CN110160029A - A kind of system and method for biomass carbon vapour coproduction - Google Patents
A kind of system and method for biomass carbon vapour coproduction Download PDFInfo
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- CN110160029A CN110160029A CN201910450973.8A CN201910450973A CN110160029A CN 110160029 A CN110160029 A CN 110160029A CN 201910450973 A CN201910450973 A CN 201910450973A CN 110160029 A CN110160029 A CN 110160029A
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- 239000002028 Biomass Substances 0.000 title claims abstract description 45
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 title claims abstract description 21
- 229910052799 carbon Inorganic materials 0.000 title claims abstract description 21
- 238000000034 method Methods 0.000 title claims abstract description 14
- 238000002309 gasification Methods 0.000 claims abstract description 85
- 238000002485 combustion reaction Methods 0.000 claims abstract description 72
- 239000007789 gas Substances 0.000 claims abstract description 64
- 238000001816 cooling Methods 0.000 claims abstract description 42
- 239000003546 flue gas Substances 0.000 claims abstract description 41
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims abstract description 40
- 229920006395 saturated elastomer Polymers 0.000 claims abstract description 31
- 239000000567 combustion gas Substances 0.000 claims abstract description 26
- 239000003610 charcoal Substances 0.000 claims abstract description 21
- 239000002918 waste heat Substances 0.000 claims abstract description 21
- 238000000926 separation method Methods 0.000 claims abstract description 20
- 239000002245 particle Substances 0.000 claims abstract description 19
- 238000011084 recovery Methods 0.000 claims abstract description 17
- 238000010438 heat treatment Methods 0.000 claims abstract description 15
- 239000007787 solid Substances 0.000 claims abstract description 13
- 238000013459 approach Methods 0.000 claims abstract description 9
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 22
- MWUXSHHQAYIFBG-UHFFFAOYSA-N nitrogen oxide Inorganic materials O=[N] MWUXSHHQAYIFBG-UHFFFAOYSA-N 0.000 claims description 20
- 239000000446 fuel Substances 0.000 claims description 18
- 238000006243 chemical reaction Methods 0.000 claims description 12
- 238000012545 processing Methods 0.000 claims description 8
- 230000015572 biosynthetic process Effects 0.000 claims description 7
- 235000019504 cigarettes Nutrition 0.000 claims description 2
- 239000003818 cinder Substances 0.000 claims 1
- 238000004064 recycling Methods 0.000 claims 1
- 238000005516 engineering process Methods 0.000 description 6
- 239000003245 coal Substances 0.000 description 5
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 3
- 238000004519 manufacturing process Methods 0.000 description 3
- 239000001301 oxygen Substances 0.000 description 3
- 229910052760 oxygen Inorganic materials 0.000 description 3
- 239000002994 raw material Substances 0.000 description 3
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 2
- GQPLMRYTRLFLPF-UHFFFAOYSA-N Nitrous Oxide Chemical compound [O-][N+]#N GQPLMRYTRLFLPF-UHFFFAOYSA-N 0.000 description 2
- 239000003513 alkali Substances 0.000 description 2
- 230000008021 deposition Effects 0.000 description 2
- 239000002737 fuel gas Substances 0.000 description 2
- HYBBIBNJHNGZAN-UHFFFAOYSA-N furfural Chemical compound O=CC1=CC=CO1 HYBBIBNJHNGZAN-UHFFFAOYSA-N 0.000 description 2
- 239000000463 material Substances 0.000 description 2
- 239000002699 waste material Substances 0.000 description 2
- 238000004458 analytical method Methods 0.000 description 1
- 239000002585 base Substances 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000000903 blocking effect Effects 0.000 description 1
- 230000007797 corrosion Effects 0.000 description 1
- 238000005260 corrosion Methods 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 230000005611 electricity Effects 0.000 description 1
- 230000003628 erosive effect Effects 0.000 description 1
- 239000004744 fabric Substances 0.000 description 1
- 210000003608 fece Anatomy 0.000 description 1
- 238000000855 fermentation Methods 0.000 description 1
- 230000004151 fermentation Effects 0.000 description 1
- 239000008246 gaseous mixture Substances 0.000 description 1
- 239000010871 livestock manure Substances 0.000 description 1
- 238000012423 maintenance Methods 0.000 description 1
- 230000002073 mitogenetic effect Effects 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 229910052757 nitrogen Inorganic materials 0.000 description 1
- 238000007254 oxidation reaction Methods 0.000 description 1
- 238000000197 pyrolysis Methods 0.000 description 1
- 239000000779 smoke Substances 0.000 description 1
- 238000013517 stratification Methods 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
- C10B53/00—Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form
- C10B53/02—Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form of cellulose-containing material
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
- C10J3/46—Gasification of granular or pulverulent flues in suspension
- C10J3/54—Gasification of granular or pulverulent fuels by the Winkler technique, i.e. by fluidisation
- C10J3/56—Apparatus; Plants
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
- C10J3/72—Other features
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
- C10J3/72—Other features
- C10J3/82—Gas withdrawal means
- C10J3/84—Gas withdrawal means with means for removing dust or tar from the gas
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F22—STEAM GENERATION
- F22B—METHODS OF STEAM GENERATION; STEAM BOILERS
- F22B31/00—Modifications of boiler construction, or of tube systems, dependent on installation of combustion apparatus; Arrangements of dispositions of combustion apparatus
- F22B31/08—Installation of heat-exchange apparatus or of means in boilers for heating air supplied for combustion
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F22—STEAM GENERATION
- F22G—SUPERHEATING OF STEAM
- F22G7/00—Steam superheaters characterised by location, arrangement, or disposition
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23L—SUPPLYING AIR OR NON-COMBUSTIBLE LIQUIDS OR GASES TO COMBUSTION APPARATUS IN GENERAL ; VALVES OR DAMPERS SPECIALLY ADAPTED FOR CONTROLLING AIR SUPPLY OR DRAUGHT IN COMBUSTION APPARATUS; INDUCING DRAUGHT IN COMBUSTION APPARATUS; TOPS FOR CHIMNEYS OR VENTILATING SHAFTS; TERMINALS FOR FLUES
- F23L15/00—Heating of air supplied for combustion
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E20/00—Combustion technologies with mitigation potential
- Y02E20/34—Indirect CO2mitigation, i.e. by acting on non CO2directly related matters of the process, e.g. pre-heating or heat recovery
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E50/00—Technologies for the production of fuel of non-fossil origin
- Y02E50/10—Biofuels, e.g. bio-diesel
-
- 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
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
- Y02P20/129—Energy recovery, e.g. by cogeneration, H2recovery or pressure recovery turbines
Landscapes
- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Combustion & Propulsion (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Organic Chemistry (AREA)
- Mechanical Engineering (AREA)
- General Engineering & Computer Science (AREA)
- Physics & Mathematics (AREA)
- Thermal Sciences (AREA)
- Materials Engineering (AREA)
- Fluidized-Bed Combustion And Resonant Combustion (AREA)
Abstract
The present invention relates to a kind of system and methods of biomass carbon vapour coproduction, and wherein system includes: sequentially connected fluidized-bed gasification furnace, gas solid separation mechanism and gas fired-boiler；The inner wall that the combustion gas fractional combustion burns boiler is water-cooling wall, and the inside that combustion gas fractional combustion burns boiler, which is equipped with, separates combustion chamber and waste heat recovery room that gas fired-boiler is divided into bottom connection by water-cooling wall；In the burning burning chamber and gas approach is equipped with fuel-staged combustion air hose, is equipped with heating surface in the waste heat recovery room, the gas fired-boiler is connected with the back-end ductwork for flue gas to be discharged in waste heat recovery room side；The gas fired-boiler is connected with for collecting water-cooling wall, separating water-cooling wall and the drum of the superheated steam of superheater generation；Saturated vapor is fed water-cooling wall, separation water-cooling wall and superheater and recycled by the drum.The present invention is improved by the structure to system, can expeditiously produce charcoal particle and superheated steam.
Description
Technical field
The present invention relates to biomass cleans to utilize technical field, and in particular to a kind of system of biomass carbon vapour coproduction and side
Method.
Background technique
The biomass resource in China is very rich, and only agriculture and forestry waste annual output is given birth to just more than 1,000,000,000 tons by exploitation
The utilization technology of physical resources, can optimize energy resource structure at this stage, make up the utilization limitation of fossil energy resource.
The main of biomass resource has biomass direct-fired and gasification of biomass using technology at present.And gasification of biomass can lead to
Pyrolysis and heat chemistry oxidation reaction are crossed, the volatile matter being rich in biomass is converted to CH4、H2And the imflammable gas such as CO, and it is straight
Combustion technology is compared, biomass gasification fired to have the characteristics that overall efficiency height, high efficiency, cost of investment are low and raw material is multifarious,
Currently gradually by application.
Although biomass gasification fired technology provides an approach, existing work for the effective use of biomass resource
Skill there is also some problems in practical applications.
Such as, the combustible gas for largely utilizing gasification of biomass to generate in prior art using burner or internal combustion engine, and
A certain amount of tar gas and fine ash particle will certainly be generated when gasification of biomass, tar is easy to analyse when there are temperature gradient
Out, blocking pipeline and equipment.Therefore combustible gas needs to carry out deep purifying processing before entering burner or internal combustion engine, this is just
Production run cost is considerably increased, while also needing periodically to clear up relevant device, increases maintenance cost.And it is existing
There is the usual ignition temperature of fuel gas buring technique relatively high, and combustion atmosphere organizational difficulties, leads to NO in flue gasxConcentration of emission compares
It is high.
In addition, large-scale application mode can not be formed using the technique of burner or internal combustion engine, it is not able to satisfy the market demand.
In addition to this, existing biomass gasification fired technique has only focused on the efficient utilization of combustible gas, and biomass
Interior fixed carbon is often ignored, and usually and lime-ash is together as waste disposal, considers from comprehensive utilization of resources standpoint of efficiency, existing
The biomass gasification fired technique that has is simultaneously not perfect.
Summary of the invention
In view of the above-mentioned deficiencies in the prior art, it is an object of the present invention to provide system and the side of a kind of biomass carbon vapour coproduction
Method can expeditiously produce charcoal particle and superheated steam.
Technical solution provided by the present invention are as follows:
A kind of system of biomass carbon vapour coproduction, comprising: sequentially connected fluidized-bed gasification furnace, gas solid separation mechanism and combustion
Gas fractional combustion burns boiler；
The inner wall that the combustion gas fractional combustion burns boiler is water-cooling wall, and combustion gas fractional combustion, which burns boiler internal and is equipped with, to be divided
Combustion gas fractional combustion is burnt combustion chamber and the waste heat recovery room that boiler is divided into bottom connection by water proof cold wall；The combustion chamber and
It is equipped with fuel-staged combustion air hose in gas approach, superheater, evaporator, the combustion gas classification are equipped in the waste heat recovery room
It burns boiler and is connected with the back-end ductwork for flue gas to be discharged in waste heat recovery room side；
The combustion gas fractional combustion burns boiler and is connected with to be steamed for collecting water-cooling wall and separating the saturation that water-cooling wall generates
Vapour drum；Saturated water is fed water-cooling wall, separates water-cooling wall, evaporator by the drum, while saturated vapor is sent into superheater
It is recycled.
In the present invention, it is equipped with heating surface in the waste heat recovery room, can be superheater and evaporator, but be not limited to
State heating surface.
The present invention is improved by the structure to system, can effectively be produced charcoal particle and superheated steam, be avoided
Deposition and High Temperature Corrosion of the alkali species contained by biomass in heating surface, while realizing the low NOx row of flue gas
It puts.
Heretofore described burning burning chamber passes through the fuel-staged combustion air hose along combustion chamber height progress divided layer blow
Fractional combustion is realized to control the formation of nitrogen oxides in combustion process.The outlet side of the burning burning chamber is filled equipped with SNCR
It sets.By arranging that SNCR can be further reduced the nitrogen oxides in flue gas, NO is realizedxIt is ultralow that final concentration of emission reaches country
The standard of discharge.
Preferably, the heating surface includes evaporator and superheater from bottom to top.
Heretofore described waste heat recycles chamber inlet, and between superheater, there are one section of cooling chambers for cooled flue gas, make
Superheater entrance flue gas temperature is not higher than 800 DEG C, avoids the deposition that alkali species occur in superheater surface and high temperature rotten
Erosion.
It is successively arranged gasification air preheater in heretofore described back-end ductwork and burns air preheater, both are pre-
Hot device is made of two-stage preheater.Using air pipeline by high temperature air caused by gasification air preheater and fluidized bed gas
Change furnace to be attached, the hot-air for burning air preheater generation is connected with burning burning chamber, and is layered and is sent into along short transverse
Burning burning chamber.The structure setting can be effectively utilized the heat of high-temperature flue gas, high-temperature flue gas and gasification air preheater and
It burns air preheater to exchange heat, normal temperature air forms about 450 after the heating of the two-stage preheater of gasification air preheater
DEG C high temperature air, as the gasification wind in fluidized-bed gasification furnace.Since higher temperature air is sent into fluidized-bed gasification furnace lower part,
Facilitate the gasification reaction into furnace biomass fuel, moisture content can be handled up to 50% or so biomass material.
It is equipped with economizer in heretofore described back-end ductwork, is attached economizer and drum using pipeline.Save coal
Device can effectively utilize the heat of high-temperature flue gas, and warm water is heated into saturated water to be made for water-cooling wall, separation water-cooling wall and evaporator
With.
Economizer of the present invention is arranged between the two-stage preheater of gasification air preheater.
Heretofore described back-end ductwork is also successively arranged the two-stage preheater for burning air preheater, using air pipeline
Two-stage preheater and fuel air hose are sequentially connected.The heat of high-temperature flue gas can be effectively utilized in the structure setting, will
Normal temperature air is heated into after high temperature air as indoor fuel air is burnt, and is sent into burning chamber by multilayer fuel air hose.
Heretofore described fuel-staged combustion air hose includes several groups, along the direction interval cloth of high-temperature gasification flow of air
It sets.Using Researched of Air Staging Combustion Burning Pulverized Coal mode, high-temperature gasification gas is avoided to burn in burning chamber there are high temperature combustion zone and high oxygen concentration area,
The efficient stable burning and temperature for realizing high-temperature gasification gas low oxygen concentration are uniformly distributed, and greatly reduce NOxGeneration.As
It is preferred that the fuel-staged combustion air hose is including 2~15 groups, further preferably 4~10 groups, while at least, guarantee is burnt
As soon as the gas approach of room has a group air hose, gasification gas is made to burn before entering into the combustion chamber in this way, made into combustion chamber
Fuel gas temperature remains stable, guarantees that combustion gas stablizes burning in burning burning chamber.
Preferably, the outlet side temperature control of the combustion chamber parallelly installed left and right has SNCR device at 900 DEG C.The fuel
Air hose includes several groups, along the direction arranged for interval of high-temperature gasification flow of air.Using the technology groups of Researched of Air Staging Combustion Burning Pulverized Coal+SNCR
Conjunction can further control NOxIt generates.
Heretofore described gas solid separation mechanism includes two groups of concatenated cyclone separators.Series connection refers to, first whirlwind
The air outlet of separator is connect with the air inlet of second cyclone separator, so that the gaseous mixture of high-temperature gasification gas and charcoal particle connects
It is continuous to pass through gas solid separation twice.
The present invention also provides a kind of methods for carrying out the coproduction of biomass carbon vapour using such as above-mentioned system, comprising:
1) part gasification reaction generation high-temperature gasification gas and charcoal occur in fluidized-bed gasification furnace for biomass and gasification wind
Grain；
2) high-temperature gasification gas separates in gas solid separation mechanism with charcoal particle, and charcoal particle is collected, and high-temperature gasification gas enters
Combustion gas fractional combustion burns boiler；
3) high-temperature gasification gas in the gas approach of gas fired-boiler and combustion chamber with along highl stratification be sent into fuel air into
Row combustion reaction generates flue gas, and the formation of nitrogen oxides is controlled by control combustion chambers burn atmosphere and Temperature Distribution；Drum
Saturated water is provided, while providing saturated vapor for superheater for water-cooling wall, separation water-cooling wall, the evaporator in gas fired-boiler；And
The heat that the heat of flue gas and combustion reaction generate respectively with water-cooling wall, separate the saturated water and mistake of water-cooling wall, evaporator
Saturated vapor in hot device exchanges heat, and forms superheated steam；
4) flue gas generated in step 3) then enters back-end ductwork after waste heat recovery room.
Gasification wind in step 1) of the present invention is to heat to obtain by gasification air preheater by normal temperature air.High temperature
Normal temperature air is set to be thermally formed high temperature air and as the gas in fluidized-bed gasification furnace after flue gas and the heat exchange of gasification air preheater
Change wind, to efficiently use the heat of high-temperature flue gas.
Fuel air in step 3) of the present invention is to be burnt air preheater by normal temperature air to heat to obtain.High temperature cigarette
Gas and after burning air preheater heat exchange, external normal temperature air are heated into high temperature air and as the indoor fuel airs of burning, by
Multilayer fuel air hose is passed through in combustion chamber.
The saturated water that drum provides in step 3) of the present invention is to be exchanged heat by economizer and high-temperature flue gas by external warm water
It is thermally formed.Produced saturated water forms saturated vapor after heating using heating surfaces such as water-cooling wall, separation water-cooling wall, evaporators
After return into drum.The saturated vapor come out from drum enters high temperature superheater and forms high temperature super heated steam.
The flue gas that combustion reaction generates in step 3) of the present invention is handled by SNCR device, is further reduced in flue gas
Nitrogen oxide emission.
Waste heat recycles chamber inlet to be used for the cold of cooled flue gas to there are one section between superheater in step 3) of the present invention
But room makes superheater entrance flue gas temperature not higher than 800 DEG C；
In step 4) of the present invention flue gas enter after back-end ductwork respectively with gasification air preheater, economizer, burn air
Preheater exchanges heat.
Compared with the existing technology, the beneficial effects of the present invention are embodied in:
(1) present invention is improved by the structure to system, can expeditiously produce charcoal particle and superheated steam.
(2) present invention is heated to higher temperature by the air that high-temperature air preheater will go into gasification furnace, and one
Aspect can reduce combustion share of the biomass in gasification furnace and improve biomass carbon yield, on the other hand can also be improved Gao Shui
The processing capacity of mitogenetic raw material of substance.
(3) control combustion chambers burn atmosphere is passed through using Researched of Air Staging Combustion Burning Pulverized Coal measure in the present invention, realizes high-temperature gasification
Gas is uniformly distributed in the efficient stable burning of combustion chamber and temperature, reduces the production of combustion process nitrogen oxides, while being burnt
A small amount of nitrogen oxides of generation is further reduced to nitrogen using SNCR by room outlet, so that the NOx concentration in flue gas be controlled
In reduced levels.
Detailed description of the invention
Fig. 1 is the structural schematic diagram of the system of biomass carbon vapour coproduction in the present invention.
Wherein, 1, fluidized-bed gasification furnace；2, primary cyclone；3, secondary cyclone；4, combustion gas fractional combustion
Burn boiler；5, burning burning chamber；6, fuel-staged combustion air hose；7, SNCR device；8, waste heat recovery room；9, water-cooling wall；10,
Evaporator；11, superheater；12, back-end ductwork；13, gasification air preheater；14, economizer；15, air preheater is burnt；
16, drum.
Specific embodiment
Below with reference to specific embodiment and attached drawing, the present invention is described in further detail.
As described in Figure 1, the system of biomass carbon vapour coproduction includes: fluidized-bed gasification furnace 1, gas solid separation mechanism 2,3, combustion gas
Fractional combustion burns boiler 4, drum 16 and back-end ductwork 12.
The outlet of fluidized-bed gasification furnace 1 is connect with gas solid separation mechanism, and gas solid separation mechanism includes two groups of concatenated whirlwind
Separator, respectively primary cyclone 2 and secondary cyclone 3.The air outlet and second level of primary cyclone 2 revolve
The air inlet of wind separator 3 connects, so that the gas-solid mixing gas of high-temperature gasification gas and charcoal particle is continuously across gas solid separation twice.
The air outlet of secondary cyclone 3 then burns boiler 4 with combustion gas fractional combustion and connect, and high-temperature gasification gas is enabled to be passed through combustion
In the burning burning chamber 5 of gas boiler 4.
The inner wall of gas fired-boiler 4 is water-cooling wall 9, and the inside of gas fired-boiler 4 is equipped with separation water-cooling wall and is divided into gas fired-boiler 4
The burning burning chamber 5 of bottom connection and waste heat recovery room 8.
It burns in burning chamber 5 and its gas approach is equipped with fuel-staged combustion air hose 6, if fuel-staged combustion air hose includes
Dry group, along the direction arranged for interval of high-temperature gasification flow of air, the quantity of the fuel-staged combustion air hose 6 to burn in burning chamber 5
It is arranged according to the actual size of burning burning chamber 5, such as fuel-staged combustion air hose 6 includes 4~10 groups.Burning burning chamber
1 group of fuel-staged combustion air hose is at least arranged in 5 gas approach.The outlet side of combustion chamber 5 is equipped with SNCR device 7, using sky
The technical combinations of gas fractional combustion+SNCR can efficiently control NOxIt generates.
Heating surface is equipped in waste heat recovery room 8: including superheater 11 and evaporator 10, combustion gas fractional combustion burns boiler 4
It is connected with the drum 16 for collecting the saturated steam that water-cooling wall (including separating water-cooling wall) 9 and evaporator 10 generate, drum
Saturated water is fed water-cooling wall (including separating water-cooling wall) 9 and the formation saturated vapor of evaporator 10 by 16, while saturated vapor being sent
Enter superheater 11 and forms superheated steam.Combustion gas fractional combustion burns boiler 4 and is connected in 8 side of waste heat recovery room for flue gas to be discharged
Back-end ductwork 12.In addition, waste heat recycles chamber inlet to the cooling chamber for being equipped with cooled flue gas between superheater, the entrance of superheater
Flue-gas temperature is not higher than 800 DEG C.
It has been sequentially arranged gasification air preheater 13 in back-end ductwork 12, economizer 14, has burnt air preheater 15.
Gasification air preheater 13 is attached with fluidized-bed gasification furnace 1 using air pipeline, and normal temperature air is by gasification
High temperature air is formed after the two-stage preheater heating of air preheater 13, as the gasification wind in fluidized-bed gasification furnace.The structure
The heat that high-temperature flue gas can be effectively utilized is set, and improves the energy of gasification furnace processing high-moisture low heat value biomass raw material
The two-stage preheater of power, high-temperature flue gas and gasification air preheater 13 exchanges heat, and normal temperature air passes through gasification air preheater
13 are thermally formed 300-500 DEG C of high temperature air, as the gasification wind in fluidized-bed gasification furnace 1.
Economizer 14 is attached with drum 16 using pipeline, can be passed through external warm water into system by pipeline, be made
Warm water is obtained to be passed into after being thermally formed saturated water in drum 16 by drum 16 using water-cooling wall (including separating water-cooling wall) 9
It returns to after forming saturated vapor after heating with evaporator 10 into drum 16.The saturated vapor come out from drum 16 enters
High temperature superheater 11 forms high temperature super heated steam.Air preheater 15 and fuel-staged combustion air hose 6 are burnt using air pipeline
It is attached, external normal temperature air can be passed through into system by air pipeline.Height can be effectively utilized in the structure setting
The heat of warm flue gas is divided as the fuel air in combustion chamber 8 by fuel with 150-200 DEG C of high temperature air of formation after flue gas heat exchange
Grade burning air hose 6 is passed into combustion chamber 5.
Process flow:
External normal temperature air is sent into stream respectively after gasification air preheater 13 is heated to 300~500 DEG C as gasification wind
Change in bed gasification furnace 1.
Biomass is fed in fluidized-bed gasification furnace 1, biomass can select stalk, sawdust and processing fent etc..Gasify wind
With the biomass fermentation first portion gasification reaction fed in fluidized-bed gasification furnace 1, reaction temperature is 650~700 DEG C, and reaction generates high
Wet gas and charcoal particle, the charcoal particle that high-temperature gasification gas carries pass through primary cyclone 2, second level cyclonic separation respectively
It is separated when device 3 and is used as charcoal product.
External normal temperature air respectively with burn after air preheater 15 exchanges heat, 150~200 DEG C are heated to, as combustion gas point
The fuel air that grade burns boiler 4 is sent into combustion gas fractional combustion through multi-stage fuel air hose 6 and is burnt in boiler 4.From second level whirlwind
The high-temperature gasification gas that separator 3 comes out enter combustion gas fractional combustion burn in the burning burning chamber 5 of boiler 4 with multi-stage fuel air hose
6 fuel airs being sent into burn, and the reaction temperature for burning chamber 5 of burning is at 900~950 DEG C.The flue gas that burning burning chamber 5 generates
Discharged nitrous oxides concentration reaches national minimum discharge standard (being less than 50mg/Nm3), combustion gas classification after the processing of SNCR device 7
The flue-gas temperature for burning the outlet of boiler 4 is 500~600 DEG C.
External warm water forms saturated water after the heating of economizer 14, is sent in drum 16 and steam-water separation occurs, isolate
Saturated water be fed through water-cooling wall (including separate water-cooling wall) 9 and evaporator 10 respectively, be further heated into saturated vapor weight
Return steam-water separation in drum 16.The superheated steam that produced saturated vapor is sent into the formation different pressures of superheater 11 is directly outer for making
With.And smoke processing system is then transported to from the flue gas that back-end ductwork 12 comes out and carries out deep purifying processing.
Specific example:
Biomass selects furfural dregs, feeding coal 24t/h, in fluidized-bed gasification furnace 1 and from gasification air preheater 13
300 DEG C of high-temperature gasification wind occur part gasification reaction, 650 DEG C of reaction temperature or so, reaction generate high-temperature gasification gas, charcoal particle
And a small amount of fine ash particle.Charcoal particle is separated with high-temperature gasification gas through primary cyclone 2, secondary cyclone 3, charcoal
Particle production is 2.52t/h.Produced charcoal particle can be used as charcoal product for producing active carbon, charcoal base manure material etc..
The high-temperature gasification gas come out from secondary cyclone 3 enters in the combustion chamber 5 of gas fired-boiler 4 and multi-stage fuel
The fuel air that air hose 6 is sent into burns, and 900 DEG C of ignition temperature or so.NO in the flue gas that burning generatesxConcentration is in SNCR device
96mg/Nm is measured to obtain through flue gas analyzer before 73Left and right, measures to obtain 38mg/Nm after SNCR device 73(conversion to 6% oxygen amount
Under), it is lower than NOxThe limit value of national minimum discharge normal concentration 50mg/Nm3.The 11 superheated steam pressure come out are steamed from superheater
420 DEG C of 3.2Mpa, temperature, which can be used for generating electricity or industrial heating.
Claims (10)
1. a kind of system of biomass carbon vapour coproduction characterized by comprising sequentially connected fluidized-bed gasification furnace, gas-solid point
It disembarks structure and combustion gas fractional combustion burns boiler；
The inner wall that the combustion gas fractional combustion burns boiler is water-cooling wall, and combustion gas fractional combustion, which burns boiler internal and is equipped with, separates water
Combustion gas fractional combustion is burnt burning burning chamber and the waste heat recovery room that boiler is divided into bottom connection by cold wall；It is described to burn
Indoor and gas approach is equipped with fuel-staged combustion air hose；Heating surface, the combustion gas classification combustion are equipped in the waste heat recovery room
It combusts cinder boiler and is connected with the back-end ductwork for flue gas to be discharged in waste heat recovery room side；
The combustion gas fractional combustion burns boiler and is connected with for collecting water-cooling wall and separating the saturated vapor vapour of water-cooling wall generation
Packet；Saturated water is fed water-cooling wall, separates water-cooling wall, evaporator formation saturated vapor by the drum, while saturated vapor being sent
Enter superheater and forms superheated steam.
2. the system of biomass carbon vapour coproduction according to claim 1, which is characterized in that the outlet of the burning burning chamber
Side is equipped with SNCR device.
3. the system of biomass carbon vapour coproduction according to claim 1, which is characterized in that the heating surface wraps from bottom to top
Include evaporator and superheater.
4. the system of biomass carbon vapour coproduction according to claim 1, which is characterized in that the waste heat recycling chamber inlet is extremely
The cooling chamber of cooled flue gas is equipped between superheater, the entrance flue gas temperature of superheater is not higher than 800 DEG C.
5. the system of biomass carbon vapour coproduction according to claim 1, which is characterized in that successively set in the back-end ductwork
There is gasification air preheater and burns air preheater, the gasification air preheater and to burn air preheater pre- by two-stage
Hot device is constituted, and is attached high temperature air caused by gasification air preheater and fluidized-bed gasification furnace using air pipeline,
The hot-air for burning air preheater generation is connected with burning burning chamber, and is layered along short transverse and is sent into burning burning chamber.
6. the system of biomass carbon vapour coproduction according to claim 1 or 5, which is characterized in that set in the back-end ductwork
There is economizer, is attached economizer and drum using pipeline.
7. the system of biomass carbon vapour coproduction according to claim 6, which is characterized in that the economizer setting is being gasified
It air preheater and burns between air preheater.
8. the system of biomass carbon vapour coproduction according to claim 1, which is characterized in that the gas solid separation mechanism includes
Two groups of concatenated cyclone separators.
9. a kind of method that the system using as described in claim 1~8 is any carries out the coproduction of biomass carbon vapour, feature exist
In, comprising:
1) part gasification reaction generation high-temperature gasification gas and charcoal particle occur in fluidized-bed gasification furnace for biomass and gasification wind；
2) high-temperature gasification gas separates in gas solid separation mechanism with charcoal particle, and charcoal particle is collected, and high-temperature gasification gas enters combustion gas
Boiler；
3) high-temperature gasification gas is in the gas approach of gas fired-boiler and burning burning chamber and through fuel-staged combustion air hose along high
The fuel air that degree layering is sent into carries out combustion reaction and generates flue gas, and passes through control combustion chambers burn atmosphere and Temperature Distribution control
The formation of nitrogen oxides；Drum provides saturated water, while being for water-cooling wall, separation water-cooling wall, the evaporator in gas fired-boiler
Hot device provides saturated vapor；And the heat that the heat of flue gas and combustion reaction generate respectively with water-cooling wall, separate water-cooling wall, steam
The saturated water and the saturated vapor in superheater for sending out device exchange heat, and form superheated steam.；
4) flue gas generated in step 3) then enters back-end ductwork after waste heat recovery room.
10. according to the method described in claim 9, it is characterized in that, the cigarette that the reaction of burning burning chamber generates in the step 3)
Gas enters waste heat recovery room after the processing of SNCR device.
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