CN105062570A - Combined type circulating fluidized bed gasification device and method - Google Patents
Combined type circulating fluidized bed gasification device and method Download PDFInfo
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Abstract
The invention relates to a combined type circulating fluidized bed gasification device and method, and relates to the technical field of fluidized bed gasification. The device and the method are mainly used for gasifying one or more solid carbonaceous matters in organic waste such as gasified coal, petroleum coke, biomass, garbage, sludge and the like or mixtures of the solid carbonaceous matters and other gas and liquid organic matters, higher gasification efficiency is obtained through improvement of raw material adaptability, and clean low-cost fuel gas or synthesis gas is produced. The main technical scheme is that the combined type circulating fluidized bed gasification device comprises a pyrolysis chamber, a gasifying chamber and a cyclone separator which are connected sequentially, wherein a raw material inlet, a pyrolysis gas outlet and a semi-coke outlet are formed in the pyrolysis chamber respectively, and the pyrolysis gas outlet is formed above the semi-coke outlet; a primary air inlet, a pyrolysis gas inlet and a semi-coke inlet are formed in the gasifying chamber, the pyrolysis gas outlet is connected with the pyrolysis gas inlet, and the semi-coke outlet is connected with the semi-coke inlet through an overflow pipe; a gas outlet is formed in the cyclone separator.
Description
Technical field
The present invention relates to fluidized-bed gasification technical field, particularly relate to a kind of combined type circulating fluidized-bed gasification devices and methods therefor.
Background technology
Gasification is the important means of the organic waste clean utilizations such as coal, biomass, rubbish, mud, has been widely used in the fields such as chemical industry, metallurgy, civilian and industrial combustion gas.The performance of gasification technology directly has influence on the sound development of these industries, has very important status at its energy-saving and emission-reduction controlling party mask, is that it realizes the important leverage of national relevant control target.Coal gasification has had the development course of upper a century, and the gasification technology of the organic wastes such as biomass have also been obtained fast development from the eighties in last century.At present, industrialized gasification technology mainly contains fixed bed gasification technology, fluidized-bed gasification technology, entrained flow bed gasification technology.Fixed bed gasification technology is the simplest, also most widely used, but fixed bed is difficult to adapt to large fuel treatment amount, industrial scale is little; Raw material many uses high-quality lump coal, adds fuel cost undoubtedly; Gasification temperature is lower, easily brings the secondary pollution problems such as phenol water, and environmental protection pressure is comparatively large, can not meet national requirements for environmental protection; Fluidized-bed gasification technology is compared with fixed bed, single stove treatment capacity has had remarkable increase, the gasified raw material of small particle size can be processed, component and the calorific value of the combustion gas of producing are more stable, but still containing tar in coal gas, fundamentally do not solve environmental issue, the calorific value of gas is lower simultaneously, in lime-ash, carbon residue content is high, and efficiency of carbon conversion is lower; Entrained flow bed gasification technology is obviously better than fixed bed and fluidized-bed gasification technology in single stove gas production rate, efficiency of carbon conversion etc., relatively be suitable for large-scale Coal Chemical Engineering Project, but its adaptability to raw material aspect is poor, especially the solid carbon organism high for ash oontent, particle diameter is larger is more inapplicable, and specific investment is huge, also limit it to prepare etc. industry application in combustion gas.
Wherein, fixed bed gasification technology, fluidized-bed gasification technology, entrained flow bed gasification technology respectively have quality, but from the extensive feasibility processing wide particle diameter distribute fuel, fluidized-bed gasification technology most competitive power.This technical equipment is simple, is applicable to amplifying.But the various shortcomings of fluidized-bed gasification technology (see described above) make it not be subject to the favor of practical application.For this reason, for overcoming the shortcoming of fluidized-bed gasification technology, more and more receive publicity in conjunction with the two-part gasification process of fluidized-bed reactor (mainly in order to remove tar removing and improve efficiency of carbon conversion) and technique in other gasification process.
Fluidized-bed gasification device of the prior art generally comprises fluidized bed pyrolyzer and airflow bed gasification furnace, and pyrolyzer is connected with vapourizing furnace by a upflow tube.Solid carbon gasified raw material and gasifying gas react in pyrolyzer, generate semicoke and pyrolysis gas.This semicoke and pyrolysis gas enter in vapourizing furnace by same upflow tube, and wherein, semicoke completes being gasified totally of semicoke in vapourizing furnace, and pyrolysis gas completes and removes burnt oil handling in vapourizing furnace, thus produce clean combustion gas.
State in realization in the process of technical scheme, contriver finds that in prior art, at least there are the following problems: enter in vapourizing furnace because of the semicoke and pyrolysis gas that react generation in pyrolyzer by same upflow tube, during long-term operation, fluent meterial in pyrolysis gas such as tar etc. can because the reactions such as generation Pintsch process and semicoke can condense and coking after combining on the tube wall of upflow tube, even block upflow tube, reacted solid product and gaseous product in pyrolyzer is made to be difficult to be circulated in vapourizing furnace smoothly, thus affect the steady running of whole gasification installation, in addition, solid and gaseous product are entered in vapourizing furnace by same upflow tube simultaneously, and the flow field can destroyed in airflow bed gasification furnace is stablized, and then has influence on the gasification performance of airflow bed gasification furnace.In addition, the flying dust that in prior art, cyclonic separator is separated directly and pyrolysis char mix and enter vapourizing furnace, inevitably cause the cross influence between pyrolysis char and returning charge flying dust, cannot fine adjustment and control the internal circulating load of returning charge flying dust, cause the fluctuation of gasification furnace temperature, gasification installation coking or slagging scorification may be there is simultaneously, affect the steady running of device.
Summary of the invention
In view of this, the invention provides a kind of combined type circulating fluidized-bed gasification devices and methods therefor, main purpose is that the product improved in the pyrolysis chamber of gasification installation enters the unobstructed degree in vaporizer, improves the operation stability of gasification installation, obtain the clean fuel gas of high heating value, and realize cleaner production.
For achieving the above object, the present invention mainly provides following technical scheme:
On the one hand, embodiments of the invention provide a kind of combined type circulating fluidized-bed gasification device, comprise connect successively pyrolysis chamber, vaporizer and cyclonic separator;
Described pyrolysis chamber is respectively arranged with feed(raw material)inlet, pyrolysis gas outlet and semicoke outlet, described pyrolysis gas outlet is arranged on the top of described semicoke outlet;
Described vaporizer is respectively arranged with First air entrance, pyrolysis gas entrance and semicoke entrance, described pyrolysis gas outlet is connected with described pyrolysis gas entrance, and described semicoke outlet is connected with described semicoke entrance by upflow tube;
Described cyclonic separator is provided with pneumatic outlet.
The object of the invention to solve the technical problems also can be applied to the following technical measures to achieve further.
Aforesaid combined type circulating fluidized-bed gasification device, also comprises returning charge room;
Described returning charge room exports with the first flying dust on described cyclonic separator and is connected;
Described returning charge room is also respectively arranged with loosening gas entrance and the outlet of the second flying dust;
Described vaporizer is also provided with flying dust entrance, and described flying dust entrance exports with described second flying dust and is connected.
Aforesaid combined type circulating fluidized-bed gasification device, wherein,
Flying dust entrance on described vaporizer is arranged on the below of described semicoke entrance.
Aforesaid combined type circulating fluidized-bed gasification device, wherein,
Described vaporizer comprises three sections of bodys, is respectively:
First body, described first body is respectively equipped with described First air entrance, described pyrolysis gas entrance, described semicoke entrance and described flying dust entrance;
Second body, one end of described second body is connected with one end of described first body;
3rd body, one end of described 3rd body is connected with the other end of described second body, and the other end of described 3rd body is connected with the gas inlet of described cyclonic separator;
Wherein, described first body, described second body and described 3rd body three set gradually from the bottom to top, and the internal diameter of three increases successively.
Aforesaid combined type circulating fluidized-bed gasification device, wherein,
Described first body comprises tube body and is arranged on the first air compartment of described tube body lower end, and the upper end of described tube body is connected with one end of described second body; Described first air compartment is connected with described tube body by the first gas distributor, is communicated with to make the inner and described tube body inside of described first air compartment;
Described first air compartment is provided with described First air entrance;
Described tube body is respectively equipped with described pyrolysis gas entrance, described semicoke entrance and described flying dust entrance.
Aforesaid combined type circulating fluidized-bed gasification device, wherein,
One end of described first body is connected with one end of described second body by the first tapered tube, and the internal diameter of described first tapered tube is the trend increased gradually by the direction of described first body extremely described second body;
And/or,
The other end of described second body is connected with one end of described 3rd body by the second tapered tube, and the internal diameter of described second tapered tube is the trend increased gradually by the direction of described second body extremely described 3rd body.
Aforesaid combined type circulating fluidized-bed gasification device, wherein,
Described second body is also provided with at least one secondary air entrance.
Aforesaid combined type circulating fluidized-bed gasification device, wherein,
Described pyrolysis chamber comprises pyrolysis chamber's body and is arranged on the second air compartment of body lower end, described pyrolysis chamber, and described second air compartment is connected with described pyrolysis chamber body by the second gas distributor, is communicated with described pyrolysis chamber body interior to make described second air compartment inside; Described second air compartment is provided with air intake vent, and described pyrolysis chamber body is respectively equipped with described feed(raw material)inlet, described pyrolysis gas outlet and the outlet of described semicoke;
And/or,
Described returning charge room comprises returning charge room body and is arranged on the 3rd air compartment of body lower end, described returning charge room, described returning charge room body exports with described first flying dust and is connected, described 3rd air compartment is connected with described returning charge room body by the 3rd gas distributor, is communicated with described returning charge room body interior to make described 3rd air compartment inside; Described 3rd air compartment is provided with described loosening gas entrance, and described returning charge room body is provided with the second described flying dust outlet.
On the other hand, embodiments of the invention also provide a kind of combined type circulating fluidized bed gasification method, for above-mentioned combined type circulating fluidized-bed gasification device described in any one with the use of, described combined type circulating fluidized bed gasification method comprises the following steps:
Join in described pyrolysis chamber by solid carbon gasified raw material and the first gasifying gas, described raw material and described first gasifying gas react in described pyrolysis chamber, generate semicoke and pyrolysis gas;
Described semicoke is sent in described vaporizer by the semicoke outlet in described pyrolysis chamber and the semicoke entrance on described vaporizer successively; Send in described vaporizer by the second gasifying gas via the First air entrance on vaporizer, described second gasifying gas and described semicoke react, and generate coal gas;
Described pyrolysis gas is sent in described vaporizer by the pyrolysis gas entrance on the pyrolysis gas outlet in described pyrolysis chamber and described vaporizer successively and carries out detar process;
Coal gas in described vaporizer is sent into dedusting in described cyclonic separator, the pneumatic outlet of the coal gas after dedusting through described cyclonic separator is discharged.
Aforesaid combined type circulating fluidized bed gasification method, wherein,
The particle diameter of described solid carbon gasified raw material is 0-10mm;
And/or the pyrolysis temperature in described pyrolysis chamber is 500-900 DEG C;
And/or the superficial gas velocity of described pyrolysis chamber is 0.5-5.0m/s;
And/or the gasification temperature in described vaporizer is 700-1100 DEG C;
The superficial gas velocity of described vaporizer is 0.5-15.0m/s.
By technique scheme, combined type circulating fluidized-bed gasification devices and methods therefor of the present invention at least has following beneficial effect:
In the technical scheme that the embodiment of the present invention provides, because the pyrolysis gas outlet in pyrolysis chamber is connected with the pyrolysis gas entrance on vaporizer, semicoke outlet in pyrolysis chamber is connected with the semicoke entrance on vaporizer, in pyrolysis chamber, reaction Heat of Formation is vented one's spleen and can be flowed to the upper strata of inside, pyrolysis chamber, and enters vaporizer from the chamber exit being positioned at top, the semicoke that in pyrolysis chamber, reaction generates is positioned at the lower floor of inside, pyrolysis chamber, and enters vaporizer from the semicoke outlet being positioned at below, relative to prior art, should the pyrolysis gas that generate in pyrolysis chamber and semicoke enter separately in vaporizer respectively by two different passages, and both are independent of each other mutually in the process entering vaporizer, thus this pyrolysis gas can not in pyrolysis gas entrance and the coking of pyrolysis gas outlet place when entering in vaporizer separately, same, this semicoke also can not in semicoke entrance and the coking of semicoke exit when entering separately vaporizer, thus make the product in pyrolysis chamber to enter in vaporizer smoothly, and then the product that improve in the pyrolysis chamber of embodiment of the present invention combined type circulating fluidized-bed gasification device enters the unobstructed degree in vaporizer, the operation stability of embodiment of the present invention combined type circulating fluidized-bed gasification device is also better.
In addition, all enter in vaporizer by the same entrance on vaporizer relative to the pyrolysis gas in pyrolysis chamber in prior art and semicoke, the pyrolysis gas that in the embodiment of the present invention, in pyrolysis chamber, reaction generates and semicoke enter in vaporizer from the different entrance of two vaporizer respectively, this pyrolysis gas and semicoke are less to the impact in the flow field in vaporizer respectively, make the flowing field stability in vaporizer better.
Above-mentioned explanation is only the general introduction of technical solution of the present invention, in order to better understand technique means of the present invention, and can be implemented according to the content of specification sheets, coordinates accompanying drawing to be described in detail as follows below with preferred embodiment of the present invention.
Accompanying drawing explanation
Fig. 1 is the structural representation of a kind of combined type circulating fluidized-bed gasification device that one embodiment of the invention provide;
Fig. 2 is the structural representation of the another kind of combined type circulating fluidized-bed gasification device that one embodiment of the invention provide;
Fig. 3 is the structured flowchart of a kind of combined type circulating fluidized bed gasification method that one embodiment of the invention provide.
Embodiment
For further setting forth the present invention for the technique means reaching predetermined goal of the invention and take and effect, below in conjunction with accompanying drawing and preferred embodiment, to according to the embodiment of the present patent application, structure, feature and effect thereof, be described in detail as follows.In the following description, the not necessarily same embodiment that different " embodiment " or " embodiment " refers to.In addition, special characteristic, structure or feature in one or more embodiment can be combined by any suitable form.
As shown in Figure 1, a kind of combined type circulating fluidized-bed gasification device that one embodiment of the present of invention propose, comprise connect successively pyrolysis chamber 30, vaporizer 7 and cyclonic separator 16.Pyrolysis chamber 30 is respectively arranged with feed(raw material)inlet 26, pyrolysis gas outlet 22 and semicoke outlet 23.Pyrolysis gas outlet 22 is arranged on the top of semicoke outlet 23.Vaporizer 7 is respectively arranged with First air entrance 3, pyrolysis gas entrance 21 and semicoke entrance 24.Pyrolysis gas outlet 22 is connected with pyrolysis gas entrance 21, and semicoke outlet 23 is connected with semicoke entrance 24 by upflow tube (not indicating in figure).Cyclonic separator 16 is provided with pneumatic outlet 17.
Above-described embodiment is specifically when implementing, as shown in Figure 1, user can add solid carbon gasified raw material and gasifying gas by feed(raw material)inlet 26 in pyrolysis chamber 30, and solid carbon gasified raw material and gasifying gas react in pyrolysis chamber 30, and Heat of Formation is vented one's spleen and semicoke.This pyrolysis gas enters in vaporizer 7 via pyrolysis gas outlet 22 and pyrolysis gas entrance 21, and this semicoke enters in vaporizer 7 via semicoke entrance 24, upflow tube and semicoke outlet 23.The coal gas that in vaporizer 7, reaction generates, after cyclonic separator 16 is separated, is discharged from the pneumatic outlet 17 of cyclonic separator 16, thus obtains clean combustion gas.
In the technical scheme that above-described embodiment provides, as shown in Figure 1, because the pyrolysis gas outlet 22 in pyrolysis chamber 30 is connected with the pyrolysis gas entrance 21 on vaporizer 7, semicoke outlet 23 in pyrolysis chamber 30 is connected with the semicoke entrance 24 on vaporizer 7, the pyrolysis gas that in pyrolysis chamber 30, reaction generates can flow to the upper strata of inside, pyrolysis chamber 30, and enters vaporizer 7 from the pyrolysis gas outlet 22 being positioned at top, the semicoke that in pyrolysis chamber 30, reaction generates is positioned at the lower floor of inside, pyrolysis chamber 30, and enters vaporizer 7 from the semicoke outlet 23 being positioned at below, relative to prior art, should the pyrolysis gas of generation pyrolysis chamber 30 in and semicoke enter separately in vaporizer 7 respectively by two different passages, and both are independent of each other mutually in the process entering vaporizer 7, thus pyrolysis gas can not in pyrolysis gas entrance 21 and pyrolysis gas outlet 22 place's coking when entering separately in vaporizer 7, same, this semicoke also can not export the coking of 23 places at semicoke entrance 24 and semicoke when entering separately vaporizer 7, thus the product in pyrolysis chamber 30 can be entered in vaporizer 7 smoothly, and then the product that improve in the pyrolysis chamber 30 of embodiment of the present invention combined type circulating fluidized-bed gasification device enters the unobstructed degree in vaporizer 7, the operation stability of embodiment of the present invention combined type circulating fluidized-bed gasification device is also better.
In addition, all enter in vaporizer 7 by the same entrance on vaporizer 7 relative to the pyrolysis gas in pyrolysis chamber in prior art 30 and semicoke, the pyrolysis gas that in the embodiment of the present invention, in pyrolysis chamber 30, reaction generates and semicoke enter in vaporizer 7 from the different entrance of two vaporizer 7 respectively, this pyrolysis gas and semicoke are less to the impact in the flow field in vaporizer 7 respectively, make the flowing field stability in vaporizer 7 better.
Specifically when implementing, as shown in Figure 2, the combined type circulating fluidized-bed gasification device of the embodiment of the present invention can also comprise returning charge room 14.Cyclonic separator 16 is also provided with the first flying dust outlet (not indicating in figure).Returning charge room 14 exports with the first flying dust on cyclonic separator 16 and is connected.Returning charge room 14 is also respectively arranged with loosening gas entrance 12 and the second flying dust outlet 10.Vaporizer 7 is also provided with flying dust entrance 5, and this flying dust entrance 5 exports 10 with the second flying dust on returning charge room 14 and is connected.In the present embodiment, loosening gas can be air, oxygen-rich air, rare gas element (as nitrogen, carbonic acid gas etc.), or water vapor and air, oxygen-rich air mixture, or the mixture of oxygen and water vapor, or the coal gas etc. after purification.
In the above-described embodiments, as shown in Figure 2, the flying dust of combustion gas in vaporizer 7 after cyclonic separator 16 is separated can enter in returning charge room 14 via the first flying dust outlet, loosening gas can be sent in returning charge room 14 via the loosening gas entrance on returning charge room 14 by user, loosening gas sends in vaporizer 7 by the flying dust in returning charge room 14 through the second flying dust outlet 10 and flying dust entrance 5, flying dust continues generating gasification reaction in vaporizer 7, to improve the gasification efficiency of flying dust.Wherein, user can also by controlling the loosening tolerance entered in returning charge room 14, and control flying dust enters the internal circulating load in vaporizer 7 indirectly, to realize pressure equilibrium and the stable operation of system.
Above-mentioned cyclonic separator 16 is a kind of equipment of the separation for gas-solid system or liquid-solid system.Principle of work is tangentially introduce the rotary motion caused by air-flow, makes to have to get rid of compared with the solid particulate of Great inertia centrifugal force or drop to separate to outside wall surface.The concrete structure of cyclonic separator 16 is common technology of the prior art, can choose in the prior art as required, not repeat them here.Wherein, in a concrete application example, aforesaid cyclonic separator 16 can be tornado dust collector, the coal gas of discharging from vaporizer 7 can be carried out dust removal process by tornado dust collector, the flying dust produced can enter in returning charge room 14 via the first flying dust outlet, and the clean fuel gas after dedusting can be discharged via pneumatic outlet 17.
During concrete enforcement, as shown in Figure 2, the first flying dust outlet on aforementioned cyclonic separator 16 can be connected with returning charge room 14 by dipleg 15, with the isolated flying dust of remote conveying warp let-off cyclonic separator 16.
Specifically when implementing, as shown in Figure 2, the flying dust entrance 5 on aforementioned vaporizer 7 can be arranged on the below of semicoke entrance 24.On the one hand, because both semicoke entrance 24 and flying dust entrance 5 are arranged apart, the cross influence between pyrolysis char and returning charge flying dust can effectively be avoided; On the other hand, because the flying dust entrance 5 on vaporizer 7 is positioned at the below of semicoke entrance 24, under the effect of vaporized chemical, semicoke particle is utilized to be greater than the synergy of fly ash granule, the gasification reaction time of effective increase flying dust and reduction coal gas carrying flying dust, make the gasification efficiency of flying dust higher.
Specifically when implementing, as shown in Figure 2, aforesaid vaporizer 7 can comprise three sections of bodys, is respectively the first body 6, second body 8 and the 3rd body 9.First body 6, second body 8 and the 3rd body 9 three set gradually from the bottom to top, and the internal diameter of three increases successively.One end of second body 8 is connected with one end of the first body 6, and the other end of the second body 8 is connected with one end of the 3rd body 9, and the other end of the 3rd body 9 is connected with cyclonic separator 16.The other end of the 3rd body 9 can be provided with pneumatic outlet 19, and the pneumatic outlet 19 that cyclonic separator 16 can be provided with on the body 9 of gas inlet the 18, three is connected with the gas inlet 18 on cyclonic separator 16.First body 6 is respectively equipped with aforesaid First air entrance 3, aforesaid pyrolysis gas entrance 21, aforesaid semicoke entrance 24 and aforesaid flying dust entrance 5.Gasifying gas, pyrolysis gas, semicoke and flying dust all enter in the first body 6 by corresponding entrance, on the one hand, because the first body 6 is positioned at three sections of bodys bottom, the product generated in first body 6 is in the process rising to the 3rd body 9 discharge, generating gasification reaction can be continued, thus extend the time of raw material generating gasification reaction in vaporizer 7, make the gasification of raw material more abundant, gasification efficiency is higher.On the other hand, because the first body 6, second body 8 and the 3rd body 9 three from the bottom to top internal diameter increase successively, make the flow velocity of coal gas from the first body 6 to the 3rd body 9 in the trend reduced gradually, coal dust larger for particle can be separated from coal gas like this, in the reaction of vaporizer 7 internal recycle, make the extended residence time of coal dust in vaporizer 7 simultaneously, enable coal dust generating gasification reaction fully in vaporizer 7, accordingly, the composition of the coal gas of discharging in vaporizer 7 is better.
In the above-described embodiments, as shown in Figure 2, on the one hand, in pyrolysis chamber 30, reacted semicoke enters in vaporizer 7 by the semicoke outlet 23 in pyrolysis chamber 30, reacts produce coal gas with the gasifying gas generating gasification entered from First air entrance 3.This gasifying gas can be air, oxygen-rich air, oxygen, or water vapor and air, oxygen-rich air mixture, or the mixture etc. of oxygen and water vapor.Wherein, the gasifying gas entered in vaporizer 7 via First air entrance 3 can account for the 60-90% of gasifying gas total amount in vaporizer 7.Gasification temperature in vaporizer 7 is 700-1100 DEG C, and the superficial gas velocity of vaporizer 7 controls at 0.5-15.0m/s.On the other hand, the pyrolysis gas outlet 22 of raw gas in pyrolysis chamber 30 produced in pyrolysis chamber 30 enters in vaporizer 7, utilize the waste heat of coal gas of high temperature in vaporizer 7 and the katalysis of semicoke particle, tar in raw gas is carried out Pintsch process, gasification and catalytic reforming reaction, to realize removing of tar.The coal gas that in vaporizer 7, reaction generates enters in cyclonic separator 16 via the 3rd body 9 and carries out dust removal operation.
Specifically when implementing, as shown in Figure 2, aforesaid first body 6 can comprise tube body (not indicating in figure) and be arranged on the first air compartment 2 of tube body lower end.The upper end of tube body is connected with one end of the second body 8.First air compartment 2 is connected with tube body by the first gas distributor 4, and such as the first air compartment 2 can be connected with the bottom of tube body by the first gas distributor 4, and to make, the first air compartment 2 is inner to be communicated with tube body inside.First air compartment 2 is provided with aforesaid First air entrance 3.Tube body is respectively equipped with aforesaid pyrolysis gas entrance 21, aforesaid semicoke entrance 24 and aforesaid flying dust entrance 5.Gasifying gas can enter in vaporizer 7 via from First air entrance 3 and the first gas distributor 4 by user.
Specifically when implementing, as shown in Figure 2, the bottom of aforesaid tube body can be provided with at least one lime-ash outlet 1, to be discharged from this lime-ash outlet 1 by the lime-ash in vaporizer 7.In a concrete application example, the quantity of lime-ash outlet 1 can be multiple, and the plurality of lime-ash exports 1 and is circumferentially evenly distributed in the bottom of tube body, with the technique effect that the lime-ash facilitated bottom vaporizer is discharged.
Specifically when implementing, as shown in Figure 2, one end of aforementioned first body 6 can be connected with one end of the second body 8 by the first tapered tube 71.The internal diameter of this first tapered tube 71 is the trend increased gradually by the direction of the first body 6 to the second body 8.Internal diameter due to the first body 6 is less than the internal diameter of the second body 8, first body 6 is connected with the second body 8 by the first tapered tube 71, make can be level and smooth between the inner chamber of the inner chamber of the first body 6 and the second body 8 transition, thus enable air-flow flow to the second body 8 from the first body 6 reposefully, and then make the flow field in vaporizer 7 more stable.
Here it should be noted that: as shown in Figure 2, the other end of the second body 8 also can be connected with one end of the 3rd body 9 by the second tapered tube 72.The internal diameter of the second tapered tube 72 by the second body 8 to the direction of the 3rd body 9 in the trend increased gradually.Internal diameter due to the second body 8 is less than the internal diameter of the 3rd body 9, second body 8 is connected with the 3rd body 9 by the second tapered tube 72, make can be level and smooth between the inner chamber of the inner chamber of the second body 8 and the 3rd body 9 transition, thus enable air-flow flow to the 3rd body 9 from the second body 8 reposefully, and then make the flow field in vaporizer 7 more stable.
Specifically when implementing, as shown in Figure 2, aforesaid second body 8 can be provided with at least one secondary air entrance 20.User can add gasifying gas again by this secondary air entrance 20, and unreacted completely semicoke can gasify again on the top of vaporizer 7, thus can make full use of the tar content regasified for reducing in combustion gas.In a concrete application example, the quantity of secondary air entrance 20 can be multiple, and the plurality of secondary air entrance 20 is along the circumferential direction evenly distributed on the second body 8.Further, the quantity of secondary air entrance 20 can be 3 to 24, specifically can arrange according to the actual demand of user.
Wherein, the amount entering the gasifying gas of vaporizer 7 through secondary air entrance 20 can account for the 10-40% of gasifying gas total amount in vaporizer stove.
As depicted in figs. 1 and 2, aforesaid pyrolysis chamber 30 has the inner chamber of hollow, pyrolysis gas outlet 22 can be arranged on the top of pyrolysis chamber 30 inner chamber, due to the lighter in weight of pyrolysis gas, pyrolysis gas after flowing to the upper strata of inner chamber the easier pyrolysis gas outlet 22 from being positioned at inner chamber top flow out.Wherein, semicoke outlet 23 can be arranged on the medium position of pyrolysis chamber 30 inner chamber, and the semicoke that in pyrolysis chamber 30, reaction generates, after exceeding semicoke outlet 23, can be spilled in vaporizer 7 from upflow tube.Above-mentioned feed(raw material)inlet 26 can be arranged on the bottom of pyrolysis chamber 30 inner chamber, manually in pyrolysis chamber 30, adds solid carbon gasified raw material to facilitate.Further, the top of aforementioned pyrolysis chamber 30 inner chamber can have pyramidal structure, and the internal diameter of this pyramidal structure is from the bottom to top in the trend reduced gradually, and pyrolysis gas outlet 22 is arranged on the top of pyramidal structure.Wherein, pyramidal structure can lead for pyrolysis gas, is conducive to pyrolysis gas and flows out from the pyrolysis gas outlet 22 on pyramidal structure top.
As shown in Figure 2, pyrolysis chamber 30 can comprise pyrolysis chamber's body 25 and be arranged on the second air compartment 28 of pyrolysis chamber's body 25 lower end.Second air compartment 28 is connected with pyrolysis chamber's body 25 by the second gas distributor 27, and such as the second air compartment 28 is connected with the bottom of pyrolysis chamber's body 25 by the second gas distributor 27, and to make, the second air compartment 28 is inner to be communicated with pyrolysis chamber's body 25 inside.Second air compartment 28 is provided with air intake vent 29.Pyrolysis chamber's body 25 is respectively equipped with aforesaid feed(raw material)inlet 26, aforesaid pyrolysis gas outlet 22 and aforesaid semicoke outlet 23.Feed(raw material)inlet 26, pyrolysis gas outlet 22 and semicoke outlet 23 concrete setting position see above-mentioned description, can not repeat them here.In the present embodiment, gasifying gas can be delivered in pyrolysis chamber's body 25 via the second gas distributor 27 by the air intake vent 29 on the second air compartment 28 by user.This gasifying gas can be air, oxygen-rich air, oxygen, or water vapor and air, oxygen-rich air mixture, or the mixture etc. of oxygen and water vapor.Wherein, the pyrolysis temperature in pyrolysis chamber's body 25 can control at 500-900 DEG C, and the superficial gas velocity of pyrolysis chamber's body 25 can control at 0.5-5.0m/s.Solid carbon gasified raw material generation pyrolysis in gasifying gas and pyrolysis chamber's body 25 and mild-gasification react, and Heat of Formation is vented one's spleen and semicoke.
As shown in Figure 2, returning charge room 14 can comprise returning charge room body and be arranged on the 3rd air compartment 11 of lower end, returning charge room.Returning charge room body exports with the first flying dust of cyclonic separator 16 and is connected.3rd air compartment 11 is connected with returning charge room body by the 3rd gas distributor 13, is communicated with returning charge room body interior to make the 3rd air compartment 11 inside.3rd air compartment 11 is provided with aforesaid loosening gas entrance 12, and returning charge room body is provided with aforesaid second flying dust outlet 10.Loosening gas can enter in the body of returning charge room via the loosening gas entrance 12 on the 3rd air compartment 11 and the 3rd gas distributor 13, and is sent in vaporizer 7 via the second flying dust outlet 10 by intrinsic for returning charge room flying dust.
Here it should be noted that: the first above-mentioned gas distributor 4, second gas distributor 27 and the 3rd gas distributor 13 are all distribution apparatus of gas, its concrete structure is common technology of the prior art, can choose in the prior art as required, not repeat them here.
As shown in Figure 3, embodiments of the invention also provide a kind of combined type circulating fluidized bed gasification method, for combined type circulating fluidized-bed gasification device with the use of.Wherein, combined type circulating fluidized-bed gasification device, comprise connect successively pyrolysis chamber, vaporizer and cyclonic separator; Pyrolysis chamber is respectively arranged with feed(raw material)inlet, pyrolysis gas outlet and semicoke outlet, pyrolysis gas outlet is arranged on the top of semicoke outlet; Vaporizer is respectively arranged with First air entrance, pyrolysis gas entrance and semicoke entrance, pyrolysis gas outlet is connected with pyrolysis gas entrance, and semicoke outlet is connected with semicoke entrance by upflow tube; Cyclonic separator is provided with pneumatic outlet.
Here it should be noted that: combined type circulating fluidized-bed gasification device involved in the present embodiment can adopt the described combined type circulating fluidized-bed gasification apparatus structure in above-described embodiment, concrete realization and principle of work see the corresponding content in above-described embodiment, can repeat no more herein.
The combined type circulating fluidized bed gasification method of above-described embodiment specifically can comprise the following steps:
Step 101: join in pyrolysis chamber 30 by solid carbon gasified raw material and the first gasifying gas, raw material and the first gasifying gas react in pyrolysis chamber 25, generate semicoke and pyrolysis gas.
Step 102: semicoke is sent in vaporizer 7 by the semicoke outlet 23 in pyrolysis chamber 30 and the semicoke entrance 24 on vaporizer 7 successively; Send in vaporizer 7 by the second gasifying gas via the First air entrance 3 on vaporizer 7, the second gasifying gas and semicoke react, and generate coal gas.
Step 103: pyrolysis gas is sent in vaporizer 7 by the pyrolysis gas outlet 22 in pyrolysis chamber 30 and the pyrolysis gas entrance 21 on vaporizer 7 successively and carries out detar process.
Step 104: the coal gas in vaporizer 7 is sent into dedusting in cyclonic separator 16, the pneumatic outlet 17 of the coal gas after dedusting through cyclonic separator 16 is discharged.
In above-mentioned combined type circulating fluidized bed gasification method, the particle diameter of solid carbon gasified raw material is can be 0-10mm.Pyrolysis temperature in pyrolysis chamber can be 500-900 DEG C.The superficial gas velocity of pyrolysis chamber can control at 0.5-5.0m/s.Gasification temperature in vaporizer 7 can be 700-1100 DEG C.The superficial gas velocity of vaporizer 7 can control at 0.5-15.0m/s.
Further, aforesaid combined type circulating fluidized bed gasification method can also comprise the following steps:
Step 105: will send in returning charge room 14 through the isolated flying dust of cyclonic separator 16.
Step 106: add loosening gas in returning charge room 14, continues reaction to be sent to by the flying dust in returning charge room 14 in vaporizer 7.
Further, aforesaid combined type circulating fluidized bed gasification method can also comprise the following steps:
By the secondary air entrance 20 on vaporizer 7, the 3rd gasifying gas is passed in vaporizer 7, unreacted completely semicoke again gasifies with the 3rd gasifying gas in vaporizer 7, generates coal gas, thus can make full use of the tar content regasified for reducing in combustion gas.
Wherein, the gasifying gas entered in vaporizer 7 via First air entrance 3 can account for the 60%-90% of gasifying gas total amount in vaporizer 7.The amount entering the gasifying gas of vaporizer 7 through secondary air entrance 20 can account for the 10%-40% of gasifying gas total amount in vaporizer stove.
Wherein, in a concrete application example, above-mentioned combined type circulating fluidized bed gasification method can comprise:
The solid carbon gasified raw material of 0-6mm is sent into pyrolysis chamber's body 25 by feed(raw material)inlet 26, first gasifying gas enters in pyrolysis chamber's body 25 via air intake vent 29, second gas distributor 27 successively, solid carbon gasified raw material and the first gasifying gas generation pyrolysis and mild-gasification react, wherein, this first gasifying gas can be air, oxygen-rich air, oxygen, or water vapor and air, oxygen-rich air mixture, or the mixture etc. of oxygen and water vapor.Pyrolysis temperature in pyrolysis chamber controls at 800 DEG C, and the superficial gas velocity of pyrolysis chamber's body 25 controls at 2.0m/s.
In pyrolysis chamber's body 25, reacted semicoke enters in vaporizer 7 by semicoke outlet 23 and semicoke entrance 24, second gasifying gas enters in vaporizer 7 via primary air nozzle 3, first gas distributor 4 successively, semicoke and the second gasifying gas generating gasification are reacted and are produced coal gas, this second gasifying gas can be air, oxygen-rich air, oxygen, or water vapor and air, oxygen-rich air mixture, or the mixture etc. of oxygen and water vapor.Wherein, the gasifying gas amount entering vaporizer 7 by First air entrance 3 accounts for 90% of vaporizer 7 gasifying gas total amount.Gasification temperature in vaporizer 7 controls at 800 DEG C, and the superficial gas velocity of vaporizer 7 controls at 5.0m/s.
The raw gas that pyrolysis chamber's body 25 produces enters vaporizer 7 through pyrolysis gas outlet 22 and pyrolysis gas entrance 21, utilize the waste heat of vaporizer 7 coal gas of high temperature and the katalysis of semicoke particle, tar in raw gas is carried out Pintsch process, gasification and catalytic reforming reaction, to realize removing of tar.
The coal gas of vaporizer 7 enters dedusting in cyclonic separator 16 by the pneumatic outlet 19 on vaporizer and the gas inlet 18 on cyclonic separator, coal gas after dedusting is discharged through cyclonic separator pneumatic outlet 17, the flying dust that cyclonic separator 16 dedusting obtains enters returning charge room 14 through dipleg 15, then entered the loosening tolerance of returning charge room 14 by the loosening gas entrance 12 on returning charge room by adjustment, control the internal circulating load that flying dust enters vaporizer 7, to realize pressure equilibrium and the stable operation of system.Wherein, loosening gas can be air, oxygen-rich air, oxygen, or water vapor and air, oxygen-rich air mixture, or the mixture of oxygen and water vapor, or the coal gas etc. after purification.
The lime-ash that in vaporizer 7, gasification produces exports 1 by lime-ash and discharges.The described amount entering the gasifying gas of vaporizer 7 through secondary air entrance 20 accounts for 10% of vaporizer 7 gasifying gas total amount.
According to above embodiment, combined type circulating fluidized-bed gasification devices and methods therefor of the present invention at least has following advantages:
(1) the gasified raw material wide adaptability of combined type circulating fluidized-bed gasification device of the present invention, can gasify brown coal, long-flame coal and dirty coal, also can the organic waste such as gasified bio-matter, rubbish, mud.
(2) gasification of combined type circulating fluidized-bed gasification device of the present invention completes respectively in pyrolysis chamber 30 and vaporizer 7, can according to different gasified raw material, the residence time of gasified raw material in vapourizing furnace 7 is effectively regulated by the coordinative role of pyrolysis chamber 30 and vaporizer 7, effectively improve relative to traditional gasification technology efficiency of carbon conversion, the simultaneously customer service problem of traditional vapourizing furnace Load Regulation difficulty.
(3) combined type circulating fluidized-bed gasification device of the present invention vaporizer 7 by semicoke entrance 21 and flying dust entrance 5 arranged apart, avoid the cross influence between pyrolysis char and returning charge flying dust, can according to the gasification physical property feature of gasified raw material, the internal circulating load of fine adjustment and control returning charge flying dust, effectively can reduce gasification installation coking or slagging scorification risk simultaneously; In addition, the flying dust entrance 5 of vaporizer 7 is positioned at below semicoke entrance 24, under the effect of vaporized chemical, utilizes semicoke particle to be greater than the synergy of fly ash granule, and effectively increase the gasification reaction time of flying dust and reduce coal gas carrying flying dust, gasification efficiency is higher.
(4) raw gas produced in the pyrolysis chamber 30 of combined type circulating fluidized-bed gasification device of the present invention and semicoke enter vaporizer 7 from different entrances respectively, effectively can overcome the coking problem at chamber exit and gasification chamber inlet place, reduce raw gas to the impact in vaporizer flow field simultaneously, ensure the stability of vapourizing furnace; In raw gas, methane content is high, can improve the calorific value of coal gas.
(5) vaporizer 7 of combined type circulating fluidized-bed gasification device of the present invention utilizes the katalysis of pyrolysis chamber's semicoke and returning charge room flying dust that the tar in raw gas is carried out Pintsch process, gasification and catalytic reforming reaction, realize removing of tar, not only increase the calorific value of coal gas, and solve that traditional gasification technology coal gas brings containing tar be difficult in a large number process and the serious wastewater containing phenol and cyanide of environmental pollution and containing the problem to the discharge of the volatile organic waste gas of healthy serious harm such as benzene.
The above, it is only preferred embodiment of the present invention, not do any pro forma restriction to the present invention, any simple modification done above embodiment according to technical spirit of the present invention, equivalent variations and modification, all still belong in the scope of technical solution of the present invention.
Claims (10)
1. a combined type circulating fluidized-bed gasification device, is characterized in that, comprise connect successively pyrolysis chamber, vaporizer and cyclonic separator;
Described pyrolysis chamber is respectively arranged with feed(raw material)inlet, pyrolysis gas outlet and semicoke outlet, described pyrolysis gas outlet is arranged on the top of described semicoke outlet;
Described vaporizer is respectively arranged with First air entrance, pyrolysis gas entrance and semicoke entrance, described pyrolysis gas outlet is connected with described pyrolysis gas entrance, and described semicoke outlet is connected with described semicoke entrance by upflow tube;
Described cyclonic separator is provided with pneumatic outlet.
2. combined type circulating fluidized-bed gasification device as claimed in claim 1, is characterized in that, also comprise returning charge room;
Described returning charge room exports with the first flying dust on described cyclonic separator and is connected;
Described returning charge room is also respectively arranged with loosening gas entrance and the outlet of the second flying dust;
Described vaporizer is also provided with flying dust entrance, and described flying dust entrance exports with described second flying dust and is connected.
3. combined type circulating fluidized-bed gasification device as claimed in claim 2, is characterized in that,
Flying dust entrance on described vaporizer is arranged on the below of described semicoke entrance.
4. combined type circulating fluidized-bed gasification device as claimed in claim 2 or claim 3, is characterized in that,
Described vaporizer comprises three sections of bodys, is respectively:
First body, described first body is respectively equipped with described First air entrance, described pyrolysis gas entrance, described semicoke entrance and described flying dust entrance;
Second body, one end of described second body is connected with one end of described first body;
3rd body, one end of described 3rd body is connected with the other end of described second body, and the other end of described 3rd body is connected with the gas inlet of described cyclonic separator;
Wherein, described first body, described second body and described 3rd body three set gradually from the bottom to top, and the internal diameter of three increases successively.
5. combined type circulating fluidized-bed gasification device as claimed in claim 4, is characterized in that,
Described first body comprises tube body and is arranged on the first air compartment of described tube body lower end, and the upper end of described tube body is connected with one end of described second body;
Described first air compartment is connected with described tube body by the first gas distributor, is communicated with to make the inner and described tube body inside of described first air compartment;
Described first air compartment is provided with described First air entrance;
Described tube body is respectively equipped with described pyrolysis gas entrance, described semicoke entrance and described flying dust entrance.
6. combined type circulating fluidized-bed gasification device as claimed in claim 4, is characterized in that,
One end of described first body is connected with one end of described second body by the first tapered tube, and the internal diameter of described first tapered tube is the trend increased gradually by the direction of described first body extremely described second body;
And/or,
The other end of described second body is connected with one end of described 3rd body by the second tapered tube, and the internal diameter of described second tapered tube is the trend increased gradually by the direction of described second body extremely described 3rd body.
7. combined type circulating fluidized-bed gasification device as claimed in claim 4, is characterized in that,
Described second body is also provided with at least one secondary air entrance.
8. the combined type circulating fluidized-bed gasification device according to any one of claim 2 to 3 and 5 to 7, is characterized in that,
Described pyrolysis chamber comprises pyrolysis chamber's body and is arranged on the second air compartment of body lower end, described pyrolysis chamber, and described second air compartment is connected with described pyrolysis chamber body by the second gas distributor, is communicated with described pyrolysis chamber body interior to make described second air compartment inside; Described second air compartment is provided with air intake vent, and described pyrolysis chamber body is respectively equipped with described feed(raw material)inlet, described pyrolysis gas outlet and the outlet of described semicoke;
And/or,
Described returning charge room comprises returning charge room body and is arranged on the 3rd air compartment of body lower end, described returning charge room, described returning charge room body exports with described first flying dust and is connected, described 3rd air compartment is connected with described returning charge room body by the 3rd gas distributor, is communicated with described returning charge room body interior to make described 3rd air compartment inside; Described 3rd air compartment is provided with described loosening gas entrance, and described returning charge room body is provided with the second described flying dust outlet.
9. a combined type circulating fluidized bed gasification method, for combined type circulating fluidized-bed gasification device according to any one of claim 1 to 8 with the use of, described combined type circulating fluidized bed gasification method comprises the following steps:
Join in described pyrolysis chamber by solid carbon gasified raw material and the first gasifying gas, described raw material and described first gasifying gas react in described pyrolysis chamber, generate semicoke and pyrolysis gas;
Described semicoke is sent in described vaporizer by the semicoke outlet in described pyrolysis chamber and the semicoke entrance on described vaporizer successively; Send in described vaporizer by the second gasifying gas via the First air entrance on vaporizer, described second gasifying gas and described semicoke react, and generate coal gas;
Described pyrolysis gas is sent in described vaporizer by the pyrolysis gas entrance on the pyrolysis gas outlet in described pyrolysis chamber and described vaporizer successively and carries out detar process;
Coal gas in described vaporizer is sent into dedusting in described cyclonic separator, the pneumatic outlet of the coal gas after dedusting through described cyclonic separator is discharged.
10. combined type circulating fluidized bed gasification method as claimed in claim 9, is characterized in that,
The particle diameter of described solid carbon gasified raw material is 0-10mm;
And/or the pyrolysis temperature in described pyrolysis chamber is 500-900 DEG C;
And/or the superficial gas velocity of described pyrolysis chamber is 0.5-5.0m/s;
And/or the gasification temperature in described vaporizer is 700-1100 DEG C;
The superficial gas velocity of described vaporizer is 0.5-15.0m/s.
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