CN101942344A - Method and device for gasifying multi-segment staged converted fluidized bed - Google Patents
Method and device for gasifying multi-segment staged converted fluidized bed Download PDFInfo
- Publication number
- CN101942344A CN101942344A CN2010102915774A CN201010291577A CN101942344A CN 101942344 A CN101942344 A CN 101942344A CN 2010102915774 A CN2010102915774 A CN 2010102915774A CN 201010291577 A CN201010291577 A CN 201010291577A CN 101942344 A CN101942344 A CN 101942344A
- Authority
- CN
- China
- Prior art keywords
- coal
- gas
- pipe
- gasification
- vapourizing furnace
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Granted
Links
Images
Classifications
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E20/00—Combustion technologies with mitigation potential
- Y02E20/16—Combined cycle power plant [CCPP], or combined cycle gas turbine [CCGT]
- Y02E20/18—Integrated gasification combined cycle [IGCC], e.g. combined with carbon capture and storage [CCS]
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
- Y02P20/129—Energy recovery, e.g. by cogeneration, H2recovery or pressure recovery turbines
Landscapes
- Fluidized-Bed Combustion And Resonant Combustion (AREA)
Abstract
The invention relates to method and device for gasifying a multi-segment staged converted fluidized bed. The method comprises the following steps of: supplying coal; supplying gas; gasifying; slagging; and conveying fine powder. The device for gasifying the multi-grade staged converted fluidized bed comprises an agglomerating ash separating unit, a pyrolyzing and gasifying reactor of the multi-segment staged fluidized bed and a semicoke fine powder cyclic feeding unit. The invention has the advantages of high volume utilization rate of a gasifying oven, great handling capacity and high utilization rate of total carbon, is suitable for a coal staging and converting system and can be singly used for producing gas for mass coal-based methane synthesis and coal chemical industry.
Description
Technical field
The invention belongs to a kind of method and device of gasification, be specifically related to method and device that a kind of multistage classification of adopting pyrolysis, gasification and burning integrated transforms the fluidized bed coal gasification.
Background technology
Gasification is one of core technology of coal high-efficiency, clean utilization, is the basis of process industrials such as the coal-based chemicals production of development, coal-based liquid fuel, synthetic natural gas (SNG), IGCC generating, hydrogen manufacturing, industrial combustion gas and polygenerations systeme.China is maximum in the world Coal Gasification Technology application market, but the most of enterprises of China are also using the atmospheric fixed bed vapourizing furnace that falls behind, and vaporization ability accounts for total capacity more than 70%.Rise in price and environmental consciousness along with the energy strengthens in recent years, a large amount of external Coal Gasification Technology are introduced China, and China has introduced surplus the Texaco coal slurry gasifier 30, and the Shell coal gasification only has a cover abroad, and signed more than 20 in China, the GSP coal gasification has also been signed 4 covers.In recent ten years, the combination involving production, teaching ﹠ research has promoted the development of domestic autonomous gasification technology, comprising: the opposed coal water slurry gasification technology of four nozzles of East China University of Science; The polynary slurry gasification technology of Xibei Chemical Inst; Two sections coal water slurry gasification technology of the non-slag-slag of Tsing-Hua University; The two-part pressurization dry coal powder gasification technology of Xi'an thermal technology institute; The HT-L that the Beijing Space Petrochemical Technology Equipment Engineering Co., Ltd researches and develops voluntarily (space flight stove) entrained flow bed gasification technology etc.
But these technology all belong to entrained flow bed gasification technology, must use the high-quality coal of low ash smelting point (＜1350 ℃) and low ash content (＜10～15%), and the method that solves high-ash-fusion coal normally adds 10～30% fusing assistant, make that the ash of charging is higher, influence its operability and economy.Simultaneously, the too high service temperature of air flow bed slag gasification technology improves investment, maintenance and the running cost of air flow bed.The research report of EPRI-Electric Power Research Institute (EPRI) points out that existing industrial gas bed gasification furnace is not suitable for high ash, high ash melting point coal gasification, and the world needs industrialized fluidized-bed gasification technology.No matter fluidization is burnt or gasified all has the person's character that adapts to high ash melting point, dirty coal kind, and the successful burning gangue of circular fluid bed is clear proof.
The diversity of texture of coal and composition, complicacy have determined clean efficient utilization that any single conversion process (burning, gasification) all can not realize coal.Therefore, coal reasonable use mode is to form constructional feature according to it, coupling pyrolysis, gasification and combustion technology, and at producing and the market requirement, realize the classification trans-utilization of different components in the coal, and can realize the gasification type of furnace that the Coal Gasification Technology of this process has only fluidized-bed to be best suited for.Therefore when optimizing the slag tap technology, various countries (comprise the U.S., Britain, Germany, Australia, India, China) all in the fluidized-bed gasification technology of developing mild temperature, its working temperature is about 1000 ℃, dry method is advanced coal, dry cinder discharging, coal adaptability is stronger, overall system efficiency is higher and investment and cost are lower, as the Transport gasification technology of U.S. KBR company, the fluidized bed coal gasification technology of Foster-wheel company, the fluidized-bed pressing gasization of Australia HRL company, the BHEL fluidizations of spouted fluidized bed technique of the ABGC of Britain and India etc. are all at research and development or industrial demonstration phase.
Shanxi Coal-Chemical Inst., Chinese Academy of Sciences has succeeded in developing " Unit of Coal Gasification for Pulverized Coal with Ash " complete set technology, coal wide ranges (from brown coal to the hard coal), and be fit to high ash, high ash melting point, high-sulfur coal gasification.Finished at present and handled 100 tons of bituminous coal and 0.6MPa pressurization day 320 tons of anthracitic industrial application of high-sulfur of processing normal pressure day, on 3.0MPa pressurized gasification pilot plant, finished the molten gather qi together test of 0.6-2.5MPa hard coal pressurization ash simultaneously.But compare with advanced gasification technology and to remain: 1) vapourizing furnace scale still big inadequately (industrial 300 tons of coal/days of single stove processing power at present); 2) solved ash discharge carbon content problem well, but coal gas entrained fines amount height, total efficiency of carbon conversion low (about 90%); 3) the vapourizing furnace volume utilization is low; 4) adopt the bottom concentrated oxygen supply, be prone to localized hyperthermia and form the bad and dead band of fluidisation.
How to realize the gasified raw material localization, it is most important to the Coal Chemical Industry development of China to develop the vapourizing furnace that is fit to different coal characteristics, derived product.Promoting to a higher rank of existing gasification technology realizes that the classification of coal transforms, and also is an important trend of Coal Gasification Technology development with the different technologies integrated optimization.Also need simultaneously to develop the gasification technology that is fit to carbonaceous solids material except that coal, comprise biomass, liquefied residue, petroleum residue and carbonaceous solids waste etc.
Summary of the invention
First purpose of the present invention provides a kind of extensive pyrolysis, the gasification of various coals and integrated fluidized bed gasification method that burns of being suitable for.
Second purpose of the present invention is to design a kind of simple in structure, and cost is low, but the dry ash extraction multistage classification of production methane rich coal gas transforms the fluidized-bed gasification device.
The present invention takes extensive integrated transformation technology thinking, realize the quick gasification of coal with fluidized-bed gasification, under relatively mild condition, change the material that easily transforms in the coal into product gas, the material that is difficult for transforming is taked the integration mode that burns, change the mode of reaction kinetics, to improve total speed of reaction; Increase the fine powder circulation, improve the fine powder residence time, strengthen the gas-solid contact, improve the reactor volume utilising efficiency, improve processing power; Utilize coal gas of high temperature, realize the coal fast pyrogenation, produce the synthetic gas of high methane content.To pursue the highest efficiency of carbon conversion and the Energy efficiency of system, reduce energy consumption and running cost, satisfy the variant production needs, realize that high vaporization ability is a target.
The method that multistage classification of the present invention transforms the fluidized bed coal gasification comprises the steps:
(1) preparation of gasified raw material coal
The feed coal fragmentation is after super-dry and screening, make brown coal moisture＜10wt%, bituminous coal or hard coal moisture＜5wt%, granularity is sent into the fine breeze storehouse less than the fine breeze of 0.5mm, granularity is sent into the broken coal storehouse between the broken coal of 0.5mm-6mm, all as the fluidized-bed gasification raw coal;
(2) gasification
A. at first vapourizing furnace is carried out baker, treat the vapourizing furnace temperature of lower greater than 900 ℃, upper temp is during greater than 600 ℃, at fluidized-bed lower gas sparger bubbling air, steam, add the gasification broken coal continuously from vapourizing furnace bottom broken coal feed-pipe, and press the air coal than 2.5～3.5Nm
3/ kg, steam coal are operated than 0.3～0.6kg/kg, make coal in the vapourizing furnace internal combustion, and obtain the semicoke furnace charge, set up material in the vapourizing furnace stove gradually;
B. the bed pressure drop for the treatment of semicoke material in the vapourizing furnace reaches 5-10KPa, switches to oxygen/humidified blast after system operation is stable, and temperature is controlled at 800～900 ℃ in the handoff procedure;
C. press the oxygen coal than 0.4～0.5Nm
3/ kg, steam coal are operated gasification than 0.5～1.0kg/kg, and the vapourizing furnace bottom temp is stabilized in 900～1100 ℃ of scopes;
D. after treating that the gasification of vapourizing furnace bottom is stable, the fine breeze feed-pipe of fine breeze from the vapourizing furnace middle part added continuously, the temperature maintenance at control vapourizing furnace middle part is at 700～900 ℃; Adjust vapourizing furnace bottom inflow amount, keep the vapourizing furnace temperature of lower and be stabilized in 900～1100 ℃ of scopes; Simultaneously, feed circulating gas and oxygen steam to vapourizing furnace top combustion gas gas blow pipe, coal gas: oxygen: the water vapour volume ratio is: 1: 0.3～0.6: 0.2～0.4, keep 900-1000 ℃ of vapourizing furnace upper temp; Vapourizing furnace working pressure 0.4-3.0MPa;
(3) deslagging of vapourizing furnace
In gasification, regulate annular separator tube gas speed at 5～10m/s, the oxygen concn＜25Vol% in the gas; Central jet pipe gas speed 15～30m/s, the oxygen concn 40～60vol% in the gas, by adjusting annular release pipe gas speed, the control bed drain purge makes the interior semicoke furnace charge of vapourizing furnace keep bed pressure reduction between 4～8KPa; The lime-ash of discharging is delivered to burning in circulating fluid bed boiler with the lime-ash of rich carbon through air-transport system after separating, remaining lime-ash discharging;
(4) purification of raw gas and waste heat recovery
Spray into chilled water in the vapourizing furnace outlet, assurance whirlwind temperature in＜900 ℃, raw gas separates through primary cyclone, the semicoke fine powder that captures is through semicoke fine powder circulating solid tube, semicoke fine powder cycle control high-temperature valve, be blown into the concentrated phase fluidized-bed gasification section of pyrolytic gasification reactor lower part, participate in reaction once more; Raw gas enters secondary cyclone, and the semicoke fine powder of capture is sent into burning in circulating fluid bed boiler through semicoke fines collection/cooling tank, fine powder handling machinery; Through waste heat boiler, vapor superheater, de-oxygenised water preheater, gas temperature is reduced to 50-170 ℃ and is entered Venturi water scrubber and water-cooled eluting column through the coal gas of high temperature of roughing out, further exports gas purification workshop section to after cooling and the dedusting;
(5) vapourizing furnace stops
During orderly shutdown, at first cut off the circulating gas and the oxygen steam of vapourizing furnace top combustion gas gas blow pipe; Stop coal; Cut-out enters back system gas line, and coal gas emptying is depressurized to normal pressure gradually; Afterwards, reduce annular release pipe gas speed and strengthen the ash discharge amount, strengthen the fluidized bed steam consumption simultaneously, close oxygen valve, close the bottom of vapourizing furnace and advance the coal measures system, temperature is controlled at below 900 ℃ in the stove, after furnace charge has been arranged, stop air inlet, final system is used steam, air purge one time respectively.
A kind of simple in structure in order to realize that the present invention has designed, the multistage classification that cost is low transforms the fluidized bed coal gasification installation.
It is from the unit by molten poly-ash content that dry ash extraction multistage classification of the present invention transforms the fluidized-bed gasification device, the pyrolytic gasification reactor, semicoke fine powder circulation supply unit is formed, described molten poly-ash content is made of cylindrical gas chamber shell, circular cone grid distributor, reducing pipe, central jet pipe, annular release pipe, ash tube and grid distributor vaporized chemical inlet pipe from the unit, the circular cone grid distributor is positioned at the top of cylindrical gas chamber shell, be inverted cone shape, equally distributed pneumatic outlet is arranged on the circular cone grid distributor; Circular cone grid distributor bottom links to each other with reducing pipe, reducing pipe bottom and annular release pipe coupling, in cylindrical gas chamber shell bottom lagging material is arranged, by cylindrical gas chamber shell, the circular cone grid distributor, reducing pipe, annular release pipe and lagging material constitute circular cone grid distributor inlet plenum, the central jet pipe is arranged in the annular release pipe, and be positioned at the axis, outlet is contour with circular cone grid distributor grid distributor bottom, grid distributor vaporized chemical inlet pipe is arranged in circular cone grid distributor inlet plenum, the lower end of annular release pipe is being positioned at outside the cylindrical gas chamber shell bottom, and link to each other with ash tube, ash tube has annular release pipe inlet mouth, and the ash tube bottom is a slag-drip opening; Described pyrolytic gasification reactor is by circular body of heater, bottom concentrated phase fluidized-bed gasification section, middle part fast pyrogenation gasification reaction section, high temperature tar cracking section in top constitutes, concentrated phase fluidized-bed gasification section has the broken coal feed-pipe in the bottom, baker gas pipe and semicoke fine powder feed-pipe, and fast pyrogenation gasification reaction section has the fine breeze feed-pipe at the middle part, high temperature tar cracking section has the combustion gas gas blow pipe on top, and furnace roof has the outlet of gentleization of Quench water pipe producer gas; Described semicoke fine powder circulation supply unit is by primary cyclone, semicoke fine powder circulating solid tube, semicoke fine powder cycle control high-temperature valve is formed, primary cyclone links to each other with the gasifier gas outlet, the bottom of primary cyclone connects semicoke fine powder circulating solid tube, semicoke fine powder circulating solid tube bottom connects semicoke fine powder cycle control high-temperature valve, and semicoke fine powder cycle control high-temperature valve bottom is connected with semicoke fine powder feed-pipe by inclined tube, has fine powder to return the steam gas blow pipe on inclined tube.
Circular cone grid distributor, reducing pipe and annular release pipe constitute by fire-resistant and lagging material.
The percentage of open area of described circular cone grid distributor is 0.5%-2%, and the aperture is Φ 3-5mm, and the angle β of element of cone and central shaft is 20 °～50 °.
Described circular body of heater is by body of heater, and lagging material and refractory materials are formed, and are lagging materials between body of heater and the refractory materials.
The angle γ of the element of cone of described reducing pipe and central shaft is 5 °-20 °.
The present invention has following advantage:
1) the vapourizing furnace working pressure can reach 3.0MPa, and treatment capacity is big, and the compression energy consumption is low;
2) adopt the selectivity ash content from, dry cinder discharging, the ash discharge carbon content is low, and the coal gas entrained fines improves total vaporized carbon transformation efficiency by the high recycle ratio increase residence time;
3) adopt the coal grading conversion process, unconverted fine powder efficiently transforms by the CFB boiler combustion, produces high-temperature steam (about 600 ℃) as vaporized chemical; Can directly use broken coal, reduce the coal-grinding power consumption, the total energy consumption of system is low, and the oxygen consumption is low;
4) adopt staged addition of oxygen, vapourizing furnace volume utilization height, the slagging scorification risk is little;
5) structure of reactor is simple, no special refractory, and cost is low; Simple to operate, long service life;
6) coal wide ranges, the most of coals of gasifiable China;
7) methane content can be adjusted according to the synthetic gas purposes in the coal gas, reaches as high as more than 5%, is fit to coal preparing natural gas project.
Description of drawings
Fig. 1 gathers ash content from cell schematics for the present invention is molten
Fig. 2 transforms fluidized bed coal gasification installation structural representation for the multistage classification
Fig. 3 transforms fluidized bed coal gasifying process schema for the multistage classification
As shown in the figure, 1 is cylindrical gas chamber shell, 2 is the circular cone grid distributor, 3 is reducing pipe, 4 is the central jet pipe, 5 is the annular release pipe, 6 is the sparger joint flange, 7 is circular cone grid distributor inlet plenum, 8 are the outlet of circular cone grid distributor, 9 is lagging material, 10 is ash tube, 11 is grid distributor vaporized chemical inlet pipe, 12 is pipe core vaporized chemical inlet pipe, 13 is annular release pipe vaporized chemical inlet pipe, 14 is slag-drip opening, 15 is body of heater, 16 is lagging material, 17 is refractory materials, 18 is top coke tar cracking section, 19 is middle part fast pyrogenation gasification reaction section, 20 is bottom concentrated phase fluidized-bed gasification section, the outlet of 21 gasifier gas, 22 is primary cyclone, and 23 is semicoke fine powder circulating solid tube, and 24 is semicoke fine powder cycle control high-temperature valve, 25 is semicoke fine powder feed-pipe, 26 is the broken coal feed-pipe, and 27 is the baker gas pipe, and 28 is the fine breeze feed-pipe, 29 are the combustion gas gas blow pipe, 30 is furnace roof Quench water pipe, and 31 for fine powder returns the steam gas blow pipe, and 32 is last coal rotary conveyor, 33 is vibrating screen classifier, 34 is crusher, and 35 is moisture eliminator, and 36 is dry fine breeze rotoclone collector, 37 is dry fine breeze warehouse, 38 for taking the fine powder trap out of, and 39 is the fine breeze handling machinery, and 40 is dry broken coal rotary conveyor (1), 41 is broken coal lift (1), 42 is dry broken coal warehouse, and 43 is dry broken coal rotary conveyor (2), and 44 is dry broken coal lift (2), 45 is the broken coal hopper, 46 is rotary feeder, and 47 for the multistage classification transforms vapourizing furnace, and 48 are the ash discharge ash bucket, 49 is secondary cyclone, 50 for secondary cyclone captures fines collection jar and handling machinery, and 51 is the heating gas heat recovery boiler, and 52 is the boiler bubble, 53 is vapor superheater, 54 is the de-oxygenised water preheater, and 55 is Venturi scrubber, and 56 are column plate type washing tower, 57 is flashing tower, 58 is air water separator, and 59 is thick thionizer, and 60 is coal gas pressure regulator valve, 61 is the coal gas sub-cylinder, 62 is the oxygen sub-cylinder, and 63 is the superheated vapour steam distributor, and 64 is the air sub-cylinder.
Embodiment
Gasification process of the present invention and specific equipment accompanying drawings thereof are as follows:
Embodiment 1:
By melting poly-ash content from the unit, pyrolytic gasification reactor, semicoke fine powder circulation supply unit composition, described molten poly-ash content from the unit by cylindrical gas chamber shell 1, circular cone grid distributor 2, reducing pipe 3, central jet pipe 4, annular release pipe 5, sparger joint flange 6, lagging material 9, be ash tube 10, grid distributor vaporized chemical inlet pipe 11, pipe core vaporized chemical inlet pipe 12, annular release pipe vaporized chemical inlet pipe 13, slag-drip opening 14 constitutes.Circular cone grid distributor 2 is positioned at the top of cylindrical gas chamber shell 1, is inverted cone shape, and equally distributed pneumatic outlet 8 is arranged on the circular cone grid distributor 2; Circular cone grid distributor 2 bottoms link to each other with reducing pipe 3, reducing pipe 3 bottoms are connected with annular release pipe 5, in cylindrical gas chamber shell 1 bottom lagging material 9 is arranged, by cylindrical gas chamber shell 1, circular cone grid distributor 2, reducing pipe 3, annular release pipe 5 and lagging material 9 constitute circular cone grid distributor inlet plenum 7, central jet pipe 4 is arranged in annular release pipe 5, and be positioned at the axis, outlet is contour with circular cone grid distributor 2 grid distributors bottom, in circular cone grid distributor inlet plenum 7, inlet pipe 11 is arranged, the lower end of annular release pipe (5) is being positioned at outside cylindrical gas chamber shell (1) bottom, and link to each other with ash tube (10), ash tube 10 has annular release pipe inlet mouth 13, and ash tube 10 bottoms are slag-drip opening 14; Described pyrolytic gasification reactor is by circular body of heater 15, bottom concentrated phase fluidized-bed gasification section 20, middle part fast pyrogenation gasification reaction section 19, top high temperature tar cracking section 18 constitutes, in bottom concentrated phase fluidized-bed gasification section 20 broken coal feed-pipe 26 is arranged, baker gas pipe 27 and semicoke fine powder feed-pipe 25 have fine breeze feed-pipe 28 in middle part fast pyrogenation gasification reaction section 19, in top high temperature tar cracking section 18 combustion gas gas blow pipe 29 is arranged, furnace roof has Quench water pipe 30 and gasifier gas outlet 21; Described semicoke fine powder circulation supply unit is by primary cyclone 22, semicoke fine powder circulating solid tube 23, semicoke fine powder cycle control high-temperature valve 24 is formed, primary cyclone 22 links to each other with gasifier gas outlet 21, the bottom of primary cyclone 22 connects semicoke fine powder circulating solid tube 23, semicoke fine powder circulating solid tube 23 bottoms connect semicoke fine powder cycle control high-temperature valve 24, semicoke fine powder cycle control high-temperature valve 24 bottoms are connected 25 by inclined tube with semicoke fine powder feed-pipe, have fine powder to return steam gas blow pipe 31 on inclined tube.
Circular cone grid distributor 2, reducing pipe 3 and annular release pipe 5 constitute by fire-resistant and lagging material.
The percentage of open area of described circular cone grid distributor 2 is 2%, and the aperture is Φ 5mm, and the angle β of element of cone and central shaft is 20 °.
Described circular body of heater is by body of heater 15, and lagging material 16 and refractory materials form 17, are lagging materials 16 between body of heater 15 and the refractory materials 17.
The angle γ of the element of cone of described reducing pipe and central shaft is 5 °.
Concrete gasification is implemented as follows:
Shaanxi Bin County raw coal is sent into vibrating screen classifier 33 through last coal rotary conveyor 32, and granularity is crushed to the broken coal of granularity less than 6mm greater than the raw coal of 6mm through crusher 34, and raw coal enters moisture eliminator 35 dryings under the sieve of vibrating screen classifier 33.Less than 0.5mm fine breeze drying fine breeze rotoclone collector 36 with take fine powder trap 38 out of to enter dry fine breeze warehouse 37 stand-by; 0.5mm to the broken coal drying broken coal rotary conveyor 40 of 6mm, broken coal lift 41, it is stand-by to enter dry broken coal warehouse 43.
At first vapourizing furnace is carried out baker, the baker air is from air sub-cylinder 64, baker coal gas is from coal gas sub-cylinder 61, air is respectively by grid distributor vaporized chemical inlet pipe 11, pipe core vaporized chemical inlet pipe 12, annular release pipe vaporized chemical inlet pipe 13 enters vapourizing furnace, and coal gas enters vapourizing furnace by baker gas pipe 27.Treat that vapourizing furnace bottom dense phase fluidized bed gasification section 20 temperature reach 900 ℃, after top coke tar cracking section 18 temperature reach 600 ℃, by each road inlet pipe 11,12,13 bubbling air 2500Nm
3/ h and steam 400kg/h (steam comes from superheated vapour steam distributor 63) open rotary feeder 46 and quantitatively add the gasification broken coal continuously from vapourizing furnace broken coal feed-pipe 26, keep coal input quantity 1000kg/h, air capacity 2500Nm
3/ h, quantity of steam 400kg/h.Set up bed (bed in about pressure reduction 6KPa), switch to oxygen/humidified blast when temperature, pressure, flow system all reach after imposing a condition, oxygen comes from oxygen sub-cylinder 62, oxygen feeding amount 500Nm
3/ h, water vapor amount 1000kg/h, temperature is controlled at about 800～900 ℃ in the handoff procedure, slowly regulate oxygen, steam flow then, guarantee flow velocity, oxygen concn that circular cone grid distributor 2, annular release pipe 5 and central jet pipe 4 need, progressively regulate gasification system pressure to 0.6MP, regulate coal input quantity simultaneously to 1500kg/h, amount of oxygen is to 750Nm
3/ h, quantity of steam are to 1500kg/h, and temperature-stable is at the set point value of 900～1100 ℃ of scopes.
Behind the system stability, fine breeze in the dry fine breeze warehouse 37 is passed through fine breeze handling machinery 39, quantitatively add vapourizing furnace top continuously from vapourizing furnace top fine powder feed-pipe 28, coal input quantity is controlled at about 400kg/h, and the temperature maintenance of control vapourizing furnace middle part fast pyrogenation gasification reaction section 19 is at 700～900 ℃; Adjust the bottom inflow amount, keep bottom dense phase fluidized bed gasification section 20 temperature-stables 900～1100 ℃ of scopes; Simultaneously, feed circulating gas and oxygen steam to vapourizing furnace top combustion gas gas blow pipe 29, ratio is: 1: 0.5: 0.3 (volume ratio), circulating gas amount 120Nm
3/ h, amount of oxygen 60Nm
3/ h, quantity of steam 36kg/h keeps 900-1000 ℃ of vapourizing furnace upper temp.
Lime-ash in the vapourizing furnace 47 enters in the ash discharge ash bucket 48 through vapourizing furnace bottom ash tube 10, regularly discharges lime-ash from ash discharge ash bucket 48.In operational process,, guarantee that coal gas is in vapourizing furnace temperature out＜900 ℃ by adjusting the chilled water flow in the furnace roof Quench water pipe 30.Raw gas separates through primary cyclone 22, the semicoke fine powder that captures is through semicoke fine powder circulating solid tube 23, semicoke fine powder cycle control high-temperature valve 24, the steam that is returned 31 feedings of steam gas blow pipe by fine powder is blown into vapourizing furnace dense phase fluidized bed gasification section 20, participates in reaction once more; Raw gas enters secondary cyclone 49, and the semicoke fine powder of capture is sent into down preface workshop section through secondary cyclone capture fines collection jar and handling machinery 50; Coal gas of high temperature after the roughing out is through heating gas heat recovery boiler 51, vapor superheater 53, de-oxygenised water preheater 54, gas temperature is reduced to and is entered Venturi water scrubber 55, column plate type washing tower 56, air water separator 58, thick thionizer 59 about 100 ℃, and further cooling and dedusting are after coal gas pressure regulator valve 60 exports gas purification workshop section to.
Embodiment 2:
The percentage of open area of circular cone grid distributor is 1.5%, and the aperture is Φ 4mm, and the angle β of element of cone and central shaft is 30 °.The angle γ of the element of cone of reducing pipe and central shaft is 7 °.
Fluidized-bed bottom broken coal coal input quantity 2000kg/h, oxygen feeding amount 1000Nm
3/ h, water vapor amount 2000kg/h, vapourizing furnace middle part fine breeze inlet amount 550kg/h, the vapourizing furnace pressure-controlling is at 1.0MPa, top burner noz(zle) circulating gas amount 180Nm
3/ h, amount of oxygen 90Nm
3/ h, quantity of steam 55kg/h, all the other are with embodiment 1.
Embodiment 3: the percentage of open area of circular cone grid distributor is 1.0%, and the aperture is Φ 4mm, and the angle β of element of cone and central shaft is 40 °.The angle γ of the element of cone of reducing pipe and central shaft is 7 °.
Fluidized-bed bottom broken coal coal input quantity 2500kg/h, oxygen feeding amount 1250Nm
3/ h, water vapor amount 2500kg/h, vapourizing furnace middle part fine breeze inlet amount 650kg/h, the vapourizing furnace pressure-controlling is at 1.5MPa, top burner noz(zle) circulating gas amount 230Nm
3/ h, amount of oxygen 115Nm
3/ h, quantity of steam 70kg/h, all the other are with embodiment 1.
Embodiment 4: the percentage of open area of circular cone grid distributor is 1.0%, and the aperture is Φ 4mm, and the angle β of element of cone and central shaft is 45 °.The angle γ of the element of cone of reducing pipe and central shaft is 8 °.
Fluidized-bed bottom broken coal coal input quantity 2900kg/h, oxygen feeding amount 1450Nm
3/ h, water vapor amount 2900kg/h, vapourizing furnace middle part fine breeze inlet amount 700kg/h, the vapourizing furnace pressure-controlling is at 2.0MPa, top burner noz(zle) circulating gas amount 260Nm
3/ h, amount of oxygen 130Nm
3/ h, quantity of steam 80kg/h, all the other are with embodiment 1.
Embodiment 5: the percentage of open area of circular cone grid distributor is 0.5%, and the aperture is Φ 4mm, and the angle β of element of cone and central shaft is 50 °.The angle γ of the element of cone of reducing pipe and central shaft is 9 °.
Fluidized-bed bottom broken coal coal input quantity 3200kg/h, oxygen feeding amount 1600Nm
3/ h, water vapor amount 3200kg/h, vapourizing furnace middle part fine breeze inlet amount 800kg/h, the vapourizing furnace pressure-controlling is at 2.5MPa, top burner noz(zle) circulating gas amount 290Nm
3/ h, amount of oxygen 145Nm
3/ h, quantity of steam 90kg/h, all the other are with embodiment 1.
List in table 1 as the novel solid slag-discharing dry-powder air-current bed gasification preparing synthetic gas gas composition of carrying out under the embodiment 1-5 condition.
The multistage classification transforms the gas composition of fluidized bed coal vaporizing system synthetic gas under table 1 different condition
| Embodiment 1 | Embodiment 2 | Embodiment 3 | Embodiment 4 | |
|
| Vapor pressure, MPa | 0.6 | 1.0 | 1.5 | 2.0 | 2.5 |
| Gasification temperature, ℃ | 1030 | 1025 | 1030 | 1025 | 1020 |
| The bottom coal input quantity, kg/h | 1500 | 2000 | 2500 | 2900 | 3200 |
| The middle part coal input quantity, kg/h | 400 | 550 | 650 | 700 | 800 |
| Total oxygen feeding amount, Nm 3/h | 810 | 1090 | 1365 | 1580 | 1745 |
| Total quantity of steam, kg/h | 1536 | 2055 | 2570 | 2980 | 3290 |
| Dry gas is formed Vol.% | |||||
| H 2 | 36.43 | 38.04 | 37.72 | 37.23 | 37.98 |
| N 2 | 8.8 | 5.17 | 5.54 | 6.05 | 5.57 |
| CO | 24.36 | 25.62 | 26.85 | 26.8 | 28.16 |
| CH 4 | 4.61 | 5.17 | 5.09 | 5.32 | 5.69 |
| CO 2 | 25.8 | 26 | 24.8 | 24.6 | 22.6 |
| Factor of created gase Nm3/kg | 2.04 | 2.05 | 2.03 | 2.02 | 2.01 |
| Caloric power of gas Kcal/Nm 3 | 2419.66 | 2566.31 | 2587.51 | 2591.59 | 2695.01 |
| Efficiency of carbon conversion % | 91 | 90 | 90.2 | 90.1 | 90.3 |
| Cold gas efficiency % | 73.67 | 78.52 | 78.40 | 78.13 | 80.85 |
Claims (6)
1. a multistage classification transforms the method that fluidized bed coal gasifies, and it is characterized in that comprising the steps:
(1) preparation of gasified raw material coal
The feed coal fragmentation is after super-dry and screening, make brown coal moisture＜10wt%, bituminous coal or hard coal moisture＜5wt%, granularity is sent into the fine breeze storehouse less than the fine breeze of 0.5mm, granularity is sent into the broken coal storehouse between the broken coal of 0.5mm-6mm, all as the fluidized-bed gasification raw coal;
(2) gasification
A. at first vapourizing furnace is carried out baker, treat the vapourizing furnace temperature of lower greater than 900 ℃, upper temp is during greater than 600 ℃, at fluidized-bed lower gas sparger bubbling air, steam, add the gasification broken coal continuously from vapourizing furnace bottom broken coal feed-pipe, and press the air coal than 2.5～3.5Nm
3/ kg, steam coal are operated than 0.3～0.6kg/kg, make coal in the vapourizing furnace internal combustion, and obtain the semicoke furnace charge, set up material in the vapourizing furnace stove gradually;
B. the bed pressure drop for the treatment of semicoke material in the vapourizing furnace reaches 5-10KPa, switches to oxygen/humidified blast after system operation is stable, and temperature is controlled at 800～900 ℃ in the handoff procedure;
C. press the oxygen coal than 0.4～0.5Nm
3/ kg, steam coal are operated gasification than 0.5～1.0kg/kg, and the vapourizing furnace bottom temp is stabilized in 900～1100 ℃ of scopes;
D. after treating that the gasification of vapourizing furnace bottom is stable, the fine breeze feed-pipe of fine breeze from the vapourizing furnace middle part added continuously, the temperature maintenance at control vapourizing furnace middle part is at 700～900 ℃; Adjust vapourizing furnace bottom inflow amount, keep the vapourizing furnace temperature of lower and be stabilized in 900～1100 ℃ of scopes; Simultaneously, feed circulating gas and oxygen steam to vapourizing furnace top combustion gas gas blow pipe, coal gas: oxygen: the water vapour volume ratio is: 1: 0.3～0.6: 0.2～0.4, keep 900-1000 ℃ of vapourizing furnace upper temp; Vapourizing furnace working pressure 0.4-3.0MPa;
(3) deslagging of vapourizing furnace
In gasification, regulate annular separator tube gas speed at 5～10m/s, the oxygen concn＜25Vol% in the gas; Central jet pipe gas speed 15～30m/s, the oxygen concn 40～60vol% in the gas, by adjusting annular release pipe gas speed, the control bed drain purge makes the interior semicoke furnace charge of vapourizing furnace keep bed pressure reduction between 4～8KPa; The lime-ash of discharging is delivered to burning in circulating fluid bed boiler with the lime-ash of rich carbon through air-transport system after separating, remaining lime-ash discharging;
(4) purification of raw gas and waste heat recovery
Spray into chilled water in the vapourizing furnace outlet, assurance whirlwind temperature in＜900 ℃, raw gas separates through primary cyclone, the semicoke fine powder that captures is through semicoke fine powder circulating solid tube, semicoke fine powder cycle control high-temperature valve, be blown into the concentrated phase fluidized-bed gasification section of pyrolytic gasification reactor lower part, participate in reaction once more; Raw gas enters secondary cyclone, and the semicoke fine powder of capture is sent into burning in circulating fluid bed boiler through semicoke fines collection/cooling tank, fine powder handling machinery; Through waste heat boiler, vapor superheater, de-oxygenised water preheater, gas temperature is reduced to 50-170 ℃ and is entered Venturi water scrubber and water-cooled eluting column through the coal gas of high temperature of roughing out, further exports gas purification workshop section to after cooling and the dedusting;
(5) vapourizing furnace stops
During orderly shutdown, at first cut off the circulating gas and the oxygen steam of vapourizing furnace top combustion gas gas blow pipe; Stop coal; Cut-out enters back system gas line, and coal gas emptying is depressurized to normal pressure gradually; Afterwards, reduce annular release pipe gas speed and strengthen the ash discharge amount, strengthen the fluidized bed steam consumption simultaneously, close oxygen valve, close the bottom of vapourizing furnace and advance the coal measures system, temperature is controlled at below 900 ℃ in the stove, after furnace charge has been arranged, stop air inlet, final system is used steam, air purge one time respectively.
2. a kind of multistage classification as claimed in claim 1 transforms the device of fluidized bed coal gasification, it is from the unit by molten poly-ash content, the pyrolytic gasification reactor, semicoke fine powder circulation supply unit is formed, described molten poly-ash content from the unit by cylindrical gas chamber shell (1), circular cone grid distributor (2), reducing pipe (3), central jet pipe (4), annular release pipe (5), lagging material (9), ash tube (10), grid distributor vaporized chemical inlet pipe (11), pipe core vaporized chemical inlet pipe (12), annular release pipe vaporized chemical inlet pipe (13), slag-drip opening (14) constitutes, circular cone grid distributor (2) is positioned at the top of cylindrical gas chamber shell (1), is inverted cone shape, and equally distributed pneumatic outlet (8) is arranged on the circular cone grid distributor (2); Circular cone grid distributor (2) bottom links to each other with reducing pipe (3), reducing pipe (3) bottom is connected with annular release pipe (5) upper end, in cylindrical gas chamber shell (1) bottom lagging material (9) is arranged, by cylindrical gas chamber shell (1), circular cone grid distributor (2), reducing pipe (3), annular release pipe (5) and lagging material (9) constitute circular cone grid distributor inlet plenum (7), central jet pipe (4) is arranged in annular release pipe (5), and be positioned at the axis, outlet is contour with circular cone grid distributor 2 grid distributors bottom, grid distributor vaporized chemical inlet pipe (11) is arranged in circular cone grid distributor inlet plenum (7), the lower end of annular release pipe (5) is being positioned at outside cylindrical gas chamber shell (1) bottom, and link to each other with ash tube (10), ash tube (10) has annular release pipe inlet mouth (13), and ash tube (10) bottom is slag-drip opening (14); Described pyrolytic gasification reactor is by circular body of heater (15), bottom concentrated phase fluidized-bed gasification section (20), middle part fast pyrogenation gasification reaction section (19), top high temperature tar cracking section (18) constitutes, in bottom concentrated phase fluidized-bed gasification section (20) broken coal feed-pipe (26) is arranged, baker gas pipe (27) and semicoke fine powder feed-pipe (25), in middle part fast pyrogenation gasification reaction section (19) fine breeze feed-pipe (28) is arranged, in top high temperature tar cracking section (18) combustion gas gas blow pipe (29) is arranged, furnace roof has Quench water pipe (30) and gasifier gas outlet (21); Described semicoke fine powder circulation supply unit is by primary cyclone (22), semicoke fine powder circulating solid tube (23), semicoke fine powder cycle control high-temperature valve (24) is formed, primary cyclone (22) links to each other with gasifier gas outlet (21), the bottom of primary cyclone (22) connects semicoke fine powder circulating solid tube (23), semicoke fine powder circulating solid tube (23) bottom connects semicoke fine powder cycle control high-temperature valve (24), semicoke fine powder cycle control high-temperature valve (24) bottom is connected with semicoke fine powder feed-pipe (25) by inclined tube, has fine powder to return steam gas blow pipe (31) on inclined tube.
3. a kind of multistage classification as claimed in claim 2 transforms the device of fluidized bed coal gasification, and (50 by fire-resistant and lagging material formation to it is characterized in that circular cone grid distributor (2), reducing pipe (3) and annular release pipe.
4. a kind of multistage classification as claimed in claim 2 transforms the device of fluidized bed coal gasification, and the percentage of open area that it is characterized in that described circular cone grid distributor (2) is 0.5%-2%, and the aperture is Φ 3-5mm, and the angle β of element of cone and central shaft is 20 °～50 °.
5. a kind of multistage classification as claimed in claim 2 transforms the device of fluidized bed coal gasification, it is characterized in that described circular body of heater (15) is by the body of heater shell, lagging material (16) and refractory materials are formed (17), are lagging material (16) between body of heater shell and the refractory materials (17).
6. a kind of multistage classification as claimed in claim 2 transforms the device of fluidized bed coal gasification, it is characterized in that the element of cone of described reducing pipe (3) and the angle γ of central shaft are 5 °-20 °.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2010102915774A CN101942344B (en) | 2010-09-20 | 2010-09-20 | Method and device for gasifying multi-segment staged converted fluidized bed |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2010102915774A CN101942344B (en) | 2010-09-20 | 2010-09-20 | Method and device for gasifying multi-segment staged converted fluidized bed |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN101942344A true CN101942344A (en) | 2011-01-12 |
| CN101942344B CN101942344B (en) | 2013-10-30 |
Family
ID=43434555
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN2010102915774A Active CN101942344B (en) | 2010-09-20 | 2010-09-20 | Method and device for gasifying multi-segment staged converted fluidized bed |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN101942344B (en) |
Cited By (48)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102226109A (en) * | 2011-05-23 | 2011-10-26 | 中国东方电气集团有限公司 | Multistage series-connection gasifier chamber structure |
| CN102353042A (en) * | 2011-09-09 | 2012-02-15 | 北京交通大学 | Adjusting method for circulating ash quantity, separator and combustion system |
| CN102533345A (en) * | 2011-12-14 | 2012-07-04 | 中国科学院山西煤炭化学研究所 | Method and device for coal gasification in combined type fluidized bed |
| CN102585907A (en) * | 2012-03-02 | 2012-07-18 | 上海交通大学 | Step oxygen supply dry slag removal pressure gasification testing system |
| WO2012162971A1 (en) * | 2011-05-27 | 2012-12-06 | 北京神雾环境能源科技集团股份有限公司 | Cyclone bed pulverized coal gasification method and system thereof |
| CN102827644A (en) * | 2012-09-18 | 2012-12-19 | 山东天力干燥股份有限公司 | Gas distributor for ash agglomerating fluidized-bed gasification furnace |
| CN103113923A (en) * | 2013-02-21 | 2013-05-22 | 山东润银生物化工股份有限公司 | Four-segment spray coal oxygen-enriched gasification method |
| CN103450947A (en) * | 2013-09-02 | 2013-12-18 | 中国天辰工程有限公司 | Novel lignite gasification process by using fluidized bed with ash circulation and equipment of novel lignite gasification process |
| CN103534339A (en) * | 2011-03-18 | 2014-01-22 | 埃克洛普有限公司 | Moving bed reactor |
| CN103740409A (en) * | 2014-01-23 | 2014-04-23 | 东南大学 | Multi-stage gas distribution high-temperature coal gasification device and method |
| CN103937552A (en) * | 2014-03-24 | 2014-07-23 | 北京交通大学 | Three-section entrained flow bed hydrogenation vaporizing furnace and combined operation system |
| CN103980945A (en) * | 2014-05-23 | 2014-08-13 | 李轼 | Biomass gasifier with external combustor and biomass gasification method |
| CN104263410A (en) * | 2014-09-28 | 2015-01-07 | 中国东方电气集团有限公司 | Coal gasification waste heat recovery system |
| CN104277882A (en) * | 2014-10-15 | 2015-01-14 | 中国科学院山西煤炭化学研究所 | Gas distributor for fluidized bed gasification furnace |
| CN104277881A (en) * | 2014-09-25 | 2015-01-14 | 上海锅炉厂有限公司 | Dry-process deslagging fluidized bed gasification reaction device |
| CN104403692A (en) * | 2014-12-11 | 2015-03-11 | 赛鼎工程有限公司 | Technology and equipment for producing clean gas by gasifying broken molten coal slag |
| CN104531224A (en) * | 2015-01-04 | 2015-04-22 | 武汉江汉化工设计有限公司 | Clean coal pressurized fluidized bed slag gasification process and system |
| CN104593088A (en) * | 2015-01-23 | 2015-05-06 | 新奥科技发展有限公司 | Coal gasification reaction device and method |
| CN104593081A (en) * | 2014-12-11 | 2015-05-06 | 赛鼎工程有限公司 | Process and device for production of clean fuel gas from coal |
| CN104726137A (en) * | 2015-03-04 | 2015-06-24 | 湖南谷力新能源科技股份有限公司 | High-utilization-ratio biomass gasification reactor |
| CN104789271A (en) * | 2015-04-07 | 2015-07-22 | 龙东生 | Low-temperature dry distillation and gasification device for powder |
| CN104804774A (en) * | 2015-04-21 | 2015-07-29 | 北京神雾环境能源科技集团股份有限公司 | Method and device for preparing fuel gas by utilizing ash coal as raw material |
| CN104830375A (en) * | 2015-04-21 | 2015-08-12 | 北京神雾环境能源科技集团股份有限公司 | Method and device for preparation of fuel gas from waste carbon as raw material |
| CN104862011A (en) * | 2015-05-25 | 2015-08-26 | 山东百川同创能源有限公司 | Pyrolysis gasification system for biomass solid waste and hazardous waste |
| CN104862015A (en) * | 2015-06-01 | 2015-08-26 | 上海河图工程股份有限公司 | Two-stage temperature-control fossil fuel gasification equipment |
| CN105419879A (en) * | 2015-11-05 | 2016-03-23 | 东华工程科技股份有限公司 | Device and method for catalytically decomposing coal substances and separating coal substances at high temperatures |
| CN105658773A (en) * | 2013-09-18 | 2016-06-08 | 林德股份公司 | Method and plant for the at least partial gasification of solid organic feedstock |
| CN106010666A (en) * | 2016-07-25 | 2016-10-12 | 上海锅炉厂有限公司 | Circulating fluidized bed gasifying system and gasifying method thereof |
| CN106590757A (en) * | 2015-10-15 | 2017-04-26 | 中国石油化工股份有限公司 | Device and method for segmented-oxygen-blowing catalytic coal gasification |
| CN106675658A (en) * | 2016-12-15 | 2017-05-17 | 华北电力大学 | Device and method for high-flux circulating fluidized bed low-rank coal gasifying |
| CN107227174A (en) * | 2017-07-18 | 2017-10-03 | 枣庄学院 | A kind of Novel brown coal gasification system and method |
| CN107446629A (en) * | 2017-08-31 | 2017-12-08 | 北京神雾电力科技有限公司 | The system and method for handling low-order coal |
| CN107937035A (en) * | 2017-11-30 | 2018-04-20 | 陕西延长石油（集团）有限责任公司 | A kind of powdered coal pressuring gasified device and method of double-circulating fluid bed two sections of couplings |
| CN108368440A (en) * | 2015-12-18 | 2018-08-03 | 三菱日立电力系统株式会社 | Gasification installation, the control device and method of gasification installation, integrated gasification combined cycle plant |
| CN108473894A (en) * | 2015-11-13 | 2018-08-31 | 金顕泳 | Industrial high temperature reformers and reforming method |
| CN108865204A (en) * | 2018-06-27 | 2018-11-23 | 陕西延长石油（集团）有限责任公司 | A kind of apparatus and method of recirculating fluidized bed fine coal high pressure thermal transition volume increase tar |
| CN108929722A (en) * | 2018-07-26 | 2018-12-04 | 新奥科技发展有限公司 | A kind of coal gasification method and gasification system |
| CN109022044A (en) * | 2018-10-19 | 2018-12-18 | 四川蓝星机械有限公司 | A kind of coal gasification reaction device |
| CN109797012A (en) * | 2018-12-19 | 2019-05-24 | 中国科学院山西煤炭化学研究所 | High-temperature fluidized bed device and its method of carbonaceous material gasification |
| CN110055115A (en) * | 2019-04-26 | 2019-07-26 | 上海电气集团股份有限公司 | A kind of start and stop method of two-section type crude material gasifying electricity generation system |
| CN110055103A (en) * | 2018-09-27 | 2019-07-26 | 新能能源有限公司 | The cooling of novel hydrogenation gasification char and collection device |
| CN110129100A (en) * | 2019-05-28 | 2019-08-16 | 彭万旺 | Highly effective combustion system and method |
| US10392572B2 (en) | 2015-01-30 | 2019-08-27 | Lummus Technology Inc. | Standpipe-fluid bed hybrid system for char collection, transport, and flow control |
| CN110540206A (en) * | 2018-05-29 | 2019-12-06 | 新特能源股份有限公司 | online slag discharging device and method for fluidized bed reactor |
| CN111763535A (en) * | 2020-06-29 | 2020-10-13 | 中国科学院山西煤炭化学研究所 | Method and device for preparing fuel gas or synthesis gas by biomass fluidized bed gasification |
| CN112238004A (en) * | 2019-07-16 | 2021-01-19 | 中国石油化工股份有限公司 | Cyclone separator and pulverized coal fluidization gasification separation device |
| CN112410076A (en) * | 2020-12-08 | 2021-02-26 | 中国科学院工程热物理研究所 | Air distribution slag cooling device and method for fluidized bed gasification furnace |
| CN112940789A (en) * | 2021-01-26 | 2021-06-11 | 中国华能集团清洁能源技术研究院有限公司 | Two-section gasification furnace with high slag capturing rate and waste boiler system |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1405277A (en) * | 2002-09-27 | 2003-03-26 | 中国科学院山西煤炭化学研究所 | Solid slag-discharing dry-powder air-current bed gasification process and apparatus |
| CN101372635A (en) * | 2008-10-15 | 2009-02-25 | 东南大学 | High-density pressurized fluidized bed coal gasification apparatus and method |
-
2010
- 2010-09-20 CN CN2010102915774A patent/CN101942344B/en active Active
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1405277A (en) * | 2002-09-27 | 2003-03-26 | 中国科学院山西煤炭化学研究所 | Solid slag-discharing dry-powder air-current bed gasification process and apparatus |
| CN101372635A (en) * | 2008-10-15 | 2009-02-25 | 东南大学 | High-density pressurized fluidized bed coal gasification apparatus and method |
Cited By (68)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103534339A (en) * | 2011-03-18 | 2014-01-22 | 埃克洛普有限公司 | Moving bed reactor |
| CN102226109A (en) * | 2011-05-23 | 2011-10-26 | 中国东方电气集团有限公司 | Multistage series-connection gasifier chamber structure |
| WO2012162971A1 (en) * | 2011-05-27 | 2012-12-06 | 北京神雾环境能源科技集团股份有限公司 | Cyclone bed pulverized coal gasification method and system thereof |
| CN102353042A (en) * | 2011-09-09 | 2012-02-15 | 北京交通大学 | Adjusting method for circulating ash quantity, separator and combustion system |
| CN102533345A (en) * | 2011-12-14 | 2012-07-04 | 中国科学院山西煤炭化学研究所 | Method and device for coal gasification in combined type fluidized bed |
| CN102585907A (en) * | 2012-03-02 | 2012-07-18 | 上海交通大学 | Step oxygen supply dry slag removal pressure gasification testing system |
| CN102585907B (en) * | 2012-03-02 | 2013-11-27 | 上海交通大学 | Step oxygen supply dry slag removal pressure gasification testing system |
| CN102827644A (en) * | 2012-09-18 | 2012-12-19 | 山东天力干燥股份有限公司 | Gas distributor for ash agglomerating fluidized-bed gasification furnace |
| CN103113923A (en) * | 2013-02-21 | 2013-05-22 | 山东润银生物化工股份有限公司 | Four-segment spray coal oxygen-enriched gasification method |
| CN103450947A (en) * | 2013-09-02 | 2013-12-18 | 中国天辰工程有限公司 | Novel lignite gasification process by using fluidized bed with ash circulation and equipment of novel lignite gasification process |
| CN103450947B (en) * | 2013-09-02 | 2016-03-09 | 中国天辰工程有限公司 | A kind of fluidized-bed brown coal hydrogasification technique with ash content circulation |
| CN105658773A (en) * | 2013-09-18 | 2016-06-08 | 林德股份公司 | Method and plant for the at least partial gasification of solid organic feedstock |
| CN103740409A (en) * | 2014-01-23 | 2014-04-23 | 东南大学 | Multi-stage gas distribution high-temperature coal gasification device and method |
| CN103740409B (en) * | 2014-01-23 | 2015-05-13 | 东南大学 | Multi-stage gas distribution high-temperature coal gasification device and method |
| CN103937552A (en) * | 2014-03-24 | 2014-07-23 | 北京交通大学 | Three-section entrained flow bed hydrogenation vaporizing furnace and combined operation system |
| CN103937552B (en) * | 2014-03-24 | 2015-11-18 | 北京交通大学 | A kind of three-section type entrained flow bed coal hydrogenation gasification stove and combined operation system |
| CN103980945A (en) * | 2014-05-23 | 2014-08-13 | 李轼 | Biomass gasifier with external combustor and biomass gasification method |
| CN104277881A (en) * | 2014-09-25 | 2015-01-14 | 上海锅炉厂有限公司 | Dry-process deslagging fluidized bed gasification reaction device |
| CN104263410A (en) * | 2014-09-28 | 2015-01-07 | 中国东方电气集团有限公司 | Coal gasification waste heat recovery system |
| CN104277882A (en) * | 2014-10-15 | 2015-01-14 | 中国科学院山西煤炭化学研究所 | Gas distributor for fluidized bed gasification furnace |
| CN104403692A (en) * | 2014-12-11 | 2015-03-11 | 赛鼎工程有限公司 | Technology and equipment for producing clean gas by gasifying broken molten coal slag |
| CN104593081B (en) * | 2014-12-11 | 2017-01-04 | 赛鼎工程有限公司 | The technique of coal clean gas and device |
| CN104593081A (en) * | 2014-12-11 | 2015-05-06 | 赛鼎工程有限公司 | Process and device for production of clean fuel gas from coal |
| CN104403692B (en) * | 2014-12-11 | 2016-08-24 | 赛鼎工程有限公司 | The gasification of broken coal slag produces the Processes and apparatus of clean gas |
| CN104531224B (en) * | 2015-01-04 | 2017-02-22 | 武汉江汉化工设计有限公司 | Clean coal pressurized fluidized bed slag gasification process and system |
| CN104531224A (en) * | 2015-01-04 | 2015-04-22 | 武汉江汉化工设计有限公司 | Clean coal pressurized fluidized bed slag gasification process and system |
| CN104593088A (en) * | 2015-01-23 | 2015-05-06 | 新奥科技发展有限公司 | Coal gasification reaction device and method |
| US10392572B2 (en) | 2015-01-30 | 2019-08-27 | Lummus Technology Inc. | Standpipe-fluid bed hybrid system for char collection, transport, and flow control |
| CN104726137A (en) * | 2015-03-04 | 2015-06-24 | 湖南谷力新能源科技股份有限公司 | High-utilization-ratio biomass gasification reactor |
| CN104789271A (en) * | 2015-04-07 | 2015-07-22 | 龙东生 | Low-temperature dry distillation and gasification device for powder |
| CN104804774B (en) * | 2015-04-21 | 2017-06-06 | 北京神雾环境能源科技集团股份有限公司 | A kind of method and apparatus for preparing combustion gas as raw material with dirty coal |
| CN104830375A (en) * | 2015-04-21 | 2015-08-12 | 北京神雾环境能源科技集团股份有限公司 | Method and device for preparation of fuel gas from waste carbon as raw material |
| CN104804774A (en) * | 2015-04-21 | 2015-07-29 | 北京神雾环境能源科技集团股份有限公司 | Method and device for preparing fuel gas by utilizing ash coal as raw material |
| CN104862011A (en) * | 2015-05-25 | 2015-08-26 | 山东百川同创能源有限公司 | Pyrolysis gasification system for biomass solid waste and hazardous waste |
| CN104862015A (en) * | 2015-06-01 | 2015-08-26 | 上海河图工程股份有限公司 | Two-stage temperature-control fossil fuel gasification equipment |
| CN106590757A (en) * | 2015-10-15 | 2017-04-26 | 中国石油化工股份有限公司 | Device and method for segmented-oxygen-blowing catalytic coal gasification |
| CN105419879B (en) * | 2015-11-05 | 2020-07-10 | 东华工程科技股份有限公司 | Device and method for catalytic decomposition and high-temperature separation of coal substances |
| CN105419879A (en) * | 2015-11-05 | 2016-03-23 | 东华工程科技股份有限公司 | Device and method for catalytically decomposing coal substances and separating coal substances at high temperatures |
| CN108473894A (en) * | 2015-11-13 | 2018-08-31 | 金顕泳 | Industrial high temperature reformers and reforming method |
| CN108368440B (en) * | 2015-12-18 | 2021-03-05 | 三菱动力株式会社 | Gasification device, control device and method for gasification device, and gasification combined power generation facility |
| CN108368440A (en) * | 2015-12-18 | 2018-08-03 | 三菱日立电力系统株式会社 | Gasification installation, the control device and method of gasification installation, integrated gasification combined cycle plant |
| CN106010666B (en) * | 2016-07-25 | 2022-03-22 | 上海锅炉厂有限公司 | Circulating fluidized bed gasification system and gasification method thereof |
| CN106010666A (en) * | 2016-07-25 | 2016-10-12 | 上海锅炉厂有限公司 | Circulating fluidized bed gasifying system and gasifying method thereof |
| CN106675658A (en) * | 2016-12-15 | 2017-05-17 | 华北电力大学 | Device and method for high-flux circulating fluidized bed low-rank coal gasifying |
| CN106675658B (en) * | 2016-12-15 | 2020-05-05 | 华北电力大学 | High-flux circulating fluidized bed low-order coal gasification device and method |
| CN107227174A (en) * | 2017-07-18 | 2017-10-03 | 枣庄学院 | A kind of Novel brown coal gasification system and method |
| CN107446629A (en) * | 2017-08-31 | 2017-12-08 | 北京神雾电力科技有限公司 | The system and method for handling low-order coal |
| CN107937035B (en) * | 2017-11-30 | 2023-09-26 | 陕西延长石油（集团）有限责任公司 | Pulverized coal pressurized gasification device and method with two sections of double-circulation fluidized bed coupled |
| CN107937035A (en) * | 2017-11-30 | 2018-04-20 | 陕西延长石油（集团）有限责任公司 | A kind of powdered coal pressuring gasified device and method of double-circulating fluid bed two sections of couplings |
| CN110540206A (en) * | 2018-05-29 | 2019-12-06 | 新特能源股份有限公司 | online slag discharging device and method for fluidized bed reactor |
| CN110540206B (en) * | 2018-05-29 | 2021-05-11 | 新特能源股份有限公司 | Online slag discharging device and method for fluidized bed reactor |
| CN108865204A (en) * | 2018-06-27 | 2018-11-23 | 陕西延长石油（集团）有限责任公司 | A kind of apparatus and method of recirculating fluidized bed fine coal high pressure thermal transition volume increase tar |
| CN108929722A (en) * | 2018-07-26 | 2018-12-04 | 新奥科技发展有限公司 | A kind of coal gasification method and gasification system |
| CN108929722B (en) * | 2018-07-26 | 2020-05-12 | 新奥科技发展有限公司 | Coal gasification method and coal gasification system |
| CN110055103A (en) * | 2018-09-27 | 2019-07-26 | 新能能源有限公司 | The cooling of novel hydrogenation gasification char and collection device |
| CN110055103B (en) * | 2018-09-27 | 2023-11-07 | 新能能源有限公司 | Novel hydro-gasification semicoke cooling and collecting device |
| CN109022044A (en) * | 2018-10-19 | 2018-12-18 | 四川蓝星机械有限公司 | A kind of coal gasification reaction device |
| CN109022044B (en) * | 2018-10-19 | 2023-10-20 | 四川蓝星机械有限公司 | Coal gasification reaction device |
| CN109797012A (en) * | 2018-12-19 | 2019-05-24 | 中国科学院山西煤炭化学研究所 | High-temperature fluidized bed device and its method of carbonaceous material gasification |
| CN110055115A (en) * | 2019-04-26 | 2019-07-26 | 上海电气集团股份有限公司 | A kind of start and stop method of two-section type crude material gasifying electricity generation system |
| CN110129100A (en) * | 2019-05-28 | 2019-08-16 | 彭万旺 | Highly effective combustion system and method |
| CN110129100B (en) * | 2019-05-28 | 2023-12-22 | 彭万旺 | Efficient combustion system and method |
| CN112238004A (en) * | 2019-07-16 | 2021-01-19 | 中国石油化工股份有限公司 | Cyclone separator and pulverized coal fluidization gasification separation device |
| CN111763535A (en) * | 2020-06-29 | 2020-10-13 | 中国科学院山西煤炭化学研究所 | Method and device for preparing fuel gas or synthesis gas by biomass fluidized bed gasification |
| CN111763535B (en) * | 2020-06-29 | 2021-09-03 | 中国科学院山西煤炭化学研究所 | Method and device for preparing fuel gas or synthesis gas by biomass fluidized bed gasification |
| CN112410076A (en) * | 2020-12-08 | 2021-02-26 | 中国科学院工程热物理研究所 | Air distribution slag cooling device and method for fluidized bed gasification furnace |
| CN112410076B (en) * | 2020-12-08 | 2021-10-08 | 中国科学院工程热物理研究所 | Air distribution slag cooling device and method for fluidized bed gasification furnace |
| CN112940789A (en) * | 2021-01-26 | 2021-06-11 | 中国华能集团清洁能源技术研究院有限公司 | Two-section gasification furnace with high slag capturing rate and waste boiler system |
Also Published As
| Publication number | Publication date |
|---|---|
| CN101942344B (en) | 2013-10-30 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN101942344B (en) | Method and device for gasifying multi-segment staged converted fluidized bed | |
| CN102533345B (en) | Method and device for coal gasification in combined type fluidized bed | |
| CN100577775C (en) | Coal gasification device of circulating fluidized bed and method for generating coal gas by using coal gasification device | |
| CN101412929B (en) | High temperature gasification technological process and system for preparing synthesis gas by using biomass | |
| CN103436296B (en) | Slag gasifier for pressurized fixed bed | |
| CN1931959B (en) | Compositely circulating high temperature gasifying process for making synthetic gas with biomass | |
| CN101418239B (en) | High temperature gasification technological process and system for preparing synthesis gas by using biomass | |
| CN201395576Y (en) | Fluidized bed pulverized coal low-temperature dry distillation poly-generation device | |
| CN106010666A (en) | Circulating fluidized bed gasifying system and gasifying method thereof | |
| CN102358841B (en) | Multistage pulverized coal multiple-tube rotary low temperature dry distillation technology and system | |
| CN101418240B (en) | High-temperature gasification process method and system for producing synthesis gas by using biomass | |
| CN102618330A (en) | High temperature normal pressure biomass gasification island process | |
| CN101108986A (en) | Gray melting poly-fluid bed powder coal gasification method | |
| CN102911686B (en) | Coal destructive distillation method and apparatus | |
| CN101412930B (en) | Quality improving reaction device for high-moisture solid fuel and process thereof | |
| CN101418238B (en) | High temperature gasification technological process and system for preparing synthesis gas by using biomass | |
| CN109852429A (en) | A kind of hydrogen generating system and method for coal combustion coupling rubbish steam gasification | |
| CN201046952Y (en) | Coal gasification device of circulating fluidized bed | |
| CN100362084C (en) | Internal and external circulation coal gasification method and device | |
| CN201530809U (en) | Two-stage-plasma high temperature gasification equipment | |
| CN103740409A (en) | Multi-stage gas distribution high-temperature coal gasification device and method | |
| CN103113905A (en) | Composite pulverized coal destructive distillation device and method | |
| CN105273763A (en) | Heat pipe heating type biomass and coal segmented collaborative pyrolysis system | |
| CN204058390U (en) | Solid fuel classification gasification-burning double bed polygenerations systeme | |
| CN106995706A (en) | A kind of heat accumulating type external heat pressurization pyrolysis of coal device and method |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant |