CN103756696B - Double fluidized bed combustible solid waste pyrolysis oil-gas coproduction device and method - Google Patents
Double fluidized bed combustible solid waste pyrolysis oil-gas coproduction device and method Download PDFInfo
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- CN103756696B CN103756696B CN201410036675.1A CN201410036675A CN103756696B CN 103756696 B CN103756696 B CN 103756696B CN 201410036675 A CN201410036675 A CN 201410036675A CN 103756696 B CN103756696 B CN 103756696B
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Abstract
The invention discloses a double fluidized bed combustible solid waste pyrolysis oil-gas coproduction device and method. The double fluidized bed combustible solid waste pyrolysis oil-gas coproduction device comprises a pyrolysis reactor and a combustion reactor which are vertically arranged; a pyrolysis reactor bottom air distribution device and a pyrolysis reactor tubular air distribution device are arranged in the pyrolysis reactor; a combustion reactor plate-type air distribution device is arranged in the combustion reactor; a pyrolysis reactor air outlet is connected to a pyrolysis reactor cyclone separator; a combustion reactor air outlet is connected to a combustion reactor cyclone separator. The double fluidized bed combustible solid waste pyrolysis oil-gas coproduction device and method combine the current situations of complex raw material source and ingredients in an urban garbage pyrolysis technology, solve the problems of instability for production supply, large type variation and the like of agricultural and forestry wastes faced by an agricultural and forestry waste pyrolysis technology in the actual industrial application, are convenient to control, stable to operate and have a wide range of regulating operating parameters.
Description
Technical field
The present invention relates to a kind of double-fluidized-bed flammable solid pyrolysis of waste oil gas combination preparing device and method, for comprising the recycling of the flammable solid waste of agriculture and forestry organic waste material and domestic waste, belonging to the thermal treatment reutilization technology of flammable solid waste.
Background technology
China is agricultural big countries, and the agriculture and forestry organic waste material total amount produced in annual agricultural and forestry production is considerable, and the quantity being often only agricultural crop straw and forestry felling industrial wood waste just reaches more than 10 hundred million tons, is about as much as 500,000,000 tons of standard coals.Wherein, as byproduct stalk the most common in agriculture production, along with its national output of volume increase year after year of China's agricultural has broken through 800,000,000 tons, 3.8 hundred million tons of standard coals are roughly equal to.With regard to forestry waste, the Eleventh Five-Year Plan period, the forestry logging residue amount that China produces every year reaches 1.09 hundred million tons.Therefore, the agriculture and forestry organic waste material so big to total amount carries out efficiency utilization, no matter be alleviation for energy problem of China or the enforcement for China's strategy of sustainable development all has great importance and impact.The current Energy conversion reutilization technology relating to agriculture and forestry organic waste material is a lot, pyrolytic technique in numerous option, due to its production technology relative to easy handling, industrialization amplify difficulty lower while the gas that produces of pyrolysis and solid energy product energy density higher and easy to use and paid close attention to widely and apply.But the generation due to agriculture and forestry organic waste material has certain seasonality and region, the realization of agriculture and forestry organic waste material pyrolytic technique is stablized in the process of industrialization operation and there is certain difficulty, the agriculture and forestry organic waste material production and supply amount fluctuation being embodied in pyrolysis production is comparatively large, and the composition formation change of agriculture and forestry organic waste material frequently makes product proportion of composing also there is certain unstable.
On the other hand, along with the rapid growth of China's economy and steadily improving of standard of living, the output of municipal solid wastes increases sharply, and calorific value is also improving constantly.How Appropriate application municipal wastes while that safety processing neatly is carried out to the municipal wastes of quantity sharp increase and be converted into effective energy, attract the attention of more and more investigator, and current by a kind of Assessment of MSW Disposal Technologies pyrolytic technique just extensively noted.Combustion Properties of Municipal Solid Waste can process the difficult thing being unsuitable for burning and landfill, claims flammable gas or liquid simultaneously.But because the composition of municipal wastes is quite complicated, the while of causing the pyrolysis of municipal wastes in practical application in industry to control there is certain difficulty, each moiety ratio change of product is also more obvious.
Summary of the invention
Goal of the invention: unstable and kind changes the problem such as greatly for the agriculture and forestry organic waste material turnout supply faced by agriculture and forestry organic waste material pyrolytic technique is in practical application in industry, in conjunction with the present situation of the raw material sources existed in urban refuse thermal decomposition technology and complicated component, the object of the invention is to provide and a kind of controls convenient, stable and operating parameter setting range extensively, the double-fluidized-bed pyrolysis oil gas combination preparing device that the multiple flammable solid rubbish being applicable to mainly comprise agriculture and forestry organic waste material and municipal wastes alternately utilizes and method.
Technical scheme: for achieving the above object, the technical solution used in the present invention is:
A kind of double-fluidized-bed flammable solid pyrolysis of waste oil gas combination preparing device, comprises the pyrolysis reactor and combustion reactor that vertically arrange;
Air-distributing device and pyrolysis reactor tubular distributor bottom pyrolysis reactor is provided with in described pyrolysis reactor, the sidewall of pyrolysis reactor is from top to bottom provided with pyrolysis reactor flash mouth, pyrolysis reactor opening for feed, pyrolysis reactor two-way material returning device returning charge mouth and pyrolysis reactor unidirectional material returning device returning charge mouth, the bottom of pyrolysis reactor is provided with pyrolysis reactor slag-drip opening, the top of pyrolysis reactor is provided with pyrolysis reactor exhaust outlet; Described pyrolysis reactor tubular distributor position is higher than air-distributing device bottom pyrolysis reactor, pyrolysis reactor gating location is higher than pyrolysis reactor tubular distributor, and pyrolysis reactor two-way material returning device returning charge mouth and pyrolysis reactor unidirectional material returning device returning charge mouth position height to be placed in bottom pyrolysis reactor between air-distributing device and pyrolysis reactor tubular distributor; Raw materials device is connected with pyrolysis reactor opening for feed;
The board-like air-distributing device of combustion reactor is provided with in described combustion reactor, the sidewall of combustion reactor is from top to bottom provided with combustion reactor flash mouth, combustion reactor opening for feed and combustion reactor returning charge mouth, the bottom of combustion reactor is provided with combustion reactor slag-drip opening, the top of combustion reactor is provided with combustion reactor exhaust outlet; Described combustion reactor returning charge mouth position is higher than the board-like air-distributing device of combustion reactor; Auxiliary fuel feeder is connected with combustion reactor opening for feed;
Described pyrolysis reactor exhaust outlet access pyrolysis reactor cyclonic separator, the bottom discharge end of described pyrolysis reactor cyclonic separator is connected with the feed-pipe of two-way material returning device by the first returning charge downtake, and the first returning charge inclined tube of two-way material returning device and the second returning charge inclined tube respectively material returning device returning charge mouth two-way with pyrolysis reactor are connected with combustion reactor returning charge mouth; Described pyrolysis reactor flash mouth is communicated with the first returning charge downtake by the first downward-sloping inclined tube, and the first inclined tube is provided with pyrolysis reactor flash device; The upper exhaust side access first step condenser of described pyrolysis reactor cyclonic separator carries out pyrolysis product recovery;
Described combustion reactor exhaust outlet access combustion reactor cyclonic separator, the bottom discharge end of described combustion reactor cyclonic separator is connected with the feed end of unidirectional material returning device by the second returning charge downtake, and the discharge end of unidirectional material returning device is connected with pyrolysis reactor unidirectional material returning device returning charge mouth; Described combustion reactor flash mouth is communicated with the second returning charge downtake by the second downward-sloping inclined tube, and the second inclined tube is provided with combustion reactor flash device; The upper exhaust side access hot tube heat exchanger of described combustion reactor cyclonic separator carries out energy recovery.
Preferably, the upper exhaust side access first step condenser of described pyrolysis reactor cyclonic separator; The liquid exit of first step condenser accesses the first pyrolysis oil holding tank, the pneumatic outlet access second stage condenser of first step condenser; The liquid exit of second stage condenser accesses the second pyrolysis oil holding tank, the pneumatic outlet access dehydration tower of second stage condenser; Dehydration tower pneumatic outlet is divided into two-way, a road access pyrolysis gas output of products passage, another road access hot tube heat exchanger lower inlet;
End entrance on the upper exhaust side access hot tube heat exchanger of described combustion reactor cyclonic separator; Hot tube heat exchanger upper end outlet and pyrolysis reactor tubular distributor are connected with air-distributing device bottom pyrolysis reactor, and the outlet of hot tube heat exchanger lower end is connected with smoke eliminator, and smoke eliminator pneumatic outlet is connected with sack cleaner.
Preferably, described pyrolysis reactor flash device regulates pyrolysis reactor to work in bubbling fluidization state, turbulent fluidised state or fast fluidization state; Described combustion reactor flash device regulates combustion reactor to work in bubbling fluidization state, turbulent fluidised state or fast fluidization state.
Preferably, the height of described pyrolysis reactor is H, by the bottom of pyrolysis reactor: the height of pyrolysis reactor tubular distributor is 0.2 ~ 0.3H, the height of pyrolysis reactor opening for feed is 0.35 ~ 0.45H, the height of pyrolysis reactor flash mouth is 0.6 ~ 0.8H, the height of pyrolysis reactor two-way material returning device returning charge mouth and pyrolysis reactor unidirectional material returning device returning charge mouth is 0.05 ~ 0.15H, and the height of pyrolysis reactor two-way material returning device returning charge mouth is not less than the height of the unidirectional material returning device of pyrolysis reactor; The diameter of pyrolysis reactor is D; Bottom pyrolysis reactor air-distributing device be osculum under cone shaped distributor, along being placed in bottom pyrolysis reactor, axis is vertical, and the angle of the conical surface and horizontal plane is 60 ° at its end; The angle of the first inclined tube and horizontal plane is 45 °.
Preferably, the height of described combustion reactor is L, L=0.8 ~ 1H, by the bottom of combustion reactor: the height of combustion reactor opening for feed is 0.3 ~ 0.4L, the height of combustion reactor flash mouth is 0.6 ~ 0.8L, and the height of combustion reactor returning charge mouth is 0.15 ~ 0.25L; Combustion reactor be W, W=0.8 ~ 1.2D so far; Be small end bottom combustion reactor under pyramidal structure, the board-like air-distributing device of combustion reactor is arranged on the large end position of pyramidal structure, pyramidal structure and the board-like air-distributing device of combustion reactor form combustion reactor air compartment jointly, and the conical surface of pyramidal structure and the angle of horizontal plane are 60 °; The angle of the second inclined tube and horizontal plane is 45 °.
Preferably, described two-way material returning device comprises rectangular parallelepiped cavity volume, described rectangular parallelepiped cavity volume is divided into three chambers by T-shaped dividing plate, wherein a chamber at rear is feed chamber, two chambers in front are respectively the first returning charge room and the second returning charge room, feed chamber is connected with the first returning charge downtake, and the first returning charge room is connected with the first returning charge inclined tube, and the second returning charge room is connected with the second returning charge inclined tube; In described feed chamber, air distribution plate is set, isolates the feed chamber air compartment of below; Described first returning charge indoor are provided with air distribution plate, isolate the first returning charge room air compartment of below; Described second returning charge indoor are provided with air distribution plate, isolate the second returning charge room air compartment of below;
The width b of described feed chamber
2with the width b of the width/the second returning charge room of the first returning charge room
1equal, the length a of the first returning charge room
1with the length a of the second returning charge room
2equal; The diameter of the first returning charge downtake is d
1, the diameter of the first returning charge inclined tube is d
2, the diameter of the second returning charge inclined tube is d
3, d
2=d
3=0.625d
1; The angle of the first returning charge inclined tube and vertical direction is α, and the angle of the second returning charge inclined tube and vertical direction is that β, α and β are all less than 45 °; The percentage of open area of described air distribution plate is 10 ~ 15%.
Pyrolysis reactor in said apparatus and combustion reactor are respectively arranged with flash structure and gas-solid separating device, achieve the adaptability to multiple working ordeies such as bubbling fluidization state, turbulent fluidised state and fast fluidization states, by the adjustment of operating parameter can one in a big way in change the residence time of mixture in bed and mixed characteristic, make this device can adapt to the fuel of complicated kind.It should be pointed out that the valve should closed when pyrolysis reactor or combustion reactor are in fast fluidization state running status on corresponding overflow spout.
Pyrolysis reactor in said apparatus is provided with tubular distributor and bottom air-distributing device, the degree of mixing that fluidizing agent strengthens the material in pyrolysis reactor is passed into by classification, and make pyrolysis gas product can be taken away pyrolysis reactor rapidly, make whole device have good reaction efficiency.
Matter Transfer between two reactors of said apparatus is controlled by the material returning device (unidirectional material returning device and two-way material returning device) of pneumatic control, and feed flow can regulate according to two reactor actual operating states to improve reaction efficiency; Controllably distributed the solids flux of feeding pyrolysis reactor and combustion reactor thus by two-way material returning device, make whole device to control to send into the amount of combustion reactors burning according to two reactor temperatures thus to realize the accurate object controlling whole device internal temperature.
A kind of double-fluidized-bed flammable solid pyrolysis of waste oil gas co-production, comprises the steps:
(1) in combustion reactor, add auxiliary fuel by auxiliary fuel feeder, auxiliary fuel is by the Air Fluidized that injected by the board-like air-distributing device of combustion reactor and burn, and reaches operating requirement in order to promote temperature in combustion reactor; High temperature inert Solid Bed material enters pyrolysis reactor through unidirectional material returning device, for pyrolysis reactor provides the heat needed for pyrolysis, makes temperature in pyrolysis reactor increase gradually;
(2) flammable solid waste is added in pyrolysis reactor by raw materials device, in pyrolysis reactor, supply pyrolysis gas by air-distributing device bottom pyrolysis reactor tubular distributor and pyrolysis reactor, described pyrolysis gas is as fluidisation mixed bed material;
(3) according to the pyrolysis characteristics of flammable solid waste and the combustioncharacteristics of pyrolysis solid product, by the switch-mode regulation of the adjustment of fluidization gas, the switch-mode regulation of pyrolysis reactor flash device valve and combustion reactor flash device valve, adjust the fluidized state in pyrolysis reactor and combustion reactor, pyrolysis gas and pyrolysis oil output are optimized and combine;
(4) along with reaction is stablized gradually, pyrolysis reactor gaseous product is separated through cyclonic separator and exports, cool in collecting biological oil to the first pyrolysis oil holding tank and pyrolysis oil second holding tank through first step condenser and second stage condenser, residual gas product removes after moisture through dehydration tower and obtains pyrolysis gas, part pyrolysis gas is exported by pyrolysis gas output of products passage, and another part pyrolysis gas accesses hot tube heat exchanger, vents one's spleen as the internal heat of pyrolysis reactor; If the internal heat as pyrolysis reactor is vented one's spleen under-supply, then by venting one's spleen supplement to the parallel external heat that passes into of hot tube heat exchanger, described internal heat is vented one's spleen and external heat the is vented one's spleen common pyrolysis gas forming pyrolysis reactor;
(5) pyrolysis reactor solid product is admitted to two-way material returning device after pyrolysis reactor cyclonic separator is separated, according to two-way material returning device internal temperature situation, by regulating the flow of the pyrolysis solid product of two-way material returning device Fluidization wind rate adjustment feeding combustion reactor combustion;
(6) flue gas that the flue gas that combustion reactor generates obtains after combustion reactor cyclonic separator gas solid separation is admitted to the pyrolysis gas of hot tube heat exchanger for preheating pyrolysis reactor, flue gas is admitted to flue gas cleaner and purifies subsequently, and exports after sack cleaner dedusting;
(7) the inert solid bed material in pyrolysis reactor solid product is admitted to two-way material returning device after pyrolysis reactor cyclonic separator is separated, then is sent back to combustion reactor by two-way material returning device and again added thermosetting high temperature inert Solid Bed material; Described high temperature inert Solid Bed material is admitted to unidirectional material returning device after combustion reactor cyclonic separator is separated, and is being delivered to pyrolysis reactor, form the energy between double-fluidized-bed reactor and material cycle by unidirectional material returning device.
In aforesaid method, the running status of pyrolysis reactor and combustion reactor can be adjusted respectively according to the combustioncharacteristics of the pyrolysis characteristics of flammable solid waste and pyrolysis solid product; Specifically, fluidization gas can be reduced for the fuel that pyrolysis oil productive rate is relatively low and increase the residence time of flammable raw material in pyrolysis reactor, thus obtain more pyrolysis gas by pyrolytic reaction, to realize the utilising efficiency higher to raw material; On the other hand, for the pyrolysis solid product that the combustion rate in air atmosphere is relatively low, pyrolysis solid product is made to have time enough to burn completely by reducing fluidization gas in combustion reactor.
Aforesaid method applies layered fluidized method in pyrolysis reactor, gas-solid, the solid-solid blend intensity in the air-distributing device fluidization gas of two-layer setting reinforcement pyrolysis reactor is divided by conservative control, and make pyrolysis gas product easilier can must leave pyrolytic reaction region, play the effect improving reaction efficiency and accelerate speed of reaction.
Aforesaid method requires that the working temperature in pyrolysis reactor is 450 ~ 650 DEG C, and the working temperature in combustion reactor is 1000 ~ 1100 DEG C; Should notice preventing that temperature in combustion reactor is too high makes residue melting cause fluidization operation difficulty, should prevent the too low dioxin that causes of temperature in combustion reactor from can not decompose completely simultaneously.
Beneficial effect: double-fluidized-bed flammable solid pyrolysis of waste oil gas combination preparing device provided by the invention and method, relative to prior art, have following advantage:
1, the pyrolysis reactor of this device and combustion reactor can adapt to the operating requirement of regulating parameter on a large scale, two reactors both also can be run as fast bed reactor as bubbling bed reactor, also can be regarded as the requirement that this device can meet conventional thermo-cracking and fast pyrolysis, the complicated kind flammable solid waste of process can be successfully managed, and reaction efficiency can be improved to greatest extent by the adjustment of operating parameter, thus realize the efficiency utilization of material and energy;
2, be provided with the collection processing system implementing of pyrolysis oil and pyrolysis gas, the coproduction requirement of pyrolysis oil and pyrolysis gas can be adapted to;
3, the change of material component can be adapted to by adjustment working parameter, can meet when not stop gear work the alternate treatment comprising agriculture and forestry organic waste material and urban solid garbage multiclass flammable solid waste;
4, the structure formation adopting pyrolysis reactor to be coupled with combustion reactor, with inert particle bed material for thermal barrier, circulates, achieves the efficiency utilization of energy between two reactors; Control bed material internal circulating load by pneumatic returning charge valve simultaneously, reach the object accurately controlling temperature in pyrolysis reactor.
Accompanying drawing explanation
Fig. 1 is structural representation of the present invention;
Fig. 2 is the scantlings of the structure figure of pyrolysis reactor;
Fig. 3 is the scantlings of the structure figure of combustion reactor;
Fig. 4 is the scantlings of the structure figure of two-way material returning device;
Comprise: raw materials device 1, pyrolysis reactor tubular distributor 2, air-distributing device 3 bottom pyrolysis reactor, pyrolysis reactor 4, pyrolysis reactor cyclonic separator 5, pyrolysis reactor flash device 6, two-way material returning device 7, first returning charge downtake 7-1, first returning charge inclined tube 7-2, second returning charge inclined tube 7-3, feed chamber 7-4, first returning charge room 7-5, second returning charge room 7-6, first returning charge room air compartment 7-7, second returning charge room air compartment 7-8, feed chamber air compartment 7-9, pyrolysis reactor slag-drip opening 8, combustion reactor cyclonic separator 9, combustion reactor flash device 10, unidirectional material returning device 11, combustion reactor 12, the board-like air-distributing device 13 of combustion reactor, combustion reactor slag-drip opening 14, auxiliary fuel feeder 15, first step condenser 16, first step nozzle 16-1, second stage nozzle 16-2, circulated sprinkling liquid heat exchanger 17, first pyrolysis oil holding tank 18, second stage condenser 19, second pyrolysis oil holding tank 20, dehydration tower 21, hot tube heat exchanger 22, smoke eliminator 23, sack cleaner 24.
Flammable solid waste a, pyrolysis reactor first step fluidized wind b, pyrolysis reactor second stage fluidized wind c, auxiliary fuel d, combustion reactor fluidized wind e, second stage condenser condenses medium f, pyrolysis gas product g, external heat is vented one's spleen h, flue gas i, feed chamber fluidized wind j-1, the first returning charge wind j-2, the second returning charge wind j-3.
Embodiment
Below in conjunction with accompanying drawing, the present invention is further described.
Be illustrated in figure 1 a kind of double-fluidized-bed flammable solid pyrolysis of waste oil gas combination preparing device, comprise the pyrolysis reactor 4 and combustion reactor 12 that vertically arrange.
Air-distributing device 3 and pyrolysis reactor tubular distributor 2 bottom pyrolysis reactor is provided with in described pyrolysis reactor 4, the sidewall of pyrolysis reactor 4 is from top to bottom provided with pyrolysis reactor flash mouth, pyrolysis reactor opening for feed, pyrolysis reactor two-way material returning device returning charge mouth and pyrolysis reactor unidirectional material returning device returning charge mouth, the bottom of pyrolysis reactor 4 is provided with pyrolysis reactor slag-drip opening 8, the top of pyrolysis reactor 4 is provided with pyrolysis reactor exhaust outlet; Described pyrolysis reactor tubular distributor 2 position is higher than air-distributing device bottom pyrolysis reactor 3, pyrolysis reactor gating location is higher than pyrolysis reactor tubular distributor 2, and pyrolysis reactor two-way material returning device returning charge mouth and pyrolysis reactor unidirectional material returning device returning charge mouth position height to be placed in bottom pyrolysis reactor between air-distributing device 3 and pyrolysis reactor tubular distributor 2; Raw materials device 1 is connected with pyrolysis reactor opening for feed, and flammable solid waste a is sent in pyrolysis reactor 4 by raw materials device 1.
The board-like air-distributing device 13 of combustion reactor is provided with in described combustion reactor 12, the sidewall of combustion reactor 12 is from top to bottom provided with combustion reactor flash mouth, combustion reactor opening for feed and combustion reactor returning charge mouth, the bottom of combustion reactor 12 is provided with combustion reactor slag-drip opening 14, the top of combustion reactor 12 is provided with combustion reactor exhaust outlet; Described combustion reactor returning charge mouth position is higher than the board-like air-distributing device 13 of combustion reactor; Auxiliary fuel feeder 15 is connected with combustion reactor opening for feed, and auxiliary fuel d is sent in combustion reactor 12 by auxiliary fuel feeder 15.
Described pyrolysis reactor exhaust outlet access pyrolysis reactor cyclonic separator 5, the bottom discharge end of described pyrolysis reactor cyclonic separator 5 is connected with the feed-pipe 7-1 of two-way material returning device 7 by the first returning charge downtake 7-1, and the first returning charge inclined tube 7-2 of two-way material returning device 7 and the second returning charge inclined tube 7-3 respectively material returning device returning charge mouth two-way with pyrolysis reactor are connected with combustion reactor returning charge mouth; Described pyrolysis reactor flash mouth is communicated with the first returning charge downtake by the first downward-sloping inclined tube, and the first inclined tube is provided with pyrolysis reactor flash device 6; The upper exhaust side access first step condenser 16 of described pyrolysis reactor cyclonic separator 5; The liquid exit of first step condenser 16 accesses the first pyrolysis oil holding tank 18, the pneumatic outlet access second stage condenser 19 of first step condenser 16; The liquid exit of second stage condenser 19 accesses the second pyrolysis oil holding tank 20, the pneumatic outlet access dehydration tower 21 of second stage condenser 19; Dehydration tower 21 pneumatic outlet is divided into two-way, a road access pyrolysis gas output of products passage, another road access hot tube heat exchanger 22 lower inlet.
Described combustion reactor exhaust outlet access combustion reactor cyclonic separator 9, the bottom discharge end of described combustion reactor cyclonic separator 9 is connected by the feed end of the second returning charge downtake with unidirectional material returning device 11, and the discharge end of unidirectional material returning device 11 is connected with pyrolysis reactor unidirectional material returning device returning charge mouth; Described combustion reactor flash mouth is communicated with the second returning charge downtake by the second downward-sloping inclined tube, and the second inclined tube is provided with combustion reactor flash device 10; End entrance on the upper exhaust side access hot tube heat exchanger 22 of described combustion reactor cyclonic separator 9; Hot tube heat exchanger 22 upper end outlet and pyrolysis reactor tubular distributor 2 are connected with air-distributing device 3 bottom pyrolysis reactor, and the outlet of hot tube heat exchanger 22 lower end is connected with smoke eliminator 23, and smoke eliminator 23 pneumatic outlet is connected with sack cleaner 24.
Described pyrolysis reactor flash device 6 regulates pyrolysis reactor 4 to work in bubbling fluidization state, turbulent fluidised state or fast fluidization state; Described combustion reactor flash device 10 regulates combustion reactor 12 to work in bubbling fluidization state, turbulent fluidised state or fast fluidization state.
The height of described pyrolysis reactor 2 is H, by the bottom of pyrolysis reactor 2: the height of pyrolysis reactor tubular distributor 2 is 0.2 ~ 0.3H, the height of pyrolysis reactor opening for feed is 0.35 ~ 0.45H, the height of pyrolysis reactor flash mouth is 0.6 ~ 0.8H, the height of pyrolysis reactor two-way material returning device returning charge mouth and pyrolysis reactor unidirectional material returning device returning charge mouth is 0.05 ~ 0.15H, and the height of pyrolysis reactor two-way material returning device returning charge mouth is not less than the height of the unidirectional material returning device of pyrolysis reactor; The diameter of pyrolysis reactor 2 is D; Bottom pyrolysis reactor air-distributing device 3 be osculum under cone shaped distributor, along being placed in bottom pyrolysis reactor 2, axis is vertical, and the angle of the conical surface and horizontal plane is 60 ° at its end; The angle of the first inclined tube and horizontal plane is 45 °.
The height of described combustion reactor 12 is L, L=0.8 ~ 1H, by the bottom of combustion reactor 12: the height of combustion reactor opening for feed is 0.3 ~ 0.4L, the height of combustion reactor flash mouth is 0.6 ~ 0.8L, and the height of combustion reactor returning charge mouth is 0.15 ~ 0.25L; Combustion reactor 12 be W, W=0.8 ~ 1.2D so far; Be small end bottom combustion reactor 12 under pyramidal structure, the board-like air-distributing device of combustion reactor 13 is arranged on the large end position of pyramidal structure, pyramidal structure and the board-like air-distributing device 13 of combustion reactor form combustion reactor air compartment jointly, and the conical surface of pyramidal structure and the angle of horizontal plane are 60 °; The angle of the second inclined tube and horizontal plane is 45 °.
Described two-way material returning device 7 comprises rectangular parallelepiped cavity volume, described rectangular parallelepiped cavity volume is divided into three chambers by T-shaped dividing plate, wherein a chamber at rear is feed chamber 7-4, two chambers in front are respectively the first returning charge room 7-5 and the second returning charge room 7-6, feed chamber 7-4 is connected with the first returning charge downtake 7-1, first returning charge room 7-5 is connected with the first returning charge inclined tube 7-2, and the second returning charge room 7-6 is connected with the second returning charge inclined tube 7-3; In described feed chamber 7-4, air distribution plate is set, isolates the feed chamber air compartment 7-9 of below; Be provided with air distribution plate in described first returning charge room 7-5, isolate the first returning charge room air compartment 7-7 of below; Be provided with air distribution plate in described second returning charge room 7-6, isolate the second returning charge room air compartment 7-8 of below;
The width b of described feed chamber 7-4
2with the width b of the width/the second returning charge room 7-6 of the first returning charge room 7-5
1equal, the length a of the first returning charge room 7-5
1with the length a of the second returning charge room 7-6
2equal; The diameter of the first returning charge downtake 7-1 is d
1, the diameter of the first returning charge inclined tube 7-2 is d
2, the diameter of the second returning charge inclined tube 7-3 is d
3, d
2=d
3=0.625d
1; The angle of the first returning charge inclined tube 7-2 and vertical direction is α, and the angle of the second returning charge inclined tube 7-3 and vertical direction is that β, α and β are all less than 45 °; The percentage of open area of described air distribution plate is 10 ~ 15%.
In feed chamber air compartment 7-9, pass into feed chamber fluidized wind j-1, in the first returning charge room air compartment 7-7, pass into the first returning charge wind j-2, in the second returning charge room air compartment 7-8, pass into the second returning charge wind j-3; By regulating fluidizing agent (feed chamber fluidized wind j-1, the first returning charge wind j-2 and the second returning charge wind j-3) flow that passes in two-way material returning device 7 and allocation proportion can the flux of controlled circulation material.
Based on the double-fluidized-bed flammable solid pyrolysis of waste oil gas co-production of said apparatus, comprise the steps:
(1) in combustion reactor 12, add auxiliary fuel by auxiliary fuel feeder 15, auxiliary fuel is by the Air Fluidized that injected by the board-like air-distributing device 13 of combustion reactor and burn, and reaches operating requirement in order to promote temperature in combustion reactor 12; High temperature inert Solid Bed material enters pyrolysis reactor 4 through unidirectional material returning device 11, for pyrolysis reactor 4 provides the heat needed for pyrolysis, makes temperature in pyrolysis reactor 4 increase gradually;
(2) flammable solid waste is added in pyrolysis reactor 4 by raw materials device 1, in pyrolysis reactor 4, supply pyrolysis gas by air-distributing device 3 bottom pyrolysis reactor tubular distributor 2 and pyrolysis reactor, described pyrolysis gas is as fluidisation mixed bed material;
(3) according to the pyrolysis characteristics of flammable solid waste and the combustioncharacteristics of pyrolysis solid product, by the switch-mode regulation of the adjustment of fluidization gas, the switch-mode regulation of pyrolysis reactor flash device 6 valve and combustion reactor flash device 10 valve, adjust the fluidized state in pyrolysis reactor 4 and combustion reactor 12, pyrolysis gas and pyrolysis oil output are optimized and combine;
(4) along with reaction is stablized gradually, pyrolysis reactor 4 gaseous product is separated through cyclonic separator 5 and exports, cool in collecting biological oil to the first pyrolysis oil holding tank 18 and pyrolysis oil second holding tank 20 through first step condenser 16 and second stage condenser 19, residual gas product removes after moisture through dehydration tower 21 and obtains pyrolysis gas, part pyrolysis gas is exported by pyrolysis gas output of products passage, and another part pyrolysis gas accesses hot tube heat exchanger 22, vents one's spleen as the internal heat of pyrolysis reactor 4; If the internal heat as pyrolysis reactor 4 is vented one's spleen under-supply, then by venting one's spleen supplement to the parallel external heat that passes into of hot tube heat exchanger 22, described internal heat is vented one's spleen and external heat the is vented one's spleen common pyrolysis gas forming pyrolysis reactor 4;
(5) pyrolysis reactor 4 solid product is admitted to two-way material returning device 7 after pyrolysis reactor cyclonic separator 5 is separated, according to two-way material returning device 7 internal temperature situation, by regulating the flow of the pyrolysis solid product of two-way material returning device 7 Fluidization wind rate adjustment feeding combustion reactor 12 combustion;
(6) flue gas that the flue gas that combustion reactor 12 generates obtains after combustion reactor cyclonic separator 9 gas solid separation is admitted to the pyrolysis gas of hot tube heat exchanger 22 for preheating pyrolysis reactor 4, flue gas is admitted to flue gas cleaner 23 and purifies subsequently, and exports after sack cleaner 24 dedusting;
(7) the inert solid bed material in pyrolysis reactor 4 solid product is admitted to two-way material returning device 7 after pyrolysis reactor cyclonic separator 5 is separated, then is sent back to combustion reactor 12 by two-way material returning device 7 and again added thermosetting high temperature inert Solid Bed material; Described high temperature inert Solid Bed material is admitted to unidirectional material returning device 11 after combustion reactor cyclonic separator 9 is separated, and being delivered to pyrolysis reactor 4 by unidirectional material returning device 11, forms the energy between double-fluidized-bed reactor and material cycle.
Based on said apparatus and method, below in conjunction with embodiment, the present invention is made further instructions.
Embodiment 1
Material choice stalk, quartz sand (mainly SiO selected by inert solid bed material
2).Because stalk pyrolysis oil preparation effectiveness comparison is good, its pyrolysis solid product combustion rate in air atmosphere is very fast simultaneously, thus make pyrolysis reactor 4 as fast fluidization bed operating by closing the valve that pyrolysis reactor overflow device 6 is arranged and meet the operating requirement of fast pyrogenation, controlling mean residence time in pyrolysis reactor 4 is 1 ~ 3s; Make combustion reactor 12 as fast fluidization bed operating by closing the valve that combustion reactor overflow device 10 is arranged, in control combustion reactor 12, mean residence time is 7 ~ 9s.Pyrolysis reactor 4 fluidized wind tolerance is assigned as: pyrolysis reactor tubular distributor 2 is 35% ~ 45%, air-distributing device 3 is 55% ~ 65% bottom pyrolysis reactor.
During starter gear, send into combustion reactor 12 using coal as auxiliary fuel through auxiliary fuel feeder 15, air to be admitted in combustion reactor 12 for fluidized bed material by the board-like air-distributing device 13 of combustion reactor and to provide combustion-supporting gas (O
2).In combustion reactor 12 mixed bed material and flue gas altogether fluidisation rise after in combustion reactor cyclonic separator 9 place gas solid separation, high temperature inert Solid Bed material to enter in pyrolysis reactor 4 and in this release of heat through unidirectional material returning device 11.Isolated high-temperature flue gas is then admitted to the fluidizing agent of hot tube heat exchanger 22 for preheating pyrolysis reactor 4, and the flue gas after heat exchange discharges after purifying treatment and dedusting.Meanwhile, utilize external heat to vent one's spleen as the fluidizing agent of pyrolysis reactor 4, bottom pyrolysis reactor, air-distributing device 3 and pyrolysis reactor tubular distributor 2 enter in pyrolysis reactor 4 for fluidized bed material respectively.Along with burning is carried out, pyrolysis reactor 4 improves gradually with the temperature in combustion reactor 12.Controlling temperature in pyrolysis reactor 4 is 500 ± 50 DEG C, and in control combustion reactor 12, temperature is 1000 ± 50 DEG C.
When temperature in pyrolysis reactor 4 reaches after operating temperature requires, added through super-dry and the stalk pulverized to pyrolysis reactor 4 by raw materials device 1, stalk at this by fast fluidization, material generation pyrolysis in the bed of violent mixing.Pyrogenous origin mix products and part inert solid bed material are fluidized gas and bring pyrolysis reactor cyclonic separator 5 into, and after this carries out gas solid separation, gaseous product enters first step condenser 16 by upper end, and solid product enters two-way material returning device 7 downwards.Gaseous product first step condenser 16 and second stage condenser 17 respectively through spraying cooling with indirectly cool to 40 ~ 70 DEG C, in process of cooling, condensable gas is condensed into pyrolysis oil and enters the first pyrolysis oil holding tank 18 with pyrolysis oil by the second pyrolysis oil holding tank 20.Remaining not condensable gas is admitted to dehydration tower 21 and is removed unnecessary moisture, obtains pyrolysis gas.Pyrolysis gas is divided into two-way after dehydration tower process, and a road exports as pyrolysis gas product g, and another road is admitted to hot tube heat exchanger 22 as fluidizing agent and is got back in pyrolysis reactor 4 by after high-temperature flue gas preheating.The solid materials including pyrolysis solid product and inert solid bed material is sent into pyrolysis reactor 4 and combustion reactor 12 through the first returning charge inclined tube 7-2 and the second returning charge inclined tube 7-3 respectively in proportion by according to two reactor temperature situations in two-way material returning device 7.Enter pyrolysis solid product (mainly burnt) the rapid perfect combustion in air atmosphere in combustion reactor 12, inert solid bed material is then again heated in combustion reactor 12, forms the circulation of material and energy between two reactors.To stablize and temperature of reaction reduces the add-on of auxiliary fuel coal gradually after reaching requirement to plant running, device relies on pyrolysis solid product to burn the operation of the energy holdout device provided.
Embodiment 2
Material choice forestry logging residue, quartz sand selected by inert solid bed material.Due to timber xylogen large percentage compared with stalk, the flow process relative complex required for Particle size requirements reaching fast pyrogenation pulverized by timber simultaneously, makes to utilize forestry logging residue to carry out pyrolysis oil also be not as suitable as stalk.Therefore, making pyrolysis reactor 4 as bubbling fluidization bed operating by opening the valve that pyrolysis reactor overflow device 6 is arranged, regulating mean residence time in pyrolysis reactor 4 to be 200 ~ 300s; Making combustion reactor 12 as fast fluidization bed operating by closing the valve that combustion reactor overflow device 10 is arranged, regulating gas residence time in combustion reactor 12 to be 7 ~ 9s.Controlling temperature in pyrolysis reactor 4 is 500 ± 50 DEG C, and in control combustion reactor 12, temperature is 1000 ± 50 DEG C.Pyrolysis reactor fluidized wind tolerance is assigned as: pyrolysis reactor tubular distributor 2 is 35% ~ 45%, air-distributing device 3 is 55% ~ 65% bottom pyrolysis reactor.
Coal is utilized to provide institute's energy requirement as auxiliary fuel in the initial launch that combustion reactor 12 combustion is device.When after device steady running, raw material through super-dry and pulverizing is added to pyrolysis reactor 4 by raw materials device 1, in the pyrolysis reactor 4 running on bubbling state, raw material is by deep layer pyrolysis, the pyrolysis gas product obtained is mainly micromolecular not condensable gases, after a small amount of tar removed by first step condenser 16 and second stage condenser 17, after pyrolysis gas removes moisture by dehydration tower 21, a point two-way exports as fluidized gas and gas product.The solid product that pyrolysis obtains then is admitted to combustion reactor 12 and burns for the operation of device provides heat with air mixed.
Embodiment 3
Material choice domestic waste, quartz sand selected by inertia circulation bed material.Owing to containing certain pollutent in the solid product of Combustion Properties of Municipal Solid Waste, especially dioxin, thus need to carry out slightly long pyroprocessing to remove pollutent to pyrolysis solid product in combustion reactor 12.Make pyrolysis reactor 4 as fast fluidization bed operating by closing the valve that pyrolysis reactor overflow device 6 is arranged and meet the operating requirement of fast pyrogenation, controlling mean residence time in pyrolysis reactor 4 is 1 ~ 3s; Make combustion reactor 12 as bubbling fluidization bed operating by opening the valve that combustion reactor overflow device 10 is arranged, in control combustion reactor 12, mean residence time is 200 ~ 300s.Controlling temperature in pyrolysis reactor 4 is 550 ± 50 DEG C, and in control combustion reactor 12, temperature is 1150 ± 50 DEG C.Pyrolysis reactor fluidized wind tolerance is assigned as: pyrolysis reactor tubular distributor 2 is 35% ~ 45%, air-distributing device 3 is 55% ~ 65% bottom pyrolysis reactor.
Coal is utilized to provide institute's energy requirement as auxiliary fuel in the initial launch that combustion reactor 12 combustion is device.When after device steady running, added through sorting and the raw material of drying and crushing to pyrolysis reactor 4 by raw materials device 1, in pyrolysis reactor 4, the gaseous product that raw material fast pyrogenation obtains is after pyrolysis reactor cyclonic separator 5 gas solid separation, the collection to pyrolysis oil is completed through first step condenser 16 and second stage condenser 17, eliminate through spray in first step condenser 16 simultaneously and can not coagulate sour gas a small amount of in pyrolysis gas, after pyrolysis gas removes moisture by dehydration tower 21, a point two-way exports as fluidized gas and gas product.The solid product that pyrolysis obtains then is admitted to combustion reactor 12 and burns for the operation of device provides heat with air mixed.The pyrolysis solid product long period is in the combustion reactor 12 more than 1100 DEG C, can decompose the pollutent such as dioxin and furans in raw material completely
The above is only the preferred embodiment of the present invention; be noted that for those skilled in the art; under the premise without departing from the principles of the invention, can also make some improvements and modifications, these improvements and modifications also should be considered as protection scope of the present invention.
Claims (6)
1. a double-fluidized-bed flammable solid pyrolysis of waste oil gas combination preparing device, is characterized in that: comprise the pyrolysis reactor (4) and combustion reactor (12) that vertically arrange;
Air-distributing device bottom pyrolysis reactor (3) and pyrolysis reactor tubular distributor (2) is provided with in described pyrolysis reactor (4), the sidewall of pyrolysis reactor (4) is from top to bottom provided with pyrolysis reactor flash mouth, pyrolysis reactor opening for feed, pyrolysis reactor two-way material returning device returning charge mouth and pyrolysis reactor unidirectional material returning device returning charge mouth, the bottom of pyrolysis reactor (4) is provided with pyrolysis reactor slag-drip opening (8), the top of pyrolysis reactor (4) is provided with pyrolysis reactor exhaust outlet; Described pyrolysis reactor tubular distributor (2) position is higher than air-distributing device bottom pyrolysis reactor (3), pyrolysis reactor gating location is higher than pyrolysis reactor tubular distributor (2), and pyrolysis reactor two-way material returning device returning charge mouth and pyrolysis reactor unidirectional material returning device returning charge mouth position height are placed between air-distributing device bottom pyrolysis reactor (3) and pyrolysis reactor tubular distributor (2); Raw materials device (1) is connected with pyrolysis reactor opening for feed;
The board-like air-distributing device of combustion reactor (13) is provided with in described combustion reactor (12), the sidewall of combustion reactor (12) is from top to bottom provided with combustion reactor flash mouth, combustion reactor opening for feed and combustion reactor returning charge mouth, the bottom of combustion reactor (12) is provided with combustion reactor slag-drip opening (14), the top of combustion reactor (12) is provided with combustion reactor exhaust outlet; Described combustion reactor returning charge mouth position is higher than the board-like air-distributing device of combustion reactor (13); Auxiliary fuel feeder (15) is connected with combustion reactor opening for feed;
Described pyrolysis reactor exhaust outlet access pyrolysis reactor cyclonic separator (5), the bottom discharge end of described pyrolysis reactor cyclonic separator (5) is connected with the feed-pipe (7-1) of two-way material returning device (7) by the first returning charge downtake (7-1), and the first returning charge inclined tube (7-2) of two-way material returning device (7) and the second returning charge inclined tube (7-3) respectively material returning device returning charge mouth two-way with pyrolysis reactor are connected with combustion reactor returning charge mouth; Described pyrolysis reactor flash mouth is communicated with the first returning charge downtake by the first downward-sloping inclined tube, and the first inclined tube is provided with pyrolysis reactor flash device (6); Upper exhaust side access first step condenser (16) of described pyrolysis reactor cyclonic separator (5) carries out pyrolysis product recovery;
Described combustion reactor exhaust outlet access combustion reactor cyclonic separator (9), the bottom discharge end of described combustion reactor cyclonic separator (9) is connected with the feed end of unidirectional material returning device (11) by the second returning charge downtake, and the discharge end of unidirectional material returning device (11) is connected with pyrolysis reactor unidirectional material returning device returning charge mouth; Described combustion reactor flash mouth is communicated with the second returning charge downtake by the second downward-sloping inclined tube, and the second inclined tube is provided with combustion reactor flash device (10); The upper exhaust side access hot tube heat exchanger of described combustion reactor cyclonic separator (9) carries out energy recovery.
2. double-fluidized-bed flammable solid pyrolysis of waste oil gas combination preparing device according to claim 1, is characterized in that: upper exhaust side access first step condenser (16) of described pyrolysis reactor cyclonic separator (5); The liquid exit of first step condenser (16) accesses the first pyrolysis oil holding tank (18), pneumatic outlet access second stage condenser (19) of first step condenser (16); The liquid exit of second stage condenser (19) accesses the second pyrolysis oil holding tank (20), pneumatic outlet access dehydration tower (21) of second stage condenser (19); Dehydration tower (21) pneumatic outlet is divided into two-way, a road access pyrolysis gas output of products passage, another road access hot tube heat exchanger (22) lower inlet;
The upper end entrance of upper exhaust side access hot tube heat exchanger (22) of described combustion reactor cyclonic separator (9); Hot tube heat exchanger (22) upper end outlet and pyrolysis reactor tubular distributor (2) are connected with air-distributing device (3) bottom pyrolysis reactor, the outlet of hot tube heat exchanger (22) lower end is connected with smoke eliminator (23), and smoke eliminator (23) pneumatic outlet is connected with sack cleaner (24).
3. double-fluidized-bed flammable solid pyrolysis of waste oil gas combination preparing device according to claim 1, is characterized in that: described pyrolysis reactor flash device (6) regulates pyrolysis reactor (4) to work in bubbling fluidization state, turbulent fluidised state or fast fluidization state; Described combustion reactor flash device (10) regulates combustion reactor (12) to work in bubbling fluidization state, turbulent fluidised state or fast fluidization state.
4. double-fluidized-bed flammable solid pyrolysis of waste oil gas combination preparing device according to claim 1, is characterized in that:
The height of described pyrolysis reactor (2) is H, by the bottom of pyrolysis reactor (2): the height of pyrolysis reactor tubular distributor (2) is 0.2 ~ 0.3H, the height of pyrolysis reactor opening for feed is 0.35 ~ 0.45H, the height of pyrolysis reactor flash mouth is 0.6 ~ 0.8H, the height of pyrolysis reactor two-way material returning device returning charge mouth and pyrolysis reactor unidirectional material returning device returning charge mouth is 0.05 ~ 0.15H, and the height of pyrolysis reactor two-way material returning device returning charge mouth is higher than the height of the unidirectional material returning device of pyrolysis reactor; The diameter of pyrolysis reactor (2) is D; Bottom pyrolysis reactor air-distributing device (3) for osculum under cone shaped distributor, its, axis was vertical, and the angle of the conical surface and horizontal plane is 60 ° along being placed in pyrolysis reactor (2) bottom end; The angle of the first inclined tube and horizontal plane is 45 °;
The height of described combustion reactor (12) is L, L=0.8 ~ 1H, by the bottom of combustion reactor (12): the height of combustion reactor opening for feed is 0.3 ~ 0.4L, the height of combustion reactor flash mouth is 0.6 ~ 0.8L, and the height of combustion reactor returning charge mouth is 0.15 ~ 0.25L; The diameter of combustion reactor (12) is W, W=0.8 ~ 1.2D; Combustion reactor (12) bottom be small end under pyramidal structure, the board-like air-distributing device of combustion reactor (13) is arranged on the large end position of pyramidal structure, pyramidal structure and the board-like air-distributing device of combustion reactor (13) form combustion reactor air compartment jointly, and the conical surface of pyramidal structure and the angle of horizontal plane are 60 °; The angle of the second inclined tube and horizontal plane is 45 °.
5. double-fluidized-bed flammable solid pyrolysis of waste oil gas combination preparing device according to claim 1, it is characterized in that: described two-way material returning device (7) comprises rectangular parallelepiped cavity volume, described rectangular parallelepiped cavity volume is divided into three chambers by T-shaped dividing plate, wherein a chamber at rear is feed chamber (7-4), two chambers in front are respectively the first returning charge room (7-5) and the second returning charge room (7-6), feed chamber (7-4) is connected with the first returning charge downtake (7-1), first returning charge room (7-5) is connected with the first returning charge inclined tube (7-2), second returning charge room (7-6) is connected with the second returning charge inclined tube (7-3), in described feed chamber (7-4), air distribution plate is set, isolates the feed chamber air compartment (7-9) of below, be provided with air distribution plate in described first returning charge room (7-5), isolate the first returning charge room air compartment (7-7) of below, be provided with air distribution plate in described second returning charge room (7-6), isolate the second returning charge room air compartment (7-8) of below,
The width b of described feed chamber (7-4)
2with the width b of the width/the second returning charge room (7-6) of the first returning charge room (7-5)
1equal, the length a of the first returning charge room (7-5)
1with the length a of the second returning charge room (7-6)
2equal; The diameter of the first returning charge downtake (7-1) is d
1, the diameter of the first returning charge inclined tube (7-2) is d
2, the diameter of the second returning charge inclined tube (7-3) is d
3, d
2=d
3=0.625d
1; First returning charge inclined tube (7-2) is α with the angle of vertical direction, and the second returning charge inclined tube (7-3) is that β, α and β are all less than 45 ° with the angle of vertical direction; The percentage of open area of described air distribution plate is 10 ~ 15%.
6. a double-fluidized-bed flammable solid pyrolysis of waste oil gas co-production, is characterized in that: comprise the steps:
(1) in combustion reactor (12), auxiliary fuel is added by auxiliary fuel feeder (15), auxiliary fuel is by the Air Fluidized that injected by the board-like air-distributing device of combustion reactor (13) and burn, and reaches operating requirement in order to promote combustion reactor (12) interior temperature; High temperature inert Solid Bed material enters pyrolysis reactor (4) through unidirectional material returning device (11), for pyrolysis reactor (4) provides the heat needed for pyrolysis, makes pyrolysis reactor (4) interior temperature increase gradually;
(2) flammable solid waste is added in pyrolysis reactor (4) by raw materials device (1), by the supply pyrolysis gas in pyrolysis reactor (4) of air-distributing device (3) bottom pyrolysis reactor tubular distributor (2) and pyrolysis reactor, described pyrolysis gas is as fluidisation mixed bed material;
(3) according to the pyrolysis characteristics of flammable solid waste and the combustioncharacteristics of pyrolysis solid product, by the switch-mode regulation of the adjustment of fluidization gas, the switch-mode regulation of pyrolysis reactor flash device (6) valve and combustion reactor flash device (10) valve, adjust the fluidized state in pyrolysis reactor (4) and combustion reactor (12), pyrolysis gas and pyrolysis oil output are optimized and combine;
(4) along with reaction is stablized gradually, pyrolysis reactor (4) gaseous product is separated through cyclonic separator (5) and exports, cool in collecting biological oil to the first pyrolysis oil holding tank (18) and pyrolysis oil second holding tank (20) through first step condenser (16) and second stage condenser (19), residual gas product obtains pyrolysis gas after dehydration tower (21) removes moisture, part pyrolysis gas is exported by pyrolysis gas output of products passage, another part pyrolysis gas access hot tube heat exchanger (22), internal heat as pyrolysis reactor (4) is vented one's spleen, if vent one's spleen under-supply as the internal heat of pyrolysis reactor (4), then by venting one's spleen supplement to the parallel external heat that passes into of hot tube heat exchanger (22), described internal heat is vented one's spleen and external heat is vented one's spleen forms the pyrolysis gas of pyrolysis reactor (4) jointly,
(5) pyrolysis reactor (4) solid product is admitted to two-way material returning device (7) after pyrolysis reactor cyclonic separator (5) is separated, according to two-way material returning device (7) internal temperature situation, by regulating the flow of the pyrolysis solid product of two-way material returning device (7) Fluidization wind rate adjustment feeding combustion reactor (12) combustion;
(6) flue gas that the flue gas that combustion reactor (12) generates obtains after combustion reactor cyclonic separator (9) gas solid separation is admitted to the pyrolysis gas of hot tube heat exchanger (22) for preheating pyrolysis reactor (4), flue gas is admitted to flue gas cleaner (23) and purifies subsequently, and exports after sack cleaner (24) dedusting;
(7) the inert solid bed material in pyrolysis reactor (4) solid product is admitted to two-way material returning device (7) after pyrolysis reactor cyclonic separator (5) is separated, then is sent back to combustion reactor (12) by two-way material returning device (7) and again added thermosetting high temperature inert Solid Bed material; Described high temperature inert Solid Bed material is admitted to unidirectional material returning device (11) after combustion reactor cyclonic separator (9) is separated, being delivered to pyrolysis reactor (4) by unidirectional material returning device (11), form the energy between double-fluidized-bed reactor and material cycle.
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