CN209188514U - One kind being based on ammonia process-SCR combined desulfurization and denitration system - Google Patents
One kind being based on ammonia process-SCR combined desulfurization and denitration system Download PDFInfo
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- CN209188514U CN209188514U CN201822037971.XU CN201822037971U CN209188514U CN 209188514 U CN209188514 U CN 209188514U CN 201822037971 U CN201822037971 U CN 201822037971U CN 209188514 U CN209188514 U CN 209188514U
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- flue gas
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Abstract
One kind of the utility model is based on ammonia process-SCR combined desulfurization and denitration system, is related to sintered pollutant technical field of emission reduction.The utility model includes flue collector, ammonia process desulfuration tower, ring cold machine, ring cold heat exchanger and Benitration reactor；Flue collector is connected with ammonia process desulfuration tower, and ammonia process desulfuration tower, ring cold heat exchanger are connected with Benitration reactor；The flue gas of ring cold machine is connected to ring cold heat exchanger, and ring cold flue gas carries out heat exchange heating to sintering flue gas by ring cold heat exchanger.The utility model makes the sintering flue gas temperature after heat exchange reach denitration reaction temperature required for subsequent Benitration reactor, and the ammonia process of desulfurization is rationally cooperated with Benitration reactor, and then realizes SO in sintering flue gas2With NOxInexpensive joint emission reduction, while it is white to realize effectively taking off for discharge flue gas.
Description
Technical field
The utility model relates to sintered pollutant technical field of emission reduction, are based on ammonia process-SCR more specifically to one kind
Combined desulfurization and denitration system.
Background technique
NOx is one of current Air Pollutants, in an atmosphere NOx acid rain easy to form and photochemical fog, is influenced
It ecological environment and is detrimental to health, and steel industry NOx emission status is especially severe.According to statistics, steel industry NOx gas
Discharge amount accounts for 10% or so of industrial total release, and wherein sintering process is one of the main source for generating NOx, accounts for NOx row
Put 50% or so of total amount.Agglomeration for iron mine process energy consumption is mainly the consumption of the fossil fuels such as solid fuel coke powder, anthracite, about
The 75~80% of process total energy consumption are accounted for, and 90% or more the NOx of sintering process discharge is transformed by the nitrogen in fuel.
NOx emission new standard specified on January 1st, 2015 " steel sintering, pelletizing industrial air pollution object discharge standard " is existing
Enterprise comes into effect, and sintering process is faced with huge NOx abatement pressure.
Sintering flue gas NO at presentxEmission-reduction technology mainly includes that activated coke method, oxidizing process denitration and selective catalytic reduction are de-
Nitre (SCR), activated coke method remove the multiple pollutant in sintering flue gas by using activated coke, but its cost compared with
Height, enterprise are difficult to undertake；Oxidizing process denitration realizes denitration purpose by oxidizing NO, and using existing wet desulphurization, but
It is that still immature and its energy consumption is excessively high at present, denitration efficiency is relatively low for this method；And SCR denitration technology denitration efficiency is high, and
Relative low price is used by domestic many enterprises, but sintering process SCR limitation is at present: SCR denitration technology
Required temperature is difficult to match with sintering flue gas temperature, and the operating temperature section of SCR denitration technology is about 200~300 DEG C,
And sintering flue gas temperature is generally 130~150 DEG C, which is far not achieved the operating temperature of SCR denitration technology, so general burn
Knot factory can first heat up sintering flue gas frequently by heating methods such as electric heating, then flue gas is carried out SCR denitration, although which
Effective denitration of sintering flue gas may be implemented, but the mode that flue gas individually heats undoubtedly considerably increases emission reduction cost, violates
The original intention of energy-saving and emission-reduction.
And SCR denitration technology also has certain requirement for the flue gas of processing, needs the SO in sintering flue gas2Only
Change to lower concentration, avoids SO2Catalytic-reduction denitrified process is had adverse effect on, so sintering flue gas SCR is de- at present
Can all there be the step of desulfurization before nitre.Nowadays the mode of desulfurization mainly has dry method/semidry method desulphurization and wet desulphurization, dry method/half
Dry desulfurization principle mainly by quick lime or the emulsus desulfurizing agent being configured to lime water, carries out flue gas countercurrently or suitable
Stream spray carries out desulfurization, and emission reduction efficiency is lower, and can generate a large amount of solid waste；Wet desulphurization is mainly by passing through flue gas
Equal alkaline solutions containing ammonia carry out washing and realize desulfurization, and desulfurization effect is higher, and desulfuration byproduct generated has
Wide purposes；But the smoke temperature drop after wet desulphurization is larger, can generally be reduced by the flue-gas temperature after wet desulphurization
To 70 DEG C or so, so much sintering enterprise cooperates the subsequent SCR denitration link of desulfurization, Zhi Nengwu to reduce denitration cost
How the poor dry method/semidry method desulphurization technology of selective sweetening effect carries out desulfurization, how to be achieved at low cost wet desulphurization with
SCR denitration technology preferably combines, and is the problem of current this field urgent need to resolve.
In addition, sintering circular-cooler flue gas has certain heat, wind-warm syndrome can reach 500 DEG C or so, but burn at present
Knot ring cold flue gas is chiefly used in cogeneration, and generating efficiency is lower, with the development of low-temperature cogeneration technology in recent years, hair
Electrical efficiency increases, but still lower on the whole, at present only using the generating efficiency of low-temperature cogeneration technology ring cold flue gas
30% or so can be reached.And device for generating power by waste heat needs to put into a large amount of manpower financial capacities.
Currently, having there is related researcher to study exchanging heat before sintering flue gas SCR denitration, such as
CN2012105337633, CN201310459262.X and CN201710369398.X, all proposing in above-mentioned several patent documents will
Sintering flue gas exchanges heat with uncooled sinter, to realize the heating of sintering flue gas, is conducive to subsequent SCR denitration link
Progress sintering flue gas is directly passed through sinter although technical solution is all conducive to SCR denitration in above-mentioned patent document
It will cause the residual and enrichment of pollutant in sintering mineral products in product to a certain extent.
Utility model content
1. utility model technical problems to be solved
The purpose of this utility model is that: for agglomeration for iron mine denitrating flue gas higher cost or efficiency are lower in the prior art
The problem of, one kind is provided based on ammonia process-SCR combined desulfurization and denitration system, by ammonia process desulfuration tower and Benitration reactor
Between mounting ring cold heat exchanger, and ring cold machine flue gas is connected to ring cold heat exchanger, so that the sintering flue gas after the ammonia process of desulfurization
Heating, carries out denitration with realizing sintering flue gas low-cost high-efficiency.
2. technical solution
In order to achieve the above objectives, technical solution provided by the utility model are as follows:
One kind of the utility model is based on ammonia process-SCR combined desulfurization and denitration system, including flue collector, ammonia process desulfuration tower, ring
Cold, ring cold heat exchanger and Benitration reactor；Flue collector is connected by pipeline with the desulfurization entrance of ammonia process desulfuration tower, and ammonia process is de-
The desulfurization outlet of sulphur tower is connected by pipeline with the denitration entrance of Benitration reactor, between ammonia process desulfuration tower and Benitration reactor
Pipeline on ring cold heat exchanger is installed；The exhanst gas outlet of ring cold machine is connected by heat supply pipeline with ring cold heat exchanger, and ring is cold
Flue gas carries out heat exchange heating to sintering flue gas by ring cold heat exchanger.
Preferably, heat supply pipeline is connected with cold one section of the exhanst gas outlet of ring, and cold one section of the flue gas of ring passes through heat supply pipeline
Into ring cold heat exchanger；And/or heat supply pipeline is connected with cold two sections of the exhanst gas outlet of ring, cold two sections of the flue gas of ring passes through heat supply
Pipeline enters ring cold heat exchanger.
Preferably, deduster is provided on the pipeline between flue collector and ammonia process desulfuration tower.
Preferably, it is provided with tail gas heat exchanger on pipeline between ammonia process desulfuration tower and ring cold heat exchanger, Benitration reactor
Denitration outlet is connected by pipeline with tail gas heat exchanger, and tail gas carries out heat exchange heating to sintering flue gas by tail gas heat exchanger.
Preferably, Benitration reactor is SCR denitration reaction device.
Preferably, ammonia process of desulfurization tower bottom is provided with desulfurization entrance, and ammonia process of desulfurization top of tower is provided with desulfurization outlet, desulfurization
Spray tube is provided in ammonia process desulfuration tower between entrance and desulfurization outlet, spray tube sprays the side's of being directed downward setting；Spray tube
It is connected with the ammonia tank of peripheral hardware.
Preferably, deduster is electric precipitator.
Preferably, the catalyst containing vanadium and/or tungsten and/or titanium and/or molybdenum is provided in SCR denitration reaction device.
Preferably, it is provided with the first exhaust fan on the pipeline between ammonia process desulfuration tower and flue collector, which will
Sintering flue gas is pumped into ammonia process desulfuration tower.
One kind of the utility model is based on the cold heat exchange Ore Sintering Process flue gas processing method of ring, and sintering flue gas is by flue collector
It is introduced into ammonia process desulfuration tower to carry out desulfurization, carry out heat exchange heating in ring cold heat exchanger, and carries out denitration in Benitration reactor.
3. beneficial effect
Using technical solution provided by the utility model, compared with existing well-known technique, there is following remarkable result:
(1) one kind of the utility model is based on ammonia process-SCR combined desulfurization and denitration system, including flue collector, the ammonia process of desulfurization
Tower, ring cold machine, ring cold heat exchanger and Benitration reactor；Flue collector is connected with the desulfurization entrance of ammonia process desulfuration tower, the ammonia process of desulfurization
Tower is connected with Benitration reactor, and ring cold heat exchanger is equipped between ammonia process desulfuration tower and Benitration reactor；The flue gas of ring cold machine
It is connected to ring cold heat exchanger, ring cold flue gas carries out heat exchange heating to sintering flue gas by ring cold heat exchanger；Sintering flue gas passes through ammonia
After method desulfurizing tower desulfurization is cooling, ring cold flue gas is subjected to heat exchange heating to the sintering flue gas after desulfurization by ring cold heat exchanger, is made
Sintering flue gas temperature after must exchanging heat reaches denitration reaction temperature required for subsequent Benitration reactor, thus the ammonia process of desulfurization and de-
Nitre reactor can rationally cooperate, and then realize SO in sintering flue gas2With NOxInexpensive joint emission reduction, while realizing ring cold smoke
The reasonable utilization of gas heat, and it is white to realize effectively taking off for discharge flue gas.
(2) one kind of the utility model is based on ammonia process-SCR combined desulfurization and denitration system, is passing through ring using ring cold flue gas
On the basis of cold heat exchanger carries out heat exchange heating to sintering flue gas, the cold one section of ring cold flue gas of ring is more specifically passed through into heat supply pipeline
It is passed through into ring cold heat exchanger, heat exchange heating is carried out to sintering flue gas；And/or the cold two sections of ring cold flue gas of ring are passed through into heat supply pipeline
It is passed through and heat exchange heating is carried out to sintering flue gas into ring cold heat exchanger, so that between the sintering flue gas after the cold heat exchange wind of ring and desulfurization
With the suitable temperature difference, to realize higher heat transfer effect.
(3) one kind of the utility model is based on ammonia process-SCR combined desulfurization and denitration system, is passing through ring using ring cold flue gas
On the basis of cold heat exchanger carries out heat exchange heating to sintering flue gas, it is provided on pipeline between ammonia process desulfuration tower and ring cold heat exchanger
The denitration outlet of tail gas heat exchanger, Benitration reactor is connected by pipeline with tail gas heat exchanger, and tail gas passes through tail gas heat exchanger
Heat exchange heating carried out to sintering flue gas, realization further utilizes tail gas heat quantity, while use tail gas to sintering flue gas into
The pre- heat exchange of row is conducive to the raising of denitration efficiency.
(4) one kind of the utility model is based on ammonia process-SCR combined desulfurization and denitration system, and Benitration reactor is that SCR denitration is anti-
Device is answered, and is provided with the catalyst containing vanadium and/or tungsten and/or titanium and/or molybdenum, the burning after heat exchange in SCR denitration reaction device
Knot flue-gas temperature matches with reaction temperature required for SCR denitration reaction device, and then improves the denitration effect of Benitration reactor
Rate.
Detailed description of the invention
Fig. 1 is a kind of structural schematic diagram based on ammonia process-SCR combined desulfurization and denitration system of the utility model.
Label declaration
100, sintering machine；200, flue collector；
300, ammonia process desulfuration tower；310, desulfurization entrance；320, desulfurization exports；
400, ring cold machine；410, heat supply pipeline；
510, ring cold heat exchanger；512, the cold heat supply outlet of ring；513, the second heated inlet；514, the second heating exit；
520, tail gas heat exchanger；521, tail gas heat supply entrance；522, tail gas heat supply exports；523, the first heated inlet；524, first adds
Heat outlet；
600, Benitration reactor；610, denitration entrance；620, denitration exports；
700, deduster；810, the first exhaust fan；820, the second exhaust fan.
Specific embodiment
Hereafter to the detailed description of the exemplary embodiment of the utility model with reference to attached drawing, which forms the one of description
Part has been shown as example the enforceable exemplary embodiment of the utility model in the figure.Although these exemplary realities
Example is applied to be described in sufficient detail so that those skilled in the art can implement the utility model, it is to be understood that it can be realized
His embodiment and can various changes can be made to the utility model in the case where not departing from the spirit and scope of the utility model.Hereafter
Required the scope of the utility model is not limited to the more detailed description of the embodiments of the present invention, and only
The description of the characteristics of in order to be illustrated and not limit to the utility model and feature, to propose to execute the utility model
Best mode, and it is sufficient to make those skilled in the art that can implement the utility model.Therefore, the scope of the utility model only by
Appended claims limit.
Hereafter the detailed description of the utility model and example embodiment are more fully understood in combination with attached drawing, wherein this reality
It is identified with novel element and feature by appended drawing reference.
Embodiment 1
As shown in Figure 1, one kind of the present embodiment is based on ammonia process-SCR combined desulfurization and denitration system, including sintering machine 100, master
Flue 200, ammonia process desulfuration tower 300, ring cold machine 400, ring cold heat exchanger 510 and Benitration reactor 600.In sintering process, sintering
Material is sintered on sintering machine 100, and generated sintering flue gas enters in flue collector 200 through draft effect.Pallet
On sintering feed sinter sinter into, then sinter is cooled down by broken be transported on ring cold machine 400 of crushing device.
Ring cold machine 400 along the cooling sequence of sinter be divided into ring is one section cold, cold two sections and cold three sections of ring of ring, the air blast of 400 bottom of ring cold machine
Machine cools down sinter by blow air, and air passes through sinter, takes away the higher ring of sinter heat formation temperature
Cold flue gas.
Flue collector 200 is connected by pipeline with the desulfurization entrance 310 of ammonia process desulfuration tower 300, and sintering flue gas is from flue collector
200 flow to desulfurization entrance 310.The bottom of ammonia process desulfuration tower 300 is arranged in desulfurization entrance 310, sets at the top of ammonia process desulfuration tower 300
It is equipped with desulfurization outlet 320, spray tube is provided in the ammonia process desulfuration tower 300 between desulfurization entrance 310 and desulfurization outlet 320, sprays
Shower pipe sprays the side's of being directed downward setting；Spray tube is connected with the ammonia tank of peripheral hardware.Sintering flue gas enters ammonia process from desulfurization entrance 310
After desulfurizing tower 300, from desulfurization entrance 310 to 320 movement of desulfurization outlet, i.e., sintering flue gas is in ammonia process desulfuration tower 300 from lower past
Upper movement, while spray tube sprays downwards ammonia, flue gas and spray ammonia counter current contacting, and gas-liquid mass transfer occurs and heat transfer, chemistry are inhaled
Receipts process is reacted as follows:
NH3+H2O+SO2→(NH4)2SO3
(NH4)2SO3+SO2+H2O→NH4HSO3
NH4HSO3+NH3→(NH4)2SO3
SO in flue gas2It is reacted with absorbent and generates ammonium sulfite, reaction rear slurry leaves absorption region, and it is de- to fall to ammonia process
The oxidation pond of 300 bottom of sulphur tower leads to oxygen by booster fan and ammonium sulfite is completely oxidized to ammonium sulfate, and sintering flue gas passes through
From 320 discharge of desulfurization outlet after desulfurization.It should be noted that the spray flow of ammonia is 1500~2000m in ammonia process desulfuration tower 3003/
H, the spray flow of ammonia is 1500m in ammonia process desulfuration tower 300 in the present embodiment3/h。
The present embodiment sintering flue gas is before entering ammonia process desulfuration tower 300, and flue-gas temperature is 120 DEG C at desulfurization entrance 310,
SO2Content is 1754mg/Nm3, NOx content 316mg/Nm3；Sintering flue gas passes through 300 desulfurization of ammonia process desulfuration tower, desulfurization outlet
Sintering flue gas temperature is 67.5 DEG C at 320, SO2Content is 100mg/Nm3, NOxContent is 239mg/Nm3, desulfurization degree is
94.3%, denitrification rate 24.15%.
The desulfurization outlet 320 of ammonia process desulfuration tower 300 is connected by pipeline with the denitration entrance 610 of Benitration reactor 600,
Ring cold heat exchanger 510 is installed on the pipeline between ammonia process desulfuration tower 300 and Benitration reactor 600；The flue gas of ring cold machine 400 goes out
Mouthful be connected with ring cold heat exchanger 510 by heat supply pipeline 410, ring cold flue gas pass through ring cold heat exchanger 510 to sintering flue gas into
Row heat exchange heating.Specifically in the present embodiment, heat supply pipeline 410 and ring cold one section and cold two sections of the exhanst gas outlet of ring are connected
Logical, cold one section of ring enters in ring cold heat exchanger 510 with cold two sections of the flue gas of ring by heat supply pipeline 410, it is of course also possible to by ring
Cold one section or cold two sections of the exhanst gas outlet of ring are individually connected with heat supply pipeline 410, are then connected to by heat supply pipeline 410
Into ring cold heat exchanger 510.The temperature of 410 ring cold flue gas of heat supply pipeline is 420~500 DEG C, is 450 DEG C in the present embodiment.
In addition, being provided with the cold heat supply of ring on ring cold heat exchanger 510 in the present embodiment exports the 512, second heated inlet 513
With the second heating exit 514, it is connected between desulfurization outlet 320 and the second heated inlet 513 by pipeline, the second heating exit
514 are connected with denitration entrance 610, and the sintering flue gas after desulfurization enters ring cold heat exchanger 510 from the second heated inlet 513, the
Sintering flue gas temperature is 65 DEG C at two heated inlets 513.Ring cold flue gas is right after the entrance ring cold heat exchanger 510 of heat supply pipeline 410
Sintering flue gas in ring cold heat exchanger 510 carries out heat exchange heating；Sintering flue gas is discharged from the second heating exit 514 after heat exchange, leads to
It crosses sintering flue gas temperature at the second heating exit 514 of heat exchange and reaches 230 DEG C；Ring cold flue gas is discharged from the cold heat supply outlet 512 of ring.
The sintering flue gas to exchange heat through ring cold heat exchanger 510 enters in Benitration reactor 600 from denitration entrance 610, this implementation
The Benitration reactor 600 of example is SCR denitration reaction device, and be provided in SCR denitration reaction device containing vanadium and/or tungsten and/or
The middle temperature catalyst of titanium and/or molybdenum, operating temperature section are 210~420 DEG C.Into the sintering flue gas of Benitration reactor 600
Temperature is in the operating temperature section of SCR denitration reaction device, it is possible to quickly carry out denitration reaction, pass through Benitration reactor
600 spray ammonia, the NO that sintering flue gas contains in Benitration reactor 600xOccur under the catalytic action of catalyst with ammonia following anti-
It answers:
4NO+4NH3+O2→4N2+6H2O
6NO2+8NH3→7N2+12H2O
Sintering flue gas after Benitration reactor 600, NOx concentration is 36mg/m in flue gas3, meet existing sintering cigarette
Ultra-low emission of NOx standard in gas, 600 emission reduction rate of Benitration reactor reach 85%.
In the present embodiment preferably, deduster is additionally provided on the pipeline between flue collector 200 and ammonia process desulfuration tower 300
700, which is electric precipitator, its role is to which the particulate matter in sintering flue gas is removed before denitration, thus
Particulate matter in sintering flue gas is avoided to have an impact the denitration effect of Benitration reactor 600.
It is further to note that being provided on pipeline in the present embodiment between ammonia process desulfuration tower 300 and flue collector 200
Sintering flue gas is pumped into ammonia process desulfuration tower 300 by the first exhaust fan 810, first exhaust fan 810；And Benitration reactor 600
The second exhaust fan 820 is provided on the pipeline at rear, which extracts sintering flue gas out Benitration reactor 600.Its
In order to guarantee that sintering flue gas can sufficiently be circulated to each pollution reduction link in sintering flue gas treatment process.
Embodiment 2
The present embodiment on the basis of embodiment 1, is arranged on pipeline between ammonia process desulfuration tower 300 and ring cold heat exchanger 510
There is tail gas heat exchanger 520, the denitration outlet 620 of Benitration reactor 600 is connected by pipeline with tail gas heat exchanger 520, tail gas
Heat exchange heating is carried out to sintering flue gas by tail gas heat exchanger 520.
Tail gas heat supply entrance 521, tail gas heat supply outlet 522, first are provided in tail gas heat exchanger 520 in the present embodiment
Heated inlet 523 and the first heating exit 524 are connected between denitration outlet 620 and the first heated inlet 523 by pipeline,
Sintering flue gas after desulfurization enters tail gas heat exchanger 520 from the first heated inlet 523, and the first of tail gas heat exchanger 520 is heated out
Mouth 524 is connected with the second heated inlet 513 of ring cold heat exchanger 510, and sintering flue gas temperature is 65 at the first heated inlet 523
℃。
Tail gas after denitration enters after tail gas heat exchanger 520 from tail gas heat supply entrance 521 to the burning in tail gas heat exchanger 520
It ties flue gas and carries out pre- heat exchange heating, temperature of the tail gas at tail gas heat supply entrance 521 after denitration is 195 DEG C,；Tail gas after heat exchange
It is discharged from the first heating exit 524, reaches 145 DEG C by sintering flue gas temperature at the first heating exit 524 of heat exchange；After denitration
Tail gas is discharged from tail gas heat supply outlet 522.
Tail gas heat exchanger 520 is provided with before ring cold heat exchanger 510, tail gas passes through 520 pairs of sintering cigarettes of tail gas heat exchanger
Gas carries out heat exchange heating, and realization further utilizes tail gas heat quantity.Using the NOx in sintering flue gas after the present embodiment denitration
Concentration is 27mg/m3, 600 denitrification rate of Benitration reactor is 89%.
Embodiment 1 and 2 embodiment of embodiment and emission reduction result are compared, comparative situation is shown in Table 1.It needs to illustrate
, because three kinds of embodiment differences only enter Benitration reactor 600 after ammonia process desulfuration tower 300 in sintering flue gas and carry out
Use which kind of heat exchange mode carries out heat exchange heating to sintering flue gas during denitration, the desulfurization to ammonia process desulfuration tower 300
Denitrification process does not influence substantially, benchmark embodiment 240mg/m in table3NOx content is sintering flue gas after ammonia process of desulfurization link
The content of middle NOx, so more can reflect the different influences to denitration efficiency of heat exchange mode as benchmark.
2 NOx abatement contrast table of 1 embodiment 1 of table and embodiment
Embodiment 1 in table is compared with benchmark as can be seen that by the sintering flue gas after 300 desulfurization of ammonia process desulfuration tower
Denitration is carried out again by the heat exchange heating of ring cold heat exchanger 510, it can be while guaranteeing desulfurization effect, so that denitration efficiency is significantly
It is promoted, realizing ammonia process desulfuration tower 300 and Benitration reactor 600 can rationally cooperate, and then realize SO in sintering flue gas2With NOx
Inexpensive joint emission reduction, and the reasonable utilization of ring cold flue gas heat is realized, solve ammonia process desulfuration tower 300 in the prior art
Desulfurization department in charge of technological work in a factory can not connect the technical problem of SCR denitration, cannot be taken off using ammonia process before also having broken SCR denitration in the prior art
The technology prejudice of the progress desulfurization of sulphur tower 300.In addition, due to being further heated up to the flue gas after desulfurization, so also achieving
Effectively taking off for discharge flue gas is white.
By in table embodiment 2 and other embodiments compare discovery, on the basis of embodiment 1, change ring is cold
Before heat, the tail gas after subsequent 600 denitration of Benitration reactor is subjected to pre- heat exchange to sintering flue gas by tail gas heat exchanger 520 and is risen
Temperature, carrying out processing to sintering flue gas through the above way can be further improved the denitration efficiency of sintering flue gas, in addition to realization pair
Tail gas heat quantity is further utilized, same to be conducive to the raising of sintering flue gas bulk temperature, and is realized and be sintered to after desulfurization
The gradual change type of flue gas heats up, and not only contributes to the heat exchange temperature rise effect for improving sintering flue gas, is also beneficial to follow-up sintering flue gas
Denitration efficiency further increases.
Embodiment 3
The present embodiment substantially with embodiment 1, the difference is that, in the present embodiment in ammonia process desulfuration tower 300 ammonia spray
Leaching amount is 1800m3/ h, the present embodiment sintering flue gas is before entering ammonia process desulfuration tower 300, and flue-gas temperature is at desulfurization entrance 310
120 DEG C, SO2Content is 1763mg/Nm3, NOxContent is 321mg/Nm3；Sintering flue gas passes through 300 desulfurization of ammonia process desulfuration tower, takes off
Sintering flue gas temperature is 63.5 DEG C at sulphur outlet 320, SO2Content is 75mg/Nm3, NOxContent is 231mg/Nm3, desulfurization degree is
95.7%, 300 denitrification rate of ammonia process desulfuration tower is 28.0%.And it is subsequent using 600 denitration of Benitration reactor, denitration outlet 620
Locate NOxContent is 29m3/ h, 600 denitrification rate of Benitration reactor are 87.8%.
Embodiment 4
The present embodiment substantially with embodiment 1, the difference is that, in the present embodiment in ammonia process desulfuration tower 300 ammonia spray
Leaching amount is 2000m3/ h, the present embodiment sintering flue gas is before entering ammonia process desulfuration tower 300, and flue-gas temperature is at desulfurization entrance 310
120 DEG C, SO2Content is 1757mg/Nm3, NOxContent is 325mg/Nm3；Sintering flue gas passes through 300 desulfurization of ammonia process desulfuration tower, takes off
Sintering flue gas temperature is 62.7 DEG C at sulphur outlet 320, SO2Content is 59mg/Nm3, NOxContent is 217mg/Nm3, desulfurization degree is
96.6%, 300 denitrification rate of ammonia process desulfuration tower is 33.2%.And it is subsequent using 600 denitration of Benitration reactor, denitration outlet 620
Locate NOxContent is 21m3/ h, 600 denitrification rate of Benitration reactor are 90.3%.
Embodiment 1, the NOx discharge of embodiment 3 and embodiment 4 and its emission reduction result are compared, comparative situation is shown in
Table 2.It should be noted that the embodiment in embodiment 1, embodiment 3 and embodiment 4 uses in ammonia process desulfuration tower 300
Different ammonia spray flows, during ammonia process desulfuration tower 300, desulfurization degree and denitrification rate is with the increase of ammonia spray flow and increasing is
It is foreseeable, so the comparison in table 2 is to be directed to after ammonia process desulfuration tower 300 the i.e. comparison of 600 denitrification rate of Benitration reactor.
4 NOx abatement contrast table of 2 embodiment 1 of table, embodiment 3 and embodiment
Above 3 embodiments are compared into discovery simultaneously, after increasing the ammonia spray flow in ammonia process desulfuration tower 300, in addition to
Outside the raising of the desulphurization denitration rate of ammonia process desulfuration tower 300 in accordance with expectation, the denitration efficiency of subsequent Benitration reactor 600 is also
Improve, in addition to the above embodiments, applicant has also carried out multiple groups and has similarly probed into test, test result all present it is identical become
Gesture, this allows applicant to feel very unexpected, and applicant has organized multiple discussion, and finally thinks: denitration after sintering flue gas heat exchange
On the one hand raising of the reactor 600 for denitration efficiency, reason are that sintering flue gas heat exchange heating has reached Benitration reactor
600 denitration temperature；When another aspect ammonia process desulfuration tower 300 carries out desulfurization to sintering flue gas, sintering flue gas after the ammonia process of desulfurization
Internal component also has greatly changed, and can contain a large amount of ammonia after the ammonia process of desulfurization in sintering flue gas, at present in the technical field
Technical staff's ammonia of all thinking to escape will cause detrimental effect, but by using the technical solution of the utility model, applicant
Think to improve the ammonia spray flow in ammonia process desulfuration tower 300 in a certain range, the extra ammonia in sintering flue gas is by exchanging heat
After step, the continuous progress of denitration reaction can be promoted in Benitration reactor 600.
The utility model is described in detail above in conjunction with specific exemplary embodiment.It is understood, however, that can be
It is carry out various modifications in the case where not departing from the scope of the utility model being defined by the following claims and modification.It is detailed to retouch
State should be to be considered only as with attached drawing it is illustrative and not restrictive, if there is any such modifications and variations, then
They fall in the scope of the utility model described herein.In addition, background technique is intended to grinding in order to illustrate this technology
It was found that shape and meaning, it is no intended to limit the application field of the utility model or the application and the utility model.
Claims (9)
1. one kind is based on ammonia process-SCR combined desulfurization and denitration system, which is characterized in that including flue collector (200), ammonia process desulfuration tower
(300), ring cold machine (400), ring cold heat exchanger (510) and Benitration reactor (600)；Flue collector (200) passes through pipeline and ammonia process
The desulfurization entrance (310) of desulfurizing tower (300) is connected, and the desulfurization outlet (320) of ammonia process desulfuration tower (300) passes through pipeline and denitration
The denitration entrance (610) of reactor (600) is connected, on the pipeline between ammonia process desulfuration tower (300) and Benitration reactor (600)
Ring cold heat exchanger (510) are installed；The exhanst gas outlet of ring cold machine (400) passes through heat supply pipeline (410) and ring cold heat exchanger (510)
It is connected, ring cold flue gas carries out heat exchange heating to sintering flue gas by ring cold heat exchanger (510).
2. according to claim 1 a kind of based on ammonia process-SCR combined desulfurization and denitration system, which is characterized in that heat supply pipeline
(410) it is connected with cold one section of the exhanst gas outlet of ring, cold one section of the flue gas of ring enters ring cold heat exchanger by heat supply pipeline (410)
(510)；And/or
Heat supply pipeline (410) is connected with cold two sections of the exhanst gas outlet of ring, cold two sections of the flue gas of ring by heat supply pipeline (410) into
Enter ring cold heat exchanger (510).
3. according to claim 1 a kind of based on ammonia process-SCR combined desulfurization and denitration system, which is characterized in that flue collector
(200) deduster (700) are provided on the pipeline between ammonia process desulfuration tower (300).
4. according to claim 1 a kind of based on ammonia process-SCR combined desulfurization and denitration system, which is characterized in that the ammonia process of desulfurization
Tail gas heat exchanger (520) are provided on pipeline between tower (300) and ring cold heat exchanger (510), the denitration of Benitration reactor (600)
Outlet (620) is connected by pipeline with tail gas heat exchanger (520), tail gas pass through tail gas heat exchanger (520) to sintering flue gas into
Row heat exchange heating.
5. according to claim 1 a kind of based on ammonia process-SCR combined desulfurization and denitration system, which is characterized in that denitration reaction
Device (600) is SCR denitration reaction device.
6. according to claim 1 a kind of based on ammonia process-SCR combined desulfurization and denitration system, which is characterized in that the ammonia process of desulfurization
Tower (300) bottom is provided with desulfurization entrance (310), desulfurization outlet (320) is provided at the top of ammonia process desulfuration tower (300), desulfurization enters
Spray tube is provided in ammonia process desulfuration tower (300) between mouth (310) and desulfurization outlet (320), spray tube spray is directed downward
Side's setting；Spray tube is connected with the ammonia tank of peripheral hardware.
7. according to claim 3 a kind of based on ammonia process-SCR combined desulfurization and denitration system, which is characterized in that deduster
It (700) is electric precipitator.
8. according to claim 5 a kind of based on ammonia process-SCR combined desulfurization and denitration system, which is characterized in that SCR denitration
The catalyst containing vanadium and/or tungsten and/or titanium and/or molybdenum is provided in reactor.
9. described in any item a kind of based on ammonia process-SCR combined desulfurization and denitration system according to claim 1~7, feature exists
In being provided with the first exhaust fan (810) on the pipeline between ammonia process desulfuration tower (300) and flue collector (200), first exhaust fan
(810) sintering flue gas is pumped into ammonia process desulfuration tower (300).
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| CN201822037971.XU CN209188514U (en) | 2018-12-04 | 2018-12-04 | One kind being based on ammonia process-SCR combined desulfurization and denitration system |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109331652A (en) * | 2018-12-04 | 2019-02-15 | 安徽工业大学 | One kind being based on ammonia process-SCR combined desulfurization and denitration system and method |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN109331652A (en) * | 2018-12-04 | 2019-02-15 | 安徽工业大学 | One kind being based on ammonia process-SCR combined desulfurization and denitration system and method |
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