CN105754621B - Pyrolysis of coal reactor-recirculating fluidized bed combined system and the method for handling coal using it - Google Patents
Pyrolysis of coal reactor-recirculating fluidized bed combined system and the method for handling coal using it Download PDFInfo
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- CN105754621B CN105754621B CN201610204385.2A CN201610204385A CN105754621B CN 105754621 B CN105754621 B CN 105754621B CN 201610204385 A CN201610204385 A CN 201610204385A CN 105754621 B CN105754621 B CN 105754621B
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- 238000000197 pyrolysis Methods 0.000 title claims abstract description 231
- 239000003245 coal Substances 0.000 title claims abstract description 196
- 238000000034 method Methods 0.000 title claims abstract description 59
- 239000000203 mixture Substances 0.000 claims abstract description 71
- 230000003134 recirculating effect Effects 0.000 claims abstract description 59
- 238000009825 accumulation Methods 0.000 claims description 61
- 238000002485 combustion reaction Methods 0.000 claims description 24
- 238000000926 separation method Methods 0.000 claims description 20
- 238000010248 power generation Methods 0.000 claims description 16
- 230000008676 import Effects 0.000 claims description 13
- 238000007670 refining Methods 0.000 claims description 12
- 238000000746 purification Methods 0.000 claims description 11
- 239000007787 solid Substances 0.000 claims description 9
- 239000008247 solid mixture Substances 0.000 claims description 6
- 238000009826 distribution Methods 0.000 claims description 3
- 230000008569 process Effects 0.000 abstract description 22
- 230000000903 blocking effect Effects 0.000 abstract description 6
- 238000004519 manufacturing process Methods 0.000 abstract description 6
- 239000007789 gas Substances 0.000 description 188
- 239000011269 tar Substances 0.000 description 44
- 239000010410 layer Substances 0.000 description 17
- 239000000463 material Substances 0.000 description 13
- 238000006243 chemical reaction Methods 0.000 description 11
- 238000010586 diagram Methods 0.000 description 11
- 239000000446 fuel Substances 0.000 description 10
- 230000005611 electricity Effects 0.000 description 8
- 238000010438 heat treatment Methods 0.000 description 7
- 238000009833 condensation Methods 0.000 description 6
- 230000005494 condensation Effects 0.000 description 6
- 238000001035 drying Methods 0.000 description 6
- 230000008901 benefit Effects 0.000 description 5
- 239000000567 combustion gas Substances 0.000 description 5
- 238000005265 energy consumption Methods 0.000 description 5
- 230000008859 change Effects 0.000 description 4
- 239000000428 dust Substances 0.000 description 4
- 238000009413 insulation Methods 0.000 description 4
- 230000035800 maturation Effects 0.000 description 4
- 238000005979 thermal decomposition reaction Methods 0.000 description 4
- 239000003208 petroleum Substances 0.000 description 3
- 238000004321 preservation Methods 0.000 description 3
- 230000009467 reduction Effects 0.000 description 3
- 239000000969 carrier Substances 0.000 description 2
- 239000003034 coal gas Substances 0.000 description 2
- 239000000571 coke Substances 0.000 description 2
- 230000009615 deamination Effects 0.000 description 2
- 238000006481 deamination reaction Methods 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 239000003517 fume Substances 0.000 description 2
- 238000009434 installation Methods 0.000 description 2
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 1
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 1
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 1
- 239000005864 Sulphur Substances 0.000 description 1
- 239000003153 chemical reaction reagent Substances 0.000 description 1
- 239000002817 coal dust Substances 0.000 description 1
- 239000011280 coal tar Substances 0.000 description 1
- 239000012141 concentrate Substances 0.000 description 1
- 230000008878 coupling Effects 0.000 description 1
- 238000010168 coupling process Methods 0.000 description 1
- 238000005859 coupling reaction Methods 0.000 description 1
- 238000006477 desulfuration reaction Methods 0.000 description 1
- 230000023556 desulfurization Effects 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 239000004744 fabric Substances 0.000 description 1
- 239000003546 flue gas Substances 0.000 description 1
- 239000002737 fuel gas Substances 0.000 description 1
- 238000002309 gasification Methods 0.000 description 1
- 238000005338 heat storage Methods 0.000 description 1
- 239000001257 hydrogen Substances 0.000 description 1
- 229910052739 hydrogen Inorganic materials 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 230000003993 interaction Effects 0.000 description 1
- 239000011229 interlayer Substances 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 239000002245 particle Substances 0.000 description 1
- 239000000843 powder Substances 0.000 description 1
- 238000010791 quenching Methods 0.000 description 1
- 230000005855 radiation Effects 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 239000000779 smoke Substances 0.000 description 1
- 239000007921 spray Substances 0.000 description 1
- 238000009827 uniform distribution Methods 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 1
- 238000003466 welding Methods 0.000 description 1
Classifications
-
- 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
-
- 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
- C10B47/00—Destructive distillation of solid carbonaceous materials with indirect heating, e.g. by external combustion
-
- 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
- C10B57/005—After-treatment of coke, e.g. calcination desulfurization
-
- 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
- C10B57/18—Modifying the properties of the distillation gases in the oven
Landscapes
- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Materials Engineering (AREA)
- Organic Chemistry (AREA)
- Combustion & Propulsion (AREA)
- Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The present invention provides pyrolysis of coal reactor-recirculating fluidized bed combined system and the methods for handling coal using it, wherein the combined system includes pyrolysis of coal reactor and recirculating fluidized bed.Pyrolysis of coal reactor and existing recirculating fluidized bed can be directly combined by combined system of the invention, without being transformed to existing recirculating fluidized bed, pyrolysis of coal reactor and recirculating fluidized bed can be relatively independent run, the two interferes with each other relatively small, and the combined system can be effective for producing combustible gas and pyrolysis oil co-production electric power, and utilize the transportation system of existing recirculating fluidized bed, realize semicoke hot sending, ensure the burning of semicoke, and reduce coal plug process costs, and cyclone separator built in the pyrolysis of coal reactor can substantially reduce the dustiness of the gas mixture for the pyrolysis reactor that produces coal, and then the possibility for blocking pipeline in subsequent handling is effectively reduced and reduces lagging facility.
Description
Technical field
The present invention relates to coal sublevel cascade utilization technical fields, and in particular, to pyrolysis of coal reactor-recirculating fluidized bed
Combined system and the method for handling coal using it.
Background technique
The semicoke generated after pyrolysis of coal can be used as fuel-fired power generation, and existing pyrolysis of coal plug technique mainly for
Recirculating fluidized bed generating set, as Chinese Academy of Sciences's process and the heat that is generated using circulating fluidized bed boiler of Zhejiang University it is grey as hot
Carrier, and realized using downlink bed process to pyrolysis of coal, and petroleum vapor recovery.Existing system is due to taking more complex consolidate
The pyrolysis of coal plug technique of body or gas heat carrier, and pyrolytic process of coal generates petroleum resources, for electricity generation system, needs
It is equipped with corresponding oil vapor treatment system, therefore existing system configuration is various, cost is high.
Fig. 1 is a kind of furnace front coal head-drawing process structure schematic diagram, which send (diagram A entrance) into solid thermal carriers gas
Makeup set in 1, by coal plug pyrolysis gas and tar after cyclone separator 6, extract petroleum resources (diagram B go out
Mouthful), the semicoke separated is sent into recirculating fluidized bed 7 (outlet diagram F), and semicoke is through 2 rear portion of material returning device (diagram G is exported)
The lower part for being sent into recirculating fluidized bed 7 is used as fuel, and a part is sent into the coal plug combustion chamber 3 of insulation, matches air burning.
The flue gas that combustion chamber 3 generates enters cyclone separator 4, and the semicoke separated enters gasification installation 1 through material returning device 5 together with coal
In, and hot fume (diagram E) is also fed into recirculating fluidized bed 7.However, the process flow is complicated, it is primarily due to the technique and adopts
Take semicoke as heat carrier, therefore process flow includes the techniques such as heating, promotion, separation, the mixing of semicoke, leads to system flow
Increase, substantially increases system failure rate；Meanwhile the semicoke that the technique generates can only be directed to fluidized-bed combustion boiler, cannot utilize
On recirculating fluidized bed.
However, recirculating fluidized bed accounting is very high in China's electricity generation system, due to circulating fluidized bed combustion to coal volatile matter and
Particle size requirements are higher, and coal plug is seldom at present for the technique of recirculating fluidized bed.
Thus, current pyrolysis of coal plug technique still has much room for improvement.
Summary of the invention
The present invention is directed to solve at least some of the technical problems in related technologies.For this purpose, of the invention
The first purpose is to propose a kind of pyrolysis of coal reactor-recirculating fluidized bed combined system and the method using its processing coal.
Specifically, the present invention is provided with a kind of New type coal plug technique for recirculating fluidized bed, combustible gas and pyrolysis are produced
Oily co-production electric power, and using the transportation system of existing recirculating fluidized bed, it realizes semicoke hot sending, ensures the burning of semicoke, and drop
Low coal plug process costs.Combined system of the invention solves the problems, such as that coal plug leading portion pyrolytic process is complicated, and is pyrolyzed and produces
Object rationally utilizes, and reduces cost of electricity-generating.
In view of this, in one aspect of the invention, the present invention provides a kind of pyrolysis of coal reactor-recirculating fluidized bed connection
Use system.According to an embodiment of the invention, the pyrolysis of coal reactor-recirculating fluidized bed combined system includes:
Pyrolysis of coal reactor, the pyrolysis of coal reactor have coal entrance, semicoke outlet and gas mixture outlet,
In, the coal entrance is set to the top of the pyrolysis of coal reactor, and the gas mixture outlet is set to the pyrolysis of coal
On the roof and/or side wall of reactor, the semicoke outlet is set to the bottom of the pyrolysis of coal reactor；
More oil gas export pipelines, gas gathering manifold, more gas-collecting branch pipes, heat accumulating type spoke are provided in the pyrolysis reactor
Pipe and cyclone separator are penetrated,
Wherein, the gas gathering manifold adjacent to the pyrolysis of coal reactor internal perisporium and be vertically arranged,
One end of the gas-collecting branch pipe is connected with the gas gathering manifold, and the other end is connected to the oil gas export pipeline；
The cyclone separator has gas-solid mixture entrance, gas vent and solid outlet, wherein the gas vent
It is connected with gas mixture outlet, the gas-solid that one end extension of the gas gathering manifold is connected to the cyclone separator is mixed
Close object entrance；
The heat accumulation type radiant tube is along the short transverse multi-tier arrangement of the pyrolysis reactor, and every layer with more in water
Square upwards heat accumulation type radiant tube parallel to each other；
Recirculating fluidized bed, is provided with semicoke entrance, bunker coal entrance and air intake on the recirculating fluidized bed, and described half
Burnt entrance is connected with semicoke outlet.
Inventors have found that pyrolysis of coal reactor of the invention can be directly combined with existing recirculating fluidized bed, without
Existing recirculating fluidized bed is transformed, with existing pyrolysis of coal plug technique-recirculating fluidized bed generating set associated be
System is compared, and in pyrolysis of coal reactor-recirculating fluidized bed combined system of the invention, pyrolysis of coal reactor and recirculating fluidized bed can
It runs relatively independently, the two interferes with each other relatively small.In addition, due to used in pyrolysis of coal reactor heat accumulation type radiant tube for
Pyrolytic process provides heat source, can realize the essence to pyrolytic process by adjusting the flow for the combustion gas for being passed through heat accumulation type radiant tube
True temperature control, and the heat accumulation type radiant tube can be by realizing quickly commutation and heat storage type combustion at both ends, it is ensured that coal heat
The uniformity in temperature field in reactor is solved, so as to significantly improve the fast pyrogenation efficiency of coal charge, with more traditional use gas
Body heat carrier or solid thermal carriers are compared as the pyrolytic reaction device of pyrolysis heat source, and coal pyrolysis reaction device of the invention is not required to
Preheating unit and carrier separative unit are set, fast pyrogenation reaction process process can be greatly simplified, to significantly reduce dress
Dust content is lower in the failure rate and gained tar set, and then can solve existing coal plug leading portion pyrolytic process complexity, and
The problem of fluctuation of service caused by existing pyrolysis reactor and circulating fluidized bed boiler coupling are high.Pyrolysis of coal of the invention
Reactor-recirculating fluidized bed combined system can be effective for producing combustible gas and pyrolysis oil co-production electric power, and utilizes existing
The transportation system of recirculating fluidized bed realizes semicoke hot sending, ensures the burning of semicoke, and reduce coal plug process costs.When this hair
Bright pyrolysis of coal reactor-recirculating fluidized bed combined system is for when generating electricity, it can be ensured that the stability of electricity generation system.Especially need
It is noted that pyrolysis of coal inside reactor is provided with cyclone separator, whirlwind heat preservation cost and tar condensing are greatly reduced
Block the possibility of pipeline.
In one embodiment of the invention, every layer of heat accumulation type radiant tube includes multiple parallel and is uniformly distributed
Heat accumulation type radiant tube, and each of each heat accumulation type radiant tube and adjacent upper layer and lower layer heat accumulation type radiant tube accumulation of heat
Formula radiant tube is parallel and is in staggered distribution in the short transverse of the pyrolysis of coal reactor.Thus, it is possible to significantly improve coal charge
Fast pyrogenation efficiency, and then improve tar yield.
In one embodiment of the invention, the gas-collecting branch pipe is parallel to each other along the length direction of the gas gathering manifold
Arrangement.
In one embodiment of the invention, the gas-collecting branch pipe is perpendicular to the gas collecting main pipe.
In one embodiment of the invention, the oil gas export pipeline is more along the short transverse of the pyrolysis reactor
Layer arrangement, every layer exports pipeline with more oil gas parallel to each other in the horizontal direction.
In one embodiment of the invention, the export of oil gas described in same layer pipeline is connected to gas collection branch described in same root
Pipe.
In one embodiment of the invention, the oil gas export pipeline and the heat accumulation type radiant tube are arranged in parallel,
And the respective left and right sides of heat accumulation type radiant tube is symmetrically arranged with two oil gas export pipelines.
In one embodiment of the invention, the pipe of oil gas the export pipeline and the neighbouring heat accumulation type radiant tube
Distance is 1/2-3 times that the oil gas exports pipe diameter d between wall.
In one embodiment of the invention, multiple through-holes are provided on the tube wall of the oil gas export pipeline.
In one embodiment of the invention, the multiple through-hole is equal on the length direction of oil gas export pipeline
Even distribution.
In one embodiment of the invention, the outer wall of the cyclone separator and the heat accumulating type spoke adjacent thereto
It penetrates and is welded with support rod between pipe.
In one embodiment of the invention, the pyrolysis of coal reactor-recirculating fluidized bed combined system further wraps
Include: gas mixture after-treatment device, the gas mixture after-treatment device are connected with gas mixture outlet.
In one embodiment of the invention, the gas mixture after-treatment device includes: Oil-gas Separation component, institute
Stating Oil-gas Separation component has gas mixture import, pyrolysis gas outlet and tar outlet, the gas mixture import and institute
Gas mixture outlet is stated to be connected；Pyrolysis gas purification assembly, the pyrolysis gas purification assembly have pyrolysis gas import and combustible gas
Outlet, the pyrolysis gas import are connected with the pyrolysis gas outlet, tar refining component, and the tar refining component has tar
Entrance and oil product outlet, the tar entrance are connected with the tar outlet.
In another aspect of this invention, mentioned-above pyrolysis of coal reactor-recycle stream is utilized the present invention provides a kind of
Change the method for bed combined system processing coal.According to an embodiment of the invention, method includes the following steps:
(1) coal is delivered to the pyrolysis of coal reactor and carries out pyrolysis processing, to obtain semicoke and gas mixture；
(2) semicoke is delivered to the recirculating fluidized bed, the semicoke is made to carry out combustion power generation；And
(3) gas mixture is delivered to the gas mixture after-treatment device to post-process, to obtain
Combustible gas and oil product.
Surprisingly, it was found that in the method, can use pyrolysis of coal reactor and existing recirculating fluidized bed
It is directly combined, without being transformed to existing recirculating fluidized bed, pyrolysis of coal reactor and recirculating fluidized bed can relatively solely
It on the spot runs, the two interferes with each other relatively small.This method can effective for producing combustible gas and pyrolysis oil co-production electric power,
And using existing recirculating fluidized bed transportation system, realize semicoke hot sending, ensure the burning of semicoke, and reduce coal plug technique at
This.Moreover, the gas mixture that pyrolysis of coal generates is before being discharged pyrolysis of coal reactor, by cyclone separator in this method
It is dusted, the heat preservation that can greatly reduce pyrolysis of coal reactor to pipeline between pyrolysis gas mixture rapid condensation device is set
It applies, reduce the thermal insulation area of equipment and reduces system heat tracing energy consumption, while greatly reducing the possibility of tar condensing blocking pipeline.
In one embodiment of the invention, step (3) includes: that (3-1) divides gas mixture progress oil gas
From processing, tar and pyrolysis gas are obtained；The pyrolysis gas is carried out purified treatment by (3-2), obtains combustible gas；(3-3) will be described
Tar carries out refinement treatment, obtains oil product.
The present invention at least has the advantages that
1) radiant tube heating downstriker pyrolysis of coal reactor and recirculating fluidized bed are combined, pyrolysis reactor of the invention is adopted
With heat accumulation type radiant tube combination downlink reactor, belong to indirect heating, such pyrolysis reactor allows and existing circulation
Fluidized bed is directly combined, without existing recirculating fluidized bed is transformed on a large scale.
2) hot semicoke is sent into recirculating fluidized bed, can be improved the capacity usage ratio of electricity generation system.
3) cyclone separator is set in pyrolysis of coal reactor, greatly reduces containing for the gas mixture for the pyrolysis reactor that produces coal
Dust quantity and pyrolysis of coal reactor reduce the guarantor of equipment to the lagging facility of pipeline between pyrolysis gas mixture rapid condensation device
Warm area and reduction system heat tracing energy consumption, while the possibility of tar condensing blocking pipeline is greatly reduced, reduce subsequent tar
Processing cost.
Additional aspect and advantage of the invention will be set forth in part in the description, and will partially become from the following description
Obviously, or practice through the invention is recognized.
Detailed description of the invention
The existing furnace front coal head-drawing process structure schematic diagram of Fig. 1.
Fig. 2 is pyrolysis of coal reactor according to an embodiment of the invention-recirculating fluidized bed combined system structural schematic diagram.
Fig. 3 is pyrolysis of coal reactor-recirculating fluidized bed combined system part-structure of another embodiment according to the present invention
Schematic diagram.
Fig. 4 is pyrolysis of coal reactor in accordance with another embodiment of the present invention-recirculating fluidized bed combined system structural representation
Figure.
Fig. 5 is pyrolysis of coal reactor-recirculating fluidized bed combined system structural representation of further embodiment according to the present invention
Figure.
Fig. 6 is utilization pyrolysis of coal reactor according to an embodiment of the invention-recirculating fluidized bed combined system processing coal
Method flow diagram.
Fig. 7 is utilization pyrolysis of coal reactor in accordance with another embodiment of the present invention-recirculating fluidized bed combined system processing
The flow diagram of the method for coal.
Specific embodiment
The embodiment of the present invention is described below in detail.The embodiments described below is exemplary, and is only used for explaining this hair
It is bright, and be not considered as limiting the invention.Particular technique or condition are not specified in embodiment, according to text in the art
It offers described technology or conditions or is carried out according to product description.Reagents or instruments used without specified manufacturer,
For can be with conventional products that are commercially available.
In the description of the present invention, it is to be understood that, term " center ", " longitudinal direction ", " transverse direction ", " length ", " width ",
" thickness ", "upper", "lower", "front", "rear", "left", "right", "vertical", "horizontal", "top", "bottom", "inner", "outside", " up time
The orientation or positional relationship of the instructions such as needle ", " counterclockwise ", " axial direction ", " radial direction ", " circumferential direction " be orientation based on the figure or
Positional relationship is merely for convenience of description of the present invention and simplification of the description, rather than the device or element of indication or suggestion meaning must
There must be specific orientation, be constructed and operated in a specific orientation, therefore be not considered as limiting the invention.
In addition, term " first ", " second " are used for descriptive purposes only and cannot be understood as indicating or suggesting relative importance
Or implicitly indicate the quantity of indicated technical characteristic.Define " first " as a result, the feature of " second " can be expressed or
Implicitly include at least one this feature.In the description of the present invention, the meaning of " plurality " is at least two, such as two, three
It is a etc., unless otherwise specifically defined.
In the present invention unless specifically defined or limited otherwise, term " installation ", " connected ", " connection ", " fixation " etc.
Term shall be understood in a broad sense, for example, it may be being fixedly connected, may be a detachable connection, or integral；It can be mechanical connect
It connects, is also possible to be electrically connected；It can be directly connected, can also can be in two elements indirectly connected through an intermediary
The interaction relationship of the connection in portion or two elements, unless otherwise restricted clearly.For those of ordinary skill in the art
For, the specific meanings of the above terms in the present invention can be understood according to specific conditions.
In the present invention unless specifically defined or limited otherwise, fisrt feature in the second feature " on " or " down " can be with
It is that the first and second features directly contact or the first and second features pass through intermediary mediate contact.Moreover, fisrt feature exists
Second feature " on ", " top " and " above " but fisrt feature be directly above or diagonally above the second feature, or be merely representative of
First feature horizontal height is higher than second feature.Fisrt feature can be under the second feature " below ", " below " and " below "
One feature is directly under or diagonally below the second feature, or is merely representative of first feature horizontal height less than second feature.
In one aspect of the invention, the present invention provides a kind of pyrolysis of coal reactor-recirculating fluidized bed combined systems.Root
According to the embodiment of the present invention, referring to Fig. 2, which includes pyrolysis of coal reactor 100
And recirculating fluidized bed 200.
According to an embodiment of the invention, pyrolysis of coal reactor 100 has coal entrance 110, semicoke outlet 120 and air-fuel mixture
Object outlet 130.Wherein, coal entrance 110 is set to the top of pyrolysis of coal reactor 100, anti-to pyrolysis of coal suitable for supplying fine coal
It answers in device 100；Gas mixture outlet 130 is set on the roof and/or side wall of pyrolysis of coal reactor 100, is suitable for coal heat
Pyrolysis of coal reactor 100 is discharged in the gas mixture that solution generates；Semicoke outlet 120 is set to the bottom of pyrolysis of coal reactor 100,
Pyrolysis of coal reactor 100 is discharged in semicoke suitable for generating pyrolysis of coal.
According to an embodiment of the invention, it is total to be provided with more oil gas export pipelines 140, gas collections in pyrolysis of coal reactor 100
Pipe 150, more gas-collecting branch pipes 160, heat accumulation type radiant tube 170 and cyclone separator 180.
According to a particular embodiment of the invention, heat accumulation type radiant tube 160 is in the inside of pyrolysis of coal reactor 100 along coal heat
The short transverse multi-tier arrangement of reactor 100 is solved, every layer has more heat accumulation type radiant tubes parallel to each other in the horizontal direction.
According to a particular embodiment of the invention, every layer of heat accumulation type radiant tube 160 includes multiple parallel and equally distributed heat accumulating type spoke
It penetrates pipe and each of each heat accumulation type radiant tube and adjacent upper layer and lower layer heat accumulation type radiant tube heat accumulation type radiant tube is parallel.Root
According to specific example of the invention, heat accumulation type radiant tube can be the round or semicircle radiant tube of DN200~300mm.As a result, may be used
To significantly improve the pyrolysis efficiency of pyrolysis material, and then improve pyrolysis oil yield.
According to a particular embodiment of the invention, the specific set-up mode of heat accumulation type radiant tube 160 is not particularly limited, ability
Field technique personnel can rationally design according to the temperature field that practical pyrolytic reaction needs.In some embodiments of the present invention
In, the specific set-up mode of heat accumulation type radiant tube 160 includes but is not limited to: adjacent 160 or so center spacing of heat accumulation type radiant tube
It can be 300~500mm, adjacent heat accumulation type radiant tube vertical centre spacing can be 400~800mm, the radiation of multilayer heat accumulating type
The number of plies of pipe can be 10-30 layers.It is to be understood that adjacent heat accumulation type radiant tube or so center spacing can be understood as same
Distance on layer between heat accumulation type radiant tube center, and adjacent heat accumulation type radiant tube vertical centre spacing can be understood as above and below adjacent
Distance between the adjacent heat accumulation type radiant tube center of two interlayers.Inventors have found that this kind of structure arrangement can make in reactor
Uniform distribution of temperature field so as to significantly improve the pyrolysis efficiency of material, and then improves the yield of pyrolysis oil.
According to a particular embodiment of the invention, heat accumulation type radiant tube can be unidirectional, gas heat-accumulated type radiant tube, that is, pass through
The heat that heat accumulation type radiant tube tube body generates combustion gas carries out heat supply in a manner of radiating.Specific implementation according to the present invention
, gas control valve (not shown) can be set on heat accumulation type radiant tube.Thus, it is possible to by adjusting gas control valve
The flow for the combustion gas for being passed through heat accumulation type radiant tube is adjusted to realize the accurate temperature controlling to pyrolytic process, so as to significantly improve object
The pyrolysis efficiency of material, and then improve the yield of pyrolysis oil.
Specifically, can realize by adjusting flow for the combustion gas for being passed through heat accumulation type radiant tube etc. to the accurate of pyrolytic process
Temperature control, the independent temperature control of every heat accumulation type radiant tube, and heat accumulation type radiant tube are using the combustion system periodically to commutate, so that individually
The temperature field of heat accumulation type radiant tube is not much different in 30 DEG C, to guarantee the uniformity of reactor temperature field, such as passes through tune
The flow of the whole combustion gas for being passed through heat accumulation type radiant tube makes pyrolysis reactor be divided into three areas from top to bottom, i.e., drying and dehydrating area,
Pyrolysis reaction region, semicoke maturation zone can realize that the temperature range in drying and dehydrating area exists by the control to heat accumulation type radiant tube
680-730 degrees Celsius, thus, it is possible to quickly slough the contained moisture of pyrolysis material, while drying and dehydrating area temperature is slightly higher, can subtract
Few drying and dehydrating section length.Pyrolysis reaction region temperature range can control at 500-650 degrees Celsius, to guarantee the abundant heat of material
Solution, semicoke maturation zone temperature can control at 500-600 degrees Celsius, thus the object that further heating a part is not pyrolyzed completely
Material.
According to an embodiment of the invention, gas gathering manifold 150 adjacent to pyrolysis of coal reactor 100 internal perisporium and be vertically arranged,
One end of gas-collecting branch pipe 160 is connected with gas gathering manifold 150, and the other end is connected to oil gas export pipeline 140.Gas-collecting branch pipe 160
Specific set-up mode be not particularly limited, for example including but be not limited to along the length direction of gas gathering manifold 150 cloth parallel to each other
It sets.Every gas-collecting branch pipe 160 can individually be connected with gas gathering manifold 150, can also two or more gas-collecting branch pipes 160 it is close
One end of gas-collecting branch pipe is connected to gas gathering manifold 150 by same connecting pipe 161.According to an embodiment of the invention, gas collection branch
It can have certain angle between pipe 160 and gas gathering manifold 150, in some specific examples, gas-collecting branch pipe 160 is perpendicular to gas collection master
Pipe 150 is arranged.Be conducive to the quick export of gas mixture as a result,.
According to an embodiment of the invention, oil gas export pipeline 140 is connected with one end of gas-collecting branch pipe 160, and oil gas
Through-hole is provided on the tube wall of delivery line 140.Pipeline is exported by setting oil gas as a result, so that the heat generated in pyrolytic process
Solution oil gas quickly exports, to effectively inhibit oil gas second pyrolysis, improves pyrolysis oil yield.According to an embodiment of the invention, logical
The quantity in hole is not particularly limited, and in some specific examples, is provided with multiple through-holes on the tube wall of oil gas export pipeline 140,
Preferably, multiple through-hole is uniformly distributed on the length direction of oil gas export pipeline 140.Be conducive to gas mixture as a result,
Quickly export.
According to an embodiment of the invention, short transverse multi-tier arrangement of the oil gas export pipeline 140 along pyrolysis reactor 100,
Every layer exports pipeline with more oil gas parallel to each other in the horizontal direction.According to a particular embodiment of the invention, same layer
Oil gas export pipeline 140 is connected to same root gas-collecting branch pipe 160.Thereby, it is possible to concentrate gas mixture, rapidly export.
According to an embodiment of the invention, oil gas export pipeline 140 and heat accumulation type radiant tube 170 are arranged in parallel, and heat accumulating type
The left and right sides of radiant tube 170 is symmetrically arranged with two oil gas export pipelines 140.Inventors have found that by every heat accumulating type
Radiant tube two sides install oil gas and export pipeline, and the gas mixture for being pyrolyzed generation is exported rapidly by exporting pipeline, to have
The second pyrolysis of oil gas is inhibited to effect, and then improves the yield of pyrolysis oil, it is good in economic efficiency.
According to an embodiment of the invention, as shown in figure 3, oil gas export pipeline 140 and neighbouring heat accumulation type radiant tube 170
Distance L is 1/2-3 times that oil gas exports pipe diameter d between tube wall.It is possible thereby to export the pyrolysis air-fuel mixture of generation at once
Object avoids pyrolysis oil-breaking, improves pyrolysis oil yield.
According to an embodiment of the invention, cyclone separator 180 has gas-solid mixture entrance 181, gas vent 182 and consolidates
Body outlet 183, wherein gas vent 182 is connected with gas mixture outlet 120, and the end of gas gathering manifold 150 extends connection
To the gas-solid mixture entrance 181 of the cyclone separator 180.Inventors have found that being revolved by being arranged in pyrolysis of coal inside reactor
Wind separator carries out gas solid separation processing to thermal decomposition product, can be effectively reduced the gas mixture of discharge pyrolysis of coal reactor
Dustiness, the pyrolysis oil gas for the pyrolysis reactor that effectively inhibits to produce coal mixes dust condensation blocking subsequent pipeline and relevant device；
Meanwhile built in cyclone separator in pyrolysis of coal reactor, pyrolysis reactor can be reduced and managed between gas mixture condensing unit
The lagging facility on road reduces the thermal insulation area of equipment and reduces system heat tracing energy consumption.
According to an embodiment of the invention, between the outer wall of cyclone separator 180 and heat accumulation type radiant tube 170 adjacent thereto
It is welded with support rod 181, thus, it is possible to the cyclone separator is firmly fixed to inside pyrolysis reactor.In general, whirlwind point
It, therefore, can be in 180 outer wall of cyclone separator and first layer heat accumulating type spoke from the top that device 180 is set to pyrolysis reactor 100
Penetrate welding support rod 181 between pipe 170.
According to an embodiment of the invention, being additionally provided with needed for heat accumulation type radiant tube burning simultaneously on pyrolysis of coal reactor 100
Fuel, the smoke entrance (not shown) after air and burning, fuel gas inlet and air intake respectively with heat accumulating type spoke
Pipe 170 is penetrated to be connected.The hot fume of generation of burning in heat accumulation type radiant tube can be used for treating the fine coal raw material of pyrolysis and be done
Thus dry and the pre-heat treatment further improves pyrolysis of coal reactor efficiency and efficiency of combustion, and realize comprehensive utilization resource,
Reduce the purpose of energy consumption.
According to an embodiment of the invention, the height and width of pyrolysis of coal reactor 100 are preferably suitable, width can be 2-6 meters,
Height can be controlled by the quantity and spacing of every layer of heat accumulation type radiant tube 170 of control, and the height of usual pyrolysis of coal reactor can
Think 5~20m.Thus, it is possible to realize the complete pyrolysis to material.It will be understood by those skilled in the art that pyrolysis of coal reactor
100 height and width is not limited to above range, and those skilled in the art can flexible choice according to actual needs.
According to an embodiment of the invention, being provided with semicoke entrance 210, bunker coal entrance 220 and sky on recirculating fluidized bed 200
Gas entrance 230, wherein semicoke entrance 210 is connected with semicoke outlet 120, and the semicoke suitable for will generate in pyrolysis of coal reactor supplies
It is respectively adapted to supply fuel into recirculating fluidized bed 200 to recirculating fluidized bed 200, bunker coal entrance 220 and air intake 230
Coal and air, in favor of carrying out combustion power generation.Specifically, recirculating fluidized bed 200 can be carried out using semicoke as sole fuel
Combustion power generation, i.e. bunker coal entrance 220 are closed, and are only supplied semicoke by semicoke entrance 210 and are carried out combustion power generation；Recirculating fluidized bed
200 can also carry out combustion power generation using the mixture of semicoke and coal as fuel, i.e., pass through bunker coal entrance 220 and semicoke simultaneously
Entrance 210 supplies coal into recirculating fluidized bed 200 respectively and semicoke carries out mixed firinor fuel burning power generation.Inventors have found that by by coal
The hot semicoke generated in pyrolysis reactor 100 is directly heat-fed to recirculating fluidized bed 200 and carries out combustion power generation, can not only ensure to follow
The combustion stability of ring fluidized bed 200, and capacity usage ratio can be significantly improved, and work as and utilize the pyrolysis of coal reactor-
Recirculating fluidized bed combined system carries out the stability that can ensure electricity generation system when combustion power generation.
According to an embodiment of the invention, referring to Fig. 4 and Fig. 5, which can be with
Further comprise: gas mixture after-treatment device 400, the gas mixture after-treatment device 400 and pyrolysis of coal reactor 100
Gas mixture outlet 130 be connected.Specifically, gas mixture after-treatment device 400 may include: Oil-gas Separation component
410, pyrolysis gas purification assembly 420 and tar refining component 430.Gas mixture after-treatment device 400 is suitable for obtaining pyrolysis
Gas mixture post-processed, carry out Oil-gas Separation, pyrolysis gas purification and the processing such as tar refining, successively to obtain clean coal
Gas and high added value oil product.
According to an embodiment of the invention, Oil-gas Separation component 410 has gas mixture import 411, pyrolysis gas outlet 412
With tar outlet 413, gas mixture import 411 is connected with the gas mixture of pyrolysis of coal reactor outlet 130, tar outlet
413 are connected with the tar entrance 431 of tar refining component 430, and the Oil-gas Separation component 410 is suitable for that thermogenetic oil gas will be solved
Mixture separation obtains pyrolysis gas and tar, and the concrete mode that Oil-gas Separation component 410 carries out Oil-gas Separation is not particularly limited,
E.g., including but be not limited to condensation, spray etc..
According to an embodiment of the invention, pyrolysis gas purification assembly 420 has pyrolysis gas import 421 and combustible gas outlet 422,
Wherein, pyrolysis gas import 421 is connected with pyrolysis gas outlet 412, and pyrolysis gas purification assembly 420 is suitable for taking off pyrolysis gas
The processes such as sulphur, deamination carry out purified treatment to obtain clean combustible gas.In some embodiments, pyrolysis gas purification assembly 420
It can be set there are two 422 (not shown)s of combustible gas outlet, one of them and the heat accumulating type in pyrolysis of coal reactor radiate
Pipe is connected, and for providing the fuel of heat accumulation type radiant tube combustion heating, realizes the reasonable utilization of thermal decomposition product, and another is pyrolyzed
Gas outlet 422 is used as product gas outlet.
According to an embodiment of the invention, tar refining component 430 has tar entrance 431 and oil product outlet 432,
In, tar entrance 431 is connected with tar outlet 413.The tar refining component 430 is suitable for refining the tar that separation obtains
Processing, to obtain high added value oil product, for example including but be not limited to carry out hydrofinishing to isolated tar.
Coal plug technique is arranged for recirculating fluidized bed in pyrolysis of coal reactor-recirculating fluidized bed combined system of the invention,
Efficiently solve the problems, such as that coal plug leading portion pyrolytic process is complicated, in combined system of the invention pyrolysis of coal reactor can with it is existing
Some recirculating fluidized beds are directly combined, and send hot semicoke by First air, and existing without being transformed to existing recirculating fluidized bed
Some pyrolysis of coal plug technique-systems associated with recirculating fluidized bed generating set are compared, pyrolysis of coal reactor-circulation of the invention
In fluidized bed combined system, pyrolysis of coal reactor and recirculating fluidized bed can be relatively independent run, the two interferes with each other relatively
Smaller, thermal decomposition product rationally utilizes, and cost of electricity-generating substantially reduces.Pyrolysis of coal reactor of the invention-recirculating fluidized bed combination system
System can be effective for producing combustible gas and pyrolysis oil co-production electric power, and utilizes the transportation system of existing recirculating fluidized bed, real
Existing semicoke is heat-fed to recirculating fluidized bed, and retains the combustion system of original recirculating fluidized bed, realizes pyrolysis char and ciculation fluidized
Coal in bed mixes burnings, ensures the stability of circulating fluidized bed combustion, while pyrolysis gas and pyrolytic tar being handled, generation
Combustible gas and prepared tar realize the economic benefit of coal plug as major product.When pyrolysis of coal reactor-recycle stream of the invention
Change bed combined system for when generating electricity, it can be ensured that the stability of electricity generation system.In particular, it should be pointed out that pyrolysis of coal reactor
It is internally provided with cyclone separator, the temperature of pyrolysis of coal gas mixture can be reduced, while reducing the pyrolysis reactor that produces coal
The dustiness of gas mixture, the dust content and tar condensing reduced in subsequent high temperature coal pyrolysis gas Quench tar block pipeline
Possibility, while reduce whirlwind heat preservation cost.
In order to reduce influence of the coal plug to coal powder boiler combustion, combined system of the invention takes heat accumulating type downlink quick
Pyrolysis oven, it is only necessary to be delivered to recirculating fluidized bed the semicoke of generation is hot, be effectively utilized self-contained aobvious of pyrolysis char
Heat, while pyrolysis gas and pyrolytic tar being handled, combustible gas and high added value oil product are generated as major product, realize that coal pulls out
The economic benefit of head.Pyrolysis primary dust removing system (i.e. cyclone separator) is built in pyrolysis reactor simultaneously, is effectively reduced
The dustiness for going out the pyrolysis gas of pyrolysis reactor, the problem of avoiding tar condensation blocking pipeline.
In another aspect of this invention, mentioned-above pyrolysis of coal reactor-recycle stream is utilized the present invention provides a kind of
Change the method for bed combined system processing coal.According to an embodiment of the invention, referring to Fig. 6, method includes the following steps:
S100: coal is delivered to the pyrolysis of coal reactor and carries out pyrolysis processing, to obtain semicoke and gas mixture.
According to an embodiment of the invention, supplying to the partial size of the coal of pyrolysis of coal reactor can be 3 millimeters hereinafter, as a result,
Pyrolysis material is heated evenly in pyrolysis reactor, and pyrolytic reaction efficiency is higher, and pyrolytic tar yield is higher.
According to a particular embodiment of the invention, the temperature on pyrolysis reactor top is 680-730 degrees Celsius, the temperature at middle part
It is 500-650 degrees Celsius, the temperature of lower part is 500-600 degrees Celsius.Specifically, pyrolysis is expected in pyrolysis reactor from top to bottom
Movement is pyrolyzed in drying and dehydrating area and expects successively by top drying and dehydrating area, middle part pyrolysis reaction region and lower part semicoke maturation zone
Moisture quickly is sloughed, then pyrolytic reaction is carried out in pyrolysis reaction region, obtains gas mixture and semicoke, gas mixture passes through
Oil gas export pipeline quickly exports, and collects through gas-collecting branch pipe, gas gathering manifold and supply to the second cyclone separator, after dedusting
Pyrolysis reactor is discharged, obtained semicoke continues to move downwardly into semicoke maturation zone, then exports discharge coal heat by semicoke
Solve reactor.
S200: being delivered to the recirculating fluidized bed for semicoke, and semicoke is made to carry out combustion power generation.
According to an embodiment of the invention, 400-600 degrees Celsius of pyrolysis high-temperature semi-coke is exported from semicoke and is arranged in the step
Out, it send through First air to recirculating fluidized bed, carries out combustion power generation.
S300: being delivered to the gas mixture after-treatment device for the gas mixture and post-process, thus
To combustible gas and oil product.
According to an embodiment of the invention, step S300 may further include following steps referring to Fig. 7: S310: by oil gas
Mixture carries out Oil-gas Separation processing, obtains tar and pyrolysis gas；S320: pyrolysis gas is subjected to purified treatment, obtains combustible gas；
And S330: tar is subjected to refinement treatment, obtains oil product.Thus, it is possible to effectively to thermal decomposition product carry out it is suitable after
Processing obtains clean combustible gas and high added value oil product.
Inventors have found that in the method, can use pyrolysis of coal reactor and be directly combined with existing recirculating fluidized bed,
Without being transformed to existing recirculating fluidized bed, pyrolysis of coal reactor and recirculating fluidized bed can be relatively independent run,
The two interferes with each other relatively small.This method can be effective for producing combustible gas and pyrolysis oil co-production electric power, and utilizes existing
There is the transportation system of recirculating fluidized bed, realizes semicoke hot sending, ensure the burning of semicoke, and reduce coal plug process costs.Moreover,
In this method, the gas mixture that pyrolysis of coal generates is dusted before pyrolysis of coal reactor is discharged by cyclone separator,
The lagging facility of pyrolysis of coal reactor to pipeline between pyrolysis gas mixture rapid condensation device can be greatly reduced, reduction is set
Standby thermal insulation area and reduction system heat tracing energy consumption, while greatly reducing the possibility of tar condensing blocking pipeline.
Referring to Fig. 5 and Fig. 7, detailed description of the present invention pyrolysis of coal reactor-recirculating fluidized bed combined system and benefit
It is described with the working condition for the method that it handles coal.
Specifically, will partial size be crushed to 3 millimeters of fine coal below by coal entrance 110 and is supplied to pyrolysis of coal in advance and reacted
Device 100, fine coal from top to bottom move in pyrolysis of coal reactor 100, and heat is carried out under the temperature field that heat accumulation type radiant tube provides
Solution reaction, generates gas mixture and semicoke.On the one hand, the gas mixture obtained exports the through-hole of pipeline 140 by oil gas
Pipeline 140 is exported into oil gas, pipeline 140 is exported by oil gas and is directed into gas-collecting branch pipe 160, is then collected to gas gathering manifold
150, and cyclone separator 180 is supplied to by gas-solid mixture entrance 181 and carries out gas solid separation processing, isolated solid
It is discharged through solid outlet 183, into pyrolysis of coal reactor 100, isolated gas mixture is through gas vent 182, oil
Gas mixture outlet 130 simultaneously enters progress Oil-gas Separation processing in Oil-gas Separation component 410 by gas mixture entrance 411,
Isolated pyrolysis gas is discharged through pyrolysis gas outlet 412, then enters pyrolysis gas purification assembly 420 through pyrolysis gas import 421,
In pyrolysis gas purification assembly 420, pyrolysis gas carries out the processes such as desulfurization, deamination and carries out purified treatment, obtained purified gas part
Through 422 discharge of combustible gas outlet, combustible gas product is obtained, a part can export 422 supplies to coal heat by another combustible gas
The heat accumulation type radiant tube in reactor is solved, for combustion heating, isolated tar is successively through coke in Oil-gas Separation component 410
Oil export 413 and tar import 431 enter tar refining component 430, add at hydrogen to tar in tar refining component 430
Reason, obtained high added value oil product is through 432 discharge of oil product outlet.On the other hand, the semicoke for being pyrolyzed generation exports 120 rows through semicoke
Produce coal pyrolysis reactor 100, then enters recirculating fluidized bed 200 through semicoke entrance 210, while passing through 220 He of bunker coal entrance
Air intake 230 supplies bunker coal and air into recirculating fluidized bed 200, and semicoke and coal are mixed in recirculating fluidized bed 200
Burn power generation.
Embodiment
Pyrolyzing coal is crushed to partial size 3mm hereinafter, being sent into pyrolysis of coal reactor-recirculating fluidized bed combined system of the invention
It is handled, obtains purified gas and high-quality oil product.Specific steps are referring to above-mentioned to pyrolysis of coal reactor-recycle stream of the invention
Change the description of bed combined system and the working condition using its method for handling coal.Wherein, pyrolysis gas composition is as shown in the table, produces
Raw pyrolysis char temperature is 515 DEG C, by being mixed into circulating fluidized bed combustion power generation with power generation coal.
Compared with the fuel of recirculating fluidized bed all power generation feed coals the case where, the pyrolysis that is discharged from pyrolysis of coal reactor
When semicoke accounts for the 50% of ciculation fluidized bed material total weight, whole system energy utilization efficiency improves 3.83%, purified gas
It converts with the income of coal tar into cost of electricity-generating, cost of electricity-generating reduces about 5.61%.
In the description of the present invention, term " first ", " second " are used for description purposes only, and should not be understood as instruction or dark
Show relative importance or implicitly indicates the quantity of indicated technical characteristic.The feature of " first ", " second " is defined as a result,
It can explicitly or implicitly include one or more of the features.In the description of the present invention, the meaning of " plurality " is two
It is a or more than two, unless otherwise specifically defined.
In the description of this specification, reference term " one embodiment ", " some embodiments ", " example ", " specifically show
The description of example " or " some examples " etc. means specific features, structure, material or spy described in conjunction with this embodiment or example
Point is included at least one embodiment or example of the invention.In the present specification, schematic expression of the above terms are not
It must be directed to identical embodiment or example.Moreover, particular features, structures, materials, or characteristics described can be in office
It can be combined in any suitable manner in one or more embodiment or examples.In addition, without conflicting with each other, the skill of this field
Art personnel can tie the feature of different embodiments or examples described in this specification and different embodiments or examples
It closes and combines.
Although the embodiments of the present invention has been shown and described above, it is to be understood that above-described embodiment is example
Property, it is not considered as limiting the invention, those skilled in the art within the scope of the invention can be to above-mentioned
Embodiment is changed, modifies, replacement and variant.
Claims (13)
1. a kind of pyrolysis of coal reactor-recirculating fluidized bed combined system characterized by comprising
Pyrolysis of coal reactor, the pyrolysis of coal reactor have coal entrance, semicoke outlet and gas mixture outlet, wherein institute
The top that coal entrance is set to the pyrolysis of coal reactor is stated, the gas mixture outlet is set to the pyrolysis of coal reactor
Roof and/or side wall on, semicoke outlet is set to the bottom of the pyrolysis of coal reactor；
More oil gas export pipelines, gas gathering manifold, more gas-collecting branch pipes, heat accumulation type radiant tubes are provided in the pyrolysis reactor
And cyclone separator,
Wherein, the gas gathering manifold adjacent to the pyrolysis of coal reactor internal perisporium and be vertically arranged,
One end of the gas-collecting branch pipe is connected with the gas gathering manifold, and the other end is connected to the oil gas export pipeline；
The cyclone separator has gas-solid mixture entrance, gas vent and solid outlet, wherein the gas vent and institute
It states gas mixture outlet to be connected, one end of the gas gathering manifold extends the gas-solid mixture for being connected to the cyclone separator
Entrance；
The heat accumulation type radiant tube is along the short transverse multi-tier arrangement of the pyrolysis reactor, and every layer with more in level side
Heat accumulation type radiant tube parallel to each other upwards；
Recirculating fluidized bed is provided with semicoke entrance, bunker coal entrance and air intake on the recirculating fluidized bed, and the semicoke enters
Mouth is connected with semicoke outlet,
The oil gas export pipeline and the heat accumulation type radiant tube are arranged in parallel, and the respective left and right two of the heat accumulation type radiant tube
Side is symmetrically arranged with two oil gas export pipelines,
Distance is that the oil gas exports pipeline between the oil gas export pipeline and the tube wall of the neighbouring heat accumulation type radiant tube
1/2-3 times of caliber d.
2. pyrolysis of coal reactor-recirculating fluidized bed combined system according to claim 1, which is characterized in that described in every layer
Heat accumulation type radiant tube includes multiple parallel and equally distributed heat accumulation type radiant tube, and each heat accumulation type radiant tube and phase
Each of adjacent upper layer and lower layer heat accumulation type radiant tube heat accumulation type radiant tube is parallel and along the height of the pyrolysis of coal reactor
It is in staggered distribution on direction.
3. pyrolysis of coal reactor-recirculating fluidized bed combined system according to claim 1, which is characterized in that the gas collection
Branch pipe is arranged parallel to each other along the length direction of the gas gathering manifold.
4. pyrolysis of coal reactor-recirculating fluidized bed combined system according to claim 3, which is characterized in that the gas collection
Branch pipe is perpendicular to the gas gathering manifold.
5. pyrolysis of coal reactor-recirculating fluidized bed combined system according to claim 1, which is characterized in that the oil gas
Pipeline is exported along the short transverse multi-tier arrangement of the pyrolysis reactor, every layer parallel to each other in the horizontal direction with more
Oil gas exports pipeline.
6. pyrolysis of coal reactor-recirculating fluidized bed combined system according to claim 5, which is characterized in that same layer institute
It states oil gas export pipeline and is connected to gas-collecting branch pipe described in same root.
7. pyrolysis of coal reactor-recirculating fluidized bed combined system according to claim 1, which is characterized in that the oil gas
It exports and is provided with multiple through-holes on the tube wall of pipeline.
8. pyrolysis of coal reactor-recirculating fluidized bed combined system according to claim 7, which is characterized in that the multiple
Through-hole is uniformly distributed on the length direction of oil gas export pipeline.
9. pyrolysis of coal reactor-recirculating fluidized bed combined system according to claim 1, which is characterized in that the whirlwind
Support rod is welded between the outer wall of separator and the heat accumulation type radiant tube adjacent thereto.
10. pyrolysis of coal reactor-recirculating fluidized bed combined system according to claim 1, which is characterized in that further packet
It includes:
Gas mixture after-treatment device, the gas mixture after-treatment device are connected with gas mixture outlet.
11. pyrolysis of coal reactor-recirculating fluidized bed combined system according to claim 10, which is characterized in that the oil
Gas mixture after-treatment device includes:
Oil-gas Separation component, the Oil-gas Separation component has gas mixture import, pyrolysis gas outlet and tar outlet, described
Gas mixture import is connected with gas mixture outlet；
There is pyrolysis gas import and combustible gas to export for pyrolysis gas purification assembly, the pyrolysis gas purification assembly, the pyrolysis gas into
Mouth is connected with the pyrolysis gas outlet,
There is tar entrance and oil product to export for tar refining component, the tar refining component, the tar entrance with it is described
Tar outlet is connected.
12. a kind of handle coal using the described in any item pyrolysis of coal reactors of claim 1-11-recirculating fluidized bed combined system
Method characterized by comprising
(1) coal is delivered to the pyrolysis of coal reactor and carries out pyrolysis processing, to obtain semicoke and gas mixture；
(2) semicoke is delivered to the recirculating fluidized bed, the semicoke is made to carry out combustion power generation；
(3) gas mixture is delivered to the gas mixture after-treatment device to post-process, to obtain flammable
Gas and oil product.
13. according to the method for claim 12, which is characterized in that step (3) includes:
The gas mixture is carried out Oil-gas Separation processing by (3-1), obtains tar and pyrolysis gas；
The pyrolysis gas is carried out purified treatment by (3-2), obtains combustible gas；
The tar is carried out refinement treatment by (3-3), obtains oil product.
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