CN106765244A - Three wastes stove combustion system and denitration method for flue gas - Google Patents
Three wastes stove combustion system and denitration method for flue gas Download PDFInfo
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- CN106765244A CN106765244A CN201611192529.3A CN201611192529A CN106765244A CN 106765244 A CN106765244 A CN 106765244A CN 201611192529 A CN201611192529 A CN 201611192529A CN 106765244 A CN106765244 A CN 106765244A
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES
- F23J15/00—Arrangements of devices for treating smoke or fumes
- F23J15/006—Layout of treatment plant
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES
- F23J15/00—Arrangements of devices for treating smoke or fumes
- F23J15/02—Arrangements of devices for treating smoke or fumes of purifiers, e.g. for removing noxious material
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES
- F23J2215/00—Preventing emissions
- F23J2215/10—Nitrogen; Compounds thereof
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- Treating Waste Gases (AREA)
Abstract
The invention provides a kind of three wastes stove combustion system and denitration method for flue gas.The three wastes stove combustion system includes the three wastes stove and flue gas post-processing unit that are connected by flue, the combustion system also includes SNCR devices, SNCR devices have reactor, and reactor is arranged on flue, and the reactor cross section product along flow of flue gas direction of reactor is accumulated more than the flue cross section of flue.It is improved by the reactor to SNCR devices, it is set to be accumulated more than the flue cross section of flue along the reactor cross section product in flow of flue gas direction, flow velocity is slack-off when flue gas is entered sectional area larger reactor, and then cause that reaction time of the flue gas in the reactor of SNCR devices extends relative to the reaction time before improving in flue, you can improve denitration rate to improve the hybrid reaction effect of flue gas and reducing agent.Transformation of the above-mentioned transformation to equipment is smaller, and construction is simple, invests relatively low, it is adaptable to large-scale commercial Application.
Description
Technical field
The present invention relates to field of waste treatment, in particular to a kind of three wastes stove combustion system and denitrating flue gas side
Method.
Background technology
The current chemical enterprise with coal as raw material of China, can produce substantial amounts of gas-making cinder, gas making deduster thin in production
Ash, producing gas blower, synthesis gas drop a hint with ammonia storage tank deflate etc. waste gas and waste residue.These waste gas and waste residue are and are claimed by enterprise
For the three wastes in two give up.In recent years, with the implementation of national resources comprehensive utilization industrial policy and by energy scarcity and ring
The influence of packing pressure increase, because phosphorus content and combustible component are high in waste gas, flying dust, the slag of discharge, simple discharge can be caused
The waste of the energy and the secondary pollution of environment, thus three wastes stove treatment technology have become the more commonly used treatment of enterprise give up
Water, waste gas, the mode of waste residue.Three wastes stove is by reclaiming the slag for using blowing-out gas and mixing burning Gas-making Furnace, gangue, cigarette inferior
Coal and anchracite duff produce steam for other places using the effect of energy-saving and emission-reduction is reached, yet with fuel nitrogen content mistake
Height, the nitrogen oxides in effluent content that three wastes fire grate goes out is always held at a level higher.How in flue gas nitrogen oxygen is reduced
The concentration of compound turns into a problem for needing urgent solution instantly.
Most enterprises install SCR (SCR technology) equipment additional in order to meet environmental requirement, typically, but by
In nitrogen oxides in effluent content (the about 2000mg/Nm very high that three wastes fire grate goes out3-3000mg/Nm3), directly use SCR techniques
The higher, enforcement difficulty of investment is big and operating cost is high.Therefore, most of three wastes stoves furnace outlet when using SCR technique denitrations
Nitrogen oxides needs to maintain relatively low level, just can (selective non-catalytic is also by low-NO_x combustion technology or SNCR
Former technology) technology implementation, wherein, low-NO_x combustion technology can be completed in burner hearth, and SNCR can be completed at furnace outlet, but
It is that from the point of view of current actual treatment situation, denitration rate is simultaneously not so good as the height envisioned.Denitration efficiency is up to 50% or so.
The content of the invention
It is existing to solve it is a primary object of the present invention to provide a kind of three wastes stove combustion system and denitration method for flue gas
The undesirable problem of three wastes stove denitration effect in technology.
To achieve these goals, it is according to an aspect of the invention, there is provided a kind of three wastes stove combustion system including logical
Flue connected three wastes stove and flue gas post-processing unit are crossed, the combustion system also includes SNCR devices, and SNCR devices have reaction
Device, reactor is arranged on flue, and the reactor cross section product along flow of flue gas direction of reactor is cut more than the flue of flue
Area.
Further, above-mentioned cross-sectional reactor area is 2 times to 5 times of flue cross-sectional area.
Further, above-mentioned reactor is the reactor with heat insulation function.
Further, above-mentioned reactor is U-shaped reactor, S types reactor or snakelike reactor.
Further, above-mentioned reactor has reactant entrance and product exit, and SNCR devices also include blender, mixing
Device sets in the reactor and is set near reactant entrance, and preferably blender is static mixer.
Further, above-mentioned SNCR devices also include reducing agent supply equipment, and reducing agent supply equipment is connected with reactor,
And connector is arranged on blender upstream, preferably reducing agent supply equipment includes reducing agent injector, reducing agent injector with it is anti-
Device is answered to be connected.
Further, above-mentioned flue includes：First flue section, one end is connected with three wastes stove, the other end and reactant entrance
It is connected；Second flue section, one end is connected with product exit, and the other end is connected with flue gas post-processing unit, preferred reactor and the
One flue section and the section flange connection of the second flue.
Further, above-mentioned reactor is U-shaped reactor, and U-shaped reactor includes：Entrance, reactant entrance and connection
Mouth is arranged on entrance；U-shaped main body, one end is connected with one end of entrance, and blender is arranged on the close reaction of U-shaped main body
The side of thing entrance is set；Outlet section, product exit is arranged on outlet section.
Further, above-mentioned entrance and outlet section are the straight length being connected in the way of the diameter parallel with flue.
Further, above-mentioned flue gas post-processing unit includes fume dust remover, and fume dust remover is connected with flue.
According to another aspect of the present invention, there is provided a kind of denitration method for flue gas, the method for denitration includes：By the combustion of three wastes stove
Burning the flue gas for producing carries out SNCR treatment, obtains denitration flue gas, wherein, the flow rate that control carries out flue gas when SNCR is processed is low
In carrying out the flow rate of SNCR before processings.
Further, the recovery time in controlling above-mentioned SNCR to process is 1.5~2s, and the concentration of nitrogen oxides in effluent is
2000~3000mg/Nm3。
Further, reducing agent used in above-mentioned SNCR treatment is that mass concentration is 5%~10% urea liquid or ammonia
The aqueous solution, the flow velocity that reducing agent participates in reduction is 40~60m/s.
Further, reducing agent used in above-mentioned SNCR treatment is ammonia, reducing agent participate in the flow velocity of reduction for 60~
100m/s。
Further, above-mentioned flue gas is 5~15m/s, the preferably temperature of flue gas in the flow rate for carrying out SNCR before processings
It is 800~1050 DEG C.
Further, reducing agent and flue gas are mixed using static mixer in above-mentioned SNCR treatment.
Apply the technical scheme of the present invention, be improved by the reactor to SNCR devices, make it along flow of flue gas side
To reactor cross section product more than flue flue cross section accumulate, then be disposed at when on flue by flue conveying come flue gas
It is slack-off into flow velocity during sectional area larger reactor, and then cause reaction time phase of the flue gas in the reactor of SNCR devices
Reaction time before for improving in flue extends, you can to improve the hybrid reaction effect of flue gas and reducing agent to improve
Denitration rate.Above-mentioned transformation is carried out on existing structure in the prior art, therefore smaller to the transformation of equipment, and construction is simple, investment
It is relatively low, it is adaptable to large-scale commercial Application.
Brief description of the drawings
The Figure of description for constituting the part of the application is used for providing a further understanding of the present invention, of the invention to show
Meaning property and its illustrates, for explaining the present invention, not constitute inappropriate limitation of the present invention embodiment.In the accompanying drawings：
Fig. 1 shows the three wastes stove combustion system structural representation that a kind of preferred embodiment of the invention is provided.
Wherein, above-mentioned accompanying drawing is marked including the following drawings：
10th, three wastes stove；20th, flue；30th, SNCR devices；31st, reactor；32nd, blender；33rd, reducing agent supply equipment；
40th, flue gas post-processing unit.
Specific embodiment
It should be noted that in the case where not conflicting, the feature in embodiment and embodiment in the application can phase
Mutually combination.Describe the present invention in detail below with reference to the accompanying drawings and in conjunction with the embodiments.
Present inventor has found after being analyzed to the SNCR techniques applied in current three wastes stove, due to three wastes stove
When connection is used, its structure is compact, there are problems that the region area of the temperature range for being adapted to reaction is less, causes reduction
The residence time is too short in flue gas of the agent in suitable temperature window, so cause flue gas and reducing agent cannot be sufficiently mixed reaction cause
Decline denitration rate.Based on above-mentioned discovery this application provides a kind of three wastes stove combustion system and denitration method for flue gas.
In a kind of typical implementation method of the application, there is provided a kind of three wastes stove combustion system, as shown in figure 1, this three
Useless stove combustion system includes the three wastes stove 10 and flue gas post-processing unit 40 that are connected by flue 20, and the combustion system also includes
SNCR devices 30, SNCR devices 30 have reactor 31, and reactor 31 is arranged on flue 20, and reactor 31 along flue gas stream
The sectional area of reactor 31 in dynamic direction is accumulated more than the flue cross section of flue 20.
The application is improved by the reactor 31 to SNCR devices 30, makes it along the reactor 31 in flow of flue gas direction
Sectional area is accumulated more than the flue cross section of flue 20, then be disposed at conveying the flue gas for coming entrance by flue 20 when on flue 20
Flow velocity is slack-off during sectional area larger reactor 31, and then causes reaction time of the flue gas in the reactor 31 of SNCR devices 30
Extended relative to the reaction time before improving in flue, you can to improve the hybrid reaction effect of flue gas and reducing agent to carry
Denitration rate high.Above-mentioned transformation is carried out on existing structure in the prior art, therefore smaller to the transformation of equipment, and construction is simple, is thrown
Money is relatively low, it is adaptable to large-scale commercial Application.
In order that the above-mentioned reaction time is able to be obviously prolonged and ensure the treatment effeciency of flue gas, preferably above-mentioned reactor 31
Cross-sectional area is 2 times to 5 times of flue cross-sectional area.The denitration rate of flue gas continues to improve unobvious and can cause after more than 5 times
The treatment effeciency of flue gas declines.
Additionally, the reaction efficiency in order to improve flue gas and reducing agent, preferably above-mentioned reactor 31 is with heat insulation function
Reactor 31.So that flue gas be incubated and utilize flue gas temperature provide reduction reaction needed for high temperature.Above-mentioned heat insulation function can be with
Insulation material is set in the common periphery of reactor 31 and realizes insulation.
Additionally, in order to further extend the reaction time, preferably above-mentioned reactor 31 is U-shaped reactor, S types reactor or snake
Shaped reaction device.As shown in figure 1, the flow distance of flue gas can be extended using U-shaped reactor, S types reactor or snakelike reactor,
That is reaction time of stop distance of the extension flue gas in reactor 31, and then extension flue gas in reactor 31.
In a kind of preferred embodiment of the application, as shown in figure 1, above-mentioned reactor 31 has reactant entrance and product
Outlet, SNCR devices 30 also include blender 32, and blender 32 is arranged in reactor 31 and is set near reactant entrance.Will
Blender 32 is arranged on the flue gas that will can be mixed in reactor 31 and reducing agent is quickly reduced, and improves reduction efficiency.
Certainly, the blender 32 can also be arranged on flue 20, now need to further improve flue 20 to set mixing
Device 32, improves relative to the complexity that blender 32 is arranged on equipment in reactor 31.In order to improve mixed effect, preferably
Blender 32 is static mixer, more preferably star blender.The static mixer can be firm by way of welding
Admittedly it is fixed on the inwall of reactor 31.
In the application another kind preferred embodiment, as shown in figure 1, above-mentioned SNCR devices 30 are also supplied including reducing agent
Equipment 33, reducing agent supply equipment 33 is connected with reactor 31, and connector is arranged on the upstream of blender 32.Reducing agent is supplied
It is arranged at reactor 31 to be connected, can equally reduces the change of the original structure to flue 20, the three wastes stove of the application is burnt
System is easy to make and structure is relatively easy.The reducing agent feeding mechanism of the application is with reference to using SNCR conventional in the prior art
The reducing agent feeding mechanism of device 30 is set, and preferably reducing agent supply equipment 33 includes reducing agent injector, reducing agent injection
Device is connected with reactor 31.
If reducing agent uses urea liquid or ammonia solution, reducing agent supply equipment 33 to store and produce including reducing agent
Device, dilution device, air compressor machine, metering mixed allocation device and reducing agent injector, and each other according to existing SNCR
Technology is connected (not shown in figure 1) by pipeline and pump with reducing agent injector.If reducing agent uses anhydrous ammonia (i.e. ammonia),
Reducing agent supply equipment 33 includes the injection of ammonia holding vessel, dilution device, air purge set, metered dispensing unit and reducing agent
Device, each device is connected (not shown in figure 1) by pipeline and regulating valve with reducing agent injector.Above-mentioned reducing agent injector can be with
It is spray gun and nozzle.
For the further connected mode for simplifying reactor 31 and flue 20, preferably as shown in figure 1, above-mentioned flue 20 includes
First flue section and the second flue section, one end of the first flue section are connected with three wastes stove 10, and the other end is connected with reactant entrance；
Second flue section one end be connected with product exit, the other end is connected with flue gas post-processing unit 40, more preferably reactor 31 and
First flue section and the section flange connection of the second flue.
In order to ensure fluency and then guarantee flue gas and reducing agent that flue gas flows in flue 20 and the joining place of reactor 31
Mixing, preferably above-mentioned reactor 31 be U-shaped reactor, the U-shaped reactor include entrance, U-shaped main body and outlet section, reaction
Thing entrance and connector are arranged on entrance；U-shaped main body one end is connected with one end of entrance, and blender 32 is arranged on U-shaped
The side near reactant entrance of main body is set；Outlet section product exit is arranged on outlet section.In entrance by connection
Mouth introduces reducing agent so that reducing agent and flue gas flow together；Then the blender 32 for being set in U-shaped main body fills the two
Reduction reaction is carried out after dividing mixing, that is, ensure that the utilization rate and mixed effect of the two in turn ensure that reduction effect.
For the ease of installing, preferably above-mentioned entrance and outlet section are and are connected by the way of the diameter parallel of flue 20
Straight length.Certainly, it is also feasible entrance and outlet section to be set into the structure with chamfering with U-shaped main body junction.
Above-mentioned flue gas post-processing unit 40 can include fume dust remover, and fume dust remover is connected with flue 20.When
Other conventional devices can also so be included, be will not be repeated here.
In another typical implementation method of the application, there is provided a kind of denitration method for flue gas, the method for denitration includes
The flue gas that the burning of three wastes stove is produced is carried out into SNCR treatment, denitration flue gas is obtained, wherein, control carries out flue gas when SNCR is processed
Flow rate is less than and is carrying out the flow rate of SNCR before processings.
In currently available technology in SNCR processing procedures the flow rate of flue gas and SNCR before processings flow of flue gas speed
It is identical, and the application is less than by the flow rate that control carries out flue gas when SNCR is processed and is carrying out the flowing speed of SNCR before processings
Rate so that flue gas is extended before the reaction time is participated in relative to improvement during SNCR is processed, you can to improve flue gas and reducing agent
Hybrid reaction effect improving denitration rate.
Extend the time of SNCR treatment using the control of the flow rate to flue gas, preferably by control SNCR treatment
Recovery time is 1.5~2s, relative to the recovery time of 0.3~0.4s in the treatment of SNCR in the prior art, the 1.5 of the application
The recovery time of~2s has and is obviously prolonged, therefore, it is possible to significantly improve denitration rate.Wherein, nitrogen in flue gas in above-mentioned reduction process
The concentration of oxide and the consumption of reducing agent may be referred to prior art, excellent in order to better adapt to the recovery time of the application
Choose state nitrogen oxides in effluent concentration be 2000~3000mg/Nm3, the consumption of reducing agent used can be with SNCR treatment
Selected with reference to the regulation of prior art, will not be repeated here.
In the SNCR treatment of the application, the specifically used material of reducing agent may be referred to prior art, a kind of preferred
Embodiment in, in above-mentioned SNCR treatment reducing agent used for mass concentration be 5%~10% urea liquid or ammonia spirit,
The flow velocity that reducing agent participates in reduction is 40~60m/s.
When reducing agent is urea liquid, the chemical reaction in reduction process is as follows：
Urea is decomposed：
CO(NH2)2+H2O→2NH3+CO2
NH3Reacted with nitrogen oxides：
4NH3+4NO+O2→4N2+6H2O
8NH3+6NO2→7N2+12H2O
In the application another kind preferred embodiment, reducing agent used is ammonia, reducing agent in above-mentioned SNCR treatment
The flow velocity for participating in reduction is 60~100m/s.Above two reducing agent can realize preferable reduction effect, in addition, for difference
Reducing agent species, set the flow velocity that different reducing agents participate in reduction so that the reduction effect of reducing agent is more preferable.
When reducing agent is ammonia, the chemical reaction in reduction process is as follows：
4NH3+4NO+O2→4N2+6H2O
4NH3+2NO+2O2→3N2+6H2O
8NH3+6NO2→7N2+12H2O
In addition, on the premise of reduction effect is ensured, improving denitration efficiency, preferably above-mentioned flue gas is carrying out SNCR before processings
Flow rate be 5~15m/s.In addition, the temperature in order to ensure flue gas during reduction, is preferably carrying out SNCR before processings, flue gas
Temperature be 800~1050 DEG C.
Further, in order to improve the mixed effect of flue gas and reducing agent, using static mixed in preferably above-mentioned SNCR treatment
Clutch is mixed reducing agent and flue gas.
After denitration process are completed, desulfurization or dust removal process can also be carried out to the flue gas after denitration process.Wherein, specifically
Condition may be referred to prior art, will not be repeated here.
Below with reference to embodiment and comparative example, the beneficial effect of the application is further illustrated.
Embodiment 1
The denitration process of flue gas are carried out using the combustion system of three wastes stove 10 shown in Fig. 1, flue gas goes out from the flue gas of three wastes stove 10
Mouth is discharged into the flue 20 after three wastes stove 10, and the reducing agent injection apparatus on u shaped reaction device entrances are injected to flue gas
Reducing agent, reducing agent enters the U of u shaped reaction devices after star blender reaches the state of being thoroughly mixed after tentatively mixing with flue gas
Shape main body.After flue gas enters u shaped reaction devices, because cross-sectional area becomes big so that the flow velocity reduction of flue gas.Now flue-gas temperature
The NH that temperature window in suitable denitration reduction reaction, nitrogen oxides and reducing agent are produced3React generation water and nitrogen
Etc. pollution-free product.Flue gas after subsequent denitration carries out subsequent dust removal step into combined duster.
The cross-sectional area of above-mentioned reactor 31 is 4 times of the cross-sectional area of flue 20, and the recovery time in SNCR treatment is 1.8s,
Above-mentioned reducing agent is ammonia, and reductant nozzle exit velocity will be in about 80m/s, and the intake of reducing agent is according to NSCR reduction techniques
Specify the load according to boiler, the fluctuation of nitrous oxides concentration is adjusted.The flue gas flow rate flowed out by three wastes stove 10 will keep
In 10m/s, temperature will be maintained between 800~1050 DEG C.
Embodiment 2
Difference from Example 1 is that the cross-sectional area of above-mentioned reactor 31 is 5 times of the cross-sectional area of flue 20, SNCR
Recovery time in treatment is about 2s, and above-mentioned reducing agent is ammonia, and reductant nozzle exit velocity will be in about 60m/s, reducing agent
The intake load that specifies according to boiler according to NSCR reduction techniques, the fluctuation of nitrous oxides concentration is adjusted.By the three wastes
The flue gas flow rate of the outflow of stove 10 will be maintained at 15m/s, and temperature will be maintained between 800~1050 DEG C.
Embodiment 3
Difference from Example 1 is that the cross-sectional area of above-mentioned reactor 31 is 2 times of the cross-sectional area of flue 20, SNCR
Recovery time in treatment is 1.5s, and above-mentioned reducing agent is ammonia, and reductant nozzle exit velocity will be in about 100m/s, reducing agent
The intake load that specifies according to boiler according to NSCR reduction techniques, the fluctuation of nitrous oxides concentration is adjusted.By the three wastes
The flue gas flow rate of the outflow of stove 10 will be maintained at 5m/s, and temperature will be maintained between 800~1050 DEG C.
Embodiment 4
Difference from Example 1 is that the cross-sectional area of above-mentioned reactor 31 is 4 times of the cross-sectional area of flue 20, SNCR
Recovery time in treatment is 2s, and above-mentioned reducing agent is the urea liquid that concentration is 5%, and reductant nozzle exit velocity will be about
60m/s, the intake of reducing agent specifies the load according to boiler according to NSCR reduction techniques, and the fluctuation of nitrous oxides concentration is carried out
Adjustment.The flue gas flow rate flowed out by three wastes stove 10 will be maintained at 10m/s, and temperature will be maintained between 800~1050 DEG C.
Embodiment 5
Difference from Example 1 is that the cross-sectional area of above-mentioned reactor 31 is 5 times of the cross-sectional area of flue 20, SNCR
Recovery time in treatment is 2s, and above-mentioned reducing agent is the ammoniacal liquor that concentration is 10%, and reductant nozzle exit velocity will be about
60m/s, the intake of reducing agent specifies the load according to boiler according to NSCR reduction techniques, and the fluctuation of nitrous oxides concentration is carried out
Adjustment.The flue gas flow rate flowed out by three wastes stove 10 will be maintained at 15m/s, and temperature will be maintained between 800~1050 DEG C.
Embodiment 6
Difference from Example 1 is that the cross-sectional area of above-mentioned reactor 31 is 1.5 times of the cross-sectional area of flue 20,
Recovery time in SNCR treatment is 1.2s, and above-mentioned reducing agent is the ammoniacal liquor that concentration is 10%, and reductant nozzle exit velocity will
In about 50m/s, the intake of reducing agent specifies the load according to boiler, the fluctuation of nitrous oxides concentration according to NSCR reduction techniques
It is adjusted.The flue gas flow rate flowed out by three wastes stove 10 will be maintained at 10m/s, and temperature will be maintained between 800~1100 DEG C.
Comparative example 1
Reactor in three wastes stove combustion system shown in Fig. 1 is replaced with the flue diameter identical circle being connected with it
Cylindricality reactor (structure i.e. before the application improvement), carries out the denitration process of flue gas, and flue gas is exported from three wastes kiln gas and arranged
Go out enter three wastes stove after flue, reactor inlet section on reducing agent injection apparatus to flue gas inject reducing agent, reducing agent with
Into the U-shaped main body of u shaped reaction devices after star blender reaches the state of being thoroughly mixed after flue gas tentatively mixing.Flue gas enters
After u shaped reaction devices, the NH that nitrogen oxides and reducing agent are produced3React the pollution-free products such as generation water and nitrogen.It is then de-
Flue gas after nitre carries out subsequent dust removal step into combined duster.
Recovery time in SNCR treatment is 0.4s, and above-mentioned reducing agent is ammonia, and reductant nozzle exit velocity will be about
60m/s, the intake of reducing agent specifies the load according to boiler according to NSCR reduction techniques, and the fluctuation of nitrous oxides concentration is carried out
Adjustment.The flue gas flow rate flowed out by three wastes stove will be maintained at 10m/s, and temperature will be maintained between 800~1050 DEG C.
Comparative example 2
The structure of three wastes stove combustion system is identical with comparative example 1, and the recovery time in SNCR treatment is 0.3s, above-mentioned reduction
Agent is the urea liquid that concentration is 5%, and reductant nozzle exit velocity will be in about 60m/s, and the intake of reducing agent is according to NSCR
Reduction technique specifies the load according to boiler, and the fluctuation of nitrous oxides concentration is adjusted.The flue gas flow rate flowed out by three wastes stove
10m/s is maintained at, temperature will be maintained between 800~1050 DEG C.
Comparative example 3
The structure of three wastes stove combustion system is identical with comparative example 1, and the recovery time in SNCR treatment is 0.5s, above-mentioned reduction
Agent is the ammoniacal liquor that concentration is 10%, and reductant nozzle exit velocity will be reduced in about 60m/s, the intake of reducing agent according to NSCR
Technical stipulation is adjusted according to the load of boiler, the fluctuation of nitrous oxides concentration.The flue gas flow rate flowed out by three wastes stove will be protected
Hold in 15m/s, temperature will be maintained between 800~1050 DEG C.
Flue gas after the denitration of embodiment 1 to 6 and comparative example 1 to 3 is detected, detection method is infrared method or determines electricity
Position electrolysis, testing result is shown in Table 1.
Table 1
By embodiment 1 in table 1 and comparative example 1, the contrast of embodiment 4 and comparative example 2 and embodiment 5 and comparative example 3
It can be found that denitration rate to more than 75% can be lifted relative to former facility using the present invention.Meanwhile, the application is directed to original
The improvement that some three wastes stove combustion systems are carried out, therefore it is small to reach investment, transforms convenient purpose.
As can be seen from the above description, the above embodiments of the present invention realize following technique effect：
The application is improved by the reactor to SNCR devices, it is accumulated along the reactor cross section in flow of flue gas direction
Flue cross section more than flue is accumulated, then be disposed at larger into sectional area by the next flue gas of flue conveying when on flue
Flow velocity is slack-off during reactor, so cause reaction time of the flue gas in the reactor of SNCR devices relative to improve before in flue
In reaction time extend, you can improve denitration rate to improve the hybrid reaction effect of flue gas and reducing agent.
Above-mentioned transformation is carried out on existing structure in the prior art, therefore smaller to the transformation of equipment, and construction is simple, investment
It is relatively low, it is adaptable to large-scale commercial Application.
In currently available technology in SNCR processing procedures the flow rate of flue gas and SNCR before processings flow of flue gas speed
It is identical, and the application is less than by the flow rate that control carries out flue gas when SNCR is processed and is carrying out the flowing speed of SNCR before processings
Rate so that flue gas is extended before the reaction time is participated in relative to improvement during SNCR is processed, you can to improve flue gas and reducing agent
Hybrid reaction effect improving denitration rate.
The preferred embodiments of the present invention are the foregoing is only, is not intended to limit the invention, for the skill of this area
For art personnel, the present invention can have various modifications and variations.It is all within the spirit and principles in the present invention, made any repair
Change, equivalent, improvement etc., should be included within the scope of the present invention.
Claims (14)
1. a kind of three wastes stove combustion system, including the three wastes stove (10) and flue gas post-processing unit being connected by flue (20)
(40), it is characterised in that the combustion system also includes SNCR devices (30), and the SNCR devices (30) are with reactor
(31), the reactor (31) is arranged on the flue (20), and the reactor (31) along the flow of flue gas direction
Reactor (31) sectional area more than the flue (20) flue cross section accumulate.
2. three wastes stove combustion system according to claim 1, it is characterised in that reactor (31) cross-sectional area is institute
State flue cross-sectional area 2 times to 5 times.
3. three wastes stove combustion system according to claim 1, it is characterised in that the reactor (31) is with insulation work(
Can reactor (31), preferably described reactor (31) is U-shaped reactor, S types reactor or snakelike reactor.
4. three wastes stove combustion system according to claim 1, it is characterised in that the reactor (31) enters with reactant
Mouth and product exit, the SNCR devices (30) also include blender (32), and the blender (32) is arranged on the reactor
(31) set in and near the reactant entrance, preferably described blender (32) is static mixer.
5. three wastes stove combustion system according to claim 4, it is characterised in that the SNCR devices (30) also include reduction
Agent supply equipment (33), the reducing agent supply equipment (33) is connected with the reactor (31), and connector be arranged on it is described
Blender (32) upstream, preferably described reducing agent supply equipment (33) including reducing agent injector, the reducing agent injector with
The reactor (31) is connected.
6. three wastes stove combustion system according to claim 4, it is characterised in that the flue (20) includes：
First flue section, one end is connected with the three wastes stove (10), and the other end is connected with the reactant entrance；
Second flue section, one end is connected with the product exit, and the other end is connected with the flue gas post-processing unit (40),
It is preferred that the reactor (31) is connected with first flue section and second flue section flange.
7. three wastes stove combustion system according to claim 5, it is characterised in that the reactor (31) is U-shaped reactor,
The U-shaped reactor includes：
Entrance, the reactant entrance and the connector are arranged on the entrance；
U-shaped main body, one end is connected with one end of the entrance, and the blender (32) is arranged on being close to for the U-shaped main body
The side of the reactant entrance is set；
Outlet section, the product exit is arranged on the outlet section.
8. three wastes stove combustion system according to claim 7, it is characterised in that the entrance and the outlet section are
By the straight length being connected in the way of the diameter parallel of the flue (20).
9. three wastes stove combustion system according to claim 1, it is characterised in that the flue gas post-processing unit (40) includes
Fume dust remover, the fume dust remover is connected with the flue (20).
10. a kind of denitration method for flue gas, it is characterised in that the method for denitration includes：
The flue gas that the burning of three wastes stove is produced is carried out into SNCR treatment, denitration flue gas is obtained, wherein, control carries out the SNCR treatment
The flow rate of Shi Suoshu flue gases is less than and is carrying out the flow rate of the SNCR before processings.
11. method of denitration according to claim 10, it is characterised in that the recovery time in controlling the SNCR to process is
1.5~2s, the concentration of the nitrogen oxides in effluent is 2000~3000mg/Nm3。
12. method of denitration according to claim 10, it is characterised in that reducing agent used is matter in the SNCR treatment
Amount concentration is 5%~10% urea liquid or ammonia spirit, and the flow velocity that the reducing agent participates in reduction is 40~60m/s；Or
Reducing agent used is ammonia in the SNCR treatment, and the flow velocity that the reducing agent participates in reduction is 60~100m/s.
13. method of denitration according to claim 10, it is characterised in that the flue gas is carrying out the SNCR before processings
Flow rate is 5~15m/s, and the temperature of preferably described flue gas is 800~1050 DEG C.
14. method of denitration according to claim 10, it is characterised in that will using static mixer in the SNCR treatment
Reducing agent and the flue gas are mixed.
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108982278A (en) * | 2018-07-26 | 2018-12-11 | 山东大学 | A kind of coke breeze absorption sulfur dioxide/HCl method of evaluating performance based on air flow bed |
Citations (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US6245134B1 (en) * | 1998-04-15 | 2001-06-12 | Hera, Llc | Apparatus for testing systems designed for NOx reduction in the combustion of carbonaceous fuels |
| CN203540318U (en) * | 2013-07-25 | 2014-04-16 | 北京蒂本斯工程技术有限公司 | Oxidation reaction device |
| CN104056542A (en) * | 2014-06-09 | 2014-09-24 | 广西壮族自治区建筑材料科学研究设计院 | SNCR (selective non-catalytic reduction) denitration method and SNCR denitration device |
| CN204159203U (en) * | 2014-10-30 | 2015-02-18 | 临沂龙源节能技术有限公司 | A kind of flue gas denitrification system being exclusively used in three-waste fluidized mix combustion furnace |
| CN204582956U (en) * | 2014-12-28 | 2015-08-26 | 青岛惠城石化科技有限公司 | A kind of device reducing NOX discharge in FCC flue gas |
| CN204699585U (en) * | 2015-04-16 | 2015-10-14 | 江苏中金环保科技有限公司 | A kind of device removing coking nitrogen oxides in effluent |
| CN105854554A (en) * | 2016-04-27 | 2016-08-17 | 刘国庆 | Ozone low-temperature oxidation denitration technology and system |
| CN106139852A (en) * | 2016-08-29 | 2016-11-23 | 中国恩菲工程技术有限公司 | Benitration reactor |
-
2016
- 2016-12-21 CN CN201611192529.3A patent/CN106765244A/en active Pending
Patent Citations (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US6245134B1 (en) * | 1998-04-15 | 2001-06-12 | Hera, Llc | Apparatus for testing systems designed for NOx reduction in the combustion of carbonaceous fuels |
| CN203540318U (en) * | 2013-07-25 | 2014-04-16 | 北京蒂本斯工程技术有限公司 | Oxidation reaction device |
| CN104056542A (en) * | 2014-06-09 | 2014-09-24 | 广西壮族自治区建筑材料科学研究设计院 | SNCR (selective non-catalytic reduction) denitration method and SNCR denitration device |
| CN204159203U (en) * | 2014-10-30 | 2015-02-18 | 临沂龙源节能技术有限公司 | A kind of flue gas denitrification system being exclusively used in three-waste fluidized mix combustion furnace |
| CN204582956U (en) * | 2014-12-28 | 2015-08-26 | 青岛惠城石化科技有限公司 | A kind of device reducing NOX discharge in FCC flue gas |
| CN204699585U (en) * | 2015-04-16 | 2015-10-14 | 江苏中金环保科技有限公司 | A kind of device removing coking nitrogen oxides in effluent |
| CN105854554A (en) * | 2016-04-27 | 2016-08-17 | 刘国庆 | Ozone low-temperature oxidation denitration technology and system |
| CN106139852A (en) * | 2016-08-29 | 2016-11-23 | 中国恩菲工程技术有限公司 | Benitration reactor |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108982278A (en) * | 2018-07-26 | 2018-12-11 | 山东大学 | A kind of coke breeze absorption sulfur dioxide/HCl method of evaluating performance based on air flow bed |
| CN108982278B (en) * | 2018-07-26 | 2020-05-08 | 山东大学 | Evaluation method for sulfur dioxide/HCl adsorption performance of coke breeze based on entrained flow bed |
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