CN107674693B - Multistage fluidized bed dedusting pyrolysis reactor and pyrolysis and dedusting coupling process - Google Patents
Multistage fluidized bed dedusting pyrolysis reactor and pyrolysis and dedusting coupling process Download PDFInfo
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- CN107674693B CN107674693B CN201710831359.7A CN201710831359A CN107674693B CN 107674693 B CN107674693 B CN 107674693B CN 201710831359 A CN201710831359 A CN 201710831359A CN 107674693 B CN107674693 B CN 107674693B
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
- C10B53/00—Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form
- C10B53/04—Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form of powdered coal
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
- C10B49/00—Destructive distillation of solid carbonaceous materials by direct heating with heat-carrying agents including the partial combustion of the solid material to be treated
- C10B49/02—Destructive distillation of solid carbonaceous materials by direct heating with heat-carrying agents including the partial combustion of the solid material to be treated with hot gases or vapours, e.g. hot gases obtained by partial combustion of the charge
- C10B49/04—Destructive distillation of solid carbonaceous materials by direct heating with heat-carrying agents including the partial combustion of the solid material to be treated with hot gases or vapours, e.g. hot gases obtained by partial combustion of the charge while moving the solid material to be treated
- C10B49/08—Destructive distillation of solid carbonaceous materials by direct heating with heat-carrying agents including the partial combustion of the solid material to be treated with hot gases or vapours, e.g. hot gases obtained by partial combustion of the charge while moving the solid material to be treated in dispersed form
- C10B49/10—Destructive distillation of solid carbonaceous materials by direct heating with heat-carrying agents including the partial combustion of the solid material to be treated with hot gases or vapours, e.g. hot gases obtained by partial combustion of the charge while moving the solid material to be treated in dispersed form according to the "fluidised bed" technique
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
- 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
Abstract
The present invention relates to a kind of multistage fluidized bed dedusting pyrolysis reactor and pyrolysis and dedusting coupling process, including reactor shell, topmost is provided with fluidisation heat exchange bed in reactor cylinder body, lowest part is provided with soot blowing separation bed, pyrolysis chamber is formed between fluidisation heat exchange bed and soot blowing separation bed, intracavitary at least 1 layer pyrolysis bed is provided with being pyrolyzed, in the bottom of fluidisation heat exchange bed, multi-cyclone is set, it is connected between fluidisation heat exchange bed and the pyrolysis bed of top layer by level-one overflow ducts, it is connected between pyrolysis bed and soot blowing separation bed by second level overflow ducts, multistage pyrolysis bed superposition pyrolysis to reduce load volume and is increased the residence time by the present invention, simultaneously by high temperature raw coke oven gas through the sub- dedusting of multistage cyclone, heat exchange is carried out with cryogenic particles coal again later, the surface for making the heavy molecules of high temperature raw coke oven gas be attached to coal can carry raw coke oven gas secretly Fine breeze sweep along on beans, realize the refined dedusting of raw coke oven gas, greatly improve the efficiency of dust collection of raw coke oven gas, improve product coal tar oil quality, while using the high-temperature semi-coke particle after soot blowing to the further dedusting of raw coke oven gas.
Description
Technical field
The invention belongs to coal chemical industry processing technology fields, and in particular to a kind of multistage fluidized bed dedusting pyrolysis reactor.
Background technique
High-volatile bituminous coal and lignite pyrolysis are the important channels that coal step sub-prime utilizes, and are clean coal chemical technologies,
Pyrolysis of coal plant investment is few, and low energy consumption, and the thermal efficiency is high, and water consumption is few, carbon emission is few, there is extensive market prospects and preferable warp
Ji benefit.
The pyrolytic process used according to coal particle size difference is also different, and the coal of same partial size also has different pyrolytic processes,
In numerous pyrolytic processes, fluidized bed pyrolysis mass-and heat-transfer effect is good, but load volume is big, and bigger pressure is brought to subsequent dedusting,
Make the high temperature raw coke oven gas for being difficult to dedusting originally be more difficult to cope with, at the same single-stage fluidized bed pyrolysis the residence time it is short, can not to compared with
Big particle is pyrolyzed, and needs for coal to be crushed to smaller particle, and the cascade utilization of heat is also not close reasonable.
The macromolecular of high temperature raw coke oven gas coal tar can be condensed carbon distribution, and coal tar will be precipitated after cooling, generally use now
Cyclone dust collectors rough dedusting at high temperature, but the precision of dedusting is not achieved, there are also the thin dirt in part to enter in coal tar in condensation,
Cause coal tar is subsequent utilization can not be further processed.Some use subsequent fine dust collecting process, but since regenerative system is too complicated
It is difficult to long-term operation.
Application No. is a kind of pyrolysis of 201520499924.0 fluidized bed coal for Beijing Lei Hao eco-friendly power source Technology Co., Ltd.
System patent pyrolytic process in fluidized reactor gasification and fluidized-bed reactor is realized using multicompartment fluidized bed reactor
Coupling, but just pyrolysis does not reduce fluidized carrier gas using the area of multistage fluidized bed diminution single-stage fluidized bed to the patented technology
Amount, and rough dedusting is carried out only with cyclone separator to the UTILIZATION OF VESIDUAL HEAT IN of raw coke oven gas, and in terms of dedusting, for being less than 10um
Thin dirt can not be removed by cyclone separator, therefore, be not well solved to the dust-laden problem of coal tar, in coal tar
Olein efficiency of dust collection is difficult to ensure.
Summary of the invention
In order to overcome deficiency present in the fluidized-bed reactor of the prior art, the present invention provides a kind of by pyrolysis and dedusting
It couples and load volume is big, fluidizes the small multistage fluidized bed dedusting pyrolysis reactor of good dedusting effect, energy consumption.
The technical scheme adopted by the invention is that:
The multistage fluidized bed dedusting pyrolysis reactor, including reactor shell 41, in reactor shell 41, topmost is set
Being equipped with can be to fine coal preheating and to the fluidisation heat exchange bed 42 of raw coke oven gas filtering, and lowest part, which is provided with, utilizes high temperature raw coke oven gas half-and-half
The soot blowing separation bed 49 of coke fluidisation soot blowing, forms pyrolysis chamber between fluidisation heat exchange bed 42 and soot blowing separation bed 49, in pyrolysis chamber
It is inside provided at least 1 layer pyrolysis bed 46 that can make fine coal fluidisation pyrolysis, being arranged in the bottom of fluidisation heat exchange bed 42 can be to heat
Solution raw coke oven gas and coal gas of high temperature are dusted, the separation of the multistage cyclone of Oil-gas Separation is combined.
It further limits, beans entrance 4f and raw coke oven gas export mouth 4a is offered at the top of reactor shell 41, anti-
It answers the bottom of device cylinder 41 to offer coal gas of high temperature entrance 4d, is higher than high temperature famine coal in the bottom of reactor shell 41 or side
The position of gas entrance 4d is provided with semicoke discharge port 4e；Between the fluidisation heat exchange bed 42 and pyrolysis bed 46, soot blowing separation bed 49
It is respectively arranged with solid overflow ducts and airflow channel；Position corresponding with pyrolysis bed 46 is opened on the side wall of reactor shell 41
Equipped with pyrolysis high temperature heat source entrance 4b.
It further limits, the multistage cyclone separation combination includes that setting exchanges heat in fluidisation 42 bottom of heat exchange bed and with fluidisation
The multi-cyclone 45 for forming the ring baffle 43 of air-flow caching chamber between bed 42 and being arranged on ring baffle 43, it is multistage
The top of cyclone separator 45 extends to 43 top of ring baffle, and the lower dipleg Oil-gas Separation dust of multi-cyclone 45 goes out
Mouth 4c is extended to outside reactor shell 41.
It further limits, the pyrolysis bed 46 is 2~6 layers.
It further limits, the solid overflow ducts include that connection fluidisation heat exchange bed 42 and the adjacent level-one for being pyrolyzed bed 46 are overflow
It second level overflow ducts 48 between circulation road 44, connection soot blowing separation bed 49 and adjacent pyrolysis bed 46 and is connected to and is pyrolyzed bed two-by-two
Pyrolysis overflow ducts 47 between 46.
It further limits, the level-one overflow ducts 44, pyrolysis overflow ducts 47 and about 48 second level overflow ducts are wrong
Bit distribution.
It further limits, the pyrolysis bed 4-6 and fluidisation heat exchange bed 42 and soot blowing separation bed 49 are obliquely installed and adjacent
The inclined direction of bed is on the contrary, the tilt angle of itself and horizontal plane is 5 °~25 °.
It further limits, the feeding inlet of pyrolysis 47 upper end of overflow ducts is higher than the height of corresponding pyrolysis bed 46；Level-one
The upper end feeding inlet of overflow ducts 44 is higher than 42 height of fluidisation heat exchange bed, and the upper end feeding inlet of second level overflow ducts 48 is higher than most lower
The height of layer pyrolysis bed 46.
Further limit, the feeding inlet of pyrolysis 47 upper end of overflow ducts be higher by 46 surface 80 of corresponding pyrolysis bed~
200mm and lower end is apart from next layer of 46 40~100mm of surface of pyrolysis bed；The upper end feeding inlet of the level-one overflow ducts 44 is higher by
Fluidize the 46 40~100mm of surface of pyrolysis bed of 42 80~200mm of surface of heat exchange bed and lower end apart from top layer；The second level overflow
The upper end feeding inlet in channel 48 is higher by lowest level pyrolysis 46 80~200mm of surface of bed and lower end apart from 49 surface 40 of soot blowing separation bed
~100mm.
It further limits, the pyrolysis bed 46, fluidisation heat exchange bed 42 offer airflow hole, shape on soot blowing separation bed 49
At the airflow channel between adjacent bed；The airflow hole is in the thickness for being pyrolyzed bed 46, fluidisation heat exchange bed 42, soot blowing separation bed 49
Direction inclination, and with pyrolysis bed 46, fluidisation heat exchange bed 42, soot blowing separation bed 49 surface between form 5 °~25 ° of angle, gas
The percent opening of discharge orifice is 5%~25%.
A method of realizing that pyrolysis is coupled with dedusting using above-mentioned multistage fluidized bed dedusting pyrolysis reactor comprising
Following steps: fluidisation heat exchange is carried out to fine coal with fine coal adverse current using coal gas of high temperature from bottom to top, later under the high temperature conditions
Fluidisation pyrolysis is carried out to fine coal, recycles coal gas to carry out adverse current soot blowing to pyrogenous origin semicoke, obtains semicoke product；And simultaneously
The raw coke oven gas that high temperature raw coke oven gas from bottom to top generates in flow process with soot blowing fine powder and pyrolysis revolves after mixing through multistage
Heat exchange cooling is fluidized after wind dust removal process with fine coal, cooling be precipitated of heavy molecules in raw coke oven gas is attached to fine coal surface, fine powder
Dirt is also swept along on fine coal surface as fine coal moves from top to bottom, and then obtains the raw coke oven gas of refined dedusting.
The above method specifically:
(1) the coal gas of high temperature entrance 4d for reacted 41 bottom of device cylinder of high temperature raw coke oven gas that temperature is 480~550 DEG C is under
And it is upper enter in reactor shell 41, carry out fluidisation heat exchange through fluidisation heat exchange bed 42 and fine coal, make fine coal be heated to 360~
380 DEG C, meanwhile, fine coal surface, fine dust, which are attached to, after the cooling precipitation of heavy molecules in coal gas is also swept along on fine coal surface
As fine coal overflow enters pyrolysis chamber through level-one overflow ducts 44；
(2) in pyrolysis chamber, 750~850 DEG C of fine coal and pyrolysis high temperature heat source entrance 4b entrance after step (1) heating
High temperature heat source mixing, and further fluidisation pyrolysis, pyrolysis temperature are 480~650 DEG C, are pyrolyzed the raw coke oven gas of generation with from anti-
Answer the coal gas of high temperature of device cylinder 41 to enter further dedusting in multi-cyclone 45 from bottom to top, after through air-flow cache chamber
It flows through fluidisation heat exchange bed 42 after collecting to cool down, further refined dedusting, later by the raw coke oven gas export mouth at 41 top of reactor shell
4a discharge, obtains the raw coke oven gas of refined dedusting；
(3) semicoke generated after being pyrolyzed enters soot blowing separation bed 49 with second level overflow ducts 48, enters from high temperature raw coke oven gas
The coal gas of high temperature that mouthful 4d enters is from bottom to top in flow process with semicoke adverse current, and air-flow drives dust to realize soot blowing, after soot blowing
Semicoke is discharged as product, and pulverized coal pyrolysis effect, output high-quality semicoke are greatly improved while realizing raw coke oven gas dedusting.
Multistage fluidized bed dedusting pyrolysis reactor of the invention is pyrolyzed multistage pyrolysis bed superposition to reduce load volume simultaneously
Increase the residence time, while by high temperature raw coke oven gas after multi-stage fluidized bed coarse filtration again through the sub- dedusting of multistage cyclone, Zhi Houzai
Heat exchange is carried out with the cryogenic particles coal after drying, the heavy molecules of high temperature raw coke oven gas is made to be attached to the table of coal since cooling is precipitated
Face can by raw coke oven gas carry secretly fine breeze sweep along on fine coal, not only can with recovery section waste heat again can further dedusting, realize famine
The refined dedusting of coal gas greatly improves the efficiency of dust collection of raw coke oven gas, and the semicoke after soot blowing also can be used as the filtrate of further refined dedusting,
Furthermore the present invention can also improve the quality of product coal tar, accomplish pyrolysis and dedusting by macromolecular tar by being pyrolyzed again
Coupling, filtrate take full advantage of the waste heat of raw coke oven gas, significantly reduce the energy consumption of device, also save without regeneration and heating
Investment.
Detailed description of the invention
Fig. 1 is the multistage fluidized bed dedusting pyrolysis reactor structural schematic diagram of the embodiment of the present invention 1.
Fig. 2 is the multistage fluidized bed dedusting pyrolysis reactor structural schematic diagram of the embodiment of the present invention 2.
Fig. 3 is the structural schematic diagram of soot blowing separation bed 49.
Specific embodiment
Technical solution of the present invention is further described now in conjunction with drawings and examples.
Embodiment 1
As shown in Figure 1, the multistage fluidized bed dedusting pyrolysis reactor of the present embodiment includes reactor shell 41, in reactor
The top of cylinder 41 offers fine coal entrance 4f and raw coke oven gas export mouth 4a, offers high temperature famine in the bottom of reactor shell 41
Gas entry 4d is provided with fluidisation heat exchange bed 42, lower part in 41 internal upper part of reactor shell and is provided with soot blowing separation bed, fluidizing
Pyrolysis chamber is formd between heat exchange bed 42 and soot blowing separation bed, be pyrolyzed it is intracavitary be provided with 2 layers of pyrolysis bed 46, but pyrolysis bed 46
It can be adjusted between 2~6 layers according to the volume size and process lot size of reactor shell 41.Fluidize heat exchange bed 42 and heat
Solid overflow ducts are respectively arranged between solution bed 46, soot blowing separation bed 49, make solid from top to down by solid overflow ducts
Flowing, solid overflow ducts include connection fluidisation heat exchange bed 42 with it is adjacent be pyrolyzed bed 46 level-one overflow ducts 44, be connected to soot blowing
Separation bed 49 and the adjacent second level overflow ducts 48 being pyrolyzed between bed 46 and the pyrolysis overflow being connected between pyrolysis bed 46 two-by-two
Channel 47；Spacing i.e. between the fluidisation heat exchange bed 42 pyrolysis bed 46 adjacent with lower section is 3000~5000mm, and passes through one
Grade overflow ducts 44 are connected to, and the spacing between soot blowing separation bed 49 and adjacent pyrolysis bed 46 is 500~600mm, and passes through two
Grade overflow ducts 48 are connected to, and the spacing between antipyretic intracavitary adjacent pyrolysis bed 46 is 500~700mm, and is pyrolyzed between bed 46 and leads to
Cross the connection of pyrolysis overflow ducts 47.The spacing between bed can be adjusted according to 41 size of reactor shell two-by-two.In heat
Pyrolysis high temperature heat source entrance pyrolysis high temperature heat source entrance 4b is offered on the side wall of solution chamber to be connected to high-temperature semi-coke channel, makes high temperature
Semicoke, which is mixed as the heat source of pyrolysis with fine coal, occurs pyrolytic reaction, therefore is pyrolyzed high temperature heat source entrance and is pyrolyzed high temperature heat source entrance
4b is preferably disposed on 46 top of pyrolysis bed of top layer.It is corresponding with soot blowing separation bed 49 in the bottom side of the wall of reactor shell 41
Position open up there are two semicoke discharge port 4e, semicoke discharge port 4e can be in the top of soot blowing separation bed 49 along reaction
It opens up multiple on 41 side wall of device cylinder, and is evenly distributed on reactor shell 41, by semicoke discharge port 4e by soot blowing
Reactor shell 41 is discharged in semicoke product after separation.
The bottom of fluidisation heat exchange bed 42 is provided with multistage cyclone separation combination, multistage cyclone separation combination includes annular gear
Plate 43 and multi-cyclone 45, ring baffle 43 are concave plates, and the bottom of fluidisation heat exchange bed 42 is arranged in, makes ring baffle
Air-flow is formed between 43 and fluidisation heat exchange bed 42 and caches chamber, and circular hole is offered at the center of ring baffle 43 and is installed on it
There is multi-cyclone 45, the multi-cyclone 45 of the present embodiment includes one cyclonic and second level Whirlwind cyclone, level-one
Whirlwind cyclone and the series connection of second level Whirlwind cyclone, i.e. the purification gas outlet of one cyclonic are connected to the air inlet of second level Whirlwind cyclone, second level
The purification gas outlet of Whirlwind cyclone extends to the centre bore of ring baffle 43, the feed opening i.e. oil of one cyclonic and second level Whirlwind cyclone
Gas separation dust outlet 4c extends to 41 outside of reactor shell.In order to guarantee shape after the pyrolysis of the heavy molecules in high temperature raw coke oven gas
At lighter molecules, and the raw coke oven gas being pyrolyzed can carry out heat exchange with the fine coal of the fluidisation heat exchange bed 42 on upper layer, and multistage is revolved
The top for being pyrolyzed intracavitary i.e. top layer pyrolysis bed 46 is arranged in wind separator 45, the raw coke oven gas and fluidisation generated through pyrolysis chamber pyrolysis
Raw coke oven gas be mixed into multi-cyclone 45 and carry out primary dust removing and two-stage dust removal through level-one, second level Whirlwind cyclone, remove
Through fluidisation heat exchange bed 4-2 and fine coal heat exchange occurs for raw coke oven gas after dirt, is heated fine coal, through waste coal after raw coke oven gas cooling down
Conductance exports 4a discharge.The whirlwind subseries of multi-cyclone 4-5 can also be adjusted according to except dust quantity size.For
Guarantee reactor shell 41 interior air-flow is smooth, offers item on pyrolysis bed 46 and fluidisation heat exchange bed 42, soot blowing separation bed
Shape airflow hole forms airflow channel；The percent opening of bar shaped airflow hole is 5%~25%.Referring to Fig. 3, bar shaped airflow hole is being pyrolyzed
The thickness direction inclination of bed 46, fluidisation heat exchange bed 42, soot blowing separation bed 49, and with pyrolysis bed 46, fluidisation heat exchange bed 42, soot blowing point
5 °~25 ° of angle is formed between surface from bed 49, in order to the flowing of solid material, high temperature raw coke oven gas enters reactor cylinder
Half focus layer is passed through in body 41 uniformly to circulate from bottom to top by airflow hole, on the one hand the raw coke oven gas of flowing can loose half focus layer,
Its agglomeration is avoided, uniform air distribution, on the other hand, raw coke oven gas pass through half focus layer, and bulky grain is trapped in semicoke, as semicoke is heavy
Drop.
In order to guarantee that raw coke oven gas and fine coal have certain time of contact, and fine coal is evenly distributed under airflow function, above-mentioned
It is the pyrolysis bed of 80~200mm and lower end apart from top layer that the upper end feeding inlet of level-one overflow ducts 44, which is higher by fluidisation heat exchange bed 42,
46 surfaces are 40~100mm；The upper end feeding inlet of the second level overflow ducts 48 be higher by lowest level pyrolysis 46 surface of bed be 80~
Apart from soot blowing separation bed 40~100mm of surface, the upper end feeding inlet for being pyrolyzed overflow ducts 47 is higher by corresponding pyrolysis for 200mm and lower end
It apart from lower layer's pyrolysis 46 surface of bed is 40~100mm that 46 surfaces of bed, which are 80~200mm and lower end,.In addition, the level-one of the present embodiment
Overflow ducts 44, pyrolysis overflow ducts 47, about 48 second level overflow ducts are dislocatedly distributed.
Embodiment 2
As shown in Fig. 2, the multistage fluidized bed dedusting pyrolysis reactor of the present embodiment includes reactor shell 41, in reactor
The top of cylinder 41 offers fine coal entrance 4f and raw coke oven gas export mouth 4a, offers high temperature famine in the bottom of reactor shell 41
Gas entry 4d is provided with fluidisation heat exchange bed 42, lower part in 41 internal upper part of reactor shell and is provided with soot blowing separation bed, fluidizing
Pyrolysis chamber is formd between heat exchange bed 42 and soot blowing separation bed 49, be pyrolyzed it is intracavitary be provided with 2 layers of pyrolysis bed 46, but pyrolysis bed
46 can adjust between 2~6 layers according to the volume size and process lot size of reactor shell 41.Fluidize heat exchange bed 42 with
Pyrolysis bed 46 is respectively arranged with solid overflow ducts between soot blowing separation bed 49, makes solid from upper by solid overflow ducts
Lower flowing, solid overflow ducts include connection fluidisation heat exchange bed 42 with it is adjacent be pyrolyzed bed 46 level-one overflow ducts 44, be connected to and blow
Grey separation bed 49 and the adjacent second level overflow ducts 48 being pyrolyzed between bed 46 and the pyrolysis being connected between pyrolysis bed 46 two-by-two are overflow
Circulation road 47；It fluidizes between heat exchange bed 42 and adjacent pyrolysis bed 46 and is connected to by level-one overflow ducts 44, soot blowing separation bed 49
It is connected between adjacent pyrolysis bed 46 by second level overflow ducts 48, is connected between adjacent pyrolysis bed 46 by pyrolysis overflow ducts 47
It is logical.Pyrolysis high temperature heat source entrance pyrolysis high temperature heat source entrance 4b is offered on the side wall of pyrolysis chamber and high-temperature semi-coke channel connects
It is logical, it mixes high-temperature semi-coke with fine coal as the heat source of pyrolysis and pyrolytic reaction occurs, therefore it is high to be pyrolyzed high temperature heat source entrance pyrolysis
Warm source inlet 4b is preferably disposed on 46 top of pyrolysis bed of top layer.At corresponding 41 bottom of reactor shell of soot blowing separation bed 49
Portion offers semicoke discharge port 4e, and reactor shell 41 is discharged by the semicoke product that semicoke discharge port 4e separates soot blowing.
The pyrolysis bed 46 and fluidisation heat exchange bed 42 and soot blowing separation bed 49 of the present embodiment are obliquely installed, and fluidize heat exchange bed
Inclination side between 42 and adjacent pyrolysis bed 46, soot blowing separation bed 49 and adjacent pyrolysis 46 soot blowing separation bed 49 of bed, pyrolysis bed 46
To on the contrary, tilt angle between horizontal plane be within the scope of 5 °~25 ° it is adjustable, convenient for fine coal under air-flow impetus smoothly
Flowing.In order to guarantee the time of contact of raw coke oven gas and semicoke, the fluidisation heat exchange bed 42 of the present embodiment pyrolysis bed adjacent with lower section
Spacing between 46 is 3000~5000mm, and the spacing between soot blowing separation bed 49 and adjacent pyrolysis bed 46 is 500~600mm,
Spacing between antipyretic intracavitary adjacent pyrolysis bed 46 is 500~700mm.The spacing between bed can be according to reactor cylinder two-by-two
41 size of body is adjusted.
In order to guarantee that 41 interior air-flow of reactor shell is smooth, in pyrolysis bed 46 and fluidisation heat exchange bed 42, soot blowing separation bed 49
On offer bar shaped airflow hole, and percent opening is 5%~25%.Bar shaped airflow hole is being pyrolyzed bed 46, fluidisation heat exchange bed 42, is blowing
The thickness direction of grey separation bed tilts, and 5 ° are formed between the surface of heat exchange bed 42, soot blowing separation bed 49 with being pyrolyzed bed 46, fluidizing
~25 ° of angle, in order to the flowing of solid material.
In order to guarantee that fine coal, semicoke can be evenly distributed on corresponding bed, the level-one overflow ducts 44 of the present embodiment, heat
Solution overflow ducts 47 and second level overflow ducts 48 are dislocatedly distributed up and down along 41 side wall of reactor shell.
The components such as its ring baffle 43, multi-cyclone 45 are same as Example 1, the principle of dedusting pyrolysis coupling with
Embodiment 1 is identical.
Three-stage cyclone separator can also be used for the multi-cyclone 45 in above-described embodiment, i.e., revolved by level-one
Wind, second level Whirlwind cyclone and three-level Whirlwind cyclone are composed in series and the Whirlwind cyclone number of every level-one can be multiple, increasing dedusting
Amount.
Pyrolysis can be achieved with above-described embodiment 1 or 2 multistage fluidized bed dedusting pyrolysis reactor of embodiment to couple with dedusting
Method, comprising the following steps:
Fluidisation heat exchange is carried out to fine coal with fine coal adverse current using high temperature raw coke oven gas from bottom to top, later under the high temperature conditions
Fluidisation pyrolysis is carried out to fine coal, recycles raw coke oven gas to carry out adverse current soot blowing to pyrogenous origin semicoke, obtains semicoke product；And it is same
When the raw coke oven gas mixed pyrolysis that is generated in flow process with soot blowing fine powder and pyrolysis of high temperature raw coke oven gas from bottom to top into one
Step fluidizes heat exchange with fine coal after multilevel cyclone dust collection is handled after so that heavy molecules is cracked into lighter molecules and cools down, in raw coke oven gas
The cooling precipitation of remaining heavy molecules is attached to fine coal surface, fine dust and is also swept along on fine coal surface as fine coal moves from top to bottom
It is dynamic, and then obtain the raw coke oven gas of refined dedusting.
Specifically includes the following steps:
(1) the high temperature raw coke oven gas entrance 4d for reacted 41 bottom of device cylinder of coal gas of high temperature that temperature is 480~550 DEG C is under
And it is upper enter in reactor shell 41, carry out fluidisation heat exchange through fluidisation heat exchange bed 42 and fine coal, make fine coal be heated to 360~
380 DEG C, meanwhile, fine coal surface, fine dust, which are attached to, after the cooling precipitation of heavy molecules in raw coke oven gas is also swept along in fine coal table
Face is pyrolyzed chamber as fine coal overflow enters through level-one overflow ducts 44；
(2) in pyrolysis chamber, 750~850 DEG C of fine coal and pyrolysis high temperature heat source entrance 4b entrance after step (1) heating
High temperature heat source (can be high-temperature semi-coke) mixing, and further fluidisation pyrolysis, pyrolysis temperature be 480~650 DEG C, pyrolysis generate
Raw coke oven gas further remove with entering in multi-cyclone 45 from bottom to top from the high temperature raw coke oven gas of reactor shell 41
Dirt, after through air-flow caching chamber collect after flow through fluidisation heat exchange bed 42 cool down, further refined dedusting, later by reactor shell 41
The raw coke oven gas export mouth 4a at top is discharged, and obtains the raw coke oven gas of refined dedusting；
(3) semicoke generated after being pyrolyzed enters soot blowing separation bed 49 with second level overflow ducts 48, enters from high temperature raw coke oven gas
The coal gas of high temperature that mouthful 4d enters is from bottom to top in flow process with semicoke adverse current, and air-flow drives dust to realize soot blowing, after soot blowing
Semicoke is discharged as product, and pulverized coal pyrolysis effect, output high-quality semicoke are greatly improved while realizing raw coke oven gas dedusting.
Claims (12)
1. a kind of multistage fluidized bed dedusting pyrolysis reactor, including reactor shell (41), which is characterized in that in reactor shell
(41) in, topmost is provided with can be to fine coal preheating and to the fluidisation heat exchange bed (42) of raw coke oven gas filtering, and lowest part is provided with
Using coal gas of high temperature to semicoke fluidisation soot blowing soot blowing separation bed (49), fluidisation heat exchange bed (42) and soot blowing separation bed (49) it
Between formed pyrolysis chamber, be pyrolyzed it is intracavitary be provided at least 1 layer can make fine coal fluidisation pyrolysis pyrolysis bed (46), fluidisation exchange heat
The bottom of bed (42), which is arranged, to be dusted pyrolysis raw coke oven gas and coal gas of high temperature, the multistage cyclone separation group of Oil-gas Separation
It closes.
2. multistage fluidized bed dedusting pyrolysis reactor according to claim 1, it is characterised in that: in reactor shell (41)
Top offer beans entrance (4f) and raw coke oven gas export mouth (4a), offer high-temperature coal in the bottom of reactor shell (41)
Gas entrance (4d) is provided with semicoke in the position of the bottom of reactor shell (41) or side higher than coal gas of high temperature entrance (4d)
Discharge port (4e)；Solid is respectively arranged between the fluidisation heat exchange bed (42) and pyrolysis bed (46), soot blowing separation bed (49) to overflow
Circulation road and airflow channel；Position corresponding with pyrolysis bed (46) offers pyrolysis high temperature on the side wall of reactor shell (41)
Thermal source inlet (4b).
3. multistage fluidized bed dedusting pyrolysis reactor according to claim 1, it is characterised in that: the multistage cyclone separation
Combination includes setting in fluidisation heat exchange bed (42) bottom and keeps off the annular for forming air-flow caching chamber between heat exchange bed (42) is fluidized
The top of plate (43) and the multi-cyclone (45) being arranged on ring baffle (43), multi-cyclone (45) extends
Above to ring baffle (43), the lower dipleg Oil-gas Separation dust outlet (4c) of multi-cyclone (45) extends to reactor
Cylinder (41) is external.
4. multistage fluidized bed dedusting pyrolysis reactor according to claim 1, it is characterised in that: the pyrolysis bed (46) is
2~6 layers.
5. multistage fluidized bed dedusting pyrolysis reactor according to claim 2, it is characterised in that: the solid overflow ducts
Including connection fluidisation heat exchange bed (42) with it is adjacent pyrolysis bed (46) level-one overflow ducts (44), be connected to soot blowing separation bed (49) and
Second level overflow ducts (48) and connection between adjacent pyrolysis bed (46) are pyrolyzed the pyrolysis overflow ducts between bed (46) two-by-two
(47)。
6. multistage fluidized bed dedusting pyrolysis reactor according to claim 5, it is characterised in that: the level-one overflow ducts
(44), overflow ducts (47) are pyrolyzed and second level overflow ducts (48) are dislocatedly distributed up and down.
7. multistage fluidized bed dedusting pyrolysis reactor according to claim 6, it is characterised in that: the pyrolysis bed (46) and
It fluidizes heat exchange bed (42) and soot blowing separation bed (49) is obliquely installed and the inclined direction of adjacent bed is on the contrary, itself and horizontal plane
Tilt angle is 5 °~25 °.
8. multistage fluidized bed dedusting pyrolysis reactor according to claim 5, it is characterised in that: the pyrolysis overflow ducts
(47) feeding inlet of upper end is higher than the height of corresponding pyrolysis bed (46)；The upper end feeding inlet of level-one overflow ducts (44) is higher than fluidisation
Heat exchange bed (42) height, the upper end feeding inlet of second level overflow ducts (48) are higher than the height of lowest level pyrolysis bed (46).
9. multistage fluidized bed dedusting pyrolysis reactor according to claim 8, it is characterised in that: the pyrolysis overflow ducts
(47) feeding inlet of upper end is higher by corresponding pyrolysis bed (46) 80~200mm of surface and lower end apart from next layer of pyrolysis bed (46) surface
40~100mm；The upper end feeding inlet of the level-one overflow ducts (44) be higher by fluidisation heat exchange bed (42) 80~200mm of surface and under
Hold pyrolysis bed (46) 40~100mm of surface apart from top layer；The upper end feeding inlet of the second level overflow ducts (48) is higher by most
Lower layer is pyrolyzed bed (46) 80~200mm of surface and lower end apart from soot blowing separation bed (49) 40~100mm of surface.
10. described in any item multistage fluidized bed dedusting pyrolysis reactors according to claim 1~9, it is characterised in that: the heat
Solution bed (46), fluidisation heat exchange bed (42), soot blowing separation bed offer airflow hole on (49), form the air-flow between adjacent bed
Channel；The airflow hole is tilted in the thickness direction of pyrolysis bed (46), fluidisation heat exchange bed (42), soot blowing separation bed (49), and with
Be pyrolyzed bed (46), fluidisation heat exchange bed (42), soot blowing separation bed (49) surface between form 5 °~25 ° of angle, airflow hole
Percent opening is 5%~25%.
11. a kind of side for realizing that pyrolysis is coupled with dedusting using multistage fluidized bed dedusting pyrolysis reactor described in claim 1
Method, which comprises the following steps: fluidisation is carried out to fine coal with fine coal adverse current using coal gas of high temperature from bottom to top and is changed
Heat carries out fluidisation pyrolysis to fine coal under the high temperature conditions later, and coal gas is recycled to carry out adverse current soot blowing to pyrogenous origin semicoke,
Obtain semicoke product；And the famine that high temperature raw coke oven gas from bottom to top generates in flow process with soot blowing fine powder and pyrolysis simultaneously
Fluidize heat exchange cooling after coal gas mixing with fine coal after multilevel cyclone dust collection is handled, the heavy molecules cooling in raw coke oven gas is precipitated attached
Also swept along on fine coal surface as fine coal moves from top to bottom in fine coal surface, fine dust, and then obtain the famine of refined dedusting
Coal gas.
12. the side according to claim 11 for realizing that pyrolysis is coupled with dedusting using multistage fluidized bed dedusting pyrolysis reactor
Method, which is characterized in that specifically:
(1) the coal gas of high temperature entrance (4d) for reacted device cylinder (41) bottom of high temperature raw coke oven gas that temperature is 480~550 DEG C is under
And it is upper interior into reactor shell (41), fluidisation heat exchange is carried out through fluidisation heat exchange bed (42) and fine coal, fine coal is made to be heated to 360
~380 DEG C, meanwhile, fine coal surface, fine dust, which are attached to, after the cooling precipitation of heavy molecules in coal gas is also swept along in fine coal table
Face is pyrolyzed chamber as fine coal overflow enters through level-one overflow ducts (44)；
(2) in pyrolysis chamber, enter 750~850 DEG C of fine coal and pyrolysis high temperature heat source entrance (4b) after step (1) heating
High temperature heat source mixing, and further fluidisation pyrolysis, pyrolysis temperature are 480~650 DEG C, are pyrolyzed the raw coke oven gas of generation with from reaction
The coal gas of high temperature of device cylinder (41) enters further dedusting in multi-cyclone (45) from bottom to top, after cached through air-flow
Chamber flows through fluidisation heat exchange bed (42) cooling, further refined dedusting, later by the raw coke oven gas at the top of reactor shell (41) after collecting
Export mouth (4a) discharge, obtains the raw coke oven gas of refined dedusting；
(3) semicoke generated after being pyrolyzed enters soot blowing separation bed (49) with second level overflow ducts (48), enters from high temperature raw coke oven gas
The coal gas of high temperature that mouthful (4d) enters is from bottom to top in flow process with semicoke adverse current, and air-flow drives dust to realize soot blowing, after soot blowing
Semicoke as product be discharged, pulverized coal pyrolysis effect, output high-quality semicoke are greatly improved while realizing raw coke oven gas dedusting.
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