CN104762108B - Fluidized-bed gasification furnace and gasification system - Google Patents
Fluidized-bed gasification furnace and gasification system Download PDFInfo
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- CN104762108B CN104762108B CN201510104909.6A CN201510104909A CN104762108B CN 104762108 B CN104762108 B CN 104762108B CN 201510104909 A CN201510104909 A CN 201510104909A CN 104762108 B CN104762108 B CN 104762108B
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
- C10J3/46—Gasification of granular or pulverulent flues in suspension
- C10J3/54—Gasification of granular or pulverulent fuels by the Winkler technique, i.e. by fluidisation
- C10J3/56—Apparatus; Plants
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
- C10J3/46—Gasification of granular or pulverulent flues in suspension
- C10J3/54—Gasification of granular or pulverulent fuels by the Winkler technique, i.e. by fluidisation
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J2200/00—Details of gasification apparatus
- C10J2200/09—Mechanical details of gasifiers not otherwise provided for, e.g. sealing means
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J2200/00—Details of gasification apparatus
- C10J2200/15—Details of feeding means
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- Engineering & Computer Science (AREA)
- Combustion & Propulsion (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Organic Chemistry (AREA)
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Abstract
The present invention discloses a kind of fluidized-bed gasification furnace and gasification system, is related to gasification furnace technical field, and it is difficult that while both ensured the fluidisation of bulky grain coal dust, the problem of little particle fine coal is taken out of is prevented again to solve fluidized-bed gasification furnace of the prior art.Fluidized-bed gasification furnace of the present invention, including gasification furnace body, the top of the gasification furnace body are provided with gasification agent inlet provided with solid material inlet, bottom；The intrinsic lower area of gasification furnace is gasification reaction area, and the bottom internal diameter in the gasification reaction area is less than the top internal diameter in the gasification reaction area.Present invention is mainly applied in gasification process field.
Description
Technical field
The present invention relates to gasification furnace technical field, more particularly to a kind of fluidized-bed gasification furnace and gasification system.
Background technology
Coal gasification reaction is a thermochemical process, using fine coal (general diameter is less than 5mm fine coal) as raw material, in height
With gasifying agent reaction generation raw gas and tar light oil under warm condition of high voltage.
In coal gasification field, fluidized-bed gasification furnace is a kind of conventional coal gasification reaction device, its principle mainly to
Gasifying agent is passed through in gasification furnace, and rationally controls the gas flow of gasifying agent, so that the gas flow rate of gasifying agent reaches fine coal
The minimum fluidization velocity of grain, so that fine coal is in suspended state, and fully contacts with gasifying agent carry out gasification reaction.Wherein,
Pulverized coal particle meeting self exfoliation, the i.e. fine coal of part bulky grain can sink to the gas distribution grid of gasification furnace bottom under gravity
, so as to be easily caused congregate of the fine coal in gasification furnace of bulky grain, there is flow dead phenomenon in region.Specifically, in order to
Avoid the fine coal of bulky grain from dead band phenomenon occur in gasification furnace bottom, can improve big by increasing the gas flow rate of gasifying agent
The flow regime of particle fine coal；But, with the progress of gasification reaction, the gas volume in gasification furnace will increase, gas body
Long-pending increase can cause the increase of gas flow rate again, so that easily causing short grained fine coal is carried over gasification furnace.
Therefore when being passed through gasifying agent into fluidized-bed gasification furnace, ideal situation is：The gas flow rate of gasifying agent
It should ensure to make the fine coal of bulky grain reach flow regime, so as to avoid the defluidization phenomenon of fluidized-bed gasification furnace；While with
The progress of gasification reaction, the gas flow rate of gasifying agent again can not be excessive, in order to avoid take excessive little particle fine coal out of gasification furnace, from
And cause the utilization ratio of fine coal to reduce.
However, the gas flow rate of gasifying agent generally increases with the progress of reaction in fluidized-bed gasification furnace in the prior art
Greatly, therefore be difficult both to have ensured the fluidisation of bulky grain fine coal simultaneously, taking out of for little particle fine coal is prevented again.
The content of the invention
The present invention provides a kind of fluidized-bed gasification furnace and gasification system, solves fluidized-bed gasification furnace of the prior art very
The difficult fluidisation for both having ensured bulky grain fine coal simultaneously, prevents the problem of little particle fine coal is taken out of again.
To reach above-mentioned purpose, the present invention is adopted the following technical scheme that：
A kind of fluidized-bed gasification furnace, including gasification furnace body, the top of the gasification furnace body provided with solid material inlet,
Bottom is provided with gasification agent inlet；The intrinsic lower area of gasification furnace is gasification reaction area, the bottom in the gasification reaction area
Internal diameter is held to be less than the top internal diameter in the gasification reaction area.
Wherein, the ratio of the bottom internal diameter in the top internal diameter in the gasification reaction area and the gasification reaction area is d, and institute
State 1 ＜ d≤2.
Further, the inner side barrel in the gasification reaction area and the angle of horizontal direction are 75 in the gasification furnace body
Degree -85 is spent.
During practical application, the intrinsic upper zone of gasification furnace is pyrolysis zone, the inwall of the gasification furnace body
Buffering necking is provided with the bottom of the pyrolysis zone.
Wherein, the necking internal diameter in the buffering necking corresponding to smallest cross-section area is less than upper in the buffering necking
Bottom opening internal diameter, so as to be not more than the minimum fluidization velocity of material by the gas flow rate of gasifying agent at the buffering necking.
Specifically, the minimum fluidization velocity of the material refers to the minimum fluidization velocity of material average grain diameter.
Preferably, in the cohesive position between the buffering necking and the gasification furnace body, and the buffering necking
Reentrant diameter position be arc-shaped transition structure.
Further, the corresponding setting scope of angle in the buffering necking between the two side of the same side should be able to be protected
Exhibit material smoothly drops down onto down the gasification reaction area in the gasification furnace body from the pyrolysis zone.
During practical application, the angle in the buffering necking between the upper and lower two side of the same side is 60 degree -180 degree.
Preferably, the angle in the buffering necking between the upper and lower two side of the same side is 80 degree of -120 degree.
In the fluidized-bed gasification furnace that the present invention is provided, including gasification furnace body, the top of gasification furnace body is provided with solids
Expect that entrance, bottom are provided with gasification agent inlet；The intrinsic lower area of gasification furnace is gasification reaction area, the bottom in gasification reaction area
Internal diameter is that D1, the top internal diameter in gasification reaction area are D2, and D1 is less than D2.Thus analysis is understood, is entered by taking coal gasification reaction as an example
Row explanation, fine coal is entered in gasification furnace body by the solid material inlet at top, the gasification agent inlet that gasifying agent passes through bottom
Into in gasification furnace body, and fully contacted in gasification reaction area with fine coal and occur gasification reaction.Wherein, gasification reaction area
Bottom internal diameter is that D1, the top internal diameter in gasification reaction area are D2, and D1 is less than D2, therefore the intrinsic gasification reaction area of gasification furnace
Inboard cylinder footpath D2 is gradually increased to by D1 from bottom to top so that with the progress of gasification reaction, gas body in gasification reaction area
During product increase, the increase of gasification reaction area diameter can effectively offset the increase of gas volume in gasification furnace body, and then make gas
The gas flow rate of agent keeps constant or reduction.Therefore the fluidized-bed gasification furnace that the present invention is provided carries out reducing in gasification reaction area
Design, the gas flow rate and coal gasification reaction that can make gasifying agent match, so as to effectively solve large and small variable grain fine coal
The operating difficulties of fluidized-bed gasification furnace caused by flowing property difference, and then can improve the flow regime of bulky grain fine coal,
The band for reducing little particle fine coal simultaneously goes wrong, so that coal gasification reaction is more abundant, improves the utilization rate of fine coal.
The present invention also provides a kind of gasification system, including the fluidized-bed gasification furnace described in any of the above-described.
The gasification system that the present invention is provided has identical advantage with fluidized-bed gasification furnace, therefore will not be repeated here.
Brief description of the drawings
Fig. 1 is a kind of structural representation of fluidized-bed gasification furnace provided in an embodiment of the present invention；
Fig. 2 is the mplifying structure schematic diagram in gasification reaction area in a kind of fluidized-bed gasification furnace provided in an embodiment of the present invention；
Fig. 3 is the structural representation of another fluidized-bed gasification furnace provided in an embodiment of the present invention；
Fig. 4 is the mplifying structure schematic diagram of pyrolysis zone in another fluidized-bed gasification furnace provided in an embodiment of the present invention；
Fig. 5 is the structural representation of gasification system provided in an embodiment of the present invention.
In figure, 1- gasification furnace bodies；11- solid material inlets；12- gasification agent inlets；2- gas distribution grids；3- buffering contractings
Mouthful；4- dust removing systems；5- gas solid separation systems；A- gasification reactions area；B- pyrolysis zones.
Embodiment
A kind of fluidized-bed gasification furnace and gasification system provided in an embodiment of the present invention are retouched in detail below in conjunction with the accompanying drawings
State.
The embodiment of the present invention provides a kind of fluidized-bed gasification furnace, as shown in figure 1, including gasification furnace body 1, gasify furnace body
1 top is provided with gasification agent inlet 12 provided with solid material inlet 11, bottom；The lower area gasified in furnace body 1 is gasification
Reaction zone A, gasification reaction area A bottom internal diameter are that D1, gasification reaction area A top internal diameter are D2, and D1 is less than D2.
In fluidized-bed gasification furnace provided in an embodiment of the present invention, including gasification furnace body, the top of gasification furnace body is provided with
Solid material inlet, bottom are provided with gasification agent inlet；The intrinsic lower area of gasification furnace is gasification reaction area, gasification reaction area
Bottom internal diameter be that D1, the top internal diameter in gasification reaction area are D2, and D1 is less than D2.Thus analysis is understood, with coal gasification reaction
Exemplified by illustrate, fine coal is entered in gasification furnace body by the solid material inlet at top, the gasification that gasifying agent passes through bottom
Agent entrance enters in gasification furnace body, and is fully contacted in gasification reaction area with fine coal and occur gasification reaction.Wherein, gasified reverse
The bottom internal diameter for answering area is that D1, the top internal diameter in gasification reaction area are D2, and D1 is less than D2, therefore the intrinsic gasification of gasification furnace
The inboard cylinder footpath of reaction zone gradually increases to D2 by D1 from bottom to top, so that with the progress of gasification reaction, in gasification reaction area
During gas volume increase, the increase of gasification reaction area diameter can effectively offset the increase of gas volume in gasification furnace body, enter
And the gas flow rate of gasifying agent is kept constant or reduction.Therefore fluidized-bed gasification furnace provided in an embodiment of the present invention is in gasified reverse
Answer area to carry out variable diameter design, the gas flow rate and coal gasification reaction that can make gasifying agent match, thus effectively solve it is large and small not
With the operating difficulties of the fluidized-bed gasification furnace caused by the flowing property difference of particle fine coal, and then bulky grain fine coal can be improved
Flow regime, while the band for reducing little particle fine coal goes wrong, so that coal gasification reaction is more abundant, improve the utilization of fine coal
Rate.
Herein it should be added that, when gasifying agent, from gasification reaction area A to continue upwardly into internal diameter isometrical for D2
Gasify after furnace body 1, gas flow rate can keep constant, and the gas flow rate can be less than the carrying velocity of little particle fine coal,
It is carried over therefore, it is possible to be prevented effectively from the little particle fine coal in furnace body 1 that gasifies, so as to improve the utilization ratio of fine coal.
During practical application, in order that the gasifying agent entered from gasification agent inlet 12 in gasification furnace body 1 can be in gasified reverse
Answer dispersed at area A, to improve the efficiency of gasification reaction, the area of gasification agent inlet 12 can be closed on inside gasification furnace body 1
Gas distribution grid 2 is provided with domain, so that gasifying agent can be dispersed to gasification reaction area by the through hole on gas distribution grid 2
At A.Wherein, in order to improve the efficiency that gasifying agent enters in gasification furnace body 1, as shown in Fig. 2 gasification agent inlet 12 can be set
For two, so as to be passed through gasifying agent into gasification furnace body 1 simultaneously by two gasification agent inlets 12, to improve during unit
The influx of interior gasifying agent, and then improve the efficiency that gasifying agent enters in gasification furnace body 1.Specifically, in order that gas point
Fabric swatch 2 can be with two cooperatings of gasification agent inlet 12, and as depicted in figs. 1 and 2, gas distribution grid 2 can be to tilt down
The conical hopper formula structure of setting, so that in order to which the gasifying agent for flowing through one of entrance can be directly entered gasification reaction area
A, the gasifying agent for flowing through another entrance can be by gas distribution grid 2 even into gasification reaction area A, and then gasifying agent can
Gasification reaction area A is entered by two ways simultaneously, and fully contacted and stronger gasification reaction with fine coal.
Herein it should be added that, in order to avoid there is dead angle in gasification furnace body 1, influence coal gasification reaction enters
OK, as depicted in figs. 1 and 2, the bottom of gasification furnace body 1 is arcuate structure, that is, is between the side wall and bottom wall of the furnace body 1 that gasifies
Arc-shaped transition, so as to avoid the presence of dead angle area in the gasification furnace body 1 of right-angle structure, influences the progress of gasification reaction.
Specifically, above-mentioned D1 and D2 physical length, can rationally be set according to material characteristic or coal property, this
In the fluidized-bed gasification furnace that inventive embodiments are provided, in order to the flow regime for making bulky grain fine coal keep stable, subtract simultaneously
When young particle fine coal is taken out of, and above-mentioned D2 and D1 ratio can be d, and the d can be preferably 1 ＜ d≤2, so that such a ratio
The setting of example can make the gas flow rate of the gasifying agent at the region of gas distribution grid 2 be more than the initial flow of bulky grain fine coal well
Change speed, and less than the carrying velocity of little particle fine coal.
Further, in order that gasification reaction area A space is larger, in favor of the progress of gasification reaction, such as Fig. 1 and Fig. 2
Shown, gasification reaction area A inner side barrel and the angle of horizontal direction can be 75-85 degree in gasification furnace body 1, so as to
Ensure that gasification reaction area A changeover portion height is longer, to increase reaction compartment, and then be conducive to the coal gas in gasification reaction area A
Change the progress that reaction can more fully, stable.
In the practical application of coal gasification reaction, fine coal enters after gasification furnace body 1, by solid in the presence of self gravitation
Body material inlet 11 is fallen rapidly, because coal dust fall time is shorter, thus gasification furnace body 1 in middle and upper part pyrolysis zone B
Preferably can not fully carry out effecting reaction in the dropping process at place, and under drop down onto gasifying agent at gasification reaction area A with high temperature
After contact, coal dust is brought rapidly up, and temperature can exceed the optimum temperature of pyrolysis to cause coal dust to be fully pyrolyzed, finally
Also result in the utilization rate reduction of fine coal.
In another fluidized-bed gasification furnace provided in an embodiment of the present invention, under solving above-mentioned fine coal at the B of pyrolysis zone
The problem of terminal-velocity degree is very fast, as shown in Figure 3 and Figure 4, can be provided with gasification furnace body 1 at the pyrolysis zone B of upper zone
Necking 3 is buffered, the buffering necking 3 can be specifically arranged on the inwall of gasification furnace body 1.Therefore it can lead at the B of pyrolysis zone
The buffering necking 3 is crossed to adjust the gas flow rate in gasification furnace body 1, is dropped down onto so as to extend coal dust under solid material inlet 11
Time at gasification reaction area A, and then coal dust is fully reacted, improve its utilization rate.
Wherein, the necking internal diameter in buffering necking 3 corresponding to smallest cross-section area can for D3, the open internal diameter in top and the bottom
Think D2, and D3 is less than D2；When actual production is manufactured, this is not restricted for the concrete structure of buffering necking 3, as long as ensure that
Make the minimum fluidization velocity for being not more than material by buffering the gas flow rate of gasifying agent at necking 3.Specifically, for the ease of
The manufacture of necking 3 is buffered, and ensures that it has good buffering effect, as shown in Figure 3 and Figure 4, buffering necking 3 can be " ＞ ＜ "
Type structure, and " the middle part necking internal diameter of the buffering necking 3 of ＞ ＜ " type structures can be that D3, the open internal diameter in top and the bottom can be D2,
That is D3 ＜ D2.The internal diameter D2 for being less than gasification furnace body 1 due to buffering the middle part necking internal diameter D3 of necking 3 (buffers necking about 3
Open internal diameter D2), thus buffering necking 3 at gasifying agent gas flow rate it is higher, the raising of gas flow rate can produce drag force, from
And to offset the part gravity of coal dust, and then cushioning effect is played to the whereabouts of coal dust, fine coal is gathered at the B of pyrolysis zone
Collection, and extend residence time of the coal dust at the B of pyrolysis zone.Another fluidized-bed gasification furnace provided in an embodiment of the present invention, can
Coal dust is set to have time enough to carry out pyrolytic reaction with the gasifying agent from gasification reaction area A, so as to be effectively increased tar and first
The thermal decomposition products such as alkane, and to improve the economy of gasification process.
Specifically, the minimum fluidization velocity of above-mentioned material can refer to the minimum fluidization velocity of material average grain diameter；It is actual
In, in order that the gas flow rate of gasifying agent is not more than the minimum fluidization velocity of material (fine coal) average grain diameter at the B of pyrolysis zone,
So that the drag force produced by the gas flow rate improved can offset the part gravity of material, the both sides of the same side in buffering necking 3
The corresponding setting scope of angle between wall should be able to ensure that material is smoothly dropped down onto down in gasification furnace body 1 from pyrolysis zone B
Gasification reaction area A.Further, the angle in buffering necking 3 between the upper and lower two side of the same side can be 60-180 degree,
Preferably 80-120 degree；Using to provided in an embodiment of the present invention " in the buffering necking 3 of ＞ ＜ " type structures, such as Fig. 3 and Fig. 4 institutes
Show, above-mentioned " angle between the upper and lower sloped sidewall of the buffering necking 3 of ＞ ＜ " type structures can be 80-120 degree.
Wherein, in order to avoid forming deposition dead angle at the buffering necking 3 in gasification furnace body 1, fluidized-bed gasification furnace is influenceed
Gasification result, as shown in Figure 3 and Figure 4, necking 3 and gasification furnace sheet are buffered in fluidized-bed gasification furnace provided in an embodiment of the present invention
Reentrant diameter position in cohesive position between body 1, and buffering necking 3 can be arc-shaped transition structure.
Fluidized-bed gasification furnace provided in an embodiment of the present invention, with reference to gasifier operation and catalysis gasification technique, solves stream
Change the gas flow rate of gasifying agent and the fluidized state of pulverized coal particle and reaction matching problem in bed gasification furnace operating process, so that
Pulverized coal pyrolysis is more abundant, and improving flow regime in gasification furnace makes fine coal fully react, and then improves the utilization ratio of fine coal.
The embodiment of the present invention also provides a kind of gasification system, as shown in figure 5, including the fluid bed gas described in any of the above-described
Change stove.Wherein, the bottom of fluidized-bed gasification furnace can be connected with dust removing system 4, the tip side wall of fluidized-bed gasification furnace can connect
Be connected to gas solid separation system 5, thus coal dust can by solid material inlet 11 enter gasification furnace body 1, and under drop down onto on
At the pyrolysis zone B in portion, and occurs pyrolytic reaction；Then fine coal is dropped down onto at gasification reaction area A under continuing, and is contacted and is gone forward side by side with gasifying agent
Row gasification reaction；After occurring pyrolytic reaction and gasification reaction, fine coal discharges gas by the dust removing system 4 of the bottom of gasification furnace body 1
Change stove；Meanwhile, the gaseous product entrainment small part pulverized coal particle generated after reaction, the gas solid separation by the top of gasification furnace body 1
System 5 discharges gasification furnace, it is possible to carry out gas solid separation by cyclone separator, so that the solid powder after separation can be returned
Secondary response again is carried out at bottom gasification reaction area A in gasification furnace body 1, and the gaseous products after separation is entered follow-up
Subsequent treatment is carried out in cooling system.
In fluidized-bed gasification furnace and gasification system provided in an embodiment of the present invention, the structure of fluidized-bed gasification furnace is according to gasification
Reaction characteristicses are set, and the gas flow change during gasification reaction, and the flowing of control material can be adjusted, so as to effectively change
The flow regime of kind gasification furnace bottom section, it is to avoid flow dead occur, and then improve stop of the large granular materials in stove
Time, and the conversion ratio of large granular materials is improved, while taking out of for small particles material can be avoided, to improve the utilization of material
Efficiency, reduces the processing pressure of follow-up system.In addition, in fluidized-bed gasification furnace pyrolysis zone buffering necking setting, can
Effectively extension coal dust makes coal dust fully carry out hydropyrolysis reaction, so as to improve coal utilization in the residence time of pyrolysis zone
Rate, adds the thermal decomposition products such as tar and methane, and wherein tar yield can bring up to 3-5% by the 1-2% of traditional gasification furnace, enter
And effectively increase the economy of gasification process.
The foregoing is only a specific embodiment of the invention, but protection scope of the present invention is not limited thereto, any
Those familiar with the art the invention discloses technical scope in, the change or replacement that can be readily occurred in, all should
It is included within the scope of the present invention.Therefore, protection scope of the present invention should using the scope of the claims as
It is accurate.
Claims (10)
1. a kind of fluidized-bed gasification furnace, including gasification furnace body, the top of the gasification furnace body is provided with solid material inlet, bottom
Portion is provided with gasification agent inlet；The intrinsic lower area of gasification furnace is gasification reaction area, it is characterised in that the gasified reverse
The bottom internal diameter in area is answered to be less than the top internal diameter in the gasification reaction area；
The intrinsic upper zone of gasification furnace is pyrolysis zone, the bottom of the inwall of the gasification furnace body in the pyrolysis zone
Portion is provided with buffering necking；
The top and the bottom that necking internal diameter in the buffering necking corresponding to smallest cross-section area is less than in the buffering necking are open
Internal diameter, so as to be not more than the minimum fluidization velocity of material by the gas flow rate at the buffering necking.
2. fluidized-bed gasification furnace according to claim 1, it is characterised in that the top internal diameter in the gasification reaction area and institute
The ratio for stating the bottom internal diameter in gasification reaction area is d, and 1 ＜ d≤2.
3. fluidized-bed gasification furnace according to claim 1, it is characterised in that the gasification reaction in the gasification furnace body
The inner side barrel in area and the angle of horizontal direction are 75 degree of -85 degree.
4. fluidized-bed gasification furnace according to claim 1, it is characterised in that the minimum fluidization velocity of the material refers to thing
Expect the minimum fluidization velocity of average grain diameter.
5. fluidized-bed gasification furnace according to claim 1, it is characterised in that the buffering necking and the gasification furnace body
Between cohesive position, and it is described buffering necking in reentrant diameter position be arc-shaped transition structure.
6. the fluidized-bed gasification furnace according to claim any one of 1-5, it is characterised in that the same side in the buffering necking
Two side between angle corresponding set scope to ensure material in the gasification furnace body from the pyrolysis zone
The gasification reaction area is smoothly dropped down onto down.
7. fluidized-bed gasification furnace according to claim 6, it is characterised in that the same side is upper and lower in the buffering necking
Angle between two side is 60 degree -180 degree.
8. fluidized-bed gasification furnace according to claim 7, it is characterised in that the same side is upper and lower in the buffering necking
Angle between two side is 80 degree of -120 degree.
9. fluidized-bed gasification furnace according to claim 1, it is characterised in that the gasification furnace body interior closes on the gas
Agent entrance area is provided with gas distribution grid, and the gas distribution grid is the conical hopper formula structure for tilting down setting.
10. a kind of gasification system, it is characterised in that including the fluidized-bed gasification furnace described in the claims any one of 1-9.
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| CN108726507B (en) * | 2017-04-21 | 2020-11-13 | 山东大展纳米材料有限公司 | Device and method for single-stage continuous preparation of carbon nanotubes |
| CN107177384B (en) * | 2017-07-11 | 2020-06-19 | 新奥科技发展有限公司 | Catalytic gasification device, system and method |
| CN110129076B (en) * | 2019-04-23 | 2021-07-06 | 湖南现代环境科技股份有限公司 | Biomass low-temperature carbon gas co-production device, biomass low-temperature carbon gas co-production device and biomass low-temperature carbon gas co-production method |
| CN110205164B (en) * | 2019-06-11 | 2020-11-03 | 中国科学院工程热物理研究所 | Circulating fluidized bed gasification device and circulating fluidized bed gasification method |
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