CN101942344B - 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
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- CN101942344B CN101942344B CN2010102915774A CN201010291577A CN101942344B CN 101942344 B CN101942344 B CN 101942344B CN 2010102915774 A CN2010102915774 A CN 2010102915774A CN 201010291577 A CN201010291577 A CN 201010291577A CN 101942344 B CN101942344 B CN 101942344B
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- 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
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- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E20/00—Combustion technologies with mitigation potential
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- 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
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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 a kind ofly adopt pyrolysis, gasification and method and the device of the integrated gasifying multi-segment staged converted fluidized bed that burns.
Background technology
Gasification is one of core technology of coal high-efficiency, clean utilization, is the basis of the 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 China's most enterprises is 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 Texaco coal slurry gasifier more than 30 platforms, 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, so that the ash of charging is higher, affect 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, it is to form constructional feature according to it that coal reasonably utilizes mode, coupling pyrolysis, gasification and combustion technology, and for the production ﹠ marketing demand, realize the staged conversion utilization of different components in the coal, and can realize the gasification type of furnace that the Coal Gasification Technology of this process only has 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, such as the Transport gasification technology of U.S. KBR company, the In The Fluidized Bed Coal Gasification Technology of Foster-wheel company, the fluidized-bed pressing gas of Australia HRL company, the BHEL fluidizations of the spouted fluidized bed technique of the ABGC of Britain and India etc. are all in research and development or Industrial demonstration stage.
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.Finish at present the industrial application of processing 100 tons of bituminous coal and 0.6MPa pressurization day 320 tons of Anthracites 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 large not (at present industrial 300 tons of coal/days of single stove processing power); 2) solved well ash discharge carbon content problem, but coal gas entrained fines amount is high, 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 Development of Coal Chemical Industry of China to develop the vapourizing furnace that is fit to Coal rank characteristic, derived product.Promoting to a higher rank of existing gasification technology, the staged conversion of realization coal 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 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 staged conversion fluidized-bed gasification device of production methane rich coal gas.
The present invention takes large-scale integrated transformation technology thinking, realize the Quick-gasifying 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 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 high carbon conversions and the Energy efficiency of system, reduce energy consumption and running cost, satisfy the variant production needs, realize that high vaporization ability is target.
The method of gasifying multi-segment staged converted fluidized bed of the present invention comprises the steps:
(1) gasified raw material preparation of coal
The feed coal fragmentation is by 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 passes into air, steam at fluidized-bed lower gas sparger during greater than 600 ℃, add continuously the gasification broken coal from vapourizing furnace bottom broken coal feed-pipe, and press the air coal than 2.5～3.5Nm
3/ kg, steam coal operate than 0.3～0.6kg/kg, make coal in the vapourizing furnace internal combustion, and obtain the semicoke furnace charge, set up gradually material in the vapourizing furnace stove;
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 operate gasification than 0.5～1.0kg/kg, and the vapourizing furnace bottom temp is stabilized in 900～1100 ℃ of scopes;
D. after 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 at control vapourizing furnace middle part maintains 700～900 ℃; Adjust vapourizing furnace bottom inflow amount, keep the vapourizing furnace temperature of lower and be stabilized in 900～1100 ℃ of scopes; Simultaneously, pass into circulating gas and oxygen/water 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 separator tube 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, again participate in reaction; 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 down 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 circulating gas and the oxygen/water steam of vapourizing furnace top combustion gas gas blow pipe; Stop coal; Cut-out enters rear 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 simultaneously the fluidized bed steam consumption, 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 is drained, stop air inlet, final system is used respectively steam, air purge one time.
A kind of simple in structure in order to realize that the present invention has designed, the gasifying multi-segment staged converted fluidized bed device that cost is low.
Dry ash extraction multistage staged conversion fluidized-bed gasification device of the present invention is from the unit by molten poly-ash content, the pyrolytic gasification reactor, semicoke fine powder circulation supply unit forms, 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, the reducing pipe bottom is connected with the annular release pipe, 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 consist of 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 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 consists of, 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 forms, 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 at inclined tube.
Circular cone grid distributor, reducing pipe and annular release pipe consist of 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 form, 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 large, 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 produces high-temperature steam (about 600 ℃) as vaporized chemical by CFB boiler combustion Efficient Conversion; 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, the vapourizing furnace volume utilization is high, and the slagging scorification risk is little;
5) structure of reactor is simple, and without special refractory, 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 is that the molten poly-ash content of the present invention is from cell schematics
Fig. 2 is gasifying multi-segment staged converted fluidized bed apparatus structure synoptic diagram
Fig. 3 is the gasifying multi-segment staged converted fluidized bed process flow sheet
As shown in the figure, 1 is cylindrical gas chamber shell, 2 is the circular cone grid distributor, 3 is reducing pipe, jet pipe centered by 4,5 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, pipe vaporized chemical inlet pipe centered by 12,13 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 upper 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 is multistage staged conversion vapourizing furnace, and 48 are the ash discharge ash bucket, 49 is secondary cyclone, 50 for secondary cyclone captures fines collection tank 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 consists of.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 consist of 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 consists of, 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 forms, 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 at inclined tube.
Circular cone grid distributor 2, reducing pipe 3 and annular release pipe 5 consist of 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 upper coal rotary conveyor 32, and granularity is crushed to granularity less than the broken coal of 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 ℃, pass into air 2500Nm by each road inlet pipe 11,12,13
3/ h and steam 400kg/h (steam comes from superheated vapour steam distributor 63) open rotary feeder 46 and quantitatively add continuously the gasification broken coal 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, then slowly regulate oxygen, steam flow, 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 simultaneously coal input quantity 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 continuously vapourizing furnace top from vapourizing furnace top fine powder feed-pipe 28, coal input quantity is controlled at about 400kg/h, and the temperature of control vapourizing furnace middle part fast pyrogenation gasification reaction section 19 maintains 700～900 ℃; Adjust the bottom inflow amount, keep bottom dense phase fluidized bed gasification section 20 temperature-stables 900～1100 ℃ of scopes; Simultaneously, pass into circulating gas and oxygen/water 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, by adjusting the chilled water flow in the furnace roof Quench water pipe 30, guarantee that coal gas is in vapourizing furnace temperature out＜900 ℃.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, returned the steam that steam gas blow pipe 31 passes into by fine powder and be blown into vapourizing furnace dense phase fluidized bed gasification section 20, again participate in reaction; Raw gas enters secondary cyclone 49, and the semicoke fine powder of capture captures fines collection tank and handling machinery 50 through secondary cyclone and sends into lower order workshop section; 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 down 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 export gas purification workshop section to by coal gas pressure regulator valve 60.
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 such as the New Solid deslagging dry-powder air-current bed coal-gasification preparing synthetic gas gas composition of carrying out under the embodiment 1-5 condition.
Gasifying multi-segment staged converted fluidized bed preparing synthetic gas gas composition under table 1 different condition
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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 forms 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 (4)
1. the method for a gasifying multi-segment staged converted fluidized bed is characterized in that comprising the steps:
(1) gasified raw material preparation of coal
The feed coal fragmentation is by 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 passes into air, steam at fluidized-bed lower gas sparger during greater than 600 ℃, add continuously the gasification broken coal from vapourizing furnace bottom broken coal feed-pipe, and press the air coal than 2.5～3.5Nm
3/ kg, steam coal operate than 0.3～0.6kg/kg, make coal in the vapourizing furnace internal combustion, and obtain the semicoke furnace charge, set up gradually material in the vapourizing furnace stove;
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 operate gasification than 0.5～1.0kg/kg, and the vapourizing furnace bottom temp is stabilized in 900～1100 ℃ of scopes;
D. after 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 at control vapourizing furnace middle part maintains 700～900 ℃; Adjust vapourizing furnace bottom inflow amount, keep the vapourizing furnace temperature of lower and be stabilized in 900～1100 ℃ of scopes; Simultaneously, pass into circulating gas and oxygen/water 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 separator tube 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, again participate in reaction; 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 down 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 circulating gas and the oxygen/water steam of vapourizing furnace top combustion gas gas blow pipe; Stop coal; Cut-out enters rear 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 simultaneously the fluidized bed steam consumption, 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 is drained, stop air inlet, final system is used respectively steam, air purge one time.
2. the device of a gasifying multi-segment staged converted fluidized bed, it is from the unit by molten poly-ash content, the pyrolytic gasification reactor, semicoke fine powder circulation supply unit forms, 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) consists of, 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) consist of 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 distributor 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 vaporized chemical inlet pipe (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) consists of, 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) forms, 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) at inclined tube;
Described circular cone grid distributor (2), reducing pipe (3) and annular release pipe (5) consist of by fire-resistant and lagging material;
The percentage of open area of 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 °.
3. the device of a kind of gasifying multi-segment staged converted fluidized bed as claimed in claim 2, it is characterized in that described circular body of heater (15) is by the body of heater shell, lagging material (16) and refractory materials (17) form, and are lagging material (16) between body of heater shell and the refractory materials (17).
4. the device of a kind of gasifying multi-segment staged converted fluidized bed as claimed in claim 2 is characterized in that the element of cone of described reducing pipe (3) and the angle γ of central shaft are 5 °-20 °.
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