CN106110850A - A kind of flue gas pollutant minimum discharge system and method - Google Patents
A kind of flue gas pollutant minimum discharge system and method Download PDFInfo
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- CN106110850A CN106110850A CN201610664057.0A CN201610664057A CN106110850A CN 106110850 A CN106110850 A CN 106110850A CN 201610664057 A CN201610664057 A CN 201610664057A CN 106110850 A CN106110850 A CN 106110850A
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
- B01D53/75—Multi-step processes
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D46/00—Filters or filtering processes specially modified for separating dispersed particles from gases or vapours
- B01D46/02—Particle separators, e.g. dust precipitators, having hollow filters made of flexible material
- B01D46/023—Pockets filters, i.e. multiple bag filters mounted on a common frame
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/46—Removing components of defined structure
- B01D53/48—Sulfur compounds
- B01D53/50—Sulfur oxides
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/46—Removing components of defined structure
- B01D53/54—Nitrogen compounds
- B01D53/56—Nitrogen oxides
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2258/00—Sources of waste gases
- B01D2258/02—Other waste gases
- B01D2258/0283—Flue gases
Abstract
The invention discloses a kind of flue gas pollutant minimum discharge system, including desulfurizing tower, the two ends of UNICOM's pipeline are connected with desulfurizing tower and dedusting denitration compound reactor respectively；Described dedusting denitration compound reactor includes housing, arranges the dedusting denitration unit of at least two in housing；Described each dedusting denitration unit includes outer cylinder body and inner barrel, and inner barrel is sleeved in outer cylinder body, outer cylinder body, inner barrel sidewall on be respectively provided with passage；Between the medial wall and the lateral wall of inner barrel of outer cylinder body, catalyst is set；Outer surface at outer cylinder body is set with cloth bag, and cloth bag is for there being end uncovered.The present invention provides the processing method of the flue gas pollutant minimum discharge utilizing said system to carry out the most simultaneously.
Description
Technical field
The present invention relates to a kind of fire coal boiler fume pollutant removing system and method, specifically a kind of coal-burning boiler
Flue gas pollutant minimum discharge system and method, can realize dust in flue gas, SO2Minimum discharge with NOx controls.
Background technology
China is the country with coal as main energy sources, generates substantial amounts of atmosphere pollution (such as dust, SO in coal-fired process2
And NOx), this is the main cause causing China's current atmospheric to pollute, and health and ecological environment are caused serious danger
Evil.In recent years, China has put into substantial amounts of human and material resources, financial resources carry out the improvement of coal-fired flue-gas, but flue gas pollutant discharge
Radix is the biggest, and atmospheric pollution situation is continuous worsening.To this end, country is increasingly strict to coal-fired flue-gas discharge standard, up-to-date
" fossil-fuel power plant atmospheric pollutant emission standard " (GB13223-2011) the highest to thermal power plant's flue dust, sulfur dioxide and nitrogen oxides
Concentration of emission is allowed to make new regulation: flue dust, sulfur dioxide and nitrogen in the new power plant construction flue gas discharged from coal-fired boiler of key area
Emissions of oxides concentration must not distinguish higher than 20,50 and 100mg/m3.It addition, JIUYUE in 2014 12 days, National Development and Reform Commission person
Meeting, Environmental Protection Department, National Energy Board combine and issue " coal electricity energy-saving and emission-reduction upgrading and transformation action plan (2014-2020) "
(send out and change the energy (2014) 2093) (hereinafter referred to as " energy-saving and emission-reduction action plan "), it is desirable to accelerate to promote production of energy and consumption
Revolution, promotes coal electricity high-efficiency cleaning level of development further." energy-saving and emission-reduction action plan " require eastern region (Liaoning, Beijing,
11 provinces and cities such as Tianjin, Hebei, Shandong, Shanghai, Jiangsu, Zhejiang, Fujian, Guangdong, Hainan) newly-built Thermal generation unit atmospheric pollution
Thing concentration of emission basically reach gas turbine group emission limit (i.e. under the conditions of benchmark oxygen content 6%, flue dust, SO2, NOx emission
Concentration is respectively no higher than 10,35,50mg/Nm3), it is achieved the minimum discharge of coal unit controls.
Minimum discharge refers to that coal fired boiler of power plant, during generator operation, end treatment etc., uses multiple pollutant
Efficiently cooperation-removal technology Based on Integrate System so that it is Air Pollutant Emission concentration substantially conforms to Gas Generator Set emission limit.For
Dust Control, electrostatic precipitator technology, owing to efficiency of dust collection is high, technology maturation, is widely used in coal-burning power plant.But along with state
The family's further lifting to dust emission standard, electrostatic precipitation is for 10mg/Nm3It is relatively big that following dust emission controls difficulty,
Therefore it is imperative to transform original electrostatic precipitation.In recent years, the filtrate of sack cleaner, pulse jet technology etc. are no
Breaking and improve, the life-span of cloth bag is greatly improved, and dust settling pocket technique district tends to ripe.Bag-type dust, compared with electrostatic precipitation, has
There is higher efficiency of dust collection, 10mg/Nm can be met3Following dust emission standard, so the minimum discharge for dust controls,
Bag-type dust will have more advantage；For SO2Controlling, the coal-burning boiler of China mainly uses wet method limestone-gypsum method flue gas to take off
Sulfur.But for SO2Initial concentration is more than 2000mg/Nm3Coal-fired flue-gas, 35mg/Nm to be reached3SO2Discharge standard, original
Wet method limestone-gypsum method just have certain difficulty, so it must be carried out increase-volume renovation and improving.But, also have in some
Small scall coal-fired boiler originally used dry flue gas desulphurization technology, such as Circulating Fluidized Bed Flue Gas Desulfurization Technology.Dry method flue gas
It is difficult to meet minimum discharge requirement from the point of view of on desulfurization technology general significance, so the transformation of wet desulphurization must be carried out.But, have
A little enterprises are owing to being limited by each side factor such as place, fund, it is impossible to carry out wet desulphurization transformation.How to utilize former for this
Some dry desulfurization devices realize SO2Minimum discharge have become as one of difficult problem that a lot of middle-size and small-size steam power plant faces；For
The control of NOx, currently mainly uses SNCR and SCR technology.SNCR transformation is fast, invests little, in the less demanding feelings of denitration efficiency
It is worthy to be popularized under condition.SCR denitration is effective, can meet minimum discharge requirement, but place demand is big, investment and operating cost
Height, causes a lot of middle-size and small-size coal-burning power plant to undertake.Generally speaking, how on the basis of original flue gas pollutant cleaning system
On, develop new flue gas minimum discharge technology, it has also become China's coal-fired flue-gas administers the focus in field.
Device involved by current existing SCR technology is: SCR denitrating flue gas at boiler economizer by 300～400 DEG C
High-temperature flue gas draw, catalyst volume is relatively big, it is generally required to be separately provided SCR reactor, therefore floor space is bigger；In order to full
The temperature requirements of the commercial SCR catalyst of foot, SCR denitration generally uses high dirt high-sulfur to arrange, i.e. before denitration not through dedusting with
Desulfurization.So one side dust meeting covering catalyst surface, not only cause the minimizing of catalytic reaction surface but also the weight in dust
Metal may result in catalyst poisoning, greatly reduces the service life of catalyst；On the other hand, owing to not carrying out SO2Removing,
A small amount of SO in SCR course of reaction2It is oxidized to SO3, then pass through NH3+SO3=(NH4)2SO4Generate ammonium sulfate, cause catalyst
Surface attachment ammonium sulfate reduces catalyst activity, and corrodes follow-up air preheater and flue；It addition, existing SCR reaction unit
It is difficulty with flue gas uniformly through catalyst layer, causes catalyst to reduce service life.
Summary of the invention
The technical problem to be solved in the present invention is to provide a kind of process coal-fired flue-gas pollutant and reaches super low concentration
Exhaust system and method.
In order to solve above-mentioned technical problem, the present invention provides a kind of flue gas pollutant minimum discharge system, including desulfurizing tower,
The two ends of UNICOM's pipeline are connected with desulfurizing tower and dedusting denitration compound reactor respectively；
Described dedusting denitration compound reactor includes housing, arranges the dedusting denitration unit of at least two in housing；
Described each dedusting denitration unit includes outer cylinder body and inner barrel, and inner barrel is sleeved in outer cylinder body (inner barrel
The axial line of axial line and outer cylinder body coincides), described outer cylinder body, inner barrel have been end uncovered, at outer cylinder body, inner barrel
Passage it is respectively provided with on sidewall；
Between the medial wall and the lateral wall of inner barrel of outer cylinder body, catalyst is set；
Outer surface at outer cylinder body is set with cloth bag, and cloth bag is for there being end uncovered.
Improvement as the flue gas pollutant minimum discharge system of the present invention: outside 2 adjacent dedusting denitration unit
Arranging gas baffle between the top of cylinder, described gas baffle seals with the sidewall upper of outer cylinder body and is connected.
Further improvement as the flue gas pollutant minimum discharge system of the present invention:
Described cloth bag is to be resistant to the high temperature resistant cloth bag of 150～200 DEG C, and it is made up of materials such as PPS, PTFE, P84；
Described catalyst is the low-temperature SCR catalyst that can play catalysis activity at 150～200 DEG C.
Remarks illustrate: conventional sack cleaner, and generally the temperature of tolerance is at 100～150 DEG C；For SCR denitration, logical
Often use high temperature catalyst 300～400 DEG C.
Further improvement as the flue gas pollutant minimum discharge system of the present invention:
The duct lateral arrangement of SCR catalyst, duct is perpendicular to the axial line of outer cylinder body.
Further improvement as the flue gas pollutant minimum discharge system of the present invention:
Being provided with nozzle in UNICOM's pipeline, described nozzle includes fluid injector and gas nozzle.
Described fluid injector is used for spraying NaClO2Solution,
Described gas nozzle is used for spraying NH3Gas.
Further improvement as the flue gas pollutant minimum discharge system of the present invention:
Along the circulating direction of flue gas in UNICOM's pipeline, fluid injector is first set, then gas nozzle is set.
Further improvement as the flue gas pollutant minimum discharge system of the present invention:
Described fluid injector is two-fluid spray nozzle, thus carries out 2～3 grades of sprinklings.
Described gas nozzle is two-fluid spray nozzle, thus carries out 2～3 grades of injections.
Further improvement as the flue gas pollutant minimum discharge system of the present invention:
Described desulfurizing tower is circulating fluid bed flue-gas desulfurizing device, and desulfurizing agent is Ca (OH)2, control Ca/S=2's～3:1
Mol ratio, sweetening process does not carry out moisturizing.
The present invention provides the processing method of a kind of flue gas pollutant minimum discharge utilizing said system to carry out the most simultaneously,
Comprise the following steps:
1) in, the flue gas after desulfurizing tower desulfurization processes enters UNICOM's pipeline；
It is 5～10% that the first flue gas by fluid injector after the desulfurization flowing through UNICOM's pipeline processes sprays mass concentration
NaClO2Solution, NaClO2/(SO2+ NOx)=the mol ratio of 1～2:1；
Again by gas nozzle to flow through UNICOM's pipeline desulfurization process after flue gas injection NH3Gas, NH3/ NOx=1～
1.05:1 mol ratio；
2) the flue gas entrance dedusting denitration compound reactor, from UNICOM's pipeline discharged, flue gas ecto-entad moves, first exists
The outer surface of cloth bag realizes the trapping (efficiently trapping) of dust, and the air cloth ratio of employing is 0.8～0.9m/min；The most dustless cigarette
Gas is contacted with SCR catalyst by the passage on outer cylinder body sidewall, and gas transverse flows, and NO goes back after SCR catalytic reaction
Originally it was N2, the catalyst space velocities of employing is 4000～5000h-1；Flue gas after SCR catalyst processes is by inner barrel sidewall
Passage after enter the inner chamber (this inner chamber is hollow passage) of inner barrel, then flow out from the top of inner barrel, finally arrange
Enter chimney (that is, clean flue gas flows up outflow reaction unit).
Remarks illustrate: under conditions of catalyst reaction air speed refers to regulation, and unit interval per volume of catalyst processes
Gas flow, unit is m3/(m3Catalyst h), can be reduced to h-1。
In the present invention,
Desulfurizing tower is semi-dry desulphurization tower, i.e. desulfurizing tower is circulating fluid bed flue-gas desulfurizing device；Can refer to disclose
The patent " circular suspension type semi-dry fume purifier " delivered is prepared.But in the present invention, eliminate water replanishing device；
That is, the sweetening process of the present invention does not carry out moisturizing.
It is provided with cloth bag and catalyst in each dedusting denitration unit, thus defines Bag filter device and SCR catalysis is de-
Nitre device, the present invention is organically combined both above-mentioned.
In the present invention, below high temperature resistant (150 DEG C～the 200 DEG C) cloth bag being made up of materials such as PPS, PTFE, P84 meets
Condition: (1) efficiency of dust collection is high, and typically more than 99%, can reach the dust content of gas at house outlet is 5mg/m3
Hereinafter, the fine dust to submicron particle diameter has higher grade dust-collection efficiency；(2) insensitive to Dust Characteristics, not by dust ratio
The impact of resistance；(3) can stable operation at a temperature of 160～200 DEG C, when select high-performance filtrate time, some heatproof up to
To 260 DEG C；(4) when for desulphurization system, desulfuration efficiency can be properly increased.
Its work process is as follows:
The first preliminary desulfurization in desulfurizing tower of former flue gas；It is then sprayed into NaClO2Rear reinforcing desulfuration also realizes preliminary denitration；
Finally, flue gas removing dust denitration compound reactor processes, it is achieved dust and the efficient removal of NOx；
The present invention, including the semi-dry desulphurization tower processed flue gas for the first time, NaClO2Reinforcing desulfuration section, NH3Spray into
Section, and dedusting denitration compound reactor.The present invention is suitable for the transformation of original semi-dry flue gas desulfurization device, is not changing cigarette
In the case of gas purification facility overall structure, increase NaClO2Reinforcing desulfuration device, use novel dedusting denitration multiple simultaneously
Close reactor and transform original sack cleaner, realize SO in the dry state2, NOx and the efficient removal of dust, flue gas is taken off
The development of sulfur system proposes new thinking.
The desulfurizing tower of the present invention: use Circulating Fluidized Bed Flue Gas Desulfurization Technology, utilize Ca (OH)2Directly absorb, calcium
Sulfur is than Ca/S=2～3:1.In order to not reduce flue-gas temperature, sweetening process does not carry out extra moisturizing.Generally in sweetening process
A large amount of moisturizings contribute to SO2Absorption, but in tower can be caused simultaneously smoke moisture increase, cause the knot wall blocking etc. of Desulphurization
Problem.And along with water spray process, flue-gas temperature can decline to a great extent, and does not reaches the temperature required by follow-up SCR denitration；So this
Invention sweetening process does not carry out moisturizing.
The NaClO of the present invention2Reinforcing desulfuration section: former flue gas is SO after semi-dry desulphurization tower processes2Clearance can reach
70～80%, two-fluid spray nozzle is set connecting dry desulfurizing tower outlet, sprays into the NaClO of 5～10%2Solution, by SO2Oxidation
Become SO3, then with the Ca (OH) that reacts the most completely in flue2Occur to neutralize reaction, thus reach the purpose of reinforcing desulfuration, its reaction
Mechanism be: ClO2 -+2SO2+2H2O→2H2SO4+Cl-；Ca(OH)2+H2SO4=CaSO4+2H2O.NaClO simultaneously2Addition can
Promote the oxidation of NO, generate NO2, react 2NO+ClO2 -=2NO2+Cl-Or 2NO+ClO2 -=NO2+ClO-。NO2Also may be used
The Ca (OH) reacted the most completely2Partially absorb, thus realize the preliminary removing of NOx.NaClO2Addition be preferably
NaClO2/(SO2+ NOx) (mol ratio)=1～2.The NO simultaneously generated2In follow-up SCR course of reaction, response speed is faster, de-
Nitre effect is more preferable.
The present invention sprays into NH3Section: spray into NH in the pipeline before flue gas enters dedusting denitration compound reactor3Gas,
Use 2～3 grades of two-fluid spray nozzles, wherein NH3/ NOx=1～1.05.The NH sprayed into3The reducing agent reacted as follow-up SCR, can
So that NOx remaining in flue gas is reduced to nitrogen.Additionally spray ammonia can promote SO further2Absorption, generate sulfur ammonium.And generate
Sulfur ammonium efficiently can be trapped together with Desulphurization on cloth bag surface, thus avoid in conventional scr course of reaction sulfur ammonium and generate
It is attached to catalyst surface, the problem affecting catalyst activity.
This dedusting denitrification apparatus has the advantage that
(1) structure is relatively easy, and available original sack cleaner is transformed, it is not necessary to special SCR reactor, de-
Nitre assembly of devices originally can decline to a great extent.It is particularly well-suited to the denitration transformation of existing power plant.
(2), after being positioned at desulfurization and dust arrester due to it, therefore flue gas has the characteristic of low dirt, low-sulfur, solves and urges
The problems such as the blocking of agent, abrasion, the generation of sulfur ammonium, catalyst chemical poisoning, are greatly improved catalyst activity and prolongation are urged
The service life of agent.
(3) alleviate the trace element such as K, Na, Ca, As in flying dust to the pollution of catalyst or poisoning, be greatly improved catalysis
Agent activity.
A kind of concentration of flue gas pollutants minimum discharge system and method for the present invention compared with the prior art, has following
Beneficial effect:
(1) present invention can realize dust, SO simultaneously2With the efficient removal of NOx, reach minimum discharge requirement (dust <
5mg/Nm3, SO2<35mg/Nm3, NOx < 50mg/Nm3), can be that traditional FGD provides new approaches and methods.
(2) bag-type dust is combined with SCR denitration, can transform on the basis of original sack cleaner, significantly subtract
Few SCR reactor floor space, reduces cost of investment.
(3) can without sulfur, dustless in the case of carry out SCR denitration, improve completely run at present SCR reactor height dirt,
The problem of high-sulfur, alleviates the poisoning problem of catalyst significantly, extends the life-span of catalyst.
(4) preposition NaClO2Injection, is possible not only to reinforcing desulfuration, and can promote the oxidation of NO, thus realize follow-up
Quick SCR reaction, improve denitration effect.
Accompanying drawing explanation
Below in conjunction with the accompanying drawings the detailed description of the invention of the present invention is described in further detail.
Fig. 1 is the schematic flow sheet of a kind of flue gas pollutant minimum discharge system of the present invention；
Fig. 2 is the structural representation of a dedusting denitration unit in the dedusting denitration compound reactor 2 in Fig. 1.
Detailed description of the invention
Below in conjunction with specific embodiment, the present invention is described further, but protection scope of the present invention is not limited in
This.
Embodiment 1, a kind of flue gas pollutant minimum discharge system, including desulfurizing tower 1, dedusting denitration compound reactor 2, connection
Siphunculus road 3；The two ends of UNICOM's pipeline 3 are connected with desulfurizing tower 1 and dedusting denitration compound reactor 2 respectively；Dedusting denitration is combined
The outlet of reactor 2 is connected with chimney.Desulfurizing tower 1 is circulating fluid bed flue-gas desulfurizing device.
Dedusting denitration compound reactor 2 includes housing 20, arranges multiple dedusting denitration unit (such as, in housing 20
It is illustrated in figure 14 dedusting denitration unit), the quantity of dedusting denitration unit can configure according to exhaust gas volumn and dust concentration.
Each dedusting denitration unit includes outer cylinder body 22 and inner barrel 21, and inner barrel 21 is sleeved in outer cylinder body 22, and interior
The axial line of cylinder 21 coincides with the axial line of outer cylinder body 22, and outer cylinder body 22, inner barrel 21 have been end uncovered, inner barrel 21
The bottom of bottom and outer cylinder body 22 be fixedly linked；Outer cylinder body 22, inner barrel 21 sidewall on be respectively provided with passage (passage
Aperture be 4～5mm).Catalyst 23 is set between the lateral wall of the medial wall of outer cylinder body 22 and inner barrel 21, i.e.
Catalyst filling 23 in the gap of outer cylinder body 22 and inner barrel 21, the gap between outer cylinder body 22 and inner barrel 21 determines catalysis
The loading of agent 23, can require to be designed according to denitration.Catalyst 23 is the SCR catalyst (150～200 DEG C) of low temperature, SCR
The duct lateral arrangement of catalyst, i.e. be perpendicular to the axial line of outer cylinder body 22.
Outer surface at outer cylinder body 22 is set with cloth bag 24.Top at the outer cylinder body 22 of 2 adjacent dedusting denitration unit
Between gas baffle 25 is set, described gas baffle 25 seals with the sidewall upper of outer cylinder body 22 and is connected.
Outer cylinder body 22 and inner barrel 21 are all made of stainless steel.Outer cylinder body 22 is as the skeleton of cloth bag 24 and catalyst 23
Supporter.
Described cloth bag 23 is high temperature resistant cloth bag (150～200 DEG C), and it is made up of materials such as PPS, PTFE, P84；
Being provided with nozzle in UNICOM's pipeline 3, nozzle includes fluid injector and gas nozzle, and fluid injector is used for spraying
NaClO2Solution, described gas nozzle is used for spraying NH3Gas.In UNICOM's pipeline 3, the circulating direction of gas, first arranges liquid
Body nozzle, then gas nozzle is set；That is, fluid injector is near the entrance point of UNICOM's pipeline 3, and gas nozzle is near UNICOM's pipeline 3
The port of export.Fluid injector is two-fluid spray nozzle, thus carries out 2～3 grades of sprinklings.Gas nozzle is two-fluid spray nozzle, thus enters
Row 2～3 grades of injections.
Utilize the processing method of a kind of flue gas pollutant minimum discharge that said apparatus carries out, follow the steps below successively:
1), desulfurizing tower 1 use circulating fluid bed flue-gas desulfurizing mode, directly use Ca (OH)2Absorbent, controls Ca/S=
The mol ratio of 2～3:1, sweetening process does not carry out moisturizing.Ca(OH)2Be particle diameter be the granule of 200～300 mesh.
S (that is, SO2) mole passes through raw flue gas concentration and volume measures and obtains.
Flue gas after desulfurizing tower 1 desulfurization processes enters in UNICOM's pipeline 3；
It is 5～10% that fluid injector flue gas after the desulfurization flowing through UNICOM's pipeline 3 processes sprays mass concentration
NaClO2Solution, NaClO2/SO2The mol ratio of+NOx=1～2:1；
Gas nozzle flue gas injection NH after the desulfurization flowing through UNICOM's pipeline 3 processes3Gas, NH3/ NOx=1～1.05:
The mol ratio of 1.
Remarks illustrate: need the flue gas after desulfurizing tower 1 desulfurization processes is carried out SO2, the concentration of NOx and exhaust gas volumn
Measure.
2), the flue gas discharged from UNICOM's pipeline 3 enters dedusting denitration compound reactor 2, relative to each dedusting denitration list
For unit, flue gas ecto-entad transverse movement, the first outer surface at cloth bag 24 realize the efficiently trapping of dust (dust are intercepted
Outer surface at cloth bag, it is achieved the efficient removal of dust), the air cloth ratio of employing is 0.8～0.9m/min；The most dustless flue gas
Being contacted with SCR catalyst by the passage on outer cylinder body 22 sidewall, NO is reduced to N after SCR catalytic reaction2, employing
Catalyst space velocities is 4000～5000h-1.After flue gas after SCR catalyst processes is by the passage on inner barrel 21 sidewall
Entering the inner chamber of inner barrel 21, then flow out from the top of inner barrel 21, (that is, clean flue gas is to upstream to be ultimately discharged into chimney
Dynamic outflow reaction unit).
The parameters test 1, arranging in apparatus and method described in embodiment 1 is: in demonstration project is tested, at flue gas
Reason amount 1000Nm3/ h, dust initial concentration 30g/Nm3, SO2Initial concentration 1000mg/Nm3, NO concentration 500mg/Nm3, flue gas temperature
Spend 170～180 DEG C, calcium sulfur ratio (Ca/S) 2, NaClO2/(SO2+ NOx)=1:1, NH3/ NOx=1:1, the air cloth ratio of employing is
0.9m/min, the catalyst space velocities of employing is 5000h-1。
Flue gas after original flue gas (that is, entering the flue gas before desulfurizing tower 1) and process is (that is, when being ultimately discharged into chimney
Flue gas) in the contrast of content of various compositions as shown in table 1 below:
Table 1
| Before process | After process | |
| Exhaust gas volumn Nm3/h | 1000 | 1000 |
| Flue-gas temperature DEG C | 170～180 | 160～170 |
| Dust concentration | 30g/Nm3 | 3～5mg/Nm3 |
| SO2 concentration mg/Nm3 | 1000 | 23～25 |
| NOx concentration mg/Nm3 | 500 | 43～48 |
Contrast experiment 1, " the injection NaClO cancelled in experiment 12Solution ", remaining is equal to test 1.Acquired results such as table 2
Shown in.
Table 2
| Before process | After process | |
| Exhaust gas volumn Nm3/h | 1000 | 1000 |
| Flue-gas temperature DEG C | 170～180 | 170～180 |
| Dust concentration | 30g/Nm3 | 3～5mg/Nm3 |
| SO2 concentration mg/Nm3 | 1000 | 58～71 |
| NOx concentration mg/Nm3 | 500 | 73～84 |
Contrast experiment 2, make the dedusting denitration compound reactor 2 in embodiment 1 into following structure: the left side of housing 20 is
The import of flue gas, the right side of housing 20 is the outlet of flue gas, arranges SCR catalyst in housing 20, and the duct of SCR catalyst is horizontal
To layout, and SCR catalyst covers the longitudinal cross-section of whole housing 20.That is, remove cloth bag, make the SCR reactor of routine into.
The consumption of SCR catalyst is with experiment 1.
Remaining is equal to test 1.Acquired results is as shown in table 3.
Table 3
| Before process | After process | |
| Exhaust gas volumn Nm3/h | 1000 | 1000 |
| Flue-gas temperature DEG C | 170～180 | 170～180 |
| SO2 concentration mg/Nm3 | 1000 | 58～71 |
| NOx concentration mg/Nm3 | 500 | 154～166 |
Contrast experiment 3, make the dedusting denitration compound reactor 2 in embodiment 1 into following structure: the left side of housing 20 is
The import of flue gas, the right side of housing 20 is the outlet of flue gas, arranges SCR catalyst in housing 20, and the duct of SCR catalyst is horizontal
To layout, and SCR catalyst covers the longitudinal cross-section of whole housing 20.It was provided for trapping dust before the import department of flue gas
Sack cleaner.SCR catalyst and consumption thereof are all with experiment 1.The material of sack cleaner and air cloth ratio are all with experiment 1.Institute
Obtain result as shown in table 4.
Table 4
| Before process | After process | |
| Exhaust gas volumn Nm3/h | 1000 | 1000 |
| Flue-gas temperature DEG C | 170～180 | 170～180 |
| SO2 concentration mg/Nm3 | 1000 | 36～42 |
| NOx concentration mg/Nm3 | 500 | 102～115 |
Finally, in addition it is also necessary to be only several specific embodiments of the present invention it is noted that listed above.Obviously, this
Bright it is not limited to above example, it is also possible to have many deformation.Those of ordinary skill in the art can be from present disclosure
The all deformation directly derived or associate, are all considered as protection scope of the present invention.
Claims (9)
1. a flue gas pollutant minimum discharge system, including desulfurizing tower (1), is characterized in that: the two ends of UNICOM's pipeline (3) are respectively
It is connected with desulfurizing tower (1) and dedusting denitration compound reactor (2)；
Described dedusting denitration compound reactor (2) includes housing (20), arranges the dedusting denitration of at least two in housing (20)
Unit；
Described each dedusting denitration unit includes outer cylinder body (22) and inner barrel (21), and inner barrel (21) is sleeved on outer cylinder body (22)
In, described outer cylinder body (22), inner barrel (21) have been end uncovered, outer cylinder body (22), inner barrel (21) sidewall on be all provided with
Put passage；
Catalyst (23) is set between the lateral wall of the medial wall of outer cylinder body (22) and inner barrel (21)；
Outer surface at outer cylinder body (22) is set with cloth bag (24), and cloth bag is for there being end uncovered.
A kind of flue gas pollutant minimum discharge system the most according to claim 1, is characterized in that: 2 adjacent dedustings
Gas baffle (25), described gas baffle (25) and outer cylinder body (22) are set between the top of the outer cylinder body (22) of denitration unit
Sidewall upper seals and is connected.
A kind of flue gas pollutant minimum discharge system the most according to claim 1 and 2, is characterized in that:
Described cloth bag (23) is to be resistant to the high temperature resistant cloth bag of 150～200 DEG C；
Described catalyst (23) is the low-temperature SCR catalyst that can play catalysis activity at 150～200 DEG C.
A kind of flue gas pollutant minimum discharge system the most according to claim 3, is characterized in that:
The duct lateral arrangement of SCR catalyst, described duct is perpendicular to the axial line of outer cylinder body (22).
A kind of flue gas pollutant minimum discharge system the most according to claim 4, is characterized in that:
Being provided with nozzle in UNICOM's pipeline (3), described nozzle includes fluid injector and gas nozzle；
Described fluid injector is used for spraying NaClO2Solution,
Described gas nozzle is used for spraying NH3Gas.
A kind of flue gas pollutant minimum discharge system the most according to claim 5, is characterized in that:
Along the circulating direction of flue gas in UNICOM's pipeline (3), fluid injector is first set, then gas nozzle is set.
A kind of flue gas pollutant minimum discharge system the most according to claim 6, is characterized in that:
Described fluid injector is two-fluid spray nozzle, thus carries out 2～3 grades of sprinklings；
Described gas nozzle is two-fluid spray nozzle, thus carries out 2～3 grades of injections.
A kind of flue gas pollutant minimum discharge system the most according to claim 1, is characterized in that:
Described desulfurizing tower (1) is circulating fluid bed flue-gas desulfurizing device, and desulfurizing agent is Ca (OH)2, control rubbing of Ca/S=2～3:1
That ratio, sweetening process does not carry out moisturizing.
9. a processing method for flue gas pollutant minimum discharge, is characterized in that comprising the following steps:
1) in, the flue gas after desulfurizing tower (1) desulfurization processes enters UNICOM's pipeline (3)；
It is 5～10% that the first flue gas by fluid injector after the desulfurization flowing through UNICOM's pipeline (3) processes sprays mass concentration
NaClO2Solution, NaClO2/(SO2+ NOx)=the mol ratio of 1～2:1；
Again by gas nozzle to flow through UNICOM's pipeline (3) desulfurization process after flue gas injection NH3Gas, NH3/ NOx=1～
1.05:1 mol ratio；
2) flue gas entrance dedusting denitration compound reactor (2), from UNICOM's pipeline (3) discharged, flue gas ecto-entad moves, first
Outer surface at cloth bag (24) realizes the trapping of dust, and the air cloth ratio of employing is 0.8～0.9m/min；The most dustless flue gas leads to
The passage crossed on outer cylinder body (22) sidewall contacts with SCR catalyst, and gas transverse flows, and NO goes back after SCR catalytic reaction
Originally it was N2, catalyst space velocities is 4000～5000h-1；Flue gas after SCR catalyst processes is by inner barrel (21) sidewall
Enter the inner chamber of inner barrel (21) after passage, then flow out from the top of inner barrel (21), be ultimately discharged into chimney.
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