bed combustion reactor and air preheat
Device, air blower are sequentially connected, and air first passes through air preheater heating after being blasted by air blower, are then allocated as two-way, are sent all the way
Fluidized bed combustion reactor is as fluidized wind, and another way is as Secondary Air, the dilute-phase zone from fluidized bed combustion reactor top
It is sent into.
Preferably, fluidized bed combustion reactor upper outlet connects combustion reactor cyclone separator, combustion reactor rotation
The solid outlet of wind separator is connected by the feed inlet of returning charge down-comer and material returning apparatus of fluidized bed, the discharging of material returning apparatus of fluidized bed
Mouth is connected via feed back inclined tube with fluidized bed pyrolysis reactor.Further, the exhanst gas outlet of combustion reactor cyclone separator
It is sequentially connected waste heat boiler, air preheater, denitrification apparatus, deduster, desulfurizing tower, air-introduced machine and chimney.
Flammable solid pyrolysis of waste device may also include surge bunker, and fluidized bed pyrolysis reactor centre exit passes through flash
Inclined tube is sequentially connected surge bunker and star material returning device, and the outlet of star material returning device connects via returning charge inclined tube and fluidized bed combustion reactor
It is logical.
Preferably, the bed material average grain diameter of fluidized bed pyrolysis reactor is 0.42~1.2mm, fluidized bed combustion reactor
Bed material is the mixing bed material of 0.42~1.2mm of average grain diameter and 2~4mm of average grain diameter, wherein average grain diameter for 0.42~
The bed material of 1.2mm recycles between two reactors as thermal cyclic carrier bed material.
Flammable solid pyrolysis of waste device of the invention may also include auxiliary fuel feeder, the auxiliary fuel feeder
It is connect with fluidized bed combustion reactor.When fluidized bed combustion reactor burns deficiency, auxiliary fuel can be added, to guarantee to react
The heat-carrying of heat carrier bed material in device.
Method of the present invention using above-mentioned pyrolysis installation pyrolysis flammable solid waste, includes the following steps:
(1) hot-air is passed through into fluidized bed combustion reactor as fluidized wind, fluidizing and heating keeps fluidized bed combustion anti-
Device is answered to reach running temperature, the heat absorption of heat carrier bed material reaches required temperature, and it is anti-to enter fluidized bed pyrolysis by material returning apparatus of fluidized bed
Device is answered, fluidized bed pyrolysis reactor is gradually warmed up；
(2) flammable solid waste is added in fluidized bed pyrolysis reactor, fluidisation, the heat absorbed by heat carrier bed material
Amount is pyrolyzed, and the heat carrier bed material after heat release is sent by star material returning device to fluidized bed combustion reactor；Meanwhile it being pyrolyzed and producing
Object enters pyrolysis reactor cyclone separator separation solid product char and pyrolysis oil gas, and pyrolysis oil gas is sent into fluidized bed pyrolysis all the way
For reactor as fluidized wind, another way is sent into fluidized bed combustion reactor as fuel；
(3) pyrolysis oil gas burns in fluidized bed combustion reactor heats heat carrier bed material again, and the heat after heating carries
Body bed material is again introduced into fluidized bed pyrolysis reactor by material returning apparatus of fluidized bed, provides heat for pyrolytic reaction, reach substance and
The circulation of energy.
Wherein, fluidized bed combustion reactor starts in device and initial operating stage by adding heat to reach running temperature outside, than
Such as light a fire by fuel oil or pyrolysis is passed through after device stable operation generates enough pyrolysis oil gas by electric heating
The burning of oil gas reaches running temperature；Fluidized bed pyrolysis reactor device start and initial operating stage by outside plus inert gas into
Row fluidisation after device stable operation generates enough pyrolysis oil gas, is fluidized by being pyrolyzed oil gas.
In above-mentioned steps (1), the combustion product gases that the heat carrier bed material after heat absorption is generated with fluidized bed combustion reactor are first sent
Enter combustion reactor cyclone separator gas solid separation, the heat carrier bed material after the heat absorption isolated is sent into material returning apparatus of fluidized bed, combustion
Burn flue gas be first sent into waste heat boiler carry out heat utilization, enter back into the fluidized wind of air preheater preheated fluidification bed combustion reactor with
And Secondary Air, subsequent flue gas are successively discharged after denitration process, active carbon injection, dedusting, desulfurization process.
The utility model has the advantages that compared with the prior art, the advantages of the present invention are as follows:
(1) heat carrier bed material reciprocating cycle is used.The present invention uses double-fluidized-bed reactor assembly, two fluidized bed difference
Be pyrolyzed oil gas combustion reactor as flammable solid pyrolysis of waste reactor and solid waste, it is double-fluidized-bed between using heat
Carrier bed material reciprocating cycle；The fuel of fluidized bed combustion reactor is mainly fluidized bed pyrolysis reactor pyrolysis oil gas, fluidized bed
Combustion reactor transfers heat to heat carrier bed material while combustion and pyrolysis oil gas；High-temperature heat carrier bed material enters fluidisation
Bed pyrolysis reactor transfers heat to solid waste, whole thermal energy needed for providing its pyrolysis, the system knot thus constructed
Structure is simple, can adapt to changeable solid waste material composition, is easy to large-scale continuous production；
(2) direct combustion and pyrolysis oil gas.The gaseous products of pyrolysis are directly sent into combustion furnace burning, with the pyrolysis of high heating value
Incondensable gas is only sent by main fuel of the oil gas as combustion furnace by the pyrolysis oil being pyrolyzed in oil gas condensation with existing
Combustion furnace burning is different, avoids energy consumption condensation pyrolysis oil but the problem not high using economic value；Solid substantially may be implemented
Energy needed for waste pyrolyzing oil gas burning energy-balancing pyrolysis processing solid waste, has solid waste huge
Minimizing, innoxious effect；
(3) using the returning charge form of " material returning apparatus of fluidized bed+star material returning device " coupling: due to the reaction temperature of pyrolysis reactor
Lower (450~500 DEG C) are spent, arrange that buffer bin+star is returned when recycle stock has pyrolysis reactor to enter combustion reactor
Glassware is as material-returning device；And still when material enters pyrolysis reactor by (800~900 DEG C) of the higher combustion reactor of temperature
Using traditional standpipe+material returning apparatus of fluidized bed returning charge form；Both to avoid mechanical moving element height can occur for this design
Oxidation and deformation, and can use star material returning device and guarantee excellent sealing, solid circulation flux is accurately controlled, can be realized a large amount of
Recycle stock recycling between two furnaces, while it can be effectively prevent pyrolysis oil gas and flue gas ganging up between two furnaces, it can
More easily to realize that the operation for reducing device to the pressure balanced control of device and adjusting controls difficulty；
(4) auxiliary fuel feeder is set.The present apparatus can be realized flammable solid waste self-energy balance between supply and demand, no
Need the addition of auxiliary fuel；But it is directed to the variation of solid waste calorific value and moisture content, setting auxiliary combustion in systems
Expect screw-feeder, when into solid waste water content of matter is very high, calorific value is very low, suitable biomass/coal is sent into fluidisation
Bed combustion reactor burning is made system run all right, is increased security of system with thermal energy needed for guaranteeing system；
(5) effectively control secondary pollution discharge.Due to the running temperature of fluidized bed pyrolysis reactor is low and bed in temperature
Uniformly, the synthesis reaction temperature of dioxin is not reached, heavy metal accumulation is more stable in solid residue, therefore without dioxin
It generates and heavy metals emission problem；The running temperature of fluidized bed combustion reactor is high, gas residence time is long, disturbance in reactor
The dioxin-like chemical generated in combustion can be decomposed completely strongly；Preferably, kaolinite is added in combustion reactor
The additives such as soil and activated bauxite can effectively adsorb the heavy metal released from pyrolyzing sludge carbon residue；Preferably, it is firing
The sour gas such as sulphur, chlorine, fluorine can effectively be removed by burning addition lime stone in reactor, control ignition temperature and air classification supply can
Reduce NO_x formation；Secondary pollution discharge can be effectively controlled by the above measure, it is down to most the pollution of environment
It is low.
Detailed description of the invention
Fig. 1 is the structural schematic diagram of flammable solid pyrolysis of waste device of the invention.
Specific embodiment
Technical solution of the present invention is described further with reference to the accompanying drawing.
A kind of flammable solid pyrolysis of waste device of the invention, such as Fig. 1, the device is double-fluidized-bed using reciprocating cycle,
Including fluidized bed combustion reactor and fluidized bed pyrolysis reactor.
2 upper outlet of fluidized bed pyrolysis reactor is connected with pyrolysis reactor cyclone separator 3, revolves through pyrolysis reactor
3 solid carbon of wind separator is directly collected, and gas is connected with circulating fan 4；It is anti-that pyrolysis is provided in the middle part of fluidized bed pyrolysis reactor
It answers device flash inclined tube 5 to be connected with pyrolysis reactor surge bunker 6, is re-fed into pyrolysis reactor star material returning device 7；Star material returning device
7 are connected by combustion reactor returning charge inclined tube 9 with fluidized bed combustion reactor 11；The motor of pyrolysis reactor star material returning device 7
For speed regulating motor 8, returning charge amount is controlled by control motor speed.
Fluidized bed pyrolysis reactor 2 can be bubbling fluidized bed, using low wide and up narrow pattern, pyrolysis reactor cyclone separator
3 pyrolysis oil gas accesses circulating fan 4, is then allocated as two-way, the fluidized wind as fluidized bed pyrolysis reactor 2, another all the way
Road is sent into fluidized bed combustion reactor 11 and burns, and is added from the dilute-phase zone on 11 top of fluidized bed combustion reactor, burns in furnace
While heat release, increase disturbance in furnace.It is useless for being sent into flammable solid that fluidized bed pyrolysis reactor 2 is equipped with screw-feeder 1
Gurry raw material.
Fluidized bed combustion reactor 11 can be wide particle diameter recirculating fluidized bed.11 upper outlet of fluidized bed combustion reactor and combustion
Burn reactor cyclone 12 be connected, and after through combustion reactor cyclone separator returning charge down-comer 13 and combustion reactor
High temperature fluidized bed 14 top side of material returning device is connected；Material returning apparatus of fluidized bed 14 passes through pyrolysis reactor feed back pipe 15 and fluidized bed
Pyrolysis reactor 2 is connected；The exhaust of combustion reactor cyclone separator 12 accesses waste heat boiler 16, then accesses air preheater
17, then pass sequentially through denitrification apparatus 18, active carbon injection, bag filter 19, desulfurizing tower 20 are finally led to through air-introduced machine 21
Chimney 22 is discharged.The fluidized wind of fluidized bed combustion reactor 11 is hot-air, and air first passes through air after being blasted by air blower 23
Preheater 17 heats, and is then allocated as two-way, all the way the fluidized wind as fluidized bed combustion reactor 11, and another way is sent into fluidized bed
Combustion reactor 11 is used as Secondary Air.14 upper parallel of material returning apparatus of fluidized bed is equipped with feeding warehouse and discharging bin, and material returning device lower part is simultaneously
Column are equipped with discharging bin air compartment, feeding warehouse air compartment.
There is bed material in fluidized bed pyrolysis reactor 2 and fluidized bed combustion reactor 11, the two is handed over using heat carrier bed material
Mutually circulation, wherein fluidized bed combustion reactor 11 passes through the heat carrier bed material that material returning apparatus of fluidized bed 14 will absorb heat in combustion process
It is sent into fluidized bed pyrolysis reactor 2, fluidized bed pyrolysis reactor 2 is sent the heat carrier bed material after heat release by star material returning device 7
Fluidized bed combustion reactor 11.
The settable auxiliary fuel screw-feeder 10 of fluidized bed combustion reactor 11, when such as solid waste ingredient and water
Divide variation huge, so that fluidized bed combustion reactor 11 burns when insufficient or overtemperature, can pass through and the auxiliary such as biomass, coal is added
Fuel, to guarantee the heat-carrying of the heat carrier bed material in reactor.
Flammable solid method for pyrolysis of waste based on above-mentioned apparatus, includes the following steps:
(1) air blasted by air blower 23 heats laggard fluidized bed combustion reactor 11 by air preheater 17
Fluidisation, heats, fluidized bed combustion reactor 11 is made to reach running temperature, wherein device starting and initial operating stage pass through electric heating
Or fuel oil igniting heating, pass through combustion and pyrolysis oil-gas heating after device stable operation generates enough pyrolysis oil gas；Stream
Heat carrier bed material heat absorption in fluidized bed combustion reactor 11 reaches required temperature, the heat carrier bed material (800~900 DEG C) after heat absorption
Fluid bed heat is entered by material returning apparatus of fluidized bed 14 from upper outlet by passing through after 12 gas solid separation of combustion reactor cyclone separator
Reactor 2 is solved, heat is provided for pyrolytic reaction, fluidized bed pyrolysis reactor 2 is made to be gradually heated to 450~500 DEG C；Meanwhile it flowing
The combustion product gases that fluidized bed combustion reactor 11 generates are sent into waste heat boiler after 12 gas solid separation of combustion reactor cyclone separator
16 are subject to heat utilization, enter back into fluidized wind and Secondary Air of the air preheater 17 for preheated fluidification bed combustion reactor 11,
It subsequently enters denitrification apparatus 18 and carries out denitration process, then carry out active carbon injection, and be sent into after 19 dedusting of bag filter
Desulfurizer 20 finally leads to chimney 22 by air-introduced machine 21 and is discharged.
(2) flammable solid waste is added in fluidized bed pyrolysis reactor 2 by screw feeder 1, (device opens fluidisation
Dynamic and initial operating stage is fluidized by inert gas, is flowed when device stable operation pyrolysis oil gas is enough by being pyrolyzed oil gas
Change), it is pyrolyzed by the heat of the heat carrier bed material after heat absorption, the heat carrier bed material (450~500 DEG C) after heat release passes through
Overflow inclined tube 5 enters pyrolysis reactor surge bunker 6, is re-fed into the star material returning device 7 of medium temperature formula, is subsequently sent to fluidized bed combustion
In reactor 11；Meanwhile the flue gas that pyrolytic process generates enters the separation solid product char of pyrolysis reactor cyclone separator 3 and heat
Oil gas is solved, pyrolysis oil gas is sent into fluidized bed pyrolysis reactor 2 as fluidized wind all the way, and another way is sent into fluidized bed combustion reactor
11 are used as fuel；
(3) pyrolysis oil gas burns in fluidized bed combustion reactor 11, heat carrier bed material is again heated to 800~900
DEG C, the heat carrier bed material after heating passes sequentially through combustion reactor cyclone separator from 11 upper outlet of fluidized bed combustion reactor
12 and material returning apparatus of fluidized bed 14 be again introduced into fluidized bed pyrolysis reactor 2, provide heat for pyrolytic reaction, so reach substance and
The circulation of energy.
According to the combustion characteristics of the pyrolysis characteristics of flammable solid waste and pyrolysis oil gas and auxiliary fuel, pass through adjusting
Reactor fluidized wind tolerance, material returning apparatus of fluidized bed 14 pass in and out 8 revolving speed of speed regulating motor of feed bin air compartment wind speed and star material returning device,
The material of adjustment fluidized bed pyrolysis reactor 2 and fluidized state and two material returning devices in fluidized bed combustion reactor 11 follows
Circular rector enables the system to stable operation and obtains solid from fluidized bed pyrolysis reactor cyclone separator in an optimal manner
Charcoal；Fluidized bed pyrolysis reactor 2 and the control of 11 residence time of fluidized bed combustion reactor are 2~3s, and the two is had using identical
The bed material of the larger characteristic of specific heat as thermal cyclic carrier, unlike, fluidized bed pyrolysis reactor 2 is (flat using small particle bed material
0.42~1.2mm of equal partial size), and combustion reactor 11 is using big small particle mixing (0.42~1.2mm of average grain diameter and average grain
2~4mm of diameter mixing) wide particle diameter bed material, while 11 fluidising air velocity of fluidized bed combustion reactor be higher than fluidized bed pyrolysis reactor
2, pyrolysis fluidising air velocity (0.2~1.5m/s), which reaches, makes small particle bed material be in bubbling fluidization state, and fluidized bed combustion is reacted
11 fluidising air velocity of device (1~5m/s) then needs, and so that small particle bed material reaches, pneumatic conveying state, big partial size bed material reaches base simultaneously
This fluidized state, to realize small size particle bed material as thermal cyclic carrier and recycle between two reactors and the effect of heat-carrying
Fruit.
Claims (10)
1. a kind of flammable solid pyrolysis of waste device, which is characterized in that including fluidized bed pyrolysis reactor and fluidized bed combustion
Reactor, the two use heat carrier bed material reciprocating cycle, wherein fluidized bed combustion reactor passes through material returning apparatus of fluidized bed and fluidisation
The heat carrier bed material absorbed heat in combustion process is sent into fluidized bed pyrolysis reactor, fluidized bed pyrolysis by the connection of bed pyrolysis reactor
Reactor is connected to fluidized bed combustion reactor by star material returning device, the heat carrier bed material after heat release is sent into fluidized bed combustion
Reactor；Fluidized bed pyrolysis reactor upper outlet connection pyrolysis reactor cyclone separator, separation solid product char and
Be pyrolyzed oil gas, out the pyrolysis oil gas of pyrolysis reactor cyclone separator by twice pipeline respectively with fluidized bed pyrolysis reactor,
The connection of fluidized bed combustion reactor.
2. flammable solid pyrolysis of waste device according to claim 1, which is characterized in that the fluidized bed pyrolysis reaction
The reaction temperature of device is 450~500 DEG C, and the reaction temperature of fluidized bed combustion reactor is 800~900 DEG C.
3. flammable solid pyrolysis of waste device according to claim 1, which is characterized in that the fluidized bed combustion reaction
Device is sequentially connected with air preheater, air blower, and air first passes through air preheater heating after being blasted by air blower, is then allocated as
Two-way, all the way be sent into fluidized bed combustion reactor as fluidized wind, another way as Secondary Air, from fluidized bed combustion reactor
The dilute-phase zone in portion is sent into.
4. flammable solid pyrolysis of waste device according to claim 1, which is characterized in that the fluidized bed combustion reaction
Device upper outlet connects combustion reactor cyclone separator, and the solid outlet of combustion reactor cyclone separator is declined by returning charge
Pipe is connect with the feed inlet of material returning apparatus of fluidized bed, and the discharge port of material returning apparatus of fluidized bed is reacted via feed back inclined tube with fluidized bed pyrolysis
Device is connected.
5. flammable solid pyrolysis of waste device according to claim 4, which is characterized in that the combustion reactor whirlwind
The exhanst gas outlet of separator is sequentially connected waste heat boiler, air preheater, denitrification apparatus, deduster, desulfurizing tower, air-introduced machine and cigarette
Chimney.
6. flammable solid pyrolysis of waste device according to claim 1, which is characterized in that the fluidized bed pyrolysis reaction
The bed material average grain diameter of device is 0.42~1.2mm, and the bed material of fluidized bed combustion reactor is 0.42~1.2mm of average grain diameter and puts down
The mixing bed material of 2~4mm of equal partial size, wherein the bed material that average grain diameter is 0.42~1.2mm is anti-at two as heat carrier bed material
It answers and is recycled between device.
7. flammable solid pyrolysis of waste device according to claim 1, which is characterized in that further include auxiliary fuel charging
Device, the auxiliary fuel feeder are connect with fluidized bed combustion reactor.
8. a kind of method using pyrolysis installation pyrolysis flammable solid waste described in claim 1, which is characterized in that including
Following steps:
(1) hot-air is passed through into fluidized bed combustion reactor as fluidized wind, fluidizing and heating makes fluidized bed combustion reactor
Reaching running temperature, the heat absorption of heat carrier bed material reaches required temperature, enters fluidized bed pyrolysis reactor by material returning apparatus of fluidized bed,
It is gradually warmed up fluidized bed pyrolysis reactor；
(2) by flammable solid waste be added fluidized bed pyrolysis reactor in, fluidisation, by heat carrier bed material absorb heat into
Row pyrolysis, the heat carrier bed material after heat release are sent by star material returning device to fluidized bed combustion reactor；Meanwhile thermal decomposition product into
Enter pyrolysis reactor cyclone separator and be separated into solid product char and pyrolysis oil gas, it is anti-that pyrolysis oil gas is sent into fluidized bed pyrolysis all the way
Answer device as fluidized wind, another way is sent into fluidized bed combustion reactor as fuel；
(3) pyrolysis oil gas burns in fluidized bed combustion reactor heats heat carrier bed material again, the heat carrier bed after heating
Material is again introduced into fluidized bed pyrolysis reactor by material returning apparatus of fluidized bed, provides heat for pyrolytic reaction, reaches matter and energy
Circulation.
9. the method for pyrolysis flammable solid waste according to claim 8, which is characterized in that the fluidized bed combustion is anti-
Answer device in device starting and initial operating stage by adding heat to reach running temperature outside, when device stable operation generates enough pyrolysis
After oil gas, the burning by being pyrolyzed oil gas reaches running temperature；The fluidized bed pyrolysis reactor starts in device and runs just
Phase is fluidized by additional inert gas, after device stable operation generates enough pyrolysis oil gas, is carried out by pyrolysis oil gas
Fluidisation.
10. the method for pyrolysis flammable solid waste according to claim 8, which is characterized in that in step (1), heat absorption
The combustion product gases that heat carrier bed material and fluidized bed combustion reactor afterwards generates first are sent into combustion reactor cyclone separator gas-solid
Separation, the heat carrier bed material after the heat absorption isolated are sent into material returning apparatus of fluidized bed, and combustion product gases are first sent into waste heat boiler and carry out heat
It utilizes, enters back into the fluidized wind and Secondary Air of air preheater preheated fluidification bed combustion reactor, subsequent flue gas is successively through de-
It is discharged after nitre processing, active carbon injection, dedusting, desulfurization process.
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111268881A (en) * | 2020-03-11 | 2020-06-12 | 东南大学 | Sludge reduction system charcoal system |
| CN113324244A (en) * | 2020-06-03 | 2021-08-31 | 东南大学 | System and process for treating solid fuel through auxiliary combustion of partial gasification coupling oxygen carrier |
Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP1966346A1 (en) * | 2005-09-08 | 2008-09-10 | Millennium Synfuels, LLC. | Hybrid energy system |
| CN101307244A (en) * | 2008-06-27 | 2008-11-19 | 东南大学 | Oil-making method of double-bed interactive and circling type for pyrolyzing sludge |
| CN102901102A (en) * | 2012-08-08 | 2013-01-30 | 东南大学 | Comprehensive utilization method of bio-oil prepared by city household garbage and heat energy |
| CN109456800A (en) * | 2018-12-12 | 2019-03-12 | 浙江工业大学 | A kind of house refuse gradient utilization system and method based on double bed pyrolysis |
| CN109943353A (en) * | 2019-03-12 | 2019-06-28 | 华中科技大学 | A kind of bio oil preparation system and method rich in levoglucosan |
| CN110079350A (en) * | 2019-05-30 | 2019-08-02 | 青岛科技大学 | It is a kind of using more warehouse fluidized-bed reactors as the biomass through pyrolysis production technology of core |
-
2019
- 2019-08-07 CN CN201910726577.3A patent/CN110484284A/en active Pending
Patent Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP1966346A1 (en) * | 2005-09-08 | 2008-09-10 | Millennium Synfuels, LLC. | Hybrid energy system |
| CN101307244A (en) * | 2008-06-27 | 2008-11-19 | 东南大学 | Oil-making method of double-bed interactive and circling type for pyrolyzing sludge |
| CN102901102A (en) * | 2012-08-08 | 2013-01-30 | 东南大学 | Comprehensive utilization method of bio-oil prepared by city household garbage and heat energy |
| CN109456800A (en) * | 2018-12-12 | 2019-03-12 | 浙江工业大学 | A kind of house refuse gradient utilization system and method based on double bed pyrolysis |
| CN109943353A (en) * | 2019-03-12 | 2019-06-28 | 华中科技大学 | A kind of bio oil preparation system and method rich in levoglucosan |
| CN110079350A (en) * | 2019-05-30 | 2019-08-02 | 青岛科技大学 | It is a kind of using more warehouse fluidized-bed reactors as the biomass through pyrolysis production technology of core |
Non-Patent Citations (1)
| Title |
|---|
| 岑可法: "《循环流化床锅炉理论、设计与运行》", 31 May 1998, 中国电力出版社 * |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111268881A (en) * | 2020-03-11 | 2020-06-12 | 东南大学 | Sludge reduction system charcoal system |
| CN113324244A (en) * | 2020-06-03 | 2021-08-31 | 东南大学 | System and process for treating solid fuel through auxiliary combustion of partial gasification coupling oxygen carrier |
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