CN106833753A - A kind of up flow type pyrolysis and downstriker gasification coupling prepare the device and method of coal tar oil and gas - Google Patents
A kind of up flow type pyrolysis and downstriker gasification coupling prepare the device and method of coal tar oil and gas Download PDFInfo
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- CN106833753A CN106833753A CN201710032063.9A CN201710032063A CN106833753A CN 106833753 A CN106833753 A CN 106833753A CN 201710032063 A CN201710032063 A CN 201710032063A CN 106833753 A CN106833753 A CN 106833753A
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
- C10J3/58—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels combined with pre-distillation of the fuel
- C10J3/60—Processes
- C10J3/64—Processes with decomposition of the distillation products
- C10J3/66—Processes with decomposition of the distillation products by introducing them into the gasification zone
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
- C10J3/46—Gasification of granular or pulverulent flues in suspension
- C10J3/466—Entrained flow processes
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
- C10J3/46—Gasification of granular or pulverulent flues in suspension
- C10J3/48—Apparatus; Plants
- C10J3/485—Entrained flow gasifiers
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
- C10J3/58—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels combined with pre-distillation of the fuel
- C10J3/60—Processes
- C10J3/62—Processes with separate withdrawal of the distillation products
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
- C10J3/72—Other features
- C10J3/82—Gas withdrawal means
- C10J3/84—Gas withdrawal means with means for removing dust or tar from the gas
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J2300/00—Details of gasification processes
- C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
- C10J2300/0913—Carbonaceous raw material
- C10J2300/0916—Biomass
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J2300/00—Details of gasification processes
- C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
- C10J2300/0913—Carbonaceous raw material
- C10J2300/0916—Biomass
- C10J2300/092—Wood, cellulose
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J2300/00—Details of gasification processes
- C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
- C10J2300/0913—Carbonaceous raw material
- C10J2300/093—Coal
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J2300/00—Details of gasification processes
- C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
- C10J2300/0913—Carbonaceous raw material
- C10J2300/0946—Waste, e.g. MSW, tires, glass, tar sand, peat, paper, lignite, oil shale
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J2300/00—Details of gasification processes
- C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
- C10J2300/0953—Gasifying agents
- C10J2300/0956—Air or oxygen enriched air
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J2300/00—Details of gasification processes
- C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
- C10J2300/0953—Gasifying agents
- C10J2300/0973—Water
- C10J2300/0976—Water as steam
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J2300/00—Details of gasification processes
- C10J2300/16—Integration of gasification processes with another plant or parts within the plant
- C10J2300/1603—Integration of gasification processes with another plant or parts within the plant with gas treatment
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Abstract
The present invention relates to the device and method that a kind of pyrolysis of up flow type and downstriker gasification coupling prepare coal tar oil and gas,Including downstriker entrained-flow reactor and up flow type air flow bed pyrolytic reaction pipe,The high temperature carbonaceous material for producing will be pyrolyzed carries out gasification reaction as gasified raw material,And the coal gas of high temperature for producing that gasifies is pyrolyzed as thermal source to carbonaceous material,That is pyrolysis and gasification intercouples,Without intermediate treatment link,Simplification of flowsheet,Reduce the oxygen consumption in gasification,Substantially increase the utilization rate of carbonaceous material and the yield of coal tar,And the purity of products obtained therefrom is higher,In addition,The present invention takes full advantage of the heat energy of system itself,The thermal efficiency is high,Reach energy-saving purpose,Reduce operating cost,High added value can be produced simultaneously,The oil product of lighting in high yield,And gasification of the invention and pyrolysis share a set of cleaner,Without independent mated dust removing device,That is equipment investment is few,Energy consumption is small,Technological process is simple,It is suitable to industrial applications.
Description
Technical field
The invention belongs to the deep process technology field of carbonaceous material, and in particular to a kind of up flow type pyrolysis and downstriker gasification
Coupling prepares the device and method of coal tar oil and gas.
Background technology
Carbonaceous material pyrolysis is that carbonaceous material is heated under conditions of air is completely cut off, and carbonaceous material is in different temperature
The lower complex process that the physical change and chemical reaction of a row occur, pyrolysis needs substantial amounts of heat, and carbonaceous material pyrolysis is produced
Coal tar, coal gas, while the relatively low high temperature carbonaceous material of the substantial amounts of volatile matter of output, carbonaceous material pyrolysis is carbonaceous material classification
The important channel that sub-prime high-efficiency cleaning is utilized.The speed of pyrolysis is divided into slow pyrolysis, fast pyrogenation and flashing speed oven, pyrolysis
Mode have moving bed pyrolysis, fluidized bed pyrolysis, air flow bed be pyrolyzed, be divided into solid thermal carriers, gas heat carrier, gas by thermophore
Gu heat carrier, the mode of heating is directly heated, has indirectly heat.The yield of the rate of heat addition coal tar higher being pyrolyzed in theory
It is bigger；Hydropyrolysis, coal gas activation pyrolysis can greatly improve the yield of coal tar, and the direct-fired gas-solid heat carrier thermal efficiency is most
Height, directly heats the tar yield highest that the activation pyrolysis of flash air flow bed coal gas is obtained.Carbonaceous material gasification is with gasifying agent pair
Carbonaceous material carries out heat chemistry processing, by the carbon conversion of carbonaceous material for coal gas process, from vaporous form have fixed bed gasification,
Fluidized gasification and entrained flow gasification, have up flow type gasification, downstriker gasification and horizontal mode to gasify, from gasifying agent from flow direction point
Dividing has oxygen-rich gasification and pure oxygen gasification, has dry powder to gasify and coal water slurry gasification from feeding manner point.Different pyrolysis way and not
Same gasification mode combination produces different pyrolytic gasifications combinations.
A kind of pulverized coal pyrolysis of East China science and engineering patent and the method (application number of gasification：201410257589.3), fine coal enters
Air flow bed pyrolysis oven, further pyrolysis generates low-molecular-weight hydrocarbon (methane) and Jiao to pyrogenous origin tar at high temperature
Charcoal, target product is coal gas；The pyrolysis gas method of Nippon Steel's patent coal and the pyrolysis gasifying device (application number of coal：
201180018845.8), target product is coal gas and coal tar, using the whirl wind gasified reaction of up flow type, and the up flow type for connecting
Eddy flow pyrolysis reactor, but the high-temperature semi-coke that gasification reaction is not produced using pyrolytic reaction, entirely using upper flow reactor, and it is direct
Connection, plant investment is big, and energy consumption is higher；Engineering Thermophysics research institute of Chinese Academy of Sciences patent thermal pyrolysis combination method and device (Shen
Please number：201010143097.3) pyrolysis uses low speed circulating fluidized bed, and gasification uses fluid bed, is pyrolyzed the raw coke oven gas and gasification for producing
Separated into cyclone separator after the coal gas mixing of generation, because the gas temperature that gasification is produced is high, the institute of raw coke oven gas will be pyrolyzed
The coal tar oil-breaking for containing, causes the yield of tar to decline to a great extent, and does not have the lighting oil product of high yield；The patent coal of Wu road flood adds
Hydrogen is pyrolyzed the method (application number with gasification coupling：201110021674.6), hydropyrolysis are up flow type fluidized-bed reactor, rich
Hydrogen generator is up flow type cyclone bed reactor, and cyclone separator is respectively adopted, system complex, will using fluidized-bed reactor
Ask material particles larger, belong to fast pyrogenation, oil productivity is low compared with flashing speed oven；A kind of Beijing god's mist middle low temperature coal pyrolysis gas of patent
Change system and pyrolysis gasification method (application number：201510432138.3) pyrolysis is used using fixed bed, moving bed or fluid bed
Raw material particle size is larger, is not belonging to flashing speed oven, and oil yield is low；A kind of carbonaceous material of extension oil patent extracts coal tar with synthesis
Method and device (the patent No. of gas integral：201310306726.3) up flow type pyrolysis reactor and up flow type gasified reverse are used
Device is answered, and carries out gas solid separation, system complex respectively.
To overcome the shortcomings of above-mentioned patent, in the pyrolytic gasification coupled reaction, a kind of carbonaceous material that greatly improves is developed
Utilization rate, improves the yield and concise in technology, small investment of coal tar, the device of the pyrolytic gasification coupling that the thermal efficiency is high, energy consumption is low
And method has great significance and wide market prospects.
The content of the invention
An object of the present invention is to provide a kind of concise in technology, small investment, the up flow type heat that the thermal efficiency is high, energy consumption is low
Solution and downstriker gasification coupling prepare the device of coal tar oil and gas.
The second object of the present invention is to provide a kind of above-mentioned up flow type pyrolysis to prepare coal tar with downstriker gasification coupling
The method of oil and gas, its utilization rate that can greatly improve carbonaceous material improves the yield of coal tar.
To achieve these goals, the technical solution adopted in the present invention is：
This kind of up flow type pyrolysis and downstriker gasification coupling prepare the device of coal tar oil and gas, including gasification reactor,
Gasification reactor is downstriker entrained-flow reactor, its top feed mouth of gasification reactor respectively with oxygen/air pipeline, steam
Pipeline and gasified raw material pipeline communication, bottom ashe outlet connects with ash silo, bottom gas exit passes through air and gas mixer and
Pyrolytic reaction pipe is connected, and the pyrolytic reaction pipe is up flow type air flow bed pyrolytic reaction pipe, the charging aperture and coal of pyrolytic reaction pipe
The outlet of gas blender, the port of export of pyrolytic reaction pipe are extended in dedusting expansion chamber, and the port of export of pyrolytic reaction pipe sets
It is equipped with fast parted hair and fast parted hair is below the raw coke oven gas entrance of multi-cyclone group, the top raw coke oven gas of dedusting expansion chamber goes out
Mouthful it is connected with oil scrubber by filter collector, the gas exit of oil scrubber passes through following for circulating gas pipeline and air and gas mixer
Ring gas entrance is connected；
The dedusting expansion chamber is divided into collection chamber, dedusting cabin, settling bin and intermediate buffer storehouse from top to bottom, is set in dedusting cabin
Multi-cyclone group is equipped with, the end raw coke oven gas outlet of multi-cyclone group is extended in collection chamber, gas collection ceiling
The raw coke oven gas outlet in portion is connected with the entrance of filter collector, and the bottom of dedusting cabin connects with settling bin, the connection of settling bin bottom
Intermediate buffer storehouse, the bottom in intermediate buffer storehouse offers product semicoke discharging opening and circulation semicoke discharging opening, and its circulation semicoke goes out
Material mouth is by the returning charge valve on pipeline and the gasified raw material pipeline communication of gasification reactor；The pyrolytic reaction pipe goes out
Mouth end sequentially passes through intermediate buffer storehouse and settling bin is extended in dedusting cabin.
Further limit, the outlet at bottom of above-mentioned dedusting cabin and settling bin is restrained in the funnel-form that cone angle is 55~75 °
Structure.
Further limit, stripping component is provided with the settling bin, the stripping component includes cone bucket and is arranged on
Cone bucket top and relative with cone bucket bottom taper drainage cone, the ring type steam pipe for being arranged on cone bucket bottom, in cone bucket and taper
Air-vent is offered on drainage cone, one end that one end and taper drainage cone that cone bucket is relatively large in diameter are relatively large in diameter is relative, cone bucket
Cone angle be 55~75 °, taper drainage cone cone angle be 125~105 °.
Further limit, above-mentioned multi-cyclone group is included along pyrolytic reaction pipe peripheral circumferential equally distributed 1
~3 grades of cyclone separator groups, 1 or multiple cyclone separators are included per primary cyclone group.
Further limit, above-mentioned filter collector is film tube type filter collector or gravel bed filter.
Further limit, above-mentioned fast parted hair be umbrella hat type inertia it is fast separately or cloverleaf vortex flow quick separately, three leaf
The lower swing angle of formula vortex flow quick parted hair is 18~25 °, and the ratio between outlet of aperture area and pyrolytic reaction pipe is 0.75~0.85.
A kind of above-mentioned up flow type is pyrolyzed the device for preparing coal tar oil and gas with downstriker gasification coupling and prepares coal tar
The method of oil and gas, it is to comprise the steps of：
(1) high temperature carbonaceous material gasification
Temperature is that 480~750 DEG C of high temperature carbonaceous material together enters as gasified raw material with pure oxygen/air, vapor
Carry out gasification reaction in gasification reactor, the temperature of gasification is 1300~1700 DEG C, pressure be 0.001~8MPa, gas velocity 3~
12m/s, the ash silo that the melting ash after gasification flows downward into bottom with air-flow, coal gas of high temperature is from gasification reaction after gasification reaction
The gas exit discharge of device bottom；
(2) coal gas pyrolysis activation
The coal gas of high temperature discharged from gasification reactor bottom gas exit enters in blender, be 25~80 DEG C with temperature,
Pressure is the circulating gas mixing of 0.001~8MPa, and chilling turns into 750~950 DEG C of mixed gas, while in circulating gas
Methane is by instant activation；
(3) it is pyrolyzed dedusting
The coal gas being activated mixes with from the raw material carbonaceous material of charging aperture feeding pyrolytic reaction pipe in pyrolytic reaction pipe,
Carbonaceous material issues raw pyrolytic reaction in the high temperature action of activation coal gas, and pyrolysis temperature is 480~750 DEG C, pressure and step (1)
Vapor pressure is identical, gas velocity is 5~16m/s, and raw coke oven gas and a large amount of high temperature carbonaceous materials pass through pyrolytic reaction pipe after pyrolytic reaction
The fast parted hair quick separating of the port of export, most of high temperature carbonaceous material falls to the settling bin of dedusting expansion chamber, and few part is thin
After little particle is moved into primary cyclone group with raw coke oven gas through cyclonic separation upwards, secondary cyclone is entered back into
Group is separated, and the gas collection after separation enters dedusting in filter collector in collection chamber through raw coke oven gas outlet, afterwards into oil wash
Tower carries out Oil-gas Separation, the coal tar oil and gas of separation, and a part of coal gas is through circulating gas pipeline into entering in air and gas mixer
Row is recycled, and another part is used as output of products；After being separated through primary cyclone group and secondary cyclone group
The solid material of separation enters settling bin through the flutter valve on dipleg；
(4) sedimentation caching
After pyrolysis temperature be 480~750 DEG C of high temperature carbonaceous material in settling bin by steam stripping, gas part is with famine
Coal gas enters primary cyclone group, and high temperature carbonaceous material enters intermediate buffer storehouse, and a part is former as the gasification of step (1)
Expect to be recycled into gasification reactor, another part is used as output of products.
Gasification condition in step (1) is：The temperature of gasification is 1300~1500 DEG C, pressure is 0.001~8MPa, gas velocity
8~12m/s.
Pyrolytical condition in step (3) is：Pyrolysis temperature is 480~750 DEG C, pressure is identical with step (1) vapor pressure,
Gas velocity is 8~12m/s.
Further limit, described carbonaceous material is lignite, bituminous coal, coal slime, liquefied residue, stalk, oil shale, tire,
Petroleum coke, biomass, waste plastics and any one or a few mixture in other carbonaceous materials.
Up flow type pyrolysis and downstriker gasification coupling that the present invention is provided prepare the device and method of coal tar oil and gas
It is to be coupled using downstriker entrained flow gasification reactor and up flow type air flow bed pyrolytic reaction pipe, the high temperature for producing will be pyrolyzed carbon containing
Material carries out gasification reaction as gasified raw material, and the coal gas of high temperature for producing that gasifies carries out heat as thermal source to carbonaceous material
Solution, i.e. pyrolysis and gasification intercouple, and without intermediate treatment link, simplification of flowsheet reduces the oxygen consumption in gasification, greatly
The utilization rate of carbonaceous material and the yield of coal tar are improve greatly, and the purity of products obtained therefrom is higher, additionally, the present invention is fully
The heat energy of system itself is make use of, the thermal efficiency is high, reach energy-saving purpose, reduce operating cost, while can produce high attached
The oil product of value added, lighting in high yield, and gasification of the invention and pyrolysis share a set of cleaner, without individually supporting
Dust arrester, i.e. equipment investment are few, and energy consumption is small, and technological process is simple, is suitable to industrial applications.
Brief description of the drawings
Fig. 1 is the process chart that up flow type pyrolysis and downstriker gasification coupling process carbonaceous material.
Wherein reference is：
1- gasification reactors, 2- pyrolytic reaction pipes, 3- intermediate buffers storehouse, 4- settling bins, 41- tapers drainage cone, 42- ring types
Steam pipe, 43- cone buckets, 5- dedusting cabins, 51- primary cyclone groups, 52- secondary cyclone groups, 6- collection chambers, 7- is fast
Separately, 8- filter collectors, 9- oil scrubbers, 10- ash silos, 11- air and gas mixers.
Specific embodiment
Technical scheme is further described with embodiment in conjunction with accompanying drawing, but the present invention is not limited only to
Following implementation situations.
As shown in figure 1, up flow type pyrolysis of the invention and downstriker gasification coupling prepare the device of coal tar oil and gas
Be by gasification reactor 1, air and gas mixer 11, ash silo 10, pyrolytic reaction pipe 2, intermediate buffer storehouse 3, settling bin 4, dedusting cabin 5,
Collection chamber 6, fast 7, filter collector 8 and oil scrubber 9 separately are constituted.
Wherein, gasification reactor 1 includes its top feed mouthful, the lime-ash outlet of bottom and gas exit, its top feed mouthful point
Not with oxygen/air pipeline, jet chimney and gasified raw material pipeline communication, bottom ashe outlet is connected by pipeline with ash silo 10
It is logical, the melting ash of generation of gasifying is flowed downward into the ash silo 10 of bottom with air-flow, the gas exit of bottom mixes with coal gas
The gasification gas entrance connection of device 11, the air and gas mixer 11 is additionally provided with circulating gas entrance and mixed gas outlet, and it is followed
Ring gas entry is connected by circulating gas pipeline with the gas exit of oil scrubber 9, and mixed gas is exported and pyrolytic reaction pipe 2
Gas entry is connected, and the feedstock direction of pyrolytic reaction pipe 2 and gasification reactor 1 is conversely, the horizontal feed section of the pyrolytic reaction pipe 2
Carbonaceous material entrance is reserved with, makes the mixed gas of the quenching of air and gas mixer 11 mixed in horizontal feed section with carbonaceous material
Close, and the thermal source being pyrolyzed as carbonaceous material.The up raising section of pyrolytic reaction pipe 2 is extended in dedusting expansion chamber, in pyrolysis
The port of export of reaction tube 2 is provided with fast 7, raw coke oven gas and high temperature carbonaceous material quick separating that realization pyrolysis is produced separately.
Fast parted hair 7 in above-described embodiment can select the fast parted hair of umbrella hat type inertia, it is also possible to select cloverleaf vortex flow quick
Separately, wherein umbrella hat type inertia is fast can further select square toes umbrella crown or round end umbrella crown separately, make the upper of pyrolytic reaction pipe 2
Promoting the circulation of qi is discharged under flowing through umbrella crown top barrier counter steer, and most solid particle is moved downward.Cloverleaf vortex flow quick parted hair
Lower swing angle is 18~25 °, and the ratio between outlet of aperture area and pyrolytic reaction pipe 2 is 0.75~0.85, it is ensured that up gas
Flow through three spouts and flow into three butterfly ring casings, downward eddy flow is formed in ring casing and is discharged from ring casing lower section opening, realize
Gas-solid quick separating.
The dedusting expansion chamber of the present embodiment is divided into collection chamber 6, dedusting cabin 5, settling bin 4 and intermediate buffer storehouse 3 from top to bottom,
The up raising section port of export of pyrolytic reaction pipe 2 sequentially passes through intermediate buffer storehouse 3 and settling bin 4 is extended in dedusting cabin 5, dedusting
The outlet at bottom in storehouse 5 is in funnel-shaped structure, and its cone angle can be adjusted in the range of 55~75 °, preferably 60 ° cone angles of the invention, shape
Into accelerating region, the solid particle for settling separation can speed up sedimentation.Primary cyclone group 51 is provided with dedusting cabin 5
With secondary cyclone group 52, primary cyclone group 51 and secondary cyclone group 52 are along pyrolytic reaction pipe 2
Up raising section peripheral annular distribution, i.e., primary cyclone group 51 is by 2 51 one-tenth of primary cyclone groups, two grades
Cyclone separator group 52 is by 2 52 one-tenth of secondary cyclone groups, 2 primary cyclones and 2 two grades of cyclonic separations
Device is spaced apart, and is uniformly distributed on same circumference.The raw coke oven gas outlet of 2 primary cyclones is corresponded to and 2 respectively
Individual secondary cyclone except dust and gas entrance connection, secondary cyclone raw coke oven gas outlet extend in collection chamber 6, collect
Air chamber 6 is closed, and further dust removal process after raw coke oven gas is discharged in raw coke oven gas outlet is offered at top.
In order to ensure clean-up effect, it is also possible to install three-stage cyclone separator group in dedusting cabin 5, its distribution is former with installation
Reason is identical with one-level, secondary cyclone group 52, i.e. the raw coke oven gas outlet of primary cyclone group 51 and two grades of whirlwind point
From device group 52 except the connection of dust and gas entrance, the raw coke oven gas outlet of secondary cyclone group 52 and removing for three-stage cyclone separator group
Dust and gas entrance is connected, and the raw coke oven gas outlet of three-stage cyclone separator group is extended in collection chamber 6, primary cyclone group 51,
It is distributed on same circumference and height is different, is arranged from bottom to top from one-level to three-level, to meet the up fortune of raw coke oven gas
It is dynamic.The raw coke oven gas outlet of three-stage cyclone separator group is extended in collection chamber 6.
Settling bin 4 is also associated with the bottom of dedusting cabin 5, the upper entrance of settling bin 4 connects with the outlet at bottom of dedusting cabin 5
Logical, the epimere of settling bin 4 forms decanting zone of keeping straight on, outlet at bottom is in funnel-shaped structure and cone angle can be in the range of 55~75 °
Adjustment, the high temperature carbonaceous material after the pyrolysis that dedusting cabin 5 is isolated is deposited in settling bin 4, and stripping group is provided with settling bin 4
Part, i.e. the stripping component are made up of cone bucket 43, ring type steam pipe 42 and taper drainage cone 41, and taper drainage cone 41 is fixed on
The top of cone bucket 43 and it is sleeved on the outer wall of pyrolytic reaction pipe 2, one end that it is relatively large in diameter downwards, is relatively large in diameter with cone bucket 43
Enlarging is just right, the annular that ring type steam pipe 42 is fixed on the bottom of cone bucket 43 and is arranged between cone bucket 43 and the inwall of settling bin 4
In region, the air-vent of a diameter of 1mm or so is offered on the side wall of taper drainage cone 41 and cone bucket 43, control it to breathe freely
Rate be 80~90% or so, make ring type steam pipe 42 vapours sequentially pass through cone bucket 43 and taper drainage cone 41 air-vent justify
Week dispersion, motion upwards, and separate high temperature carbonaceous material is met water vapour and aggravates to bore 41 bafflings through taper drainage, into cone bucket
43, then through the bottom funnel-form outlet discharge of settling bin 4, multiple baffling is formed, steam stripping efficiency is improved, accelerate gas solid separation.More enter
One step, in order to ensure that blanking is smooth, the cone angle of cone bucket is 55~75 °, is preferred with 60 °, the cone angle of taper drainage cone for 125~
105 °, it is preferred with 120 °,.In the bottom of settling bin 4 connection intermediate buffer storehouse 3, the high temperature carbonaceous material of sedimentation enters intermediate buffer
Storehouse 3 is cached, and product semicoke discharging opening and circulation semicoke discharging opening are offered in the bottom in intermediate buffer storehouse 3, and its circulation semicoke goes out
, by the returning charge valve on pipeline and the gasified raw material pipeline communication of gasification reactor 1, product semicoke discharging opening will for material mouth
High temperature carbonaceous material product is discharged.
The top raw coke oven gas outlet of collection chamber 6 of above-mentioned dedusting expansion chamber is connected by pipeline with the entrance of filter collector 8,
The raw coke oven gas outlet of filter collector 8 is connected by pipeline with oil scrubber 9, by the further Oil-gas Separation of raw coke oven gas after filtering,
Oil scrubber 9 includes gas exit and tar outlet, gas exit following by circulating gas pipeline and air and gas mixer 11 respectively
The connection of ring gas entrance, by output of products pipe by coal gas output of products, tar outlet discharge tar.
It should be noted that first, the gasification reactor 1 in the present invention is using downstriker gas from gasification reactor 1
Fluidized bed reactor, pyrolytic reaction pipe 2 is from up flow type air flow bed pyrolytic reaction pipe 2, downstriker entrained-flow reactor and up flow type
Air flow bed pyrolytic reaction pipe 2 is connected, to cause that the coal gas of high temperature product by the reaction that is gasified totally in gasification reactor 1 is made
It is the thermal source of pyrolytic reaction pipe 2, participates in pyrolytic reaction, and is pyrolyzed the high temperature carbonaceous material part for producing as output of products,
A part can as the gasified raw material of gasification reactor 1 so that on the one hand the heat in coal gas of high temperature can be made full use of, separately
On the one hand the required processing step that cooling treatment is carried out to coal gas of high temperature product after the completion of gasification reaction is also eliminated.
Second, the set location of the air and gas mixer 11 is not limited specifically in the present invention, as long as meet setting
Between gasification reactor 1 and pyrolytic reaction pipe 2, a part for final product coal gas is passed through as pyrolysis cyclical coal gas
In pipeline input air and gas mixer 11, mix with the coal gas of high temperature produced after gasification reaction, in the mistake mixed with coal gas of high temperature
The effect of chilling can be produced to coal gas of high temperature in journey, and the methane quilt in pyrolysis cyclical coal gas can also be made in quenching process
Activation.
3rd, the carbonaceous material in the present invention refers to lignite, bituminous coal, coal slime, liquefied residue, stalk, oil shale, wheel
Tire, petroleum coke, biomass, waste plastics and any one or a few mixture in other carbonaceous materials.
Preferably, filter collector 8 is film tube type filter collector 8 or gravel bed filter.Film tube type filter collector 8
The work of dedusting, and above two deduster can be carried out to raw coke oven gas suitable for apparatus of the present invention with gravel bed filter
With working stability, efficiency of dust collection advantage high.
Present invention also offers a kind of pyrolysis with above-mentioned up flow type coal tar oil and gas is prepared with downstriker gasification coupling
The device method for preparing coal tar oil and gas, it is realized by following steps：
(1) high temperature carbonaceous material gasification
Temperature is that 480~750 DEG C of high temperature carbonaceous material together enters as gasified raw material with pure oxygen/air, vapor
Carry out gasification reaction in gasification reactor 1, the temperature of gasification is 1300~1700 DEG C, pressure be 0.001~8MPa, gas velocity 3~
12m/s, the ash silo 10 that the melting ash after gasification flows downward into bottom with air-flow, coal gas of high temperature is from gasified reverse after gasification reaction
The bottom gas exit of device 1 is answered to discharge；
It is preferred that gasification condition is：The temperature of gasification is 1300~1500 DEG C, pressure is 0.001~8MPa, 8~12m/ of gas velocity
S,
(2) coal gas pyrolysis activation
The coal gas of high temperature discharged from the bottom gas exit of gasification reactor 1 enters in blender, be 25~80 DEG C with temperature,
Pressure is the circulating gas mixing of 0.001~8MPa, and chilling turns into 750~950 DEG C of mixed gas, while in circulating gas
Methane is by instant activation；
(3) it is pyrolyzed dedusting
The coal gas being activated is mixed with the raw material carbonaceous material from charging aperture feeding pyrolytic reaction pipe 2 in pyrolytic reaction pipe 2
Close, carbonaceous material issues raw pyrolytic reaction in the high temperature action of activation coal gas, pyrolysis temperature is 480~750 DEG C, pressure and step
(1) vapor pressure is identical, gas velocity is 5~16m/s, and raw coke oven gas and a large amount of high temperature carbonaceous materials pass through pyrolytic reaction after pyrolytic reaction
Fast 7 quick separatings separately of the port of export of pipe 2, most of high temperature carbonaceous material falls to the settling bin 4 of dedusting expansion chamber, few portion
After dividing fine particle to be moved into primary cyclone group 51 upwards with raw coke oven gas through cyclonic separation, two grades of whirlwind are entered back into
Separator group 52 is separated, and the gas collection after separation enters dedusting in filter collector 8 in collection chamber 6 through raw coke oven gas outlet, it
Oil-gas Separation is carried out into oil scrubber 9 afterwards, the coal tar oil and gas of separation, a part of coal gas enters coal gas through circulating gas pipeline
Utilization is circulated in blender 11, another part is used as output of products；Through primary cyclone group 51 and two grades of whirlwind point
The solid material of the separation after the separation of device group 52 enters settling bin 4 through the flutter valve on dipleg；
It is preferred that pyrolytical condition is：Pyrolysis temperature is 480~650 DEG C, gas velocity is 8~12m/s.
(4) sedimentation caching
After pyrolysis temperature be 480~750 DEG C of high temperature carbonaceous material in settling bin 4 by steam stripping, gas part with
Raw coke oven gas enters primary cyclone group 51, and high temperature carbonaceous material enters intermediate buffer storehouse 3, a part of conduct through Multi-level deflector
, into recycling in gasification reactor 1, another part is used as output of products for the gasified raw material of step (1).
It is when coal tar oil and gas is prepared with high temperature carbonaceous material that gasification reaction is anti-with pyrolysis by above-mentioned steps method
Process is answered to be connected, the coal gas of high temperature that gasification reaction is produced directly participates in pyrolytic reaction, coal gas of high temperature after mixing chilling
In heat be effectively used in pyrolytic reaction, it is to avoid the loss of heat is wasted, and reduces the energy consumption of device.Meanwhile,
In quenching process, it is activated for the methane in the pyrolysis cyclical coal gas that mixes with coal gas of high temperature, the methane of activation is in pyrolysis
Can also play a part of to improve pyrolytic reaction efficiency in reaction.The high temperature carbonaceous material discharged as product after pyrolytic reaction
A part is pushed in gasification reaction by vapor, and the oxygen consumption in gasification reaction, safety and environmental protection can be effectively reduced again.
Additionally, gasification reaction is of coupled connections with pyrolytic reaction, after the completion of gasification reaction and pyrolytic reaction are carried out continuously,
Dedusting is carried out to the gaseous product for exporting again, is simplified and is required to after gasification reaction and pyrolytic reaction in the prior art to output
Gaseous product carries out the tedious steps of dedusting, improves production efficiency.
The above, specific embodiment only of the invention, but protection scope of the present invention is not limited thereto, and it is any
Those familiar with the art the invention discloses technical scope in, change or replacement can be readily occurred in, should all contain
Cover within protection scope of the present invention.Therefore, protection scope of the present invention should be based on the protection scope of the described claims.
Claims (10)
1. a kind of up flow type pyrolysis and downstriker gasification coupling prepare the device of coal tar oil and gas, including gasification reactor (1),
It is characterized in that the gasification reactor (1) is downstriker entrained-flow reactor, its top feed mouthful of gasification reactor (1) is respectively
With oxygen/air pipeline, jet chimney and gasified raw material pipeline communication, bottom ashe outlet connected with ash silo (10), bottom
Gas exit is connected by air and gas mixer (11) with pyrolytic reaction pipe (2), and the pyrolytic reaction pipe (2) is up flow type air flow bed
Pyrolytic reaction pipe, the charging aperture of pyrolytic reaction pipe (2) and the outlet of air and gas mixer (11), pyrolytic reaction pipe (2) go out
Mouth end is extended in dedusting expansion chamber, and the port of export of pyrolytic reaction pipe (2) is provided with fast (7) separately and fast (7) separately in multistage
The raw coke oven gas entrance lower section of cyclone separator group, the top raw coke oven gas outlet of dedusting expansion chamber is by filter collector (8) and oil
Tower (9) connection is washed, the gas exit of oil scrubber (9) is connected by circulating gas pipeline with the circulating air entrance of air and gas mixer (11)
It is logical；
The dedusting expansion chamber is divided into collection chamber (6), dedusting cabin (5), settling bin (4) and intermediate buffer storehouse (3) from top to bottom,
Dedusting cabin (5) is provided with multi-cyclone group, and the end raw coke oven gas outlet of multi-cyclone group extends to collection chamber
(6) in, the outlet of raw coke oven gas at the top of collection chamber (6) is connected with the entrance of filter collector (8), the bottom of dedusting cabin (5) with sink
Drop storehouse (4) connection, settling bin (4) bottom connects intermediate buffer storehouse (3), and the bottom of intermediate buffer storehouse (3) offers product semicoke
Discharging opening and circulation semicoke discharging opening, its circulation semicoke discharging opening is by the returning charge valve and gasification reactor on pipeline
(1) gasified raw material pipeline communication；The port of export of the pyrolytic reaction pipe (2) sequentially passes through intermediate buffer storehouse (3) and settling bin
(4) extend in dedusting cabin (5).
2. up flow type pyrolysis according to claim 1 and downstriker gasification coupling prepare the device of coal tar oil and gas, its
It is characterised by：The outlet at bottom of the dedusting cabin (5) and settling bin (4) is restrained in the funnel-shaped structure that cone angle is 55~75 °.
3. up flow type pyrolysis according to claim 2 and downstriker gasification coupling prepare the device of coal tar oil and gas, its
It is characterised by：Stripping component is provided with the settling bin (4), the stripping component includes cone bucket (43) and is arranged on cone bucket
(43) top and relative with cone bucket (43) bottom taper drainage cone (41), be arranged on the ring type steam pipe of cone bucket (43) bottom
(42) air-vent, is offered in cone bucket (43) and taper drainage cone (41), one end and taper that cone bucket (43) is relatively large in diameter
One end that drainage cone (41) is relatively large in diameter is relative, and the cone angle of cone bucket (43) is 55~75 °, and the cone angle of taper drainage cone (41) is
125~105 °.
4. up flow type pyrolysis according to claim 1 and downstriker gasification coupling prepare the device of coal tar oil and gas, its
It is characterised by：The multi-cyclone group is included along equally distributed 1~3 grade of rotation of pyrolytic reaction pipe (2) peripheral circumferential
Wind separator group, 1 or multiple cyclone separators are included per primary cyclone group.
5. up flow type pyrolysis according to claim 1 and downstriker gasification coupling prepare the device of coal tar oil and gas, its
It is characterised by：The filter collector (8) is film tube type filter collector or gravel bed filter.
6. up flow type pyrolysis according to claim 1 and downstriker gasification coupling prepare the device of coal tar oil and gas, its
It is characterised by：The fast parted hair (7) be umbrella hat type inertia it is fast separately or cloverleaf vortex flow quick separately, the cloverleaf vortex flow quick
The lower swing angle of parted hair is 18~25 °, and the ratio between outlet of aperture area and pyrolytic reaction pipe (2) is 0.75~0.85.
7. a kind of up flow type with described in any one of claim 1~6 is pyrolyzed and downstriker gasification coupling prepares coal tar and coal
The method that the device of gas prepares coal tar oil and gas, it is characterised in that comprise the steps of：
(1) high temperature carbonaceous material gasification
Temperature is that 480~750 DEG C of high temperature carbonaceous material together enters gasification as gasified raw material and pure oxygen/air, vapor
Carry out gasification reaction in reactor (1), the temperature of gasification is 1300~1700 DEG C, pressure be 0.001~8MPa, gas velocity 3~
12m/s, the ash silo (10) that the melting ash after gasification flows downward into bottom with air-flow, coal gas of high temperature is from gasification after gasification reaction
The gas exit discharge of reactor (1) bottom；
(2) coal gas pyrolysis activation
Enter in blender from the coal gas of high temperature of gasification reactor (1) bottom gas exit discharge, be 25~80 DEG C, pressure with temperature
Power is the circulating gas mixing of 0.001~8MPa, and chilling turns into 750~950 DEG C of mixed gas, while the first in circulating gas
Alkane is by instant activation；
(3) it is pyrolyzed dedusting
The coal gas being activated is mixed with the raw material carbonaceous material from charging aperture feeding pyrolytic reaction pipe (2) in pyrolytic reaction pipe (2)
Close, carbonaceous material issues raw pyrolytic reaction in the high temperature action of activation coal gas, pyrolysis temperature is 480~750 DEG C, pressure and step
(1) vapor pressure is identical, gas velocity is 5~16m/s, and raw coke oven gas and a large amount of high temperature carbonaceous materials pass through pyrolytic reaction after pyrolytic reaction
Fast (7) quick separating separately of pipe (2) port of export, most of high temperature carbonaceous material falls to the settling bin (4) of dedusting expansion chamber,
After few part fine particle is moved into primary cyclone group (51) with raw coke oven gas through cyclonic separation upwards, enter back into
Secondary cyclone group (52) is separated, and the gas collection after separation enters dust removal by filtration in collection chamber (6) through raw coke oven gas outlet
Device (8) interior dedusting, carries out Oil-gas Separation into oil scrubber (9) afterwards, the coal tar oil and gas of separation, and a part of coal gas is through circulation
Gas piping enter air and gas mixer (11) in be circulated utilization, another part is used as output of products；Separated through one cyclonic
The solid material of the separation after device group (51) and secondary cyclone group (52) separation enters settling bin through the flutter valve on dipleg
(4)；
(4) sedimentation caching
After pyrolysis temperature be 480~750 DEG C of high temperature carbonaceous material in settling bin (4) by steam stripping, gas part is with famine
Coal gas enters primary cyclone group (51), and high temperature carbonaceous material enters intermediate buffer storehouse (3), and a part is used as step (1)
Gasified raw material enter gasification reactor (1) in recycle, another part is used as output of products.
8. the processing method of carbonaceous material according to claim 7, it is characterised in that：Gasification condition in step (1) is：
The temperature of gasification is 1300~1500 DEG C, pressure is 0.001~8MPa, 8~12m/s of gas velocity.
9. the method for preparing coal tar oil and gas according to claim 7, it is characterised in that：Pyrolysis bar in step (3)
Part is：Pyrolysis temperature is 480~750 DEG C, pressure is identical with step (1) vapor pressure, gas velocity is 8~12m/s.
10. the method for preparing coal tar oil and gas according to claim 7, it is characterised in that：The step (3) it is carbon containing
Material is lignite, bituminous coal, coal slime, liquefied residue, stalk, oil shale, tire, petroleum coke, biomass, waste plastics and other are carbon containing
Any one or a few mixture in material.
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2018218915A1 (en) * | 2017-05-31 | 2018-12-06 | 河南龙成煤高效技术应用有限公司 | Coal pyrolysis process device |
| CN111621340A (en) * | 2020-06-02 | 2020-09-04 | 新奥科技发展有限公司 | High-efficiency catalytic gasification system and method for coal |
| CN112625755A (en) * | 2019-09-24 | 2021-04-09 | 中国石油化工股份有限公司 | Circulating fluidized bed pulverized coal pyrolysis-gasification device and pulverized coal pyrolysis-gasification method |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1363410A (en) * | 2001-01-11 | 2002-08-14 | 石油大学(北京) | Serial multi-stage process and its compact equipment for fast gas-solid separation and settling |
| CN102876342A (en) * | 2012-10-24 | 2013-01-16 | 金先奎 | Method for producing coal tar through coal dry distillation and producing coal gas through coal semi-coke gasification |
-
2017
- 2017-01-17 CN CN201710032063.9A patent/CN106833753A/en active Pending
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1363410A (en) * | 2001-01-11 | 2002-08-14 | 石油大学(北京) | Serial multi-stage process and its compact equipment for fast gas-solid separation and settling |
| CN102876342A (en) * | 2012-10-24 | 2013-01-16 | 金先奎 | Method for producing coal tar through coal dry distillation and producing coal gas through coal semi-coke gasification |
Non-Patent Citations (2)
| Title |
|---|
| 中国石化集团公司催化裂化情报站等: "《催化裂化协作组第十届年会报告论文选集》", 31 January 2005, 催化裂化协作组 * |
| 尚建选等: "《低阶煤分质转化多联产技术》", 31 May 2013, 煤炭工业出版社 * |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2018218915A1 (en) * | 2017-05-31 | 2018-12-06 | 河南龙成煤高效技术应用有限公司 | Coal pyrolysis process device |
| CN112625755A (en) * | 2019-09-24 | 2021-04-09 | 中国石油化工股份有限公司 | Circulating fluidized bed pulverized coal pyrolysis-gasification device and pulverized coal pyrolysis-gasification method |
| CN111621340A (en) * | 2020-06-02 | 2020-09-04 | 新奥科技发展有限公司 | High-efficiency catalytic gasification system and method for coal |
| CN111621340B (en) * | 2020-06-02 | 2022-01-28 | 新奥科技发展有限公司 | High-efficiency catalytic gasification system and method for coal |
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