CN207210343U - The circulating fluidized bed gasification device of staged air distribution - Google Patents
The circulating fluidized bed gasification device of staged air distribution Download PDFInfo
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- CN207210343U CN207210343U CN201720952651.XU CN201720952651U CN207210343U CN 207210343 U CN207210343 U CN 207210343U CN 201720952651 U CN201720952651 U CN 201720952651U CN 207210343 U CN207210343 U CN 207210343U
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Abstract
A kind of circulating fluidized bed gasification device of staged air distribution, including burner hearth (1), gas-solid separating device (2) and revert system, are provided with auxiliary gasification agent inlet (m1~m4) on the burner hearth (1).By the circulating fluidized bed gasification device of staged air distribution of the present utility model, gasification efficiency is improved, reduces unburned carbon in flue dust.
Description
Technical field
Coal Gasification Technology field is the utility model is related to, more particularly to a kind of recirculating fluidized bed gasification dress of staged air distribution
Put.
Background technology
As a kind of clean coal technology of high-efficiency cleaning, Coal Gasification Technology is a kind of by the conversion of the solid-state such as coal primary energy
The main path of secondary energy sources is cleaned for gaseous state, the technology is mainly used in synthesizing ammonia, synthesizing methanol, hydrogen manufacturing, blast furnace reduction iron production
Deng in chemical industry metallurgical industry, combined cycle generation field, industry and domestic gas field and other numerous areas.
Classify by the motion state of solid fuel, modern coal gasifying process mainly includes moving bed (also known as fixed bed) gasification
Method, entrained flow gasification method and fluidized gasification method.In The Fluidized Bed Coal Gasification Technology is earliest industrialized gasification process, and its technique is
Gasifying agent with certain pressure is blown into from bed bottom by air distribution plate, the broken coal on bed is held up, when gasifying agent rises
When, coal grain is moved in suspended state, and rolling, carry out gasification reaction is fully contacted with gasifying agent up and down.In such technology, including
Traditional In The Fluidized Bed Coal Gasification Technology and circulation fluidized bed coal gasifying technology developed in recent years.Wherein, with traditional stream
Change bed gas burner to compare, there is the Matter Transfer loop of high circulation amount in circulation fluidized bed coal gasifying furnace zone, when fuel stops in stove
Between greatly extend, have Suitability of Coals is strong, gas-solid mixing fully, gasification reaction speed is high, whole temperature of reactor uniformly, can
Add the advantages that lime stone carries out desulfuration in furnace.
The structural behaviour of circulation fluidized bed coal gasifying stove is restricted by fluidised form law, and its advantage has benefited from this, meanwhile,
Also detrimental effect is thus brought, for example, there are the following problems for conventional circulation fluidized bed coal gasifying stove：First, material in stove
Well mixed, temperature is uniform, and produces coal gas and objectively require that reducing atmosphere must be kept in stove, that is to say, that material in stove
Higher phosphorus content must be kept, this allows for the bottom ash of circulation fluidized bed coal gasifying stove and unburned carbon in flue dust is high；2nd, in routine
Circulation fluidized bed coal gasifying stove in, the position that feeds of gasifying agent and feed coal determines that the middle and upper part of burner hearth is in reducing zone,
And material concentration is high, substantial amounts of heat is needed to obtain higher gasification efficiency, but prior art is the heat that the region provides
Relative deficiency is measured, this have impact on the raising of gasification efficiency.
Utility model content
A kind of the defects of the purpose of this utility model is to overcome prior art at least in part, there is provided recirculating fluidized bed gas
Makeup is put, and utilizes the circulating fluidized bed gasification device, it is possible to increase gasification efficiency.
The purpose of this utility model, which also resides in, provides a kind of circulating fluidized bed gasification device, and it is able to ensure that the heat in burner hearth
Amount provides, to ensure gasification efficiency.
The purpose of this utility model, which also resides in, provides a kind of circulating fluidized bed gasification device, and it can reduce flying marking
Amount.
According to the embodiment of one side of the present utility model, it is proposed that a kind of recirculating fluidized bed gasification dress of staged air distribution
Put, including burner hearth, gas-solid separating device and revert system, auxiliary gasification agent inlet is provided with the burner hearth.
According to a preferred embodiment of the present utility model, main gasification agent inlet, feed are additionally provided with the burner hearth
Mouth, returning charge mouth, furnace outlet and slag-drip opening；
The revert system includes down-comer, material returning device and returning charge inclined tube；
Wherein, the auxiliary gasification agent inlet is multiple that multiple auxiliary gasification agent inlets are in multi-tier arrangement, are distributed in burner hearth not
At height, and
Every layer of auxiliary gasification agent inlet includes at least two auxiliary gasification agent inlets.
According to a preferred embodiment of the present utility model, the auxiliary gasification agent inlet is located at the main gasification agent inlet of burner hearth
At level above h, and 0.3H<h<0.75H, and at height h burner hearth barometric gradient
Wherein, H is total effective depth of burner hearth, i.e., from the main gasification agent inlet of burner hearth to the horizontal center line of furnace outlet
Distance, p is the furnace pressures highly located of h.
According to a preferred embodiment of the present utility model, the multiple auxiliary gasification agent inlet is perpendicular to the longitudinal direction of burner hearth
Projection on the cross section of bearing of trend is not overlapping.
According to a preferred embodiment of the present utility model, the multiple auxiliary gasification agent inlet is perpendicular to the longitudinal direction of burner hearth
Projection on the cross section of bearing of trend with etc. angular separation be spaced apart.
According to a preferred embodiment of the present utility model, the auxiliary gasification agent inlet is configured such that auxiliary gasifying agent edge
Horizontal direction enters burner hearth.
According to a preferred embodiment of the present utility model, the auxiliary gasification agent inlet be configured such that auxiliary gasifying agent with
It is at an angle of and downward into burner hearth with the Longitudinal extending direction of burner hearth, the angle ranging from 0~45 °.
According to a preferred embodiment of the present utility model, the material inlet of the burner hearth is arranged on the auxiliary gasification agent inlet of multilayer
At least between two layers.
According to a preferred embodiment of the present utility model, the gas-solid separating device include one-level gas-solid separating device and
Two level gas-solid separating device, and the revert system includes one-level revert system and two level revert system.
According to a preferred embodiment of the present utility model, the circulating fluidized bed gasification device includes material inlet, described
Material inlet is arranged on revert system.
Compared to existing gasification technology, the circulating fluidized bed gasification device of staged air distribution of the present utility model is with following excellent
Point：
(1) multistage auxiliary gasifying agent is introduced at the different height of burner hearth specific region, is advantageous to the anti-of auxiliary gasifying agent and carbon
Should, the consumption of effective gas to having generated is reduced, improves effective gas yield；
(2) emulsion zone avoided in lower furnace portion introduces auxiliary gasifying agent, avoids oxidation reaction concentrating on ash concentration
High emulsion zone and highly exothermic formation high-temperature region is caused coking, improve the safety and stability of plant running；
(3) material reaction liberated heat can be carried into major gasification region in auxiliary gasifying agent and stove, for endothermic heat of reaction,
Promote the progress of gasification reaction, improve gasification efficiency.
Brief description of the drawings
Fig. 1 is the schematic diagram according to the circulating fluidized bed gasification device of the staged air distribution of embodiment of the present utility model；
Fig. 2 is the schematic diagram according to the circulating fluidized bed gasification device of the tangential air distribution of embodiment of the present utility model；
Fig. 3 is the schematic diagram according to the variable cross-section circulating fluidized bed gasification device of embodiment of the present utility model；And
Fig. 4 is the schematic diagram according to the variable cross-section circulating fluidized bed gasification device of another embodiment of the present utility model.
Embodiment
Exemplary embodiment of the present utility model is described in detail below in conjunction with the accompanying drawings, wherein same or analogous label table
Show same or analogous element.In addition, in the following detailed description, for ease of explaining, elaborate many concrete details with
Comprehensive understanding to present disclosure embodiment is provided.It should be apparent, however, that one or more embodiments are in these no details
In the case of can also be carried out.In other cases, known construction and device is diagrammatically embodied to simplify accompanying drawing.
Fig. 1 is according to the schematic diagram of the circulating fluidized bed gasification device of the staged air distribution of embodiment of the present utility model, such as
Shown in Fig. 1, the circulating fluidized bed gasification device of staged air distribution includes the burner hearth 1, gas-solid separating device 2 and the returning charge system that are sequentially connected
System, the revert system include down-comer 3, material returning device 4 and returning charge inclined tube 5.Main gasification agent inlet is provided with the burner hearth 1
Q, material inlet d, returning charge mouth f, furnace outlet g and slag-drip opening, further, four auxiliary gasifying agents are provided with the burner hearth 1
Entrance m1~m4, four auxiliary gasification agent inlet m1~m4 are in multi-tier arrangement, are distributed in Fig. 1 on two layers, are distributed in burner hearth 1
Different height at, and every layer of auxiliary gasification agent inlet includes two auxiliary gasification agent inlets.
The course of work of circulating fluidized bed gasification device shown in Fig. 1 is described below, coal gasification reaction enters in burner hearth 1
OK, it is 1100 DEG C to control fire box temperature, and coal D enters burner hearth 1, the recycle containing the carbon not reacted completely largely from material inlet d
Material enters burner hearth 1 from returning charge mouth f, and main gasifying agent Q enters burner hearth 1 from main gasification agent inlet q, and above-mentioned material is carried out in lower furnace portion
Gas-solid mixing, and reaction of the generation based on burning under fluidized state, discharge amount of heat.
Mixed gas carries the carbon that does not react completely and heat moves from bottom to top in burner hearth 1, in the process with
The consumption of oxygen, reaction are gradually converted into based on reduction reaction, and consume the heat of oxidation reaction generation.Then, auxiliary gasifying agent
Reaction based on aoxidizing occurs for the high concentration carbon particle entered from different auxiliary gasification agent inlet m1~m4 in burner hearth 1, with burner hearth 1
And heat is discharged, while can also consume CO, H that part has generated2、CH4Deng fuel gas, burn and heat release, supplemented by gasifying agent enter
The reduction reaction that mouth m1~m4 near zones are carried out provides heat, promotes the progress of the region gasification reaction.Auxiliary gasifying agent and stove
The gas-solid mixture that the heat of interior combustible reaction generation is moved upwards carries upwards, supplemented by gasification agent inlet near zone and
The gasification reaction that auxiliary gasification agent inlet area above occurs provides heat, promotes the progress of gasification reaction, improve gasification efficiency and
Efficiency of carbon con version.
The carbon for reacting the coal gas of generation and not reacting completely leaves burner hearth 1 via the furnace outlet g on the top of burner hearth 1, enters
Gas-solid separating device 2, the solid separated through gas-solid separating device 2 pass through down-comer 3, material returning device 4 and returning charge inclined tube 5 successively, pass through
Burner hearth 1 is returned to by the returning charge mouth f on burner hearth 1 and continues cycling through participation reaction；Coal gas E containing a small amount of solid particle is from gas solid separation
The gas vent of device 2 leaves circulating fluidized bed gasification device, is collected after follow-up heat exchange, purifier, and cinder L
Discharged from slag-drip opening.
By introducing auxiliary gasifying agent in burner hearth middle and upper part or can be improved along the distribution of furnace height multistage in gasification installation
Reaction temperature, unburned carbon in flue dust is reduced, on the one hand lower furnace portion ascending air speed is reduced by the introducing of multistage auxiliary gasifying agent
Degree, thus the residence time for the carbon not reacted completely is extended, further to react and separate the entrainment material in gas, separately
On the one hand the temperature of auxiliary gasifying agent introduce region is improved so that the material carried secretly in gas continues gasification reaction.
Designer has found that the introducing of auxiliary gasifying agent is highly desirable and gives special consideration, shows by experimental study, auxiliary gasification
Agent feed it is highly desirable match with burner hearth endoparticle concentration, if for example, auxiliary gasifying agent feeds excessive height, due to herein
Place's burner hearth endoparticle concentration is relatively low, and gasifying agent can react with the available gas largely generated, the promotion effect to gasification reaction
Fruit is poor, produces obvious negative impact to integrated gasification effect on the contrary.Therefore, design height of the designer to auxiliary gasification agent inlet
Studied.
As shown in figure 1, auxiliary gasification agent inlet m1 and m2 is located in the same level of burner hearth, auxiliary gasification agent inlet m3 and m4
In the same level of burner hearth.Preferably, the auxiliary gasification agent inlet m1~m4 is located at the main gasification agent inlet q of burner hearth 1
At level above h, and 0.3H<h<0.75H, and at height h burner hearth barometric gradientWherein, H is
The distance of total effective depth of burner hearth, the i.e. horizontal center line from the main gasification agent inlet q of burner hearth 1 to furnace outlet g, p are that h is high
Furnace pressure at degree.
Advantageously, auxiliary gasification agent inlet m1 and m2 is located at burner hearth cloth wind point s (highly with main gasification agent inlet q) above h1It is high
At degree, and h1=0.5H,(kPa/m is barometric gradient unit).Auxiliary gasification agent inlet m3 and m4 is located at stove
Thorax cloth wind point s above h2Highly locate, and h2=0.6H,
Preferably, the multiple auxiliary gasification agent inlet m1~m4 is perpendicular to the cross section in the Longitudinal extending direction of burner hearth 1
On projection it is not overlapping, further, the multiple auxiliary gasification agent inlet m1~m4 is perpendicular to the Longitudinal extending direction of burner hearth 1
Cross section on projection with etc. angular separation be spaced apart.The auxiliary gasification agent inlet m1~m4 is configured such that auxiliary gasifying agent edge
Horizontal direction enters burner hearth 1.As shown in figure 1, four auxiliary gasification agent inlets are divided into two layers, Fig. 1 lower right corner is burner hearth 1 along t-
The sectional view in t sections, show the auxiliary gasification agent inlet m1 and m2 of lower floor, it can be seen that two auxiliary gasification agent inlet m1 and m2 exist
Arrange with being diametrically opposed to one another.
Alternatively, the auxiliary gasification agent inlet m1~m4 is configured such that auxiliary gasifying agent with the longitudinal direction with burner hearth 1
Bearing of trend is angled and downward into burner hearth 1, the angle ranging from 0~45 °.In Fig. 1, the material inlet d of the burner hearth 1
It is arranged between two layers of the auxiliary gasification agent inlet m1~m4 of multilayer.The material inlet d of the circulating fluidized bed gasification device can also
Be arranged on revert system, behind address.
A kind of recirculating fluidized bed of staged air distribution can be obtained using the circulating fluidized bed gasification device of above-mentioned staged air distribution
Gasification process, methods described may include steps of：The circulating fluidized bed gasification device of staged air distribution is provided；By coal directly or
It is sent into by revert system in the burner hearth of circulating fluidized bed gasification device, main gasifying agent is passed through from burner hearth bottom, and from burner hearth
Auxiliary gasifying agent is passed through at different height, wherein auxiliary gasification agent inlet m1~m4 is located at the main gasification agent inlet q level above of burner hearth 1
At h, and 0.3H<h<0.75H, and at height h burner hearth barometric gradientWherein, H is the total of burner hearth
The distance of effective depth, the i.e. horizontal center line from the main gasification agent inlet q of burner hearth 1 to furnace outlet g, p are the stove that h highly locates
Gun pressure power；The coal gas of reaction generation is drawn after gas-solid separating device isolates solid particle, and the solid particle isolated is through returning
Material system sends burner hearth back to.
The main gasifying agent can be air, pure oxygen, oxygen-enriched air or the mixture of above-mentioned thrin and water vapour；Institute
It can be air, pure oxygen, oxygen-enriched air or the mixture of above-mentioned thrin and water vapour to state auxiliary gasifying agent；Advantageously, answering
It is described auxiliary when implementing the ciculation fluidized bed gasification method of staged air distribution with the circulating fluidized bed gasification device of foregoing staged air distribution
Oxygen volume accounts for 10%~40% of total oxygen volume in main gasifying agent and auxiliary gasifying agent in gasifying agent, the temperature of the main gasifying agent
Spend for 500~800 DEG C, the auxiliary gasification agent temperature is 300~800 DEG C, and the reaction temperature of the burner hearth is in 800~1300 DEG C of models
In enclosing.
As a specific embodiment, main gasifying agent is the mixed of the oxygen-enriched air that oxygen volumetric concentration is 45% and vapor
Compound, main gasification agent temperature are 600 DEG C.The component of the auxiliary gasifying agent that each auxiliary gasification agent inlet is passed through, temperature and air quantity are consistent,
The oxygen-enriched air for being 30% for oxygen volumetric concentration, auxiliary gasifying agent oxygen volume account for total carrier of oxygen in main gasifying agent and auxiliary gasifying agent
Long-pending 20%, temperature are 600 DEG C.
Compared to existing gasification technology, the circulating fluidized bed gasification device and gasification process of staged air distribution of the present utility model
Have the following advantages that：
(1) multistage auxiliary gasifying agent is introduced at the different height of burner hearth specific region, is advantageous to the anti-of auxiliary gasifying agent and carbon
Should, the consumption of effective gas to having generated is reduced, improves effective gas yield；
(2) emulsion zone avoided in lower furnace portion introduces auxiliary gasifying agent, avoids oxidation reaction concentrating on ash concentration
High emulsion zone and highly exothermic formation high-temperature region is caused coking, improve the safety and stability of plant running；
(3) material reaction liberated heat can be carried into major gasification region in auxiliary gasifying agent and stove, for endothermic heat of reaction,
Promote the progress of gasification reaction, improve gasification efficiency.
In circulating fluidized bed gasification device described above, if the auxiliary gasifying agent introduced is directly injected into burner hearth center
(radially injecting), the coal gas for the more gasification generation that can burn, and reduce with the reaction probabilities of imperfect combustion carbon, this have impact on
The raising of cold gas efficiency and the effect improved to unburned carbon in flue dust.
Therefore, the utility model gives a kind of circulating fluidized bed gasification device of tangential air distribution, Fig. 2 is according to this practicality
The schematic diagram of the circulating fluidized bed gasification device of the tangential air distribution of new embodiment.As shown in Fig. 2 the recycle stream of tangential air distribution
Change burner hearth 1, gas-solid separating device 2 and revert system that bed gasifying apparatus includes being sequentially connected, the revert system includes declining
Pipe 3, material returning device 4 and returning charge inclined tube 5, material inlet d are arranged on returning charge inclined tube 5；Main gasifying agent is provided with the burner hearth 1 to enter
Mouth q, returning charge mouth f, furnace outlet g and slag-drip opening, further, are provided with 12 auxiliary gasification agent inlets on the burner hearth 1
M1~m12,12 auxiliary gasification agent inlet m1~m12 are in multi-tier arrangement, are distributed in fig. 2 on three layers, are distributed in burner hearth 1
Different height at, every layer of auxiliary gasification agent inlet includes four auxiliary gasification agent inlet m1~m12.Importantly, the auxiliary gasification
Agent entrance m1~m12 is configured such that auxiliary gasifying agent and the side wall of the burner hearth 1 tangentially enter burner hearth 1.
In a specific embodiment, the cylindrical in shape of burner hearth 1, the auxiliary gasification agent inlet m1~m12 is by structure
Make and be tangentially arranged in the side wall outside of burner hearth 1 for pipe, the pipe, and communicated with the burner hearth 1 so that pipe is most
Outer side edges and the cross circular section of burner hearth 1 are circumscribed.
The course of work of circulating fluidized bed gasification device shown in Fig. 2 is described below, coal gasification reaction enters in burner hearth 1
OK, it is 1200 DEG C to control fire box temperature.Coal D enters returning charge inclined tube 5 from material inlet d, with containing the carbon not reacted completely largely
Passed through after recycle stock mixing and burner hearth 1 is entered by returning charge mouth f, main gasifying agent Q enters burner hearth 1, above-mentioned material from main gasification agent inlet q
In lower furnace portion gas-solid mixing, and reaction of the generation based on aoxidizing under fluidized state, discharge amount of heat.
Mixed gas carries the carbon that does not react completely and heat moves from bottom to top in burner hearth 1, in the process with
The consumption of oxygen, reaction are gradually converted into based on reduction reaction, and consume the heat of oxidation reaction generation.Then, auxiliary gasifying agent
From different auxiliary gasification agent inlet m1~m12, (such as 30 °) tangentially enter burner hearth 1 obliquely, with the carbon near wall region occur with
Reaction based on oxidation simultaneously discharges heat, while can also consume CO, H that part has generated2、CH4Deng fuel gas, burn and put
Heat, supplemented by gasification agent inlet near zone carry out gasification reaction provide heat, promote the progress of the region gasification reaction.Auxiliary gas
The agent and gas-solid mixture that is moved upwards of heat of combustible reaction generation carries upwards in stove, supplemented by gasification agent inlet it is attached
The reduction reaction that near field and auxiliary gasification agent inlet area above occur provides heat, promotes the progress of gasification reaction, improves gas
Change efficiency and efficiency of carbon con version.
The carbon for reacting the coal gas of generation and not reacting completely leaves burner hearth 1 via the furnace outlet g on the top of burner hearth 1, enters
Gas-solid separating device 2, the solid separated through gas-solid separating device 2 pass through down-comer 3, material returning device 4 and returning charge inclined tube 5 successively, pass through
Burner hearth 1 is returned to by the returning charge mouth f on burner hearth 1 and continues cycling through participation reaction；Coal gas E containing a small amount of solid particle is from gas solid separation
The gas vent of device 2 leaves circulating fluidized bed gasification device, is collected after follow-up heat exchange, purifier, and cinder L
Discharged from slag-drip opening.
Recirculating fluidized bed radially " ring core " Gas-solid Flow Characteristics are considered by the way of auxiliary gasifying agent is tangentially fed.It will match somebody with somebody
Wind tangentially feeds gasification furnace burner hearth, and adherent eddy flow is formed in gasification furnace.On the one hand, the adherent rotational flow of air distribution, disturbance is strengthened
While, fully contacted with the carbonaceous solid particulates near wall region, promote air distribution with burner hearth unburned carbon it is anti-
Should, improve the regional temperature and promote the conversion of carbon；On the other hand, the adherent rotational flow of air distribution, penetration power is weak, compared to radially matching somebody with somebody
Wind, the influence for the burner hearth central area concentrated to coal gas is smaller, and oxidation reaction occurs for the coal gas and air distribution for reducing gasification generation
Ratio, reduce because air distribution introduces influence to system cold gas efficiency.
As shown in Fig. 2 auxiliary gasification agent inlet m1~m4 is located in the same level of burner hearth, auxiliary gasification agent inlet m5~m8
In the same level of burner hearth, auxiliary gasification agent inlet m9~m12 is located in the same level of burner hearth.Preferably, it is described
Auxiliary gasification agent inlet m1~m12 is located at the main gasification agent inlet q level above h of burner hearth 1, and 0.3H<h<0.75H, and
The barometric gradient of burner hearth at height hWherein, H be burner hearth total effective depth, i.e. the main gasification from burner hearth 1
For agent entrance q to the distance of furnace outlet g horizontal center line, p is the furnace pressure that h highly locates.
Advantageously, auxiliary gasification agent inlet m1~m4 is located at burner hearth cloth wind point s (highly with main gasification agent inlet q) above h1It is high
At degree, and h1=0.4H,Auxiliary gasification agent inlet m5~m8 is located at burner hearth cloth wind point s above h2Highly locate,
And h2=0.6H,Auxiliary gasification agent inlet m9~m12 is located at burner hearth cloth wind point s above h3Highly locate, and h3
=0.7H,
Preferably, the multiple auxiliary gasification agent inlet m1~m12 is perpendicular to the cross section in the Longitudinal extending direction of burner hearth 1
On projection it is not overlapping, further, the multiple auxiliary gasification agent inlet m1~m12 is perpendicular to the Longitudinal extending side of burner hearth 1
To cross section on projection with etc. angular separation be spaced apart.The auxiliary gasification agent inlet m1~m12 is configured such that auxiliary gasification
With angled with the Longitudinal extending direction of burner hearth 1 and downward into burner hearth 1, the angle beta is 0~45 ° for agent, it is therefore preferable to
30°.As shown in Fig. 2 12 auxiliary gasification agent inlets are divided into three layers, three below Fig. 2 view is respectively the edge of burner hearth 1
The sectional view in t1-t1, t2-t2, t3-t3 section, it can be seen that circumferentially etc. angular separation is spaced apart four auxiliary gasification agent inlets.
Alternatively, the auxiliary gasification agent inlet m1~m12 is configured such that auxiliary gasifying agent enters in the horizontal direction
Burner hearth 1.Alternatively, the material inlet d of the burner hearth 1 can also be arranged at least two layers of the auxiliary gasification agent inlet m1~m12 of multilayer
Between.
A kind of recirculating fluidized bed of tangential air distribution can be obtained using the circulating fluidized bed gasification device of above-mentioned tangential air distribution
Gasification process, methods described may include steps of：The circulating fluidized bed gasification device of tangential air distribution is provided；By coal directly or
The burner hearth of circulating fluidized bed gasification device is sent into by revert system；Main gasifying agent is passed through from burner hearth bottom, and from burner hearth sidewall
Tangentially it is passed through auxiliary gasifying agent；The coal gas of reaction generation is drawn after gas-solid separating device isolates solid particle, is isolated
Solid particle sends burner hearth back to through revert system.
The main gasifying agent can be air, pure oxygen, oxygen-enriched air or the mixture of above-mentioned thrin and water vapour；Institute
It can be air, pure oxygen, oxygen-enriched air or the mixture of above-mentioned thrin and water vapour to state auxiliary gasifying agent；Advantageously, answering
It is described auxiliary when implementing the ciculation fluidized bed gasification method of tangential air distribution with the circulating fluidized bed gasification device of foregoing tangential air distribution
Oxygen volume accounts for 10%~40% of total oxygen volume in main gasifying agent and auxiliary gasifying agent in gasifying agent, the temperature of the main gasifying agent
Spend for 500~800 DEG C, the auxiliary gasification agent temperature is 300~800 DEG C, and the reaction temperature of the burner hearth is in 800~1300 DEG C of models
In enclosing.
As a specific embodiment, main gasifying agent is the mixed of the oxygen-enriched air that oxygen volumetric concentration is 70% and vapor
Compound, main gasification agent temperature are 600 DEG C.The component of the auxiliary gasifying agent that each auxiliary gasification agent inlet is passed through, temperature and air quantity are consistent,
The oxygen-enriched air for being 70% for oxygen volumetric concentration, auxiliary gasifying agent oxygen volume account for total carrier of oxygen in main gasifying agent and auxiliary gasifying agent
Long-pending 30%, temperature are 300 DEG C.
Compared to existing gasification technology, the circulating fluidized bed gasification device and gasification process of tangential air distribution of the present utility model
Have the following advantages that：
(1) in freeze profile into adherent eddy flow, the reaction of auxiliary gasifying agent and unburned carbon in burner hearth is greatly promoted,
Improve the regional temperature and promote the conversion of carbon, improve efficiency of carbon con version；
(2) greatly reduce effective gas of gasification generation and the ratio of oxidation reaction occurs for auxiliary gasifying agent, improve effective gas
Yield；
(3) the weak eddy flow that the introducing of tangential auxiliary gasifying agent is formed does not change the direction of motion of primary air, but can play pressure
Material acts on, and compared to the auxiliary gasifying agent radially fed, is more beneficial for reducing ascending air speed, the carbon that extension is not reacted completely
Residence time, further to react and separate the entrainment fine ash in gas, reduce unburned carbon in flue dust.
To sum up, the circulating fluidized bed gasification device of tangential air distribution of the present utility model and gasification process solve auxiliary gasifying agent
The problem of mode of feeding is present, auxiliary gasifying agent and the reaction for the carbon not reacted completely in burner hearth are enhanced, greatly reduces gasification
The ratio of oxidation reaction occurs for the available gas of generation and auxiliary gasifying agent, effectively reduces unburned carbon in flue dust, improves the cold coal of system
Gas efficiency.
Fig. 3 is according to the schematic diagram of the variable cross-section circulating fluidized bed gasification device of embodiment of the present utility model, such as Fig. 3 institutes
Show, variable cross-section circulating fluidized bed gasification device includes burner hearth 1, gas-solid separating device 2 and the revert system being sequentially connected, described to return
Material system includes down-comer 3, material returning device 4 and returning charge inclined tube 5.Main gasification agent inlet q, Duo Gefu are provided with the burner hearth 1
Gasification agent inlet m1~m6, material inlet d, returning charge mouth f, furnace outlet g and slag-drip opening.The main gasification agent inlet is located at burner hearth bottom
Portion, the furnace outlet are located at upper furnace.The area edge longitudinal direction of the cross section in the direction perpendicular to the longitudinally-extending of the burner hearth 1
Bearing of trend changes, wherein, the burner hearth 1 extends longitudinally direction and is divided into multistage, adjacent section it is perpendicular to the longitudinally-extending
The area of the cross section in direction increases from bottom to top, and connection transition region is provided between adjacent section.
In this embodiment, the burner hearth 1 includes emulsion zone section 1-a, development section and dilute phase section from bottom to top, described
Dilute phase section includes two sections of 1-c-2 of one section of 1-c-1 of dilute-phase zone and dilute-phase zone from bottom to top, is set on two sections of 1-c-2 of dilute-phase zone
There is the furnace outlet g；Wherein, emulsion zone section 1-a, development section, one section of 1-c-1 of dilute-phase zone and dilute-phase zone two sections of 1-c-2
The area of the cross section in direction perpendicular to the longitudinally-extending increases successively.
Two sections of emulsion zone section 1-a, development section 1-b, one section of 1-c-1 of dilute-phase zone and dilute-phase zone 1-c-2 are in cylindrical shape
Shape, a diameter of D of the emulsion zone section 1-a1, a diameter of D of the development section 1-b2-1, described one section of 1-c-1 of dilute-phase zone and dilute
Two sections of 1-c-2 diameters of phase region are respectively D3-1And D3-2, also,
1.1D1≤D2-1≤1.3D1；And 1.3D1<D3-1<D3-2≤2D1, or
1.2D1≤D2-1≤1.5D1；And 1.5D1<D3-1<D3-2≤2.5D1。
In a specific embodiment, D2-1=1.1D1, D3-1=1.5D1, D3-2=1.8D1。
Preferably, the auxiliary gasification agent inlet m1~m6 is arranged at the connection transition region of burner hearth 1, the multiple auxiliary gasification
Agent entrance m1~m6 is in multi-tier arrangement, is distributed at the different height of burner hearth 1, and every layer of auxiliary gasification agent inlet includes at least two
Auxiliary gasification agent inlet.As shown in figure 3, auxiliary gasification agent inlet is divided into three layers by different height, 2 every layer auxiliary gasification agent inlets (
Can be more), auxiliary gasification agent inlet m1 and m2 is located on the same cross section of burner hearth, and auxiliary gasification agent inlet m3 and m4 is located at
On the same cross section of burner hearth, auxiliary gasification agent inlet m5 and m6 is located on the same cross section of burner hearth, and auxiliary gasification agent inlet
M1 and m2 is located at emulsion zone section 1-a and developed at section 1-b connection transition region；Auxiliary gasification agent inlet m3 and m4 is located at development zone
At one section of 1-c-1 of section 1-b and dilute-phase zone connection transition region；Auxiliary gasification agent inlet m5 and m6 be located at one section of 1-c-1 of dilute-phase zone and
At two sections of 1-c-2 of dilute-phase zone connection transition region.
The auxiliary gasification agent inlet m1~m6 is configured such that auxiliary gasifying agent vertically enters burner hearth 1, i.e., all
Auxiliary gasification agent inlet is vertically set, suitable for making auxiliary gasifying agent be passed through burner hearth 1, and auxiliary gasification agent inlet straight up
The distance of m1~m6 to the wall of the larger burner hearth section in cross section is less than auxiliary gasification agent inlet m1~m6 to the less stove in cross section
The distance of the wall of thorax section, in the case where burner hearth section is cylinder form, auxiliary gasification agent inlet to the burner hearth section being relatively large in diameter
The distance of wall be less than the distance that auxiliary gasification agent inlet arrives the wall of the less burner hearth section of diameter, i.e., suitable for erecting auxiliary gasifying agent
Closer to inboard wall of burner hearth face after being directly passed through upwards.
Advantageously, auxiliary gasification agent inlet m1 and m2 is located at burner hearth cloth wind point s (highly with main gasification agent inlet q) above h1It is high
At degree, and h1=0.08H,(kPa/m is barometric gradient unit)；Auxiliary gasification agent inlet m3 and m4 is located at burner hearth
Cloth wind point s above h2Highly locate, and h2=0.4H,Auxiliary gasification agent inlet m5 and m6 is located at burner hearth cloth wind point
More than s h3Highly locate, and h3=0.7H,
It should be noted that in the design of burner hearth, can be determined to occur to cut on burner hearth according to the granule density in burner hearth
The position (position for connecting transition region) of face change, and granule density is reflected in measurement by barometric gradient, therefore above
The position of auxiliary gasification agent inlet is determined based on barometric gradient.In addition, the different component of main gasifying agent and auxiliary gasifying agent also can
The diameter relational design of burner hearth section is influenceed, designer provides preferable scheme based on different compositions：When main gasifying agent and
Auxiliary gasifying agent is air, or is air+vapor, or the averaged oxygen air volume concentration of main gasifying agent and auxiliary gasifying agent≤
When 30%, 1.1D1≤D2-1≤1.3D1, 1.3D1<D3-1<D3-2≤2D1；When main gasifying agent and the averaged oxygen air volume of auxiliary gasifying agent
During concentration ＞ 30%, 1.2D1≤D2-1≤1.5D1, 1.5D1<D3-1<D3-2≤2.5D1.Wherein averaged oxygen air volume concentration=(master
The carrier of oxygen of the volume flow of the oxygen volumetric concentration of the volume flow of gasifying agent × main gasifying agent+auxiliary gasifying agent × auxiliary gasifying agent
Product concentration)/(volume flow of the volume flow of main gasifying agent+auxiliary gasifying agent).
The course of work of circulating fluidized bed gasification device shown in Fig. 3 is described below, coal gasification reaction enters in burner hearth 1
OK, it is 1100 DEG C to control fire box temperature.Coal D enters burner hearth 1 from material inlet d；Recycle containing the carbon not reacted completely largely
Material enters burner hearth 1 from returning charge mouth f, and main gasifying agent Q enters burner hearth 1 from main gasification agent inlet q, and above-mentioned material is in the close phase of lower furnace portion
Section 1-a gas-solid mixings, and reaction of the generation based on burning under fluidized state, discharge amount of heat.
Mixed gas carries the carbon that does not react completely and heat moves from bottom to top in burner hearth 1, in the process with
The consumption of oxygen, reaction are gradually converted into based on reduction reaction, and consume the heat of oxidation reaction generation.With gasification reaction
Carry out, furnace gas volume increase, the cross-sectional area of burner hearth 1 also increases step by step, makes to keep reasonable and relatively low fluidisation in burner hearth 1
Speed, improve residence time of the fuel in stove.Meanwhile auxiliary gasifying agent enters straight up from different auxiliary gasification agent inlet m1~m6
Enter burner hearth 1, the reaction based on aoxidizing occurs with the high concentration carbon particle near wall region and discharges heat, while can also consume
CO, H that part has generated2、CH4Deng fuel gas, burn and heat release, supplemented by gasification agent inlet m1~m6 near zones carry out
Reduction reaction provides heat, promotes the progress of the region gasification reaction.Auxiliary gasifying agent and the heat of combustible reaction generation in stove
The gas-solid mixture moved upwards carries upwards, supplemented by gasification agent inlet near zone and auxiliary gasification agent inlet area above hair
Raw gasification reaction provides heat, promotes the progress of gasification reaction, improves gasification efficiency and efficiency of carbon con version.
The carbon for reacting the coal gas of generation and not reacting completely leaves burner hearth 1 via the furnace outlet g on the top of burner hearth 1, enters
Gas-solid separating device 2, the solid separated through gas-solid separating device 2 pass through down-comer 3, material returning device 4 and returning charge inclined tube 5 successively, pass through
Burner hearth 1 is returned to by the returning charge mouth f on burner hearth 1 and continues cycling through participation reaction；Coal gas E containing a small amount of solid particle is from gas solid separation
The gas vent of device 2 leaves circulating fluidized bed gasification device, is collected after follow-up heat exchange, purifier, and cinder L
Discharged from slag-drip opening.
A kind of ciculation fluidized bed gasification method of variable cross-section can be obtained using above-mentioned variable cross-section circulating fluidized bed gasification device,
Methods described may include steps of：Variable cross-section circulating fluidized bed gasification device is provided；By coal directly or by revert system
The burner hearth of circulating fluidized bed gasification device is sent into, and main gasifying agent is passed through from burner hearth bottom, and it is perpendicular from burner hearth connection transition region edge
Nogata is to being passed through auxiliary gasifying agent；The coal gas of reaction generation is drawn after gas-solid separating device isolates solid particle, is isolated
Solid particle sends burner hearth back to through revert system.
The main gasifying agent can be air, pure oxygen, oxygen-enriched air or the mixture of above-mentioned thrin and water vapour；Institute
It can be air, pure oxygen, oxygen-enriched air or the mixture of above-mentioned thrin and water vapour to state auxiliary gasifying agent；Advantageously, answering
When implementing the ciculation fluidized bed gasification method of variable cross-section with foregoing variable cross-section circulating fluidized bed gasification device, in the auxiliary gasifying agent
Oxygen volume accounts for 10%~40% of total oxygen volume in main gasifying agent and auxiliary gasifying agent, and the temperature of the main gasifying agent is 500
~800 DEG C, the auxiliary gasification agent temperature is 300~800 DEG C, and the reaction temperature of the burner hearth is in the range of 800~1300 DEG C.
As a specific embodiment, main gasifying agent is air, and main gasification agent temperature is 600 DEG C；Each auxiliary gasifying agent enters
The auxiliary gasifying agent that mouth is passed through is air, and temperature and air quantity are consistent, and auxiliary gasifying agent oxygen volume accounts for main gasifying agent and auxiliary gasification
The 20% of total oxygen volume in agent, temperature are 600 DEG C.
Fig. 4 is according to the schematic diagram of the variable cross-section circulating fluidized bed gasification device of another embodiment of the present utility model, Fig. 4
The difference of shown embodiment and the embodiment shown in Fig. 3 is：
Development section includes one section of development zone 1-b-1 and two sections of development zone 1-b-2, and one section of development zone 1- from bottom to top
The area of the cross section in b-1 direction perpendicular to the longitudinally-extending is less than two sections of development zone 1-b-2 direction perpendicular to the longitudinally-extending
Cross section area.
One section of development zone 1-b-1, two sections of development zone 1-b-2 also cylindrical in shape, the emulsion zone section 1-a's is a diameter of
D1, described one section of 1-b-1 in the development zone and two sections of 1-b-2 in development zone diameter is respectively D2-1And D2-2, described one section of 1- of dilute-phase zone
Two sections of 1-c-2 diameters of c-1 and dilute-phase zone are respectively D3-1And D3-2, also,
1.1D1≤D2-1=D2-2≤1.3D1；And 1.3D1<D3-1<D3-2≤2D1, or
1.2D1≤D2-1<D2-2≤1.5D1；And 1.5D1<D3-1<D3-2≤2.5D1。
In a specific embodiment, D2-1=1.3D1, D2-2=1.5D1, D3-1=2D1, D3-2=2.5D1。
The gas-solid separating device 2 includes one-level gas-solid separating device 2-1 and two level gas-solid separating device 2-2, and institute
Stating revert system includes one-level revert system and two level revert system.Burner hearth 1 and one-level gas-solid separating device 2-1, one-level returning charge
System, two level gas-solid separating device 2-2, the connection of two level revert system, wherein, one-level revert system is by one-level down-comer 3-1, one
Level material returning device 4-1 and one-level returning charge inclined tube 5-1 is connected in sequence, and two level revert system is by two level down-comer 3-2, two level returning charge
Device 4-2 and two level returning charge inclined tube 5-2 are connected in sequence.
In addition to main gasification agent inlet q, multiple auxiliary gasification agent inlet m1~m6, furnace outlet g and slag-drip opening, on burner hearth 1
One-level returning charge mouth f-1 and two level returning charge mouth f-2 are provided with, is connected respectively with one-level returning charge inclined tube 5-1 and two level returning charge inclined tube 5-2
Connect, material inlet d is provided with one-level returning charge inclined tube 5-1.
Different from embodiment illustrated in fig. 3, auxiliary gasification agent inlet m1 and m2 is located at burner hearth cloth wind point s (highly with main gasifying agent
Entrance q) above h1Highly locate, and h1=0.08H,Auxiliary gasification agent inlet m3 and m4 is located at burner hearth cloth wind point s
Above h2Highly locate, and h2=0.3H,Auxiliary gasification agent inlet m5 and m6 is located at burner hearth cloth wind point s above h3
Highly locate, and h3=0.6H,
The course of work of circulating fluidized bed gasification device shown in Fig. 4 is described below, coal gasification reaction enters in burner hearth 1
OK, it is 1200 DEG C to control fire box temperature.Coal D enters the one-level returning charge inclined tube 5-1 of circulating fluidized bed gasification device from material inlet d,
Passed through after being mixed with the recycle stock containing the carbon not reacted completely largely and burner hearth 1, main gasifying agent Q are entered by one-level returning charge mouth f-1
Enter burner hearth 1 from main gasification agent inlet q, above-mentioned material is in lower furnace portion emulsion zone section 1-a gas-solid mixings, and under fluidized state
Occur, to burn for main reaction, to discharge amount of heat.
Mixed gas carries the carbon that does not react completely and heat moves from bottom to top in burner hearth 1, in the process with
The consumption of oxygen, reaction are gradually converted into based on reduction reaction, and consume the heat of oxidation reaction generation.With gasification reaction
Carry out, furnace gas volume increase, the cross-sectional area of burner hearth 1 also increases step by step, makes to keep reasonable and relatively low fluidisation speed in burner hearth 1
Degree, improve residence time of the fuel in stove.Meanwhile auxiliary gasifying agent enters straight up from different auxiliary gasification agent inlet m1~m6
Burner hearth 1, the reaction based on aoxidizing occurs with the high concentration carbon particle near wall region and discharges heat, while can also consume portion
Divide CO, the H generated2、CH4Deng fuel gas, burn and heat release, supplemented by gasification agent inlet m1~m6 near zones carry out also
Original reaction provides heat, promotes the progress of the region gasification reaction.Auxiliary gasifying agent and the heat quilt of combustible reaction generation in stove
The gas-solid mixture moved upwards carries upwards, supplemented by gasification agent inlet near zone and auxiliary gasification agent inlet area above occur
Gasification reaction heat is provided, promote the progress of gasification reaction, improve gasification efficiency and efficiency of carbon con version.
The carbon for reacting the coal gas of generation and not reacting completely leaves burner hearth 1 via the furnace outlet g on the top of burner hearth 1, enters
One-level gas-solid separating device 2-1, the solid through one-level gas-solid separating device 2-1 separation is successively by one-level down-comer 3-1, one-level
Material returning device 4-1 and one-level returning charge inclined tube 5-1, return to burner hearth 1 via the one-level returning charge mouth f-1 on one section of development zone 1-b-1 and continue
Circulation participates in reaction；Gas-solid mixture after one-level gas-solid separating device 2-1 separation enters into two level gas-solid separating device 2-2
Row separates again, and the solid separated through two level gas-solid separating device 2-2 passes through two level down-comer 3-2, two level material returning device 4-2 successively
With two level returning charge inclined tube 5-2, return to burner hearth 1 via the two level returning charge mouth f-2 on one section of 1-c-1 of dilute-phase zone and continue cycling through participation instead
Should；The gas vent of coal gas E from gas-solid separating device 2-2 containing a small amount of solid particle leave circulating fluidized bed gasification device,
It is collected after follow-up heat exchange, purifier, and cinder L discharges from slag-drip opening.
A kind of ciculation fluidized bed gasification method of variable cross-section can be obtained using above-mentioned variable cross-section circulating fluidized bed gasification device,
Its specific steps is as previously described.
As a specific embodiment, main gasifying agent is the mixture of pure oxygen and vapor, and main gasification agent temperature is 600
℃.The component of the auxiliary gasifying agent that each auxiliary gasification agent inlet is passed through, temperature and air quantity are consistent, are the mixing of pure oxygen and water vapour
Thing, auxiliary gasifying agent oxygen volume account for 30% of total oxygen volume in main gasifying agent and auxiliary gasifying agent, and temperature is 300 DEG C.
Compared to existing gasification technology, variable cross-section circulating fluidized bed gasification device and gasification process of the present utility model have
Following advantage：
1st, the cross section of burner hearth gradually changes from bottom to top, gradually increases from emulsion zone section to dilute phase section area.With
The progress of gasification reaction, although increasing in burner hearth middle and upper part gas volume, the cross-sectional area of burner hearth also increases step by step, because
This, makes burner hearth keep reasonable and relatively low fluidizing velocity, improves residence time of the fuel in stove.So, ensureing normally
Under conditions of circulation, promote gas-solid reaction, effectively improve gasification efficiency.
2nd, by introducing auxiliary gasifying agent on the burner hearth of circulating fluidized bed gasification device or along furnace height multistage distribution, carrying
High gasification furnace interior reaction temperature, thus reduces unburned carbon in flue dust, further, enhance auxiliary gasifying agent with it is not complete in burner hearth
The reaction of the carbon of full response, the gas-solid disturbance near wall region is enhanced, unburned carbon in flue dust is effectively reduced, it is cold to improve system
Coal gas efficiency.
3rd, greatly reduce the coal gas of gasification generation and the ratio of oxidation reaction occurs for auxiliary gasifying agent, reduce due to auxiliary gas
Influence of the introducing of agent to system cold gas efficiency.
4th, the coupling of reaction and flowing in burner hearth is optimized, is advantageous to the progress of gasification reaction, improves overall carbon conversion
Rate.
5th, the fluidizing velocity more than circulating fluidized bed gasification device two level returning charge point of the present utility model is low, can be to return
The carbon not reacted completely of burner hearth provides certain residence time, improves overall efficiency of carbon con version.
To sum up, variable cross-section circulating fluidized bed gasification device and gasification process of the present utility model alleviate recirculating fluidized bed gas
The unmatched problem of interior Temperature Distribution problem unmatched with reaction profile, gasification reaction and Gas-particle Flows and auxiliary is put in makeup
Gasifying agent consumes the problem of mass efficient gas, adds residence time of the particle in stove, enhances in auxiliary gasifying agent and burner hearth
The ratio of oxidation reaction occurs with auxiliary gasifying agent for the reaction for the carbon not reacted completely, the available gas for significantly reducing gasification generation
Example, effectively reduces unburned carbon in flue dust, improves system cold gas efficiency.
While there has been shown and described that embodiment of the present utility model, for the ordinary skill in the art,
It is appreciated that these embodiments can be changed in the case where not departing from principle of the present utility model and spirit.This practicality
The new scope of application is defined by the appended claims and the equivalents thereof.
Claims (10)
1. a kind of circulating fluidized bed gasification device of staged air distribution, including burner hearth (1), gas-solid separating device (2) and revert system,
It is characterized in that：Auxiliary gasification agent inlet (m1~m4) is provided with the burner hearth (1).
2. the circulating fluidized bed gasification device of staged air distribution according to claim 1, it is characterised in that：In the burner hearth
(1) main gasification agent inlet (q), material inlet (d), returning charge mouth (f), furnace outlet (g) and slag-drip opening are additionally provided with；
The revert system includes down-comer (3), material returning device (4) and returning charge inclined tube (5)；
Wherein, the auxiliary gasification agent inlet (m1~m4) is multiple that multiple auxiliary gasification agent inlets (m1~m4) are in multi-tier arrangement, point
Cloth at the different height of burner hearth (1), and
Every layer of auxiliary gasification agent inlet includes at least two auxiliary gasification agent inlets (m1~m4).
3. the circulating fluidized bed gasification device of staged air distribution according to claim 2, it is characterised in that：The auxiliary gasifying agent
Entrance (m1~m4) is located at main gasification agent inlet (q) the level above h of burner hearth (1), and 0.3H<h<0.75H, and in height
The barometric gradient of burner hearth at h
Wherein, H is total effective depth of burner hearth, i.e., from the main gasification agent inlet (q) of burner hearth (1) to the level of furnace outlet (g)
The distance of center line, p are the furnace pressure that h highly locates.
4. the circulating fluidized bed gasification device of staged air distribution according to claim 3, it is characterised in that：The multiple auxiliary gas
Agent entrance (m1~m4) is not overlapping in the projection on the cross section in the Longitudinal extending direction of burner hearth (1).
5. the circulating fluidized bed gasification device of staged air distribution according to claim 4, it is characterised in that：The multiple auxiliary gas
Agent entrance (m1~m4) the projection on the cross section in the Longitudinal extending direction of burner hearth (1) with etc. angular separation interval
Open.
6. the circulating fluidized bed gasification device of staged air distribution according to claim 5, it is characterised in that：The auxiliary gasifying agent
Entrance (m1~m4) is configured such that auxiliary gasifying agent enters burner hearth (1) in the horizontal direction.
7. the circulating fluidized bed gasification device of staged air distribution according to claim 5, it is characterised in that：The auxiliary gasifying agent
Entrance (m1~m4) be configured such that auxiliary gasifying agent with it is angled with the Longitudinal extending direction of burner hearth (1) and downward into
Burner hearth (1), the angle ranging from 0~45 °.
8. the circulating fluidized bed gasification device of the staged air distribution according to any one of claim 2-7, it is characterised in that：Institute
The material inlet (d) for stating burner hearth (1) is arranged at least between two layers of the auxiliary gasification agent inlet of multilayer (m1~m4).
9. the circulating fluidized bed gasification device of the staged air distribution according to any one of claim 1-7, it is characterised in that：Institute
Stating gas-solid separating device (2) includes one-level gas-solid separating device (2-1) and two level gas-solid separating device (2-2), and described returns
Material system includes one-level revert system and two level revert system.
10. the circulating fluidized bed gasification device of staged air distribution according to claim 1, it is characterised in that：The recycle stream
Changing bed gasifying apparatus includes material inlet (d), and the material inlet (d) is arranged on revert system.
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN107312575A (en) * | 2017-08-01 | 2017-11-03 | 中国科学院工程热物理研究所 | The circulating fluidized bed gasification device and gasification process of staged air distribution |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN107312575A (en) * | 2017-08-01 | 2017-11-03 | 中国科学院工程热物理研究所 | The circulating fluidized bed gasification device and gasification process of staged air distribution |
| CN107312575B (en) * | 2017-08-01 | 2023-07-18 | 中国科学院工程热物理研究所 | Circulating fluidized bed gasification device with graded air distribution and gasification method |
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