CN108592016A - 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
- Publication number
- CN108592016A CN108592016A CN201810455062.XA CN201810455062A CN108592016A CN 108592016 A CN108592016 A CN 108592016A CN 201810455062 A CN201810455062 A CN 201810455062A CN 108592016 A CN108592016 A CN 108592016A
- Authority
- CN
- China
- Prior art keywords
- fuel
- loop back
- pretreater apparatus
- back device
- fuel pretreater
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Granted
Links
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 title claims abstract description 56
- 239000002028 Biomass Substances 0.000 title claims abstract description 36
- 229910052757 nitrogen Inorganic materials 0.000 title claims abstract description 28
- 239000000446 fuel Substances 0.000 claims abstract description 100
- 238000000926 separation method Methods 0.000 claims abstract description 53
- 238000000197 pyrolysis Methods 0.000 claims abstract description 12
- 230000037361 pathway Effects 0.000 claims abstract description 6
- 239000003795 chemical substances by application Substances 0.000 claims description 14
- 239000007800 oxidant agent Substances 0.000 claims description 10
- 230000001590 oxidative effect Effects 0.000 claims description 9
- 239000000463 material Substances 0.000 claims description 8
- 239000007789 gas Substances 0.000 claims description 7
- 238000002309 gasification Methods 0.000 claims description 7
- 238000012546 transfer Methods 0.000 claims description 5
- 239000004744 fabric Substances 0.000 claims description 4
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 4
- 235000019504 cigarettes Nutrition 0.000 claims 1
- 238000004140 cleaning Methods 0.000 abstract description 3
- 238000002485 combustion reaction Methods 0.000 description 11
- 230000008901 benefit Effects 0.000 description 10
- 238000006243 chemical reaction Methods 0.000 description 5
- 238000005516 engineering process Methods 0.000 description 3
- 230000007613 environmental effect Effects 0.000 description 3
- MWUXSHHQAYIFBG-UHFFFAOYSA-N nitrogen oxide Inorganic materials O=[N] MWUXSHHQAYIFBG-UHFFFAOYSA-N 0.000 description 3
- 238000010248 power generation Methods 0.000 description 3
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 2
- 230000008859 change Effects 0.000 description 2
- 238000011161 development Methods 0.000 description 2
- 239000003344 environmental pollutant Substances 0.000 description 2
- 239000003546 flue gas Substances 0.000 description 2
- QJGQUHMNIGDVPM-UHFFFAOYSA-N nitrogen group Chemical group [N] QJGQUHMNIGDVPM-UHFFFAOYSA-N 0.000 description 2
- 231100000719 pollutant Toxicity 0.000 description 2
- 238000012545 processing Methods 0.000 description 2
- 230000001172 regenerating effect Effects 0.000 description 2
- 239000007787 solid Substances 0.000 description 2
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- -1 burner hearth 1 Substances 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 230000035611 feeding Effects 0.000 description 1
- 238000011010 flushing procedure Methods 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 238000000034 method Methods 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 238000005457 optimization Methods 0.000 description 1
- 125000001477 organic nitrogen group Chemical group 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 239000002245 particle Substances 0.000 description 1
- 230000008569 process Effects 0.000 description 1
- 230000003134 recirculating effect Effects 0.000 description 1
- 239000004449 solid propellant Substances 0.000 description 1
- 230000009469 supplementation Effects 0.000 description 1
- 238000005979 thermal decomposition reaction Methods 0.000 description 1
Classifications
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23C—METHODS OR APPARATUS FOR COMBUSTION USING FLUID FUEL OR SOLID FUEL SUSPENDED IN A CARRIER GAS OR AIR
- F23C10/00—Fluidised bed combustion apparatus
- F23C10/18—Details; Accessories
- F23C10/20—Inlets for fluidisation air, e.g. grids; Bottoms
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23C—METHODS OR APPARATUS FOR COMBUSTION USING FLUID FUEL OR SOLID FUEL SUSPENDED IN A CARRIER GAS OR AIR
- F23C10/00—Fluidised bed combustion apparatus
- F23C10/18—Details; Accessories
- F23C10/24—Devices for removal of material from the bed
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23C—METHODS OR APPARATUS FOR COMBUSTION USING FLUID FUEL OR SOLID FUEL SUSPENDED IN A CARRIER GAS OR AIR
- F23C2206/00—Fluidised bed combustion
- F23C2206/10—Circulating fluidised bed
Landscapes
- Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- Combustion & Propulsion (AREA)
- Mechanical Engineering (AREA)
- General Engineering & Computer Science (AREA)
- Fluidized-Bed Combustion And Resonant Combustion (AREA)
Abstract
A kind of low NO using high nitrogen biomassxCirculating fluidized bed boiler, 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 be connected to by refeed line with burner hearth, 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 present invention 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
Invention describes a kind of low NOx drainage circulating fluidized bed boiler using high nitrogen biomass, belong to combustion apparatus
Field more particularly to circulating fluidized bed boiler field.
Background technology
In China, economy rapid development, primary energy consumption amount continue to increase the background increasingly increased with environmental protection pressure
Under, in recent years, regenerative resource has become the main pushing hands of China's Energy restructuring.As important in regenerative resource
One 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 utilizations
In technology, biomass generation is again at present technical maturity highest, the maximum one kind of development scale.
Currently, biomass direct combustion power generation technology includes mainly layer combustion and fluidized combustion two ways, middle level combustion power generation
Mode has the advantages that easy to operate, operating cost is low etc. based on water-cooling vibration furnace grate stove, but that there is also efficiencies of combustion is low, by
The problems such as hot 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, just gradually convex in the advantage of fuel tolerance, load adjustment ability, pollutant emission level etc.
It is aobvious, become the first choice of current China's biomass direct combustion power generation boiler.
For the higher biomass fuel of N element content, such as vinasse, the mass fraction of organic nitrogen is up to 3% or more,
Although circulating fluidized bed boiler has the characteristics that nitrogen oxides, raw emissions are low, but still it is ultralow to cannot be satisfied current pollutant
Requirement (NOx≤50mg/m of discharge3), it still needs to be equipped with complicated denitrating flue gas for the circulating fluidized bed boiler of the type thus
Processing 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 have in mind
In the combustion characteristics of the especially high nitrogen fuel of biomass fuel, and combine the structure of circulating fluidized bed boiler itself and operation special
Point, is improved existing equipment, not being added to this under the premise of substantially, is effectively reduced NOx in boiler raw emissions
Concentration really realizes the unification of the economic benefit, social benefit and environmental benefit of renewable energy utilization.
Invention content
The purpose of the present invention is to provide a kind of cost and discharge the lower recirculating fluidized bed for using high nitrogen biomass
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 benefit and environmental benefit.
The present invention 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 is filled with the feed separation and loopback
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：The feed and fuel Pretreater apparatus include 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
It is connected to by refeed line；Be provided at the top of the fuel Pretreater apparatus pyrolysis gaseous state product pathways and the feed separation with
Loop back device entrance 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 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 feed separation and loop back device
4~6 times of dipleg diameter D, i.e. L=(4~6) D；The height H of the fuel Pretreater apparatus is the feed separation and returns
Send the dipleg diameter D of device 3.8~4.2 times, 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, the fuel Pretreater apparatus is set up in parallel two or more, and each
Fuel Pretreater apparatus is at least correspondingly arranged a feed separation with loop back device and by the material of feed separation and loop back device
Leg connects.
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 high with the center of the fuel Pretreater apparatus junction
Spend the dipleg diameter D that h is the feed separation and loop back device 2.3~2.7 times, 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 both 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 present invention has the following advantages and beneficial effects：1) chemical reaction process of high nitrogen biomass fuel combustion has been divided into
Two stages of afterburning in material pretreatment and burner hearth, the reaction zone different by building two oxygen contents so that high nitrogen biomass fuel
Material successively experience pyrolysis and two chemical reaction processes of burning realize minimum discharge to efficiently reduce the generation of its NOx；
2) it is reasonably arranged by components such as dipleg, fuel Pretreater apparatus and refeed lines, realizes fuel and circulating ash macroscopically
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 be generated in the NOx of pyrolysis phase；3) gaseous products that will be generated after high nitrogen biomass fuel thermal decomposition, it is main
It is CO, H2And CH4Equal reducibility gas, are passed through feed separation and loop back device, to restore generated NOx, further decrease
The raw emissions of NOx.
Description of the drawings
Fig. 1 is a kind of low NOx drainage circulating fluidized bed boiler schematic diagram using high nitrogen biomass according to the present invention.
Fig. 2 is that the feed of one of which embodiment according to the present invention and the arrangement of fuel Pretreater apparatus are illustrated
Figure.
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 fill
It sets；10-the second air-distribution devices；11-the first air-distribution devices；12-diplegs.
Specific implementation mode
The specific implementation mode and its workflow of the present invention are further described below in conjunction with attached drawing.
The orientation such as upper, lower, left, right, front and rear in present specification term be position relationship based on ... shown in the drawings and
It establishes.Attached drawing is different, then corresponding position relationship is also possible to change therewith, therefore cannot be interpreted as with this to protection
The restriction of range.
As shown in Figure 1, a kind of low NOx drainage circulating fluidized bed boiler 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
A charging gear 5 and at least one fuel Pretreater apparatus 6, charging gear 5 are arranged symmetrically in fuel pretreatment processing unit 6
Both sides, fuel Pretreater apparatus 6 are arranged between burner hearth 1 and feed separation and loop back device 2.6 middle part of fuel Pretreater apparatus
It is connected to by refeed line 7 with 1 lower part of burner hearth, top is by being pyrolyzed gaseous state product pathways 8 and feed separation and loop back device 2
Entrance is connected, and 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 is filled through the second cloth wind
It sets 10 and enters fuel Pretreater apparatus 6, the flow by controlling oxidant or gasifying agent can make stream in fuel Pretreater apparatus 6
Change wind speed and is maintained at 1~2m/s or so.At this point, high nitrogen biomass fuel will occur in fuel Pretreater apparatus 6 because of anoxic
Pyrolysis is generated CO, H by pyrolytic reaction, the volatile matter that part is precipitated2And CH4Equal reducibility gas are built relatively strong in a device
Reducing atmosphere, so as to effectively inhibit NOx generate.Product after pyrolysis will leave fuel from two paths respectively
Pretreatment unit 6, the solid fuel not reacted completely will enter burner hearth 1 together with circulating ash from 7 overflow of refeed line, and be pyrolyzed
Gaseous products by being pyrolyzed gaseous state product pathways 8 will enter feed separation and loop back device 2 after then being mixed with appropriate vapor,
The NOx that also crude fuel generates in burner hearth 1 after burning.Overflow, which will enter the fuel of burner hearth 1 and circulating ash, to be filled by the first cloth wind
The oxidant for setting 11 feedings is moved upwards with the fluidising air velocity of 3~5m/s or so.The not reaction completely during moving upwards
High nitrogen biomass fuel combustion reaction will further occur, since the volatile matter of fuel at this time has removed substantially, therefore fuel fires
The stage, NOx generation amount was also less to the greatest extent, so as to realize the cleaning burning of high nitrogen-containing biomass fuel.The middle and upper part of burner hearth 1
Overfiren air port and tertiary air orifice can be arranged as needed, to improve fuel burn-off rate.Ash-laden gas after burning will be from burner hearth 1
Top enters feed separation and loop back device 2 after being mixed with the gaseous products of pyrolysis, such as cyclone separator, carries out gas solid separation.
The oxidant that the solid particle obtained after separation will be sent by third air-distribution device 9, it is left with 0.2~0.5m/s of fluidising air velocity
The right side is transmitted back to 6 lower part of fuel Pretreater apparatus by dipleg 12, to continue to participate in Matter Transfer process next time.And it detaches
The high-temperature flue gas obtained afterwards will then enter back-end ductwork 3, and air is discharged into being arranged therein after heating surface heat exchange cools down.
Technical solution as an optimization, feed separation and 12 sectional area of dipleg of loop back device 2 are 1 sectional areas of burner hearth
1/60~1/40.
Using extension distance of the device between burner hearth and dipleg as width, and it 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 feed separation and the 12 diameter D of dipleg of loop back device 2, i.e. L=
(4~6) D；The height H of fuel Pretreater apparatus 6 is the 3.8~4.2 of feed separation and the 12 diameter D of dipleg of loop back device 2
Times, i.e. H=(3.8~4.2) D.
According to boiler capacity, feed separation is set up in parallel two or more with loop back device 2.
According to boiler capacity, fuel Pretreater apparatus 6 is set up in parallel two or more, and each fuel Pretreater apparatus 6 to
It is correspondingly arranged a feed separation less with loop back device 2 and is connect 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 both 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
Loosen wind.Preferred technical solution is that the fluidising air velocity in burner hearth 1 is 3~5m/s, the fluidized wind in fuel Pretreater apparatus 6
Speed control is in 1~2m/s.
One of which embodiment as shown in Figure 2, feed separation selects adiabatic form with loop back device 2, 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 and 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 dipleg 12
Diameter D, and with the high h in center of 6 junction of fuel Pretreater apparatus1It is taken as 2.5 times of 12 diameter D of dipleg；Two charging gears
5 are symmetrically arranged at two side end faces of fuel Pretreater apparatus 6, and with the high h in center of 6 junction of fuel Pretreater apparatus2
It 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 work
The heat exchange of matter and bed side, and in the setting of its bottom, there are one bed materials to feed mouth, bed material is required supplementation with according to operation, to ensure in stove
The foundation of ash cycle.
The foregoing is only a preferred embodiment of the present invention, is not intended to restrict the invention, for the skill of this field
For art personnel, the invention may be variously modified and varied.All within the spirits and principles of the present invention, any made by
Modification, equivalent replacement, improvement etc., should all be included in the protection scope of the present invention.
Claims (10)
1. a kind of low NOx drainage circulating fluidized bed boiler 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), exhanst gas outlet and the tail portion cigarette of the feed separation with loop back device (2)
Road (3) is connected, and heat-transfer surface is disposed with 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 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 using high nitrogen biomass according to claim 1 or 2, special
Sign is：The feed separation and dipleg (12) sectional area of loop back device (2) are the 1/60~1/ of the burner hearth (1) sectional area
40。
4. a kind of low NOx drainage circulating fluidized bed boiler using high nitrogen biomass according to claim 3, feature exist
In：The depth B of the fuel Pretreater apparatus (6) is the 1 of the feed separation and dipleg (12) diameter D of 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 using high nitrogen biomass according to claim 1 or 4, special
Sign is：The fuel Pretreater apparatus (6) is set up in parallel two or more, and each fuel Pretreater apparatus (6) and at least one
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 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 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) both sides.
8. a kind of low NOx drainage circulating fluidized bed boiler 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 using high nitrogen biomass according to claim 1, feature exist
In：The first air-distribution device (11) is arranged in burner hearth (1) bottom, for being passed through oxidant；Fuel Pretreater apparatus (6) bottom
The second air-distribution device (10) is 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 using high nitrogen biomass according to claim 1, feature
It is：The burner hearth (1) selects water wall structure.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201810455062.XA CN108592016B (en) | 2018-05-11 | 2018-05-11 | Low NOx emission circulating fluidized bed boiler for burning high-nitrogen biomass |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201810455062.XA CN108592016B (en) | 2018-05-11 | 2018-05-11 | Low NOx emission circulating fluidized bed boiler for burning high-nitrogen biomass |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN108592016A true CN108592016A (en) | 2018-09-28 |
| CN108592016B CN108592016B (en) | 2024-03-26 |
Family
ID=63637408
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201810455062.XA Active CN108592016B (en) | 2018-05-11 | 2018-05-11 | Low NOx emission circulating fluidized bed boiler for burning high-nitrogen biomass |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN108592016B (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111617878A (en) * | 2020-05-12 | 2020-09-04 | 路德环境科技股份有限公司 | Impurity removing device suitable for continuous fluidized bed drying process |
Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101093108A (en) * | 2007-06-06 | 2007-12-26 | 黄立维 | Method and equipment for recovering heat energy of burning on fume in high temperature |
| CN102777895A (en) * | 2012-07-24 | 2012-11-14 | 武汉和信益科技有限公司 | Semi-tower type medium-temperature separation biomass circulating fluidized bed boiler |
| CN102974204A (en) * | 2012-12-13 | 2013-03-20 | 江苏百灵天地环境设计研究院有限公司 | Reaction device for SNCR (selective non-catalytic reduction) denitration system of circulating fluid bed |
| CN204254603U (en) * | 2014-11-28 | 2015-04-08 | 蒋俊芳 | CFBB low nitrogen burning system |
| CN106554826A (en) * | 2015-09-30 | 2017-04-05 | 中国科学院工程热物理研究所 | Circulation fluidized bed coal gasifying method and device with fine ash melting |
| CN107270281A (en) * | 2017-07-03 | 2017-10-20 | 国丰新能源江苏有限公司 | Biomass recirculating fluidized bed boiler and its operation method |
| CN208504375U (en) * | 2018-05-11 | 2019-02-15 | 清华大学 | A kind of low NOx drainage circulating fluidized bed boiler using high nitrogen biomass |
-
2018
- 2018-05-11 CN CN201810455062.XA patent/CN108592016B/en active Active
Patent Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101093108A (en) * | 2007-06-06 | 2007-12-26 | 黄立维 | Method and equipment for recovering heat energy of burning on fume in high temperature |
| CN102777895A (en) * | 2012-07-24 | 2012-11-14 | 武汉和信益科技有限公司 | Semi-tower type medium-temperature separation biomass circulating fluidized bed boiler |
| CN102974204A (en) * | 2012-12-13 | 2013-03-20 | 江苏百灵天地环境设计研究院有限公司 | Reaction device for SNCR (selective non-catalytic reduction) denitration system of circulating fluid bed |
| CN204254603U (en) * | 2014-11-28 | 2015-04-08 | 蒋俊芳 | CFBB low nitrogen burning system |
| CN106554826A (en) * | 2015-09-30 | 2017-04-05 | 中国科学院工程热物理研究所 | Circulation fluidized bed coal gasifying method and device with fine ash melting |
| CN107270281A (en) * | 2017-07-03 | 2017-10-20 | 国丰新能源江苏有限公司 | Biomass recirculating fluidized bed boiler and its operation method |
| CN208504375U (en) * | 2018-05-11 | 2019-02-15 | 清华大学 | A kind of low NOx drainage circulating fluidized bed boiler using high nitrogen biomass |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111617878A (en) * | 2020-05-12 | 2020-09-04 | 路德环境科技股份有限公司 | Impurity removing device suitable for continuous fluidized bed drying process |
Also Published As
| Publication number | Publication date |
|---|---|
| CN108592016B (en) | 2024-03-26 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN101245264B (en) | Single-bed self-heating type thermal decomposition gasification combustion reactor and thermal decomposition gasification combustion method | |
| CN106554826B (en) | Circulating fluidized bed coal gasification method and device with fine ash fusion | |
| CN100582197C (en) | Circulating fluidized bed heat-power-gas-tar multi-joint-production apparatus and method | |
| CN107043641B (en) | Coal gasification method and device of circulating fluidized bed with fine ash return | |
| CN103320175B (en) | High-efficiency clean low-carbon coal graded utilization method and device | |
| CN101024782B (en) | Dense-phase conveying-bed coal pressurizing gasifying apparatus and method | |
| CN105062528B (en) | A kind of pyrolysis of coal multi-production process and its device suitable for coal-powder boiler | |
| CN103740409B (en) | Multi-stage gas distribution high-temperature coal gasification device and method | |
| CN103361087A (en) | Pyrolysis and combustion coupled circular reaction method and device | |
| CN201241071Y (en) | Single-bed self-heating type thermal decomposition gasification combusting reactor | |
| CN102287813A (en) | Boiler device adopting cyclone-burning method | |
| CN110791326B (en) | Circulating fluidized bed gasification device with auxiliary gasification bed and gasification method | |
| CN204786347U (en) | Biomass gasification phase separating combustion furnace | |
| CN103884013A (en) | Combustion method and device of coupled environment-friendly fluidized bed boiler | |
| CN103604121B (en) | Adopt the oil shale semi-coke fluidized bed combustion syste of triple channel flow-dividing control material returning device | |
| CN208504375U (en) | A kind of low NOx drainage circulating fluidized bed boiler using high nitrogen biomass | |
| CN208776672U (en) | A kind of manifold type gasification system | |
| CN102944008B (en) | The system that a kind of double fluidized bed combustion stove prevents boiler heating surface from staiing | |
| CN101122388A (en) | Method and device for making fluid bed to produce super high-temperature fume | |
| CN108592016A (en) | A kind of low NOx drainage circulating fluidized bed boiler using high nitrogen biomass | |
| CN105419878B (en) | A kind of two sections of pyrolysis gasification systems of solid waste | |
| CN202993183U (en) | Boiler heating surface contamination prevention system for double fluidized bed combustion furnace | |
| CN205295251U (en) | Two sections pyrolysis gasification system of solid waste | |
| CN207486807U (en) | A kind of fluid bed heating center for using low calorie fuels | |
| CN105132039A (en) | Fluidized-bed fly ash back-to- furnace gasification apparatus and method |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant |