CN208504375U - A kind of low NOx drainage circulating fluidized bed boiler using high nitrogen biomass - Google Patents
A kind of low NOx drainage circulating fluidized bed boiler using high nitrogen biomass Download PDFInfo
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- CN208504375U CN208504375U CN201820707219.9U CN201820707219U CN208504375U CN 208504375 U CN208504375 U CN 208504375U CN 201820707219 U CN201820707219 U CN 201820707219U CN 208504375 U CN208504375 U CN 208504375U
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- pretreater apparatus
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Abstract
A kind of low NOx drainage circulating fluidized bed boiler using high nitrogen biomass, including burner hearth, feed separation and loop back device, back-end ductwork and feed and fuel Pretreater apparatus.Feed and fuel Pretreater apparatus include at least one charging gear and at least one fuel Pretreater apparatus, charging gear is arranged in fuel Pretreater apparatus side, and fuel Pretreater apparatus is then arranged between burner hearth and feed separation and loop back device, and it is connected to burner hearth by refeed line, and its top setting pyrolysis gaseous state product pathways is connected with feed separation with loop back device entrance.The dipleg cross-sectional area of feed separation and loop back device is the 1/60~1/40 of burner hearth cross-sectional area.The utility model does carrier using hot ash and is pyrolyzed in advance to high nitrogen biomass fuel by the way that fuel Pretreater apparatus is arranged between feed back pipe, realizes the cleaning burning of high nitrogen biomass fuel.
Description
Technical field
The utility model describes a kind of low NOx drainage circulating fluidized bed boiler for using high nitrogen biomass, belongs to burning
Apparatus field more particularly to circulating fluidized bed boiler field.
Background technique
In China, economy rapid development, primary energy consumption amount continue to increase the background increasingly increased with environmental protection pressure
Under, in recent years, renewable energy has become the main pushing hands of China's Energy restructuring.As important one in renewable energy
Ring, according to statistics, the developable Biomass Energy Resources total amount in China are about 700,000,000 tons of standard coals.And in various biomass utilization skills
In art, biomass generation is again at present technical maturity highest, the maximum one kind of development scale.National Development and Reform Commission
It is explicitly pointed out in " Renewable Energy Development " 13 " planning " of publication in 2016, arrives the biomass power generation general assembly of the year two thousand twenty China
Confidential to reach 15,000,000 kW, annual electricity generating capacity requires more than 90,000,000,000 kilowatt hours.Thus stable development biomass power generation is to realization the year two thousand twenty
Account for the target of non-renewable energy consumption specific gravity 15% and 20% respectively with the year two thousand thirty non-fossil energy, Speed-up Establishment cleaning low-carbon shows
For energy system, promotion renewable energy industry sustainable and healthy development is of great immediate significance and application value.
Currently, biomass direct combustion power generation technology mainly includes layer combustion and fluidized combustion two ways, middle layer combustion power generation
Mode has the advantages that easy to operate, operating cost is low etc. based on water-cooling vibration furnace grate furnace, but that there is also efficiencies of combustion is low, by
The problems such as heat area ash and seriously corroded；And the circulating fluidized bed boiler scheme in fluidized combustion generation mode, due to its skill
Art reaches its maturity, fuel tolerance, load adjustment ability, in terms of advantage it is just gradually convex
It is aobvious, become the first choice of current China's biomass direct combustion power generation boiler.
Biomass fuel higher for N element content, such as vinasse, the mass fraction of organic nitrogen are up to 3% or more,
Although circulating fluidized bed boiler has the characteristics that nitrogen oxides, raw emissions are low, but still are unable to satisfy the ultralow row of current pollutant
Requirement (NOx≤the 50mg/m put3), it still needs to be equipped with complicated denitrating flue gas processing for the circulating fluidized bed boiler of the type thus
System (SNCR denitration equipment even SCR denitration equipment), so that the initial outlay of unit and operating cost greatly increase, seriously
Weaken the economic advantages and competitiveness of Properties of CFB.Exactly in this context, it would be desirable to be conceived to biology
The combustion characteristics of matter fuel especially high nitrogen fuel, and the structure and operation characteristic of circulating fluidized bed boiler itself are combined, to original
There is equipment to improve, under the premise of cost is not significantly increased, is effectively reduced the concentration of NOx in boiler raw emissions, very
The unification of the positive economic benefit, social benefit and environmental benefit for realizing renewable energy utilization.
Utility model content
The purpose of this utility model is to provide a kind of cost and discharge the lower recycle stream for using high nitrogen biomass
Fluidized bed boiler, to realize the cleaning burning of high nitrogen-containing biomass fuel, to meet economic benefit, the society of renewable energy utilization
The unification of meeting benefit and environmental benefit.
The utility model is achieved through the following technical solutions:
A kind of low NOx drainage circulating fluidized bed boiler using high nitrogen biomass, the boiler include burner hearth, feed separation
With loop back device, back-end ductwork and feed and fuel Pretreater apparatus, the upper furnace and the feed separation and loopback are filled
The entrance set is connected, and the feed separation is connected with the exhanst gas outlet of loop back device with the back-end ductwork, inside back-end ductwork
It is disposed with heat-transfer surface, it is characterised in that: described be fed with fuel Pretreater apparatus includes at least one charging gear and at least one
A fuel Pretreater apparatus, the charging gear are arranged in the fuel Pretreater apparatus side；The fuel Pretreater apparatus
It is arranged between the burner hearth and the feed separation and loop back device；The fuel Pretreater apparatus and the lower furnace portion are logical
Cross refeed line connection；Pyrolysis gaseous state product pathways and the feed separation and loopback are provided at the top of the fuel Pretreater apparatus
Device portal is connected；The feed separation is connected by dipleg with the fuel Pretreater apparatus with loop back device.
In above-mentioned technical proposal, the dipleg cross-sectional area of the feed separation and loop back device is the burner hearth cross-sectional area
1/60~1/40.
In above-mentioned technical proposal, using extension distance of the device between burner hearth and dipleg as width, and in burner hearth longitudinal direction
The distance that extends is depth, and the depth B of the fuel Pretreater apparatus is the dipleg diameter D's of the feed separation and loop back device
1~1.5 times, i.e. B=(1~1.5) D；The width L of the fuel Pretreater apparatus is the material of the feed separation and loop back device
4~6 times of leg diameter D, i.e. L=(4~6) D；The height H of the fuel Pretreater apparatus is that the feed separation and loopback fill
3.8~4.2 times of the dipleg diameter D set, i.e. H=(3.8~4.2) D.
In above-mentioned technical proposal, according to boiler capacity, the feed separation and loop back device setting are more than two.
In above-mentioned technical proposal, according to boiler capacity, two or more is set side by side in the fuel Pretreater apparatus, and each
Fuel Pretreater apparatus is at least correspondingly arranged a feed separation and loop back device and passes through the material of feed separation and loop back device
Leg connection.
As further improved technical solution, the refeed line setting is more than two, described two above refeed lines
It evenly and symmetrically is arranged on the fuel Pretreater apparatus, and the centre-height with the fuel Pretreater apparatus junction
H is 2.3~2.7 times of the dipleg diameter D of the feed separation and loop back device, i.e. h=(2.3~2.7) D.
Several are arranged in the charging gear, several described charging gears are symmetrically arranged at the fuel pretreatment dress
Set two sides.
The fuel Pretreater apparatus top is provided with gasification agent inlet, and the gasification agent inlet is arranged in the pyrolysis
Below gaseous products channel, and vapor is passed through as gasifying agent.
The first air-distribution device is arranged in the burner hearth bottom, for being passed through oxidant；The fuel Pretreater apparatus bottom is set
The second air-distribution device is set, for being passed through oxidant and/or gasifying agent；Third air-distribution device is arranged in the dipleg bottom, for leading to
Enter to loosen wind.
The burner hearth selects water wall structure, preferably film water cold wall structure.
The utility model has the following advantages that and the utility model has the advantages that 1) is divided into the chemical reaction process of high nitrogen biomass fuel
Two stages of afterburning in fuel pretreatment and burner hearth, by building the different reaction zone of two oxygen contents, so that high nitrogen is biological
Matter fuel successively undergoes two chemical reaction processes of pyrolysis and burning to realize ultralow row to efficiently reduce the generation of its NOx
It puts；2) it is reasonably arranged by components such as dipleg, fuel Pretreater apparatus and refeed lines, realizes fuel and circulating ash in macroscopic view
On opposite-flushing type flowing, promote mixing and heat transfer between the two, and extend the residence time of fuel, further enhance height
Pyrolysis of the nitrogen biomass fuel in fuel Pretreater apparatus, has objectively built stronger reducing atmosphere, greatly
Ground inhibits fuel to generate in the NOx of pyrolysis phase；3) gaseous products that will be generated after high nitrogen biomass fuel thermal decomposition are mainly
CO、H2And CH4Equal reducibility gas, are passed through feed separation and loop back device, to restore generated NOx, further decrease NOx
Raw emissions.
Detailed description of the invention
Fig. 1 is that a kind of low NOx drainage circulating fluidized bed boiler for using high nitrogen biomass involved in the utility model is shown
It is intended to.
Fig. 2 is that the feed of one of which embodiment and the arrangement of fuel Pretreater apparatus involved in the utility model show
It is intended to.
In figure: 1-burner hearth；2-feed separations and loop back device；3-back-end ductworks；4-feeds are filled with fuel pretreatment
It sets；5-charging gears；6-fuel Pretreater apparatus；7-refeed lines；8-pyrolysis gaseous state product pathways；9-third cloth wind dress
It sets；10-the second air-distribution devices；11-the first air-distribution devices；12-diplegs.
Specific embodiment
Specific embodiment of the present utility model and its workflow are further described below in conjunction with attached drawing.
The positional terms such as the upper, lower, left, right, front and rear in present specification be positional relationship based on the figure and
It establishes.Attached drawing is different, then corresponding positional relationship is also possible to change therewith, therefore cannot be interpreted as with this to protection model
The restriction enclosed.
As shown in Figure 1, a kind of low NOx drainage circulating fluidized bed boiler for using high nitrogen biomass, including burner hearth 1, material
Separation and loop back device 2, back-end ductwork 3 and the parts such as feed and fuel Pretreater apparatus 4.1 top of burner hearth and feed separation with
The entrance of loop back device 2 is connected, and feed separation is connected with the exhanst gas outlet of loop back device 2 with back-end ductwork 3, in back-end ductwork 3
Portion is disposed with heat-transfer surface, such as superheater, economizer, air preheater.Feed includes at least one with fuel Pretreater apparatus 4
Charging gear 5 and at least one fuel Pretreater apparatus 6, charging gear 5 are arranged symmetrically in fuel and pre-process 6 liang of processing unit
Side, fuel Pretreater apparatus 6 are arranged between burner hearth 1 and feed separation and loop back device 2.The middle part of fuel Pretreater apparatus 6 with
1 lower part of burner hearth is connected to by refeed line 7, and top passes through pyrolysis gaseous state product pathways 8 and feed separation and 2 entrance of loop back device
It is connected, its underpart is connected with feed separation with the dipleg 12 of 2 lower part of loop back device.
When boiler operatiopn, high nitrogen biomass fuel is sent into fuel pretreatment dress such as screw(-type) feeder through charging gear 4
6 are set, 6 bottom of fuel Pretreater apparatus is installed with the second air-distribution device 10, the oxidants such as air or gasifying agent and fills through the second cloth wind
It sets 10 and enters fuel Pretreater apparatus 6, can make to fluidize in fuel Pretreater apparatus 6 by the flow of control oxidant or gasifying agent
Wind speed is maintained at 1~2m/s or so.At this point, because of anoxic heat will occur for high nitrogen biomass fuel in fuel Pretreater apparatus 6
Pyrolysis is generated CO, H by solution reaction, the volatile matter that part is precipitated2And CH4Equal reducibility gas build stronger go back in a device
Originality atmosphere generates so as to effectively inhibit NOx.Product after pyrolysis will leave fuel pretreatment from two paths respectively
Device 6, the gaseous products that the solid fuel not reacted completely will enter burner hearth 1 together with circulating ash from 7 overflow of refeed line, and be pyrolyzed
Enter feed separation and loop back device 2 by pyrolysis gaseous state product pathways 8 after then mixing with appropriate vapor, goes back crude fuel and exist
The NOx generated after burning in burner hearth 1.Overflow, which enters the fuel of burner hearth 1 and circulating ash, to be sent by the first air-distribution device 11
Oxidant is moved upwards with the fluidising air velocity of 3~5m/s or so.The high nitrogen biomass that do not reacted completely during moving upwards
Fuel is by further occurrence combustion reaction, and since the volatile matter of fuel at this time has removed substantially, therefore fuel after-flame stage NOx is generated
Amount is also less, so as to realize the cleaning burning of high nitrogen-containing biomass fuel.The middle and upper part of burner hearth 1 can be arranged as needed
Overfiren air port and tertiary air orifice, to improve fuel burn-off rate.Ash-laden gas after burning will be from the gaseous state on burner hearth 1 top and pyrolysis
Enter feed separation and loop back device 2 after product mixing, such as cyclone separator, carries out gas solid separation.Solid obtained after separation
The oxidant that particle will be sent by third air-distribution device 9 is transmitted back to 0.2~0.5m/s of fluidising air velocity or so by dipleg 12
6 lower part of fuel Pretreater apparatus, to continue to participate in Matter Transfer process next time.And high-temperature flue gas obtained after separation then will
Into back-end ductwork 3, atmosphere is discharged into being arranged therein after heating surface heat exchange cools down.
As the technical solution of optimization, 12 sectional area of dipleg of feed separation and loop back device 2 is the 1/ of 1 sectional area of burner hearth
60~1/40.
It using extension distance of the device between burner hearth and dipleg as width, and is depth in burner hearth longitudinal direction extension distance,
The depth B of fuel Pretreater apparatus 6 is 1~1.5 times of the 12 diameter D of dipleg of feed separation and loop back device 2, i.e. B=(1~
1.5)D；The width L of fuel Pretreater apparatus 6 is 4~6 times of the 12 diameter D of dipleg of feed separation and loop back device 2, i.e. L=
(4~6) D；The height H of fuel Pretreater apparatus 6 is 3.8~4.2 times of the 12 diameter D of dipleg of feed separation and loop back device 2,
That is H=(3.8~4.2) D.
According to boiler capacity, two or more is set side by side in feed separation and loop back device 2.
According to boiler capacity, fuel Pretreater apparatus 6 is set side by side two or more, and each fuel Pretreater apparatus 6 to
A feed separation is correspondingly arranged less to connect with loop back device 2 and by feed separation with the dipleg 12 of loop back device 2.
As further improved technical solution, two or more is arranged in refeed line 7, and more than two refeed lines are uniform and right
Claim ground be arranged on fuel Pretreater apparatus 6, and with the centre-height h of 6 junction of fuel Pretreater apparatus be feed separation and
2.3~2.7 times of the 12 diameter D of dipleg of loop back device 2, i.e. h=(2.3~2.7) D.
Several are arranged in charging gear 5, several charging gears are symmetrically arranged at 6 two sides of fuel Pretreater apparatus.It is excellent
Choosing, the centre-height h of charging gear 5 and 6 junction of fuel Pretreater apparatus2For the feed separation and loop back device 2
1.8~2.2 times of 12 diameter D of dipleg.
6 top of fuel Pretreater apparatus is provided with gasification agent inlet, and gasification agent inlet setting is logical in pyrolysis gaseous products
8 lower section of road, and vapor is passed through as gasifying agent.
The first air-distribution device 11 is arranged in 1 bottom of burner hearth, for being passed through oxidant；6 bottom of fuel Pretreater apparatus setting the
Two air-distribution devices 10, for being passed through oxidant and/or gasifying agent；Third air-distribution device 9 is arranged in 12 bottom of dipleg, for being passed through pine
Dynamic wind.Preferred technical solution is that the fluidising air velocity in burner hearth 1 is 3~5m/s, the fluidising air velocity in fuel Pretreater apparatus 6
Control is in 1~2m/s.
One of embodiment as shown in Figure 2, feed separation and loop back device 2 select insulation form, and left and right is each
Arrangement one, the sectional area of dipleg 12 is taken as the 1/50 of 1 sectional area of burner hearth；One fuel Pretreater apparatus 6 with it is above-mentioned two
Feed separation is respectively connected with loop back device 2, and its depth and width and height are taken as 1.5,4 and the 4 of 12 diameter of dipleg respectively
Times；Two refeed lines 7 evenly and symmetrically are arranged in the front end face of fuel Pretreater apparatus 6, and diameter d is taken as the straight of dipleg 12
Diameter D, and the high h in center with 6 junction of fuel Pretreater apparatus1It is taken as 2.5 times of 12 diameter D of dipleg；Two charging gears 5 are right
It is arranged in two side end faces of fuel Pretreater apparatus 6, and the high h in center with 6 junction of fuel Pretreater apparatus with claiming2It is taken as
2 times of 12 diameter D of dipleg.In addition, burner hearth 1 uses film water cold wall structure and is disposed with pendant superheater to carry out working medium and bed
The heat exchange of side, and its bottom is provided with a bed material supply mouth, bed material is required supplementation with according to operation, to guarantee that in-furnace dust recycles
Foundation.
The above descriptions are merely preferred embodiments of the present invention, is not intended to limit the utility model, for this
For the technical staff in field, various modifications and changes may be made to the present invention.It is all in the spirit and principles of the utility model
Within, any modification, equivalent replacement, improvement and so on should be included within the scope of protection of this utility model.
Claims (10)
1. a kind of low NOx drainage circulating fluidized bed boiler for using high nitrogen biomass, the boiler includes burner hearth (1), material point
From with loop back device (2), back-end ductwork (3) and feed and fuel Pretreater apparatus (4), burner hearth (1) top and the object
Material separation is connected with the entrance of loop back device (2), the exhanst gas outlet and the tail portion cigarette of the feed separation and loop back device (2)
Road (3) is connected, and is disposed with heat-transfer surface inside back-end ductwork (3), it is characterised in that: the feed and fuel Pretreater apparatus (4)
Including at least one charging gear (5) and at least one fuel Pretreater apparatus (6), the charging gear (5) is arranged in described
Fuel Pretreater apparatus (6) side；The fuel Pretreater apparatus (6) setting the burner hearth (1) and the feed separation with
Between loop back device (2)；The fuel Pretreater apparatus (6) is connected to the burner hearth (1) lower part by refeed line (7)；It is described
Pyrolysis gaseous state product pathways (8) and the feed separation and loop back device (2) entrance are provided at the top of fuel Pretreater apparatus (6)
It is connected；The feed separation is connected by dipleg (12) with the fuel Pretreater apparatus (6) with loop back device (2).
2. a kind of low NOx drainage circulating fluidized bed boiler for using high nitrogen biomass according to claim 1, feature exist
In: the feed separation and loop back device (2) setting are more than two.
3. a kind of low NOx drainage circulating fluidized bed boiler for using high nitrogen biomass according to claim 1 or 2, special
Sign is: dipleg (12) sectional area of the feed separation and loop back device (2) is the 1/60~1/ of the burner hearth (1) sectional area
40。
4. a kind of low NOx drainage circulating fluidized bed boiler for using high nitrogen biomass according to claim 3, feature exist
In: the depth B of the fuel Pretreater apparatus (6) is the 1 of dipleg (12) diameter D of the feed separation and loop back device (2)
~1.5 times；The width L of the fuel Pretreater apparatus (6) is dipleg (12) diameter of the feed separation and loop back device (2)
4~6 times of D；The height H of the fuel Pretreater apparatus (6) is that the feed separation and the dipleg (12) of loop back device (2) are straight
3.8~4.2 times of diameter D.
5. a kind of low NOx drainage circulating fluidized bed boiler for using high nitrogen biomass according to claim 1 or 4, special
Sign is: two or more, and each fuel Pretreater apparatus (6) and at least one is set side by side in the fuel Pretreater apparatus (6)
A feed separation is connect with the dipleg (12) of loop back device (2).
6. a kind of low NOx drainage circulating fluidized bed boiler for using high nitrogen biomass according to claim 1, feature exist
In: refeed line (7) setting is more than two, and described two above refeed lines are uniformly distributed in the fuel pretreatment dress
It sets on (6), and is the feed separation and loop back device (2) with the centre-height h of the fuel Pretreater apparatus (6) junction
2.3~2.7 times of dipleg (12) diameter D.
7. a kind of low NOx drainage circulating fluidized bed boiler for using high nitrogen biomass according to claim 1, feature exist
In: several are arranged in the charging gear (5), several described charging gears are symmetrically arranged at the fuel Pretreater apparatus
(6) two sides.
8. a kind of low NOx drainage circulating fluidized bed boiler for using high nitrogen biomass according to claim 1, feature exist
In: fuel Pretreater apparatus (6) top is provided with gasification agent inlet, and the gasification agent inlet is passed through vapor as gasification
Agent.
9. a kind of low NOx drainage circulating fluidized bed boiler for using high nitrogen biomass according to claim 1, feature exist
In: the first air-distribution device (11) are arranged in burner hearth (1) bottom, for being passed through oxidant；Fuel Pretreater apparatus (6) bottom
The second air-distribution device (10) are arranged in portion, for being passed through oxidant and/or gasifying agent；Third cloth wind is arranged in dipleg (12) bottom
Device (9), for being passed through loosening wind.
10. a kind of low NOx drainage circulating fluidized bed boiler for using high nitrogen biomass according to claim 1, feature
Be: the burner hearth (1) selects water wall structure.
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201820707219.9U CN208504375U (en) | 2018-05-11 | 2018-05-11 | A kind of low NOx drainage circulating fluidized bed boiler using high nitrogen biomass |
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| CN201820707219.9U CN208504375U (en) | 2018-05-11 | 2018-05-11 | A kind of low NOx drainage circulating fluidized bed boiler using high nitrogen biomass |
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| CN208504375U true CN208504375U (en) | 2019-02-15 |
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ID=65298618
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108592016A (en) * | 2018-05-11 | 2018-09-28 | 清华大学 | A kind of low NOx drainage circulating fluidized bed boiler using high nitrogen biomass |
| CN111006207A (en) * | 2019-12-09 | 2020-04-14 | 华中科技大学 | Biomass fluidized bed direct combustion system and denitration method thereof |
-
2018
- 2018-05-11 CN CN201820707219.9U patent/CN208504375U/en active Active
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108592016A (en) * | 2018-05-11 | 2018-09-28 | 清华大学 | A kind of low NOx drainage circulating fluidized bed boiler using high nitrogen biomass |
| CN108592016B (en) * | 2018-05-11 | 2024-03-26 | 清华大学 | Low NOx emission circulating fluidized bed boiler for burning high-nitrogen biomass |
| CN111006207A (en) * | 2019-12-09 | 2020-04-14 | 华中科技大学 | Biomass fluidized bed direct combustion system and denitration method thereof |
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