CN104449872B - A kind of fine particle biomass or the gasifying process system of solid fossil fuel - Google Patents
A kind of fine particle biomass or the gasifying process system of solid fossil fuel Download PDFInfo
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- CN104449872B CN104449872B CN201410754690.XA CN201410754690A CN104449872B CN 104449872 B CN104449872 B CN 104449872B CN 201410754690 A CN201410754690 A CN 201410754690A CN 104449872 B CN104449872 B CN 104449872B
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- 239000010419 fine particle Substances 0.000 title claims abstract description 50
- 239000007787 solid Substances 0.000 title claims abstract description 49
- 239000002028 Biomass Substances 0.000 title claims abstract description 44
- 239000002803 fossil fuel Substances 0.000 title claims abstract description 40
- 238000000034 method Methods 0.000 title claims abstract description 24
- 230000008569 process Effects 0.000 title claims abstract description 23
- 239000003034 coal gas Substances 0.000 claims abstract description 121
- 238000002309 gasification Methods 0.000 claims abstract description 57
- 238000002485 combustion reaction Methods 0.000 claims abstract description 21
- 238000004140 cleaning Methods 0.000 claims abstract description 12
- 238000005516 engineering process Methods 0.000 claims abstract description 11
- 238000012545 processing Methods 0.000 claims abstract description 9
- 239000007789 gas Substances 0.000 claims description 113
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 74
- 239000003517 fume Substances 0.000 claims description 73
- 239000000463 material Substances 0.000 claims description 51
- 239000007921 spray Substances 0.000 claims description 50
- 239000006200 vaporizer Substances 0.000 claims description 36
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims description 29
- 239000003546 flue gas Substances 0.000 claims description 29
- 238000000926 separation method Methods 0.000 claims description 26
- 238000001816 cooling Methods 0.000 claims description 25
- 239000002910 solid waste Substances 0.000 claims description 18
- 230000003134 recirculating effect Effects 0.000 claims description 17
- 238000004891 communication Methods 0.000 claims description 16
- 230000003009 desulfurizing effect Effects 0.000 claims description 13
- 238000007599 discharging Methods 0.000 claims description 13
- 238000009826 distribution Methods 0.000 claims description 13
- 239000002918 waste heat Substances 0.000 claims description 12
- 238000010438 heat treatment Methods 0.000 claims description 11
- 239000000203 mixture Substances 0.000 claims description 11
- 239000010865 sewage Substances 0.000 claims description 11
- AXCZMVOFGPJBDE-UHFFFAOYSA-L calcium dihydroxide Chemical compound [OH-].[OH-].[Ca+2] AXCZMVOFGPJBDE-UHFFFAOYSA-L 0.000 claims description 10
- 238000005243 fluidization Methods 0.000 claims description 9
- 210000005239 tubule Anatomy 0.000 claims description 8
- 239000002184 metal Substances 0.000 claims description 7
- 239000000779 smoke Substances 0.000 claims description 6
- 239000010935 stainless steel Substances 0.000 claims description 6
- 229910001220 stainless steel Inorganic materials 0.000 claims description 6
- 238000001035 drying Methods 0.000 claims description 5
- 239000004744 fabric Substances 0.000 claims description 5
- 239000003795 chemical substances by application Substances 0.000 claims description 4
- 235000019504 cigarettes Nutrition 0.000 claims description 4
- 238000001704 evaporation Methods 0.000 claims description 4
- 230000008020 evaporation Effects 0.000 claims description 4
- 239000000126 substance Substances 0.000 claims description 4
- 229910000851 Alloy steel Inorganic materials 0.000 claims description 3
- 238000007598 dipping method Methods 0.000 claims description 3
- 239000007788 liquid Substances 0.000 claims description 3
- 238000012806 monitoring device Methods 0.000 claims description 3
- 238000012544 monitoring process Methods 0.000 claims description 3
- -1 bootstrap system Substances 0.000 claims description 2
- 239000000428 dust Substances 0.000 abstract description 14
- 239000003245 coal Substances 0.000 abstract description 8
- 238000004519 manufacturing process Methods 0.000 abstract description 6
- 239000002699 waste material Substances 0.000 abstract description 4
- 239000002245 particle Substances 0.000 abstract description 2
- UCKMPCXJQFINFW-UHFFFAOYSA-N Sulphide Chemical compound [S-2] UCKMPCXJQFINFW-UHFFFAOYSA-N 0.000 abstract 1
- 238000002955 isolation Methods 0.000 abstract 1
- 238000006243 chemical reaction Methods 0.000 description 12
- 230000000694 effects Effects 0.000 description 11
- 230000002378 acidificating effect Effects 0.000 description 7
- 238000005336 cracking Methods 0.000 description 6
- 238000013461 design Methods 0.000 description 6
- 238000010586 diagram Methods 0.000 description 6
- 230000000903 blocking effect Effects 0.000 description 4
- 239000000446 fuel Substances 0.000 description 4
- 239000000654 additive Substances 0.000 description 3
- 230000000996 additive effect Effects 0.000 description 3
- 238000005422 blasting Methods 0.000 description 3
- 238000005260 corrosion Methods 0.000 description 3
- 230000007797 corrosion Effects 0.000 description 3
- 239000008187 granular material Substances 0.000 description 3
- 230000002262 irrigation Effects 0.000 description 3
- 238000003973 irrigation Methods 0.000 description 3
- 238000002156 mixing Methods 0.000 description 3
- 238000011084 recovery Methods 0.000 description 3
- 239000002253 acid Substances 0.000 description 2
- 230000015572 biosynthetic process Effects 0.000 description 2
- 239000004568 cement Substances 0.000 description 2
- 230000004907 flux Effects 0.000 description 2
- 238000000197 pyrolysis Methods 0.000 description 2
- 238000004064 recycling Methods 0.000 description 2
- 230000001502 supplementing effect Effects 0.000 description 2
- 230000032258 transport Effects 0.000 description 2
- 241000628073 Exocelina fume Species 0.000 description 1
- OAICVXFJPJFONN-UHFFFAOYSA-N Phosphorus Chemical compound [P] OAICVXFJPJFONN-UHFFFAOYSA-N 0.000 description 1
- 229910000831 Steel Inorganic materials 0.000 description 1
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 description 1
- 238000005299 abrasion Methods 0.000 description 1
- 239000003513 alkali Substances 0.000 description 1
- 230000008901 benefit Effects 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 210000000038 chest Anatomy 0.000 description 1
- 238000006477 desulfuration reaction Methods 0.000 description 1
- 230000023556 desulfurization Effects 0.000 description 1
- 238000011161 development Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 230000003628 erosive effect Effects 0.000 description 1
- 238000004880 explosion Methods 0.000 description 1
- 238000011049 filling Methods 0.000 description 1
- 239000012530 fluid Substances 0.000 description 1
- 238000009434 installation Methods 0.000 description 1
- 238000013332 literature search Methods 0.000 description 1
- 229910052698 phosphorus Inorganic materials 0.000 description 1
- 239000011574 phosphorus Substances 0.000 description 1
- 238000001556 precipitation Methods 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 230000004044 response Effects 0.000 description 1
- 229920006395 saturated elastomer Polymers 0.000 description 1
- 238000004062 sedimentation Methods 0.000 description 1
- 239000004449 solid propellant Substances 0.000 description 1
- 238000007711 solidification Methods 0.000 description 1
- 230000008023 solidification Effects 0.000 description 1
- 239000010959 steel Substances 0.000 description 1
- 239000004575 stone Substances 0.000 description 1
- 238000013517 stratification Methods 0.000 description 1
- 235000011149 sulphuric acid Nutrition 0.000 description 1
- 238000012546 transfer Methods 0.000 description 1
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
- 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
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- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Combustion & Propulsion (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Organic Chemistry (AREA)
- Fluidized-Bed Combustion And Resonant Combustion (AREA)
Abstract
The present invention is the gasifying process system of a kind of fine particle biomass or solid fossil fuel, combustion system uses fine particle biomass or the Combustion technology of circulating fluidized of solid fossil fuel and efficient cyclone isolation technics, fine particle circulating fluidized bed combustion technology have employed flat wind cap, it is achieved the refinement burning of coal particle；The fluidized bed gasification reactor system of fine particle biomass or solid fossil fuel uses fine particle gasification technology, and fine particle gasification technology have employed flat wind cap, solves the problem that in existing coal gas process system, gas production is few, aerogenesis calorific value is low；The converting heat that gasification gas is carried by bootstrap system supplies fine particle biomass or the fluidized bed gasification reactor system of solid fossil fuel in steam, utilizes self energy, reduces cost；Also include ash processing system and gasification Process Gas cleaning system, solve the heat waste problem carried of lime-ash and sulfide that gasification gas carries and the cleanest problem of dust disposal.
Description
Technical field
The invention belongs to the cleaning fuel in derived energy chemical field and convert new and high technology, be specifically related to a kind of fine particle biological
The gasifying process system of matter or solid fossil fuel.
Background technology
Owing to current Domestic Environment is polluted, destroyed acutely, the requirement of Environmental protection is more strict, does not allows
The present situation that biomass, coal directly burn, and the sustainable development of biomass to be considered, coal.Conventional gasifying process system
In system: thermophore is excessive with material particular diameter, causing mixing uneven, heat exchange is insufficient, impact gasification, cracking reaction；Whirlwind divides
Low from device separation efficiency, cause gasification gas to carry away substantial amounts of circulating ash, impact gasification, cracking reaction, and set follow-up
For causing more serious corrosion and abrasion；The high-temperature steam of gasification takes from other process systems, wastes self energy；Separate
The waste residue discharged directly discharges, and pollutes environment；The purification process of gasification gas the most thoroughly causes aerogenesis the purest, containing corrosion
Property gas and dust, long-time perishable pipeline harm safety.By literature search, China Patent No. is ZL20070063368.2
Patent of invention propose a kind of recirculating fluidized bed pyrolysis gasification method and device, China Patent No. is ZL200410070766.3
Patent of invention propose a kind of coal gas-steam combined production method and the CFBB of band pyrolysis vaporizer, Chinese patent
Number propose a kind of solid fuel decoupling fluidized bed gasification process and gasification installation for the patent of invention of ZL200710119476.7,
The patent of invention filling Patent No. ZL200410027427.7 proposes biomass mixing gasifying process and device, above-mentioned
Several devices all also exist bed, material etc. fluidisation bad, mix uneven, flow velocity is too fast, the holdup time is short, causes gas production
Less, the problem that aerogenesis calorific value is low.
Summary of the invention
It is an object of the invention to, solve existing CFBC incomplete, in flying dust, phosphorus content is high, high pollution
Problem；Solve existing gasification, cracker gas production few, the problem that calorific value is low；Make full use of own resource to carry out gasifying, cracking
Reaction, reduces cost；Become as problem precious, that solve the pollution of environment；Solve existing coal gas product the purest, low the asking of calorific value
Topic.And then the gasifying process system of a kind of fine particle biomass or solid fossil fuel is provided.
For realizing object above, by the following technical solutions:
A kind of fine particle biomass or the gasifying process system of solid fossil fuel, specifically include CFBC system
System, fine particle biomass or the fluidized bed gasification reactor system of solid fossil fuel, bootstrap system, ash processing system
With gasification Process Gas cleaning system, recirculating fluidized bed combustion system is the fluid bed gas of fine particle biomass or solid fossil fuel
Changing reactor and provide heat, the fluidized bed gasification reactor of fine particle biomass or solid fossil fuel is positioned at recirculating fluidized bed combustion
Burn between cyclone separator and the material returning device of stove, and be connected to form double-fluidized-bed with CFBC stove；UTILIZATION OF VESIDUAL HEAT IN system
Unite and reclaimed high-temperature flue gas waste heat and the fine particle biology of CFBC stove by the waterpipe type waste heat boiler of vertical
The coal gas of high temperature waste heat of the fluidized bed gasification reactor of matter or solid fossil fuel, and the high temperature mistake that bootstrap system produces
Vapours is sent in the fluidized bed gasification reactor of fine particle biomass or solid fossil fuel as gasifying agent.
Described recirculating fluidized bed combustion system includes burner, air compartment, the horizontal air distribution plate of water-cooled I, flat fixed
To blast cap I, overfire air jet, returning charge pipeline, material returning device, it is positioned at the loosening wind air compartment of material returning device bottom, is positioned at material returning device top
Material returning device returning charge entrance, fume side primary cyclone, the circulating ash that is positioned at fume side primary cyclone bottom go out
Mouth, fume side secondary cyclone, it is positioned at the ash-removing mouth of fume side secondary cyclone bottom, is positioned at fume side two grades rotation
The exhanst gas outlet I on wind separator top；Use ignition under bed Starting mode, burner arrangement under bed, the setting of First air indoor
There is startup heater；Cloth elegance, with flat wind cap I, manufactures specific flow regime, makes bed mix homogeneously with wind,
Realizing fine particle low velocity fluidization to burn, flat wind cap I is made up of heat-resistance stainless steel.Fixing of flat wind cap I
And cooling uses the horizontal air distribution plate of water-cooled I.The forward and backward wall of burner hearth arranges dipping type secondary wind entrance, for supplementing in burner hearth
Sufficient air quantity.Material returning device is connected with returning charge pipeline, prevents material returning device from blocking.Two-stage efficient cyclone separator, i.e. flue gas are set
Side primary cyclone, fume side secondary cyclone, this efficient cyclone separator uses jacket structured, and flue gas enters height
Effect cyclone separator after in chuck high speed rotating, by centrifugal force by the dust separation in flue gas out.
Described fine particle biomass or the fluidized bed gasification reactor system of solid fossil fuel include: reactor, follow
Ring ash entrance, replenishment cycles ash entrance, material inlet, flat wind cap II, the horizontal air distribution plate of water-cooled II, high-temperature steam enter
Mouth, loose metal wind entrance, the returning charge outlet of reactor, the gas exit I of reactor, coal gas side primary cyclone, it is positioned at coal
The cinder-discharging port I of primary cyclone bottom, gas side, coal gas side secondary cyclone, it is positioned at coal gas side secondary cyclone
The cinder-discharging port II of bottom, it is positioned at the gas exit II on secondary cyclone top, coal gas side；The circulating ash entrance of reactor with
The circulating ash outlet being positioned at fume side primary cyclone bottom is returned with being positioned at by pipeline communication, the returning charge outlet of reactor
The material returning device returning charge entrance at glassware top is connected by pipeline；Air distribution plate uses flat wind cap II, manufactures specific stream
Dynamic state, makes thermophore mix homogeneously with material, and thermophore is little with material contact area simultaneously, and time of contact is long, it is achieved that thin
Particle low velocity fluidization gasifies and rationally gets rid of large granular materials, and this flat wind cap II is made up of heat-resistance stainless steel, flat board
Fixing and the cooling of formula wind cap II uses the horizontal air distribution plate of water-cooled II.The hot-air that loose metal wind entrance is sent into is through flat fixed
After blast cap II sprays into reactor, spray into the high-temperature steam of reactor with high-temperature steam entrance and sent into reaction by material inlet
The material of device mixes, and carries out gasification reaction under low velocity fluidization and specific flow regime.The coal gas that gasification produces passes through
Reactor gas exit I is discharged, and passes sequentially through coal gas side primary cyclone, coal gas side secondary cyclone is carried out point
From, the lime-ash separated is pipelined to useless solid waste heat boiler and carries out waste heat recovery.
Described bootstrap system includes: drum, coal gas side superheater, coal gas side vaporizer, fume side vaporizer, cigarette
Gas side air preheater；The gas entry I of coal gas side superheater and the fluidisation being positioned at fine particle biomass or solid fossil fuel
In bed gasification reactor system, the gas exit II on secondary cyclone top, coal gas side is connected by pipeline, coal gas side
The gas exit III of superheater and the gas entry II of coal gas side vaporizer are by pipeline communication, and the flue gas of fume side vaporizer enters
The exhanst gas outlet I being positioned at fume side secondary cyclone top in mouth I and recirculating fluidized bed combustion system passes through pipeline communication,
The gas exit III of coal gas side superheater and the gas entry of coal gas side vaporizer II, the smoke inlet of fume side air preheater
II passes through pipeline communication with the exhanst gas outlet II of fume side vaporizer.There is in drum cyclone separator steam water interface is carried out
First separation, the steam after separation carries out secondary separation by screen separator again, it is ensured that after steam contains relatively low moisture
Enter coal gas side superheater, prevent the body generation pipe explosion accident of coal gas side superheater；Reasonably feedwater it is additionally provided with in drum
Device, chemicals dosing plant, continuous blow off equipment, liquid-level monitoring device, drum pressure monitoring arrangement and overpressure protection apparatus.Coal gas
The housing of side superheater, coal gas side vaporizer, fume side vaporizer and fume side air preheater all uses flanging technology, reduces
Weld seam guarantees to seal；Described coal gas side superheater body have employed serpentine coil convection heating surface, by high temperature alloy steel
Form, serpentine coil the top two array of pipes is disposed with wearing-resistant tile, effectively protects convection heating surface, between serpentine coil
Pitch reasonable in design ensures to set in the middle part of the unimpeded and suitable gas speed of gas passage, and coal gas side superheater body
Convection-type desuperheater is had to regulate final high-temperature steam outlet temperature by regulation spray water flux.After steam superheating becomes high-temperature steam
The high-temperature steam being pipelined in the fluidized bed gasification reactor system of fine particle biomass or solid fossil fuel enters
Mouthful, eventually enter into reactor and carry out gasification reaction；Described coal gas side evaporator body and fume side evaporator body all use
Angle of inclination is the convection tube group of 10 °, it is to avoid pipe internal memory air blasting pipe phenomenon occurs, joint reasonable in design between convection tube group pipe
Away from ensureing the unimpeded and suitable flue gas flow rate of exhaust gases passes, every three tubule groups are big by header connection composition one
Pipe group, the top two array of pipes of each tubule group is disposed with wearing-resistant tile, effectively protects convection heating surface.
Described ash processing system includes: useless solid waste heat boiler, useless waste heat boiler is provided with lime-ash entrance, hot water goes out admittedly
Mouth, useless cold water inlet, hot air outlet, useless solid outlet, cool air inlet；Lime-ash entrance and position in recirculating fluidized bed combustion system
The fluidized gasification reaction of ash-removing mouth, fine particle biomass or solid fossil fuel in fume side secondary cyclone bottom
Device system is positioned at the cinder-discharging port I of primary cyclone bottom, coal gas side and is positioned at secondary cyclone bottom, coal gas side
The ash port I of coal gas side superheater, the ash port II of coal gas side evaporation, fume side evaporation in cinder-discharging port II, bootstrap system
Device ash port III, fume side air preheater ash port IV pass through pipeline communication.Lime-ash is entered useless solid waste heat pot by lime-ash entrance
Stove, afterwards with the cold water entered by useless solid waste heat boiler cold water inlet and by useless solid waste heat boiler cool air inlet enter cold
Air carries out heat exchange.Lime-ash after cooling is exported discharge admittedly by the solid waste heat boiler that gives up is useless, adds additive and make water in lime-ash
After mud, pack transports.Hot water after Bei Jiare is delivered in the drum in bootstrap system through the hot water outlet of useless solid waste heat boiler
Again heat；Hot-air after Bei Jiare delivers to the air preheat in bootstrap system through useless solid waste heat boiler hot air outlet
Device heats again.Waste heat is taken back recirculating fluidized bed combustion system, fine particle biomass or solidification by this ash processing system
In the fluidized bed gasification reactor system of stone fuel and bootstrap system.
Described gasification gas cleaning system includes: coal gas side, fume side are respectively adopted identical cooling, desulfurizing dedusting
The coal gas drying equipment of tower and coal gas side.Cooling, desulfurizing gas wash tower includes gas access, for the first time spray, for the first time shower water
Loop exit, bottom sewage draining exit, second time spray, pallet I, top sewage draining exit, third time spray, pallet II, the 4th time spray,
Water separator, gas outlet, expansion chamber, secondary settlement room, a lime water recycle pond；Two gas accesses are respectively
Pass through with the gas exit IV of coal gas side vaporizer II in bootstrap system and the exhanst gas outlet III of fume side air preheater
Pipeline communication.Gas from gas entrance enters cooling, desulfurizing gas wash tower, pass sequentially through for the first time spray, second time spray, the 3rd
Secondary spray, the 4th spray, the gas after spray carries out steam-water separation through water separator again；Wherein first time shower water
Deriving from the first time shower water loop exit of tower bottom, second and third shower water derives from lime water and recycles pond, and the 4th
Secondary shower water derives from cold water.Pallet I, pallet II are made up of multi-hole orifice, will carry H in the gas after second time spray2SO4、
The acidic materials such as HCL and part dust, when by pallet I, pallet II multi-hole orifice, acidic materials and bulky grain can settle
Get off, play the effect of cooling deacidification dedusting.For preventing pallet I, pallet II from blocking and cleaning acidic materials, on pallet I
Side is provided with rinse water spray I, and pallet II is arranged over rinse water spray II, for irrigation tray.It is provided with literary composition for the third time at spray
Venturi, sprays water at trunnion, and due to Venturi effect, water droplet enters trunnion and bumps against formation droplet with high-speed gas in pipe,
And dust and droplet clash into formation bulky grain and settled down, play the effect of cooling deacidification dedusting.Vapour enters in water separation device
Have multiple corrugated sheet to combine, gas by during corrugated sheet due to airflow direction change produce effect of inertia gas is contained
Some moisture and dust separation also settle down, and for preventing vapour from entering water separation device blocking and cleaning acidic materials, enter at vapour
Water separation device is arranged over rinse water spray III, is used for rinsing the corrugated sheet that vapour enters in water separation device.
Benefit effect of the present invention: 1, recirculating fluidized bed combustion system have employed board-like wind cap manufacture and specifically flows effect
Really, extend the mixing of the time of staying in the stove of bed, beneficially bed, burn completely；
2, the fluidized bed gasification reactor system of fine particle biomass or solid fossil fuel have employed board-like wind cap
Manufacture specific flow effect, make material mix homogeneously with air, high-temperature steam, the mixture of circulating ash, and in reactor
Stay long enough carries out gasifying, cracking reaction；Recirculating fluidized bed combustion system and fine particle biomass or solid fossil
The efficient cyclone separator that the fluidized bed gasification reactor system of fuel uses inside to be chuck pattern, makes dust and gas (coal
Gas, flue gas) separation efficiency can reach more than 98%；
3, after coal gas, flue gas separate each via corresponding separator, it is respectively provided with corresponding residual heat using device, coal
Gas side residual heat using device is coal gas side superheater, coal gas side vaporizer II, and flue gas waste heat utilization device side is fume side evaporation
Device I, fume side air preheater, heat recovery coal gas, flue gas carried respectively is also transformed in high-temperature steam, and by high temperature
Steam is transmitted back to the fluidized bed gasification reactor system response device of fine particle biomass or solid fossil fuel to carry out gasifying, cracking
Reaction, utilizes self energy cost-effective；Residual heat using device housing uses flanging technology, reduces weld seam, it is ensured that device close
Feng Xing, and heating surface uses reasonable pitch to greatly reduce dust stratification and the corrosion of heating surface；
4, take the ash processing system of useless solid waste heat boiler, be heated by being arranged on the convection current within useless solid waste heat boiler
Face reduces ash temperature, improves the feed temperature of boiler to improve boiler efficiency simultaneously, it is also possible to improves and is partially into fume side
The entering air temperature of air preheater, adds additive and i.e. can be made into cement recycling, turn waste into wealth in the lime-ash after cooling
And protect environment；
5, the desulfurized dust collection column that gasification air purifying apparatus is different from the past, is provided with Venturi tube in the middle part of tower, logical
Cross Venturi effect and substantially increase dust and the efficiency of desulfurization in separation gas (coal gas, flue gas).
Accompanying drawing explanation
Fig. 1 is the main TV structure schematic diagram of the present invention
Fig. 2 is the schematic diagram of the board-like wind cap of the present invention
Fig. 3 is the efficient cyclone separator main TV structure schematic diagram of the chuck pattern of the present invention
Fig. 4 be the present invention bootstrap system in the folded edges schematic diagram of residual heat using device
Fig. 5 is the main TV structure schematic diagram of the useless solid waste heat boiler of the present invention
Fig. 6 is the main TV structure schematic diagram of the cooling, desulfurizing gas wash tower in gasification gas cleaning system of the present invention
As it can be seen, 1, burner；2, an air compartment；3, the horizontal air distribution plate of water-cooled I；4, flat wind cap I；5, two
Secondary wind nozzle；6, returning charge pipeline；7, material returning device；8, wind air compartment is loosened；9, material returning device returning charge entrance；10, fume side one cyclonic
Separator；11, circulating ash outlet；12, fume side secondary cyclone；13, ash-removing mouth；14, exhanst gas outlet I；15, reaction
Device；16, circulating ash entrance；17, replenishment cycles ash entrance；18, material inlet；19, flat wind cap II；20, water-cooled water
Plain cloth aerofoil II；21, high-temperature steam entrance；22, loose metal wind entrance；23, the returning charge outlet of reactor；24, gas exit I；25、
Coal gas side primary cyclone；26, cinder-discharging port I；27, coal gas side secondary cyclone；28, cinder-discharging port II；29, coal gas goes out
Mouth II；30, drum；31, gas entry I；32, coal gas side superheater；33, coal gas side superheater body；34, gas exit III；
35, ash port I；36, gas entry II；37, coal gas side vaporizer；38, coal gas side evaporator body；39, gas exit IV；
40, ash port II；41, smoke inlet I；42, fume side vaporizer；43, fume side evaporator body；44, exhanst gas outlet II；
45, ash port III；46, smoke inlet II；47, fume side air preheater；48, fume side air preheater body；49, flue gas
Outlet III；50, ash port IV；51, useless solid waste heat boiler；52, lime-ash entrance；53, hot water outlet；54, cold water inlet；55, heat
Air outlet slit；56, useless solid outlet；57, cool air inlet；58, cooling, desulfurizing gas wash tower；59, gas access；60, spray for the first time
Drench；61, shower water loop exit for the first time；62, bottom sewage draining exit；63, second time spray；64, rinse water spray I；65, pallet
Ⅰ；66, top sewage draining exit；67, Venturi tube；68, third time spray；69, rinse water spray II；70, pallet II；71, the 4th time
Spray；72, water separator；73, rinse water spray III；74, gas outlet；75, an expansion chamber；76, secondary settlement room；
77, lime water recycles pond；78, coal gas drying equipment.
Detailed description of the invention
Embodiment.
As it is shown in figure 1, the gasifying process system CFBC of a kind of fine particle biomass or solid fossil fuel
System, including recirculating fluidized bed combustion system, fine particle biomass or solid fossil fuel fluidized bed gasification reactor system,
Bootstrap system, ash processing system and gasification Process Gas cleaning system.
Illustrating with Fig. 3 in conjunction with Fig. 1, Fig. 2, the recirculating fluidized bed combustion system of embodiment includes: burner (1), First air
Room (2), the horizontal air distribution plate of water-cooled I (3), flat wind cap I (4), overfire air jet (5), returning charge pipeline (6), material returning device
(7), it is positioned at the loosening wind air compartment (8) of material returning device (7) bottom, is positioned at material returning device returning charge entrance (9) at material returning device (7) top, cigarette
Gas side primary cyclone (10), be positioned at fume side primary cyclone (10) bottom circulating ash outlet (11), flue gas
Side secondary cyclone (12), it is positioned at the grey mouth (13) of fume side secondary cyclone (12) bottom, is positioned at fume side
The exhanst gas outlet (14) on secondary cyclone (12) top.Burner (1) is arranged under bed, is provided with in an air compartment (2)
Starting heater, First air derives from the fume side air preheater in bootstrap system.The flat flat board of cloth elegance
Formula wind cap I (4), fuel air is 0.5 ~ 1m/s with the flow velocity of gasifying agent (gasification wind), manufactures specific flow regime, makes bed
Material is mixed homogeneously with wind, it is achieved fine particle low velocity fluidization burns and rationally gets rid of large granular materials, this flat wind cap I
(4) it is made up of heat-resistance stainless steel.Fixing and the cooling of flat wind cap I (4) uses the horizontal air distribution plate of water-cooled I (3).At stove
Arranging dipping type secondary wind entrance (5) on the forward and backward wall of thorax, for supplementing sufficient air quantity in burner hearth, secondary wind derives from waste heat
Utilize the fume side air preheater (47) in system.This system has two-stage efficient cyclone separator, i.e. fume side one-level rotation altogether
Wind separator (10), fume side secondary cyclone (12), this efficient cyclone separator uses jacket structured, and chuck is by heat-resisting
Rustless steel is made, and flue gas (950 DEG C) enters after efficient cyclone separator high speed rotating in chuck, by centrifugal force by flue gas
Dust separation out, this efficient cyclone separator separation efficiency can reach more than 98%.
Illustrate with Fig. 3 in conjunction with Fig. 1, Fig. 2, the fine particle biomass of the present embodiment or the fluidized gasification of solid fossil fuel
Reactor assembly, described system includes: reactor (15), circulating ash entrance (16), replenishment cycles ash entrance (17), material inlet
(18), flat wind cap II (19), the horizontal air distribution plate of water-cooled II (20), high-temperature steam entrance (21), loose metal wind entrance
(22), reactor returning charge outlet (23), the gas exit I (24) of reactor (15), coal gas side primary cyclone (25),
It is positioned at the cinder-discharging port I (26) of primary cyclone (25) bottom, coal gas side, coal gas side secondary cyclone (27), is positioned at coal
The cinder-discharging port II (28) of secondary cyclone (27) bottom, gas side, it is positioned at the coal on secondary cyclone (27) top, coal gas side
Gas outlet II (29), the circulating ash entrance (16) of reactor and the circulating ash being positioned at fume side primary cyclone (10) bottom
Outlet (11) is by pipeline communication, returning charge outlet (23) and the material returning device returning charge entrance being positioned at material returning device (7) top of reactor
(9) connected by pipeline.The present embodiment cloth elegance flat wind cap II (19), material air and gasifying agent (gasification wind)
Flow velocity is 0.5 ~ 1m/s, manufactures specific flow regime, makes thermophore mix homogeneously with material, and thermophore contacts with material simultaneously
Area is little, and time of contact is long, it is achieved fine particle low velocity fluidization gasifies and rationally gets rid of large granular materials, this flat wind cap
II (19) is made up of heat-resistance stainless steel.Fixing and the cooling of flat wind cap (19) uses the horizontal air distribution plate of water-cooled II
(20).The hot-air that loose metal wind entrance (22) is sent into steams with high temperature after flat wind cap II (19) sprays into reactor (15)
Vapour entrance (21) sprays into the high-temperature steam (580 DEG C) of reactor (15) and is sent into the thing of reactor (15) by material inlet (18)
Material mixes, and carries out gasifying, cracking reaction under low velocity fluidization and specific flow regime.The coal gas (850 that gasification produces
DEG C) discharged by the gas exit I (24) of reactor (15), pass sequentially through coal gas side primary cyclone (25), coal gas side
Secondary cyclone (27) separates, and the lime-ash separated is pipelined to useless solid waste heat boiler (51) and carries out
Waste heat recovery.
Illustrating in conjunction with Fig. 1 Yu Fig. 4, the bootstrap system of the present embodiment includes: drum (30), coal gas side superheater
(32), coal gas side vaporizer (37), fume side vaporizer (42), fume side air preheater (47)；Coal gas side superheater (32)
Gas entry I (31) be positioned at coal gas side in the fluidized bed gasification reactor system of fine particle biomass or solid fossil fuel
The gas exit II (29) on secondary cyclone (27) top is connected by pipeline, the coal gas of coal gas side superheater (32)
The gas entry II (36) of outlet III (34) and coal gas side vaporizer (37) is by pipeline communication, the cigarette of fume side vaporizer (42)
Gas entrance I (41) and recirculating fluidized bed combustion system are positioned at the exhanst gas outlet I on fume side secondary cyclone (12) top
(14) by pipeline communication, the gas exit III (34) of coal gas side superheater (32) enters with the coal gas of coal gas side vaporizer II (37)
Mouth (36), the smoke inlet II (46) of fume side air preheater (47) and the exhanst gas outlet II (44) of fume side vaporizer (42)
Pass through pipeline communication.There are three high efficiency cyclone separator to steam water interface (saturation temperature 209 DEG C) in drum (30)
Carrying out first separation, the steam (saturation temperature 209 DEG C) after separation carries out secondary separation by screen separator again, to ensure
Steam enters coal gas side superheater (32) after containing relatively low moisture, prevents coal gas side superheater body (33) from booster thing occurring
Therefore；Drum is provided with rational waterworks, chemicals dosing plant, continuous blow off equipment, liquid-level monitoring device, drum pressure in (30)
Monitoring arrangement and overpressure protection apparatus, it is ensured that water quality higher in drum and guarantee security of system, reliable, stable fortune
OK.
Coal gas of high temperature (850 DEG C) enters coal gas side superheater (32), and coal gas side superheater (32) housing uses flanging technology,
Reduce weld seam to guarantee to seal；Coal gas side superheater body (33) have employed serpentine coil convection heating surface, by high-temperature alloy steel
It is made；Serpentine coil the top two array of pipes is disposed with wearing-resistant tile, effectively protects convection heating surface；Serpentine coil
Between pitch (120mm ~ 180mm) reasonable in design ensure the unimpeded and suitable gas speed of gas passage；In coal gas side
Superheater body (33) middle part is provided with convection-type desuperheater and regulates final high-temperature steam outlet temperature by regulation spray water flux.
Fine particle biomass or solid fossil combustion it is pipelined to after saturated vapor (209 DEG C) overheated one-tenth high-temperature steam (580 DEG C)
High-temperature steam entrance (21) in the fluidized bed gasification reactor system of material, eventually enters into reactor (15) and carries out gasification reaction.
Coal gas of high temperature (700 DEG C) enters coal gas side vaporizer (37), and the housing of coal gas side vaporizer (37) uses flanging skill
Art, reduces weld seam and guarantees to seal.The convection tube group that coal gas side evaporator body (38) uses angle of inclination to be 10 °, it is to avoid pipe
Internal memory air blasting pipe phenomenon occurs；Pitch (120mm ~ 180mm) reasonable in design between convection tube group pipe ensures exhaust gases passes
Unimpeded and suitable flue gas flow rate；Every three tubule groups are by header connection one big pipe group of composition, at each tubule
It is disposed with wearing-resistant tile in the top two array of pipes of group, effectively protects convection heating surface.
High-temperature flue gas (950 DEG C) is by entering fume side vaporizer (42), and fume side vaporizer (42) housing uses flanging skill
Art, reduces weld seam and guarantees to seal.The convection tube group that fume side evaporator body (43) uses angle of inclination to be 10 °, it is to avoid deposit
Air blasting pipe phenomenon occurs；Pitch (120mm ~ 180mm) reasonable in design between convection tube group pipe ensures the smooth of exhaust gases passes
Logical and suitable flue gas flow rate；Every three tubule groups are by header connection one big pipe group of composition, in each tubule group
It is disposed with wearing-resistant tile in the array of pipes of the top two, effectively protects convection heating surface.
High-temperature flue gas (850 DEG C) enters fume side air preheater (47), and fume side air preheater (47) housing uses
Flanging technology, reduces weld seam and guarantees to seal.In fume side air preheater body (48) uses pipe, medium is air, manages outer Jie
Matter is the structure of high-temperature flue gas, arranges body by reasonable computation, it is ensured that tube wall temperature is higher than 160 DEG C, it is to avoid acid dew point is rotten
The generation of erosion phenomenon, and make heat transfer reach optimum state by pitch reasonable in design and pipe sizes, quantity.
After preheating, hot-air flows to the burner (1) in recirculating fluidized bed combustion system, an air compartment by pipeline
(2), secondary wind entrance (5) and the fine particle biomass of fine particle biomass or solid fossil fuel or solid fossil fuel
Loose metal wind entrance (22) in fluidized bed gasification reactor system.
Illustrating in conjunction with Fig. 1 Yu Fig. 5, the present embodiment ash processing system includes: useless solid waste heat boiler (51), useless solid waste heat pot
Stove is provided with lime-ash entrance (52), hot water outlet (53), useless cold water inlet (54), hot air outlet (55), useless solid outlet (56), cold
Air intake (57)；Lime-ash entrance (52) and recirculating fluidized bed combustion system are positioned under fume side secondary cyclone (12)
The fluidized bed gasification reactor system of ash-removing mouth (13), fine particle biomass or the solid fossil fuel in portion is positioned at coal gas side one
The cinder-discharging port I (26) of level cyclone separator (25) bottom and be positioned at the cinder-discharging port II of secondary cyclone (27) bottom, coal gas side
(28), the ash port I 35 of coal gas side superheater (32) in bootstrap system), coal gas side vaporizer (37) ash port II (40),
The ash port III (45) of fume side vaporizer (42), the ash port IV (50) of fume side air preheater (47) are connected by pipeline
Logical.After lime-ash is entered useless solid waste heat boiler (51) by lime-ash entrance (52), with the cold water entered by cold water inlet (54) and
The cold air entered by cool air inlet (57) carries out heat exchange, and the lime-ash after cooling is discharged, in lime-ash by solid outlet (56) of giving up
Add to pack after additive makes cement and transport.Hot water after Bei Jiare is delivered in bootstrap system through hot water outlet (53)
Drum heats in (30) again, and the hot-air after being heated delivers to the air in bootstrap system through used heat air outlet slit (55)
Preheater heats in (47) again.
Illustrating in conjunction with Fig. 1 Yu Fig. 6, the gasification gas cleaning system of the present embodiment includes: coal gas side, fume side are adopted respectively
With identical cooling, desulfurizing gas wash tower (58) and the coal gas drying equipment (78) of coal gas side.
Concrete cooling, desulfurizing gas wash tower includes: described cooling, desulfurizing gas wash tower (58) include gas access (59), first
Secondary spray (60), for the first time shower water loop exit (61), bottom sewage draining exit (62), second time spray (63), pallet I (65),
Top sewage draining exit (66), third time spray (68), pallet the II (70), the 4th spray (71), water separator (72), gas
Outlet (74), expansion chamber (75), secondary settlement room (76), a lime water recycle pond (77)；Two gas accesses (59)
Respectively with the gas exit IV (39) of coal gas side vaporizer II (37) in bootstrap system and fume side air preheater (47)
Exhanst gas outlet III (49) pass through pipeline communication.
In the present embodiment, gas (coal gas 300 DEG C, flue gas 200 DEG C), hence into cooling, desulfurizing gas wash tower (58), leads to successively
Cross spray (60), second time spray (63), third time spray (68), the 4th spray (71), the gas (coal after spray for the first time
Gas, flue gas) carry out steam-water separation through water separator (72) again.
Shower water derives from first time shower water loop exit (61) of tower bottom for the first time, and second and third time shower water comes
Coming from lime water and recycle pond (77), the 4th time shower water derives from cold water.
Pallet I (65) and pallet II (70) are made up of multi-hole orifice, will in the gas (coal gas, flue gas) after second time spray
Carry the acidic materials such as H2SO4, HCL and part dust, when by pallet I (65) pallet II (70) multi-hole orifice, acid
Material and bulky grain can settle down, and play the effect of cooling deacidification dedusting.For preventing pallet I (65), pallet II (70) from blocking
And cleaning acidic materials, pallet I (65) is arranged over rinse water spray I (64), pallet II (70) top rinse water spray II
(69), for irrigation tray.
Gas enters in water separation device (72) to be combined by multiple corrugated sheets, when gas (coal gas, flue gas) is by corrugated sheet
Due to changing under the effect of inertia moisture that gas (coal gas, flue gas) is contained and dust separation sedimentation produced of airflow direction
Come.Block for preventing vapour from entering water separation device (72) and clean acidic materials, entering water separation device (72) at vapour and be arranged over
Rinse water spray III (73), is used for rinsing vapour and enters the corrugated sheet in water separation device (72).
Water after spray and a sewage part for irrigation tray I (65), pallet II (70) and water separator (72)
Expansion chamber (75) finally it is transported to through top sewage draining exit (66), then to two through bottom sewage draining exit (62), a part
Secondary expansion chamber (76) is transported to lime water and recycles pond (77) after carrying out secondary precipitation, by recycling pond toward lime water
(77) add appropriate alkali liquor in and control the pH value (in alkalescence) of shower water；And recycle in pond (77) to lime water
Supplementary cold water ensures that lime water recycles and has the sufficient water yield in pond (77).
Coal gas, after cooling, desulfurizing gas wash tower (58) gas outlet (74) discharges, arrives the coal gas drying equipment of coal gas side
(78) it is dried process, to ensure that coal gas has high heating value, improves gas quality, be then fed to coal gas user and make
With.Flue gas, after cooling, desulfurizing gas wash tower (58) gas outlet (74) discharges, meets discharge standard and is transported to chimney row to greatly
Gas.
Claims (6)
1. a gasifying process system for fine particle biomass or solid fossil fuel, specifically includes CFBC system
System, fine particle biomass or the fluidized bed gasification reactor system of solid fossil fuel, bootstrap system, ash processing system
With gasification Process Gas cleaning system, it is characterised in that: recirculating fluidized bed combustion system is fine particle biomass or solid fossil combustion
The fluidized bed gasification reactor of material provides heat, and the fluidized bed gasification reactor of fine particle biomass or solid fossil fuel is positioned at
Between cyclone separator and the material returning device of CFBC stove, and it is connected to form double fluidization with CFBC stove
Bed；Bootstrap system reclaims the high-temperature flue gas waste heat of CFBC stove by the waterpipe type waste heat boiler of vertical
With the coal gas of high temperature waste heat of fine particle biomass or the fluidized bed gasification reactor of solid fossil fuel, and bootstrap system
The high temperature super heated steam produced sends into fine particle biomass or the fluidized bed gasification reactor of solid fossil fuel as gasifying agent
In；
Described recirculating fluidized bed combustion system includes burner (1), air compartment (2), the horizontal air distribution plate of water-cooled I (3), a flat board
Formula wind cap I (4), overfire air jet (5), returning charge pipeline (6), material returning device (7), it is positioned at the loosening wind of material returning device (7) bottom
Air compartment (8), it is positioned at material returning device returning charge entrance (9) at material returning device (7) top, fume side primary cyclone (10), is positioned at cigarette
The circulating ash of primary cyclone (10) bottom, gas side exports (11), fume side secondary cyclone (12), is positioned at flue gas
The ash-removing mouth (13) of side secondary cyclone (12) bottom, the flue gas being positioned at fume side secondary cyclone (12) top go out
Mouth I (14)；Burner (1) is arranged under bed, is provided with startup heater, the horizontal air distribution plate of water-cooled I in an air compartment (2)
(3) fixing and cooling uses flat wind cap I (4), and the forward and backward wall of burner hearth is arranged dipping type overfire air jet (5), returning charge
Device (7) is connected with returning charge pipeline (6)；Described flat wind cap (4) is made up of heat-resistance stainless steel, described fume side one
Level cyclone separator (10) and fume side secondary cyclone (12) all use jacket structured；
Described fine particle biomass or the fluidized bed gasification reactor system of solid fossil fuel include: reactor (15), follow
Ring ash entrance (16), replenishment cycles ash entrance (17), material inlet (18), flat wind cap II (19), the horizontal cloth of water-cooled
Aerofoil II (20), high-temperature steam entrance (21), loose metal wind entrance (22), returning charge outlet (23) of reactor, reactor (15)
Gas exit I (24), coal gas side primary cyclone (25), be positioned at primary cyclone (25) bottom, coal gas side unload ash
Mouthful I (26), coal gas side secondary cyclone (27), be positioned at the cinder-discharging port II of secondary cyclone (27) bottom, coal gas side
(28) gas exit II (29) on secondary cyclone (27) top, coal gas side, it is positioned at；The horizontal air distribution plate of water-cooled II (20) is solid
Fixed and the board-like wind cap of cooling flat II (19), the circulating ash entrance (16) of reactor be positioned at fume side primary cyclone
(10) circulating ash outlet (11) of bottom is exported (23) by pipeline communication, the returning charge of reactor and is positioned at material returning device (7) top
Material returning device returning charge entrance (9) connected by pipeline；Described flat wind cap (19) is made up of heat-resistance stainless steel；
Described bootstrap system includes: drum (30), coal gas side superheater (32), coal gas side vaporizer (37), fume side
Vaporizer (42), fume side air preheater (47)；The gas entry I (31) of coal gas side superheater (32) is given birth to being positioned at fine particle
The coal gas on coal gas side secondary cyclone (27) top in the fluidized bed gasification reactor system of material or solid fossil fuel
Outlet II (29) is connected by pipeline, gas exit III (34) and coal gas side vaporizer (37) of coal gas side superheater (32)
Gas entry II (36) by pipeline communication, the smoke inlet I (41) of fume side vaporizer (42) and CFBC
The exhanst gas outlet I (14) being positioned at fume side secondary cyclone (12) top in system passes through pipeline communication, and coal gas side is overheated
The gas exit III (34) of device (32) and the gas entry (36) of coal gas side vaporizer II (37), fume side air preheater (47)
The exhanst gas outlet II (44) of smoke inlet II (46) and fume side vaporizer (42) pass through pipeline communication.
A kind of fine particle biomass the most according to claim 1 or the gasifying process system of solid fossil fuel, its feature
Being, described ash processing system includes: useless solid waste heat boiler (51), and useless solid waste heat boiler is provided with lime-ash entrance (52), heat
Water out (53), useless cold water inlet (54), hot air outlet (55), useless solid outlet (56), cool air inlet (57)；Lime-ash entrance
(52) and recirculating fluidized bed combustion system is positioned at the ash-removing mouth (13) of fume side secondary cyclone (12) bottom, fine particle
The fluidized bed gasification reactor system of biomass or solid fossil fuel is positioned at primary cyclone (25) bottom, coal gas side
Cinder-discharging port I (26) and be positioned in the cinder-discharging port II (28) of secondary cyclone (27) bottom, coal gas side, bootstrap system
The ash port I 35 of coal gas side superheater (32)), coal gas side vaporizer (37) ash port II (40), fume side vaporizer (42)
Ash port III (45), the ash port IV (50) of fume side air preheater (47) pass through pipeline communication.
A kind of fine particle biomass the most according to claim 1 or the gasifying process system of solid fossil fuel, its feature
Being, described gasification gas cleaning system includes: coal gas side, fume side are respectively adopted identical cooling, desulfurizing gas wash tower
And the coal gas drying equipment (78) of coal gas side (58).
A kind of fine particle biomass the most according to claim 1 or the gasifying process system of solid fossil fuel, its feature
Be, be provided with in described drum (30) rational waterworks, chemicals dosing plant, continuous blow off equipment, liquid-level monitoring device,
Drum pressure monitoring arrangement and overpressure protection apparatus；Coal gas side superheater (32), coal gas side vaporizer (37), fume side evaporation
The housing of device (42) and fume side air preheater (47) all uses flanging technology；Described coal gas side superheater body (33) is adopted
With serpentine coil convection heating surface, high-temperature alloy steel it is made, serpentine coil the top two array of pipes is disposed with anti-
It is provided with convection-type desuperheater in the middle part of mill watt, and coal gas side superheater body (33)；Described coal gas side evaporator body (38) and
The convection tube group that fume side evaporator body (43) all uses angle of inclination to be 10 °, every three tubule groups are by header even
One big pipe group of logical composition, the top two array of pipes of each tubule group is disposed with wearing-resistant tile.
A kind of fine particle biomass the most according to claim 3 or the gasifying process system of solid fossil fuel, its feature
Being, described cooling, desulfurizing gas wash tower (58) includes gas access (59), for the first time spray (60), for the first time shower water circulation
Outlet (61), bottom sewage draining exit (62), second time spray (63), pallet I (65), top sewage draining exit (66), third time spray
(68), pallet the II (70), the 4th time spray (71), water separator (72), gas outlet (74), expansion chamber (75),
Secondary settlement room (76), lime water recycle pond (77)；Two gas accesses (59) respectively with coal gas in bootstrap system
The gas exit IV (39) of side vaporizer II (37) and the exhanst gas outlet III (49) of fume side air preheater (47) pass through pipeline
Connection.
A kind of fine particle biomass the most according to claim 5 or the gasifying process system of solid fossil fuel, its feature
Being, described pallet I (65) and pallet II (70) are made up of multi-hole orifice, and pallet I (65) is arranged over rinse water spray I
(64), pallet II (70) top rinse water spray II (69)；Described third time spray (68) is provided with Venturi tube (67)；Described
Vapour enter in water separation device (72) to have multiple corrugated sheet to combine, vapour enter water separation device (72) be arranged over rinse water spray
Drench III (73).
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| RU2811354C1 (en) * | 2020-06-28 | 2024-01-11 | ВИСДРИ ИНЖИНИРИНГ энд РИСЕРЧ ИНКОРПОРЕЙШН ЛИМИТЕД | Method and system for regeneration of spent hydrochloric acid in fluidized bed |
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Citations (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1074699A (en) * | 1992-01-23 | 1993-07-28 | 浙江大学 | Circulation fluidized-bed gas-steam combine producing process and device |
| CN1754945A (en) * | 2004-09-30 | 2006-04-05 | 中国科学院工程热物理研究所 | Double-circulating fluid bed coal gas-steam combined production method and device |
| WO2011101540A1 (en) * | 2010-02-17 | 2011-08-25 | Foster Wheeler Energia Oy | A fluidized bed gasification system and a method of gasifying fuel in a fluidized bed gasification system |
| CN201990639U (en) * | 2011-01-06 | 2011-09-28 | 广州迪森热能技术股份有限公司 | Biomass gasification system for two-segment circulating fluidized bed |
| CN102563630A (en) * | 2012-02-26 | 2012-07-11 | 哈尔滨锅炉厂有限责任公司 | Air distribution plate for directional wind cap used for low-speed fluidized bed boiler |
| CN202543155U (en) * | 2012-03-08 | 2012-11-21 | 华北电力大学 | Combined circulation system for gasified combustion and catalyst regeneration by adopting heat carrier as basis |
| CN103756731A (en) * | 2014-01-03 | 2014-04-30 | 东南大学 | Interactive cyclic solid fuel gasification device with double fluidized beds and method |
| CN103897743A (en) * | 2014-03-28 | 2014-07-02 | 上海锅炉厂有限公司 | Solid fuel grading gasification-combustion double-bed poly-generation system and method |
| CN204356293U (en) * | 2014-12-11 | 2015-05-27 | 余传林 | The gasifying process system of a kind of fine particle biomass or solid fossil fuel |
-
2014
- 2014-12-11 CN CN201410754690.XA patent/CN104449872B/en active Active
Patent Citations (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1074699A (en) * | 1992-01-23 | 1993-07-28 | 浙江大学 | Circulation fluidized-bed gas-steam combine producing process and device |
| CN1754945A (en) * | 2004-09-30 | 2006-04-05 | 中国科学院工程热物理研究所 | Double-circulating fluid bed coal gas-steam combined production method and device |
| WO2011101540A1 (en) * | 2010-02-17 | 2011-08-25 | Foster Wheeler Energia Oy | A fluidized bed gasification system and a method of gasifying fuel in a fluidized bed gasification system |
| CN201990639U (en) * | 2011-01-06 | 2011-09-28 | 广州迪森热能技术股份有限公司 | Biomass gasification system for two-segment circulating fluidized bed |
| CN102563630A (en) * | 2012-02-26 | 2012-07-11 | 哈尔滨锅炉厂有限责任公司 | Air distribution plate for directional wind cap used for low-speed fluidized bed boiler |
| CN202543155U (en) * | 2012-03-08 | 2012-11-21 | 华北电力大学 | Combined circulation system for gasified combustion and catalyst regeneration by adopting heat carrier as basis |
| CN103756731A (en) * | 2014-01-03 | 2014-04-30 | 东南大学 | Interactive cyclic solid fuel gasification device with double fluidized beds and method |
| CN103897743A (en) * | 2014-03-28 | 2014-07-02 | 上海锅炉厂有限公司 | Solid fuel grading gasification-combustion double-bed poly-generation system and method |
| CN204356293U (en) * | 2014-12-11 | 2015-05-27 | 余传林 | The gasifying process system of a kind of fine particle biomass or solid fossil fuel |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| RU2811354C1 (en) * | 2020-06-28 | 2024-01-11 | ВИСДРИ ИНЖИНИРИНГ энд РИСЕРЧ ИНКОРПОРЕЙШН ЛИМИТЕД | Method and system for regeneration of spent hydrochloric acid in fluidized bed |
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Effective date of registration: 20170120 Address after: 116000 30-1 District, Ganjingzi, Liaoning, spring D4 District No. Patentee after: Dalian Kelin Energy Engineering Technology Development Co., Ltd. Address before: 116000 30-1 District, Ganjingzi, Liaoning, spring D4 District No. Patentee before: Yu Chuanlin |