CN106582268A - Flue gas multi-pollutant collaborative purification process using blast furnace slag sensible heat - Google Patents
Flue gas multi-pollutant collaborative purification process using blast furnace slag sensible heat Download PDFInfo
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- CN106582268A CN106582268A CN201611030182.2A CN201611030182A CN106582268A CN 106582268 A CN106582268 A CN 106582268A CN 201611030182 A CN201611030182 A CN 201611030182A CN 106582268 A CN106582268 A CN 106582268A
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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
- B01D53/86—Catalytic processes
- B01D53/8621—Removing nitrogen compounds
- B01D53/8625—Nitrogen oxides
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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
- B01D53/46—Removing components of defined structure
- B01D53/48—Sulfur compounds
- B01D53/50—Sulfur oxides
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F27—FURNACES; KILNS; OVENS; RETORTS
- F27D—DETAILS OR ACCESSORIES OF FURNACES, KILNS, OVENS, OR RETORTS, IN SO FAR AS THEY ARE OF KINDS OCCURRING IN MORE THAN ONE KIND OF FURNACE
- F27D17/00—Arrangements for using waste heat; Arrangements for using, or disposing of, waste gases
- F27D17/008—Arrangements for using waste heat; Arrangements for using, or disposing of, waste gases cleaning gases
-
- 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
- B01D2258/025—Other waste gases from metallurgy plants
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P10/00—Technologies related to metal processing
- Y02P10/25—Process efficiency
Abstract
This invention provides a flue gas multi-pollutant collaborative purification process using blast furnace slag sensible heat, and belongs to the steel industry surplus heat utilization and the pollution control fields. The flue gas multi-pollutant collaborative purification process using the blast furnace slag sensible heat relates to a first induced draft fan, a secondary induced draft fan, a molten slag lead-in groove, a quantitative flow diverter, a molten slag granulating device, a solid slag conveying device, a first heat exchange chamber, a secondary heat exchange chamber, a dust collector, a SCR denitration device, a heat exchange boiler, a desulfurization device and a chimney, part of flue gas is sent by the first induced draft fan into the first heat exchange chamber, blast furnace molten slag introduced in by the molten slag lead-in groove is sent by the quantitative flow diverter to the molten slag granulating device for crushing into liquid droplets; then, the blast furnace slag is sent by the solid slag conveying device to the secondary heat exchange chamber, the flue gas out of the first heat exchange chamber and the secondary heat exchange chamber enters the SCR denitration device via the dust collector, then passes through the heat exchange boiler, then sent by the secondary induced draft fan to the desulfurization device and then discharged by the chimney. The flue gas multi-pollutant collaborative purification process can be used for full use of steel industry blast furnace slag sensible heat surplus energy and collaborative removal of typical multi-pollutants.
Description
Technical field
The present invention relates to steel industry UTILIZATION OF VESIDUAL HEAT IN and pollution control field, particularly relate to what a kind of blast-furnace cement sensible heat was utilized
Flue gas multiple pollutant synergistic purification technique, it is adaptable to plan to build steel mill or exemplary process flue gas (sintering/pelletizing/coking etc.) and blast furnace
The existing iron and steel enterprise for adjoining.
Background technology
Count according to Chinese Ministry of Environmental Protection, the SO of steel industry in 20142、NOx180.7 ten thousand tons are respectively with smoke-dust discharge capacity, 56.6
Ten thousand tons and 101.5 ten thousand tons, 10.4%, 4% and the 7% of industrial source total release is accounted for respectively.In steel and iron industry production process
The typical flue gas such as sintering, pelletizing and coking is the main source of iron and steel enterprise's Air Pollutant Emission.Except above-mentioned pollution beyond the region of objective existence, allusion quotation
Type flue gas also endangers gas containing a large amount of bioxin and 1～3vol.% carbon monoxides (CO) etc..
Using the more ripe dedusting of Thermal Power Generation Industry, desulfurization technology, through appropriate improvement, steel industry is widely used in
Flue gas desulfurization and dedusting engineering.In recent years, it is that leading iron and steel typical case flue gas ash removal is increasingly turned to electricity and changes bag or pocket type with electric precipitation
Dedusting.Through dry method/semidry methods such as exploration for many years and long-term engineering practice, recirculating fluidized bed, rotating spraying, dense-phase towers
Sulfur removal technology reaches its maturity, and has some superiority in terms of operation stability and economic serviceability.Chinese patent
(CN202398282U, CN102210973A) is disclosed for semi-dry desulphurization dust removal integrated plant, is widely used to head
Steel, Baosteel, elder brother's steel and climb steel etc. sinter flue gas dust-removal and desulfurizing engineering.
However, for steel industry denitrating flue gas work, comprehensively into technical scheme demonstration stage, engineer applied compared with
For limited.During steel industry is typical low-temperature flue gas (100～180 DEG C of agglomerates of sintered pellets, 210～250 DEG C of coking) because its undulatory property,
Should not directly using (the vanadium titanium system catalysis of the ripe SCR technology of thermal power plant without the drawback such as suitable thermal source or heating operating cost height
Agent, temperature window is at 300～400 DEG C).Therefore, developing low-temperature SCR catalyst, or find suitable thermal source heating low-temperature flue gas is
The Important Action of steel industry denitrating flue gas is solved at present.Additionally, substantial amounts of CO gases are He the harm gas such as bioxin in flue gas
Reduction of discharging will also become the emphasis of Environmental capacity.
Related data shows that (fume afterheat, product sensible heat, slag show the residual heat resources in China's steel and iron industry production process
Heat) recycling inefficiency.Wherein, blast-furnace slag is a large side-product-silicic acid in blast furnace ironmaking production process
Salt, is characterized in molten state, and temperature is at 1450～1600 DEG C.The cooling treatment of molten blast furnace slag adopts water quenching mostly at present,
Its shortcoming has：A large amount of sensible heats of blast furnace slag cannot be recycled；The waste and pollution of flushing cinder water resource；Sulfur-bearing, volatile gas
Deng a large amount of precipitations and directly discharge of pollutant, surrounding enviroment are caused to pollute.Water quenching technology carries out chilling and is cooled to solid slag
Process is related to the recycling of blast furnace slag and sensible heat heat recovery.Chinese patent (CN101418950A,
CN102787186A, CN103820588A, CN103060496A, CN104745751A) disclose blast-furnace cement sensible heat or washing slag water
The exhaust heat recovering method and device of steam.Blast furnace slag is except making the cement compared with high added value somehow succedaneum, China is specially
Sharp (CN103922787A, CN104556097A, CN102698737A, CN101797467A, CN101745309) is individually disclosed
Titanium-containing blast furnace slag prepares porous material, houghite and zeolite, SCR denitration and its raw material titanium tungsten powder, flue gas desulfurization and inhales
The method for receiving agent.
Chinese patent CN102228774A invents a kind of blast-furnace cement sensible heat and reclaims the method for being sintered flue gas desulfurization simultaneously
And device.Specifically, liquid slag carries out first desulphurization reaction and first time heat after being granulated reactor and be broken with sintering flue gas
Amount is exchanged, and then Jing vibrations bed carries out secondary desulfuration reaction and second heat recovery of heat again, finally in the cooling bay sending out
The form of electricity carries out the third time of heat and recycles.Patent CN103787277A discloses one kind and carries out first using blast-furnace cement sensible heat
The method and device of alkane preparing synthetic gas by reforming.The side heated by above-mentioned utilization blast-furnace cement sensible heat directly contact object gas
Method, is not directed to tap cinder amount, speed of slagging tap and target gas flow and the problems such as matching of flow velocity, is also not directed to many pollutions
Collaboration administer.
The content of the invention
The technical problem to be solved in the present invention is to provide the flue gas multiple pollutant synergistic purification that a kind of blast-furnace cement sensible heat is utilized
Technique, realizes flue gas multiple pollutant while reducing discharging and blast furnace slag waste heat efficient utilization, it is adaptable to plan to build steel mill or exemplary process cigarette
The existing iron and steel enterprise that gas (sintering/pelletizing/coking etc.) is adjoined with blast furnace.
The technique equipment therefor includes air-introduced machine, secondary air-introduced machine, slag lead-in groove, quantitative diverter, a liquid slag
Pelletizer, solid slag conveyer device, first Heat Room, secondary heat exchange room, cleaner unit, SCR denitration device, heat exchange boiler, desulfurization
Device and chimney, before No. one time air-introduced machine is arranged on first Heat Room, slag is imported quantitative diverter by slag lead-in groove, quantitatively
Diverter is followed by liquid slag pelletizer, and liquid slag pelletizer is located at first Heat Room top, and first Heat Room bottom arranges solid-state
Slag conveyer device, the solid slag conveyer device other end access secondary heat exchange room, first Heat Room and secondary heat exchange room cigarette out
Gas enters cleaner unit, and cleaner unit is followed by SCR denitration device, and SCR denitration device is followed by heat exchange boiler, and heat exchange boiler is drawn by secondary
Blower fan is connected with desulfurizer, and desulfurizer is followed by chimney.
Wherein, secondary heat exchange room could be arranged to multi-stage heat exchanger room.
SCR denitration device is controlled at 250～450 DEG C using wide temperate zone SCR technology, the operating temperature of catalyst.
In the case where the process flue gas before first heat exchange completes desulfurization, desulfurizer can be saved.
No. one time air-introduced machine is used for control into the heat exchange exhaust gas volumn of first Heat Room.
The quantitative diverter of molten blast furnace slag is to carry out accurately determining according to the process exhaust gas volumn and heat-exchange temperature of first Heat Room
The granulation amount of amount control blast furnace slag.
High-temperature molten slag is broken into drop by liquid slag pelletizer, increases the directly contact area with flue gas, improves heat exchange
Efficiency.
The flue gas of first Heat Room and the heating of secondary heat exchange room is realized converging by secondary air-introduced machine；Secondary air-introduced machine is prevented
Process slag inlet and the slag notch blowby of the first Heat Rooms of flue gas Jing and secondary heat exchange room.
The specific embodiment of the technique is as follows：
Partial fume is delivered to first Heat Room through an air-introduced machine by pending flue gas, the height imported by slag lead-in groove
Stove liquid slag is delivered to liquid slag pelletizer through quantitative diverter and is broken into drop；Into first Heat Room pending flue gas with
Blast furnace drop slag directly contact after granulation, realizes the intensification of flue gas；Convey through solid slag through the blast furnace slag of first cooling
Device enters secondary heat exchange room, for the remaining flue gas Direct Contact Heating for being introduced into first Heat Room；In first Heat Room
Under the directly contact of the high temperature thermal-state blast furnace slag of secondary heat exchange room, CO in flue gas is He the gaseous contaminant direct oxidation such as bioxin
For CO2, oxidation, purification is realized, and the heat of combustion process release further lifts flue-gas temperature；First Heat Room and secondary change
Hot cell heating flue gas out carries out dedusting by cleaner unit, into SCR denitration device, realizes NO in flue gasxRemoving；Denitration
Flue gas afterwards realizes the recycling of fume afterheat by heat exchange boiler, and then flue gas is delivered to desulfurization dress by secondary air-introduced machine
Put, further realize SO in flue gas2Removing, subsequent flue gas Jing smoke stack emissions are to atmospheric environment.
The technique makes full use of what slag high-temperature residual heat and CO oxidizing fires discharged by flue gas and blast furnace slag directly contact
Heat realizes the lifting of cigarette temperature, provides preference temperature for follow-up denitrating flue gas.The technique be provided simultaneously with flue gas in CO He bioxin
Deng the removal effect of pollutant.Specifically, flue gas is processed by straight with blast furnace slag in first Heat Room and secondary heat exchange room
Contact, CO is He the pollutant such as bioxin are direct oxidation into CO under the hot environment that blast furnace slag is provided2, CO is realized He bioxin
Deng multi-pollutant oxidation, purification.
Heat in the heat transfer process of the technique is accounted by being carried out as follows：
Process exhaust gas volumn Q1(m3/ h), CO contents x% (volume fraction, combustion heat value q=283KJ/mol), average density is
ρ1(kg/m3), mean temperature is T1(DEG C), mean specific heat are c1(KJ/kg/ DEG C), first Heat Room exhaust gas volumn Q1-1(m3/ h),
Secondary heat exchange room exhaust gas volumn Q1-2=Q1–Q1-1(m3/h)。
Molten blast furnace slag particle amount m2(kg), mean temperature is T2(DEG C), mean specific heat are c2(KJ/kg/℃).Through
Blast furnace slag temperature T after first Heat Room2-1(DEG C), it is c to spend for mean specific heat2-1(KJ/kg/℃).Behind secondary heat exchange room
Blast furnace slag temperature T2-2(℃)。
Flue-gas temperature T after first Heat Room1-1(DEG C), flue-gas temperature T behind secondary heat exchange room1-2(℃)。
The directly contact sensible heat utilization efficiency of first Heat Room is η1(%), the oxidizing fire efficiency eta of CO3；Secondary heat exchange room directly connects
Tactile sensible heat utilization efficiency is η1(%), the oxidizing fire efficiency eta of CO4。
Computing formula is Q=c × m × △ T.
First Heat Room：
(Q1-1×t×ρ1)×c1×(T1-1–T1)=m2×c2×(T2–T2-1)×η1+Q1-1× x% × 103×t×q/
[22.4×(273+T1-1)/273]×η3
Secondary heat exchange room：
[(Q1–Q1-1)×t×ρ1]×c1×(T1-2–T1)=m2×c2-1×(T2-1–T2-2)×η2+(Q1–Q1-1) × x% ×
103×t×q/[22.4×(273+T1-1)/273]×η4
Wherein t is the unit time (1h).
Preferably, by adjusting flue gas sendout, blast furnace slag granulation amount and enhanced heat exchange efficiency, optimization improves first heat exchange
The heat-exchange temperature T of flue gas1-1With the heat-exchange temperature T of secondary heat exchange flue gas1-2, it is ensured that through first Heat Room and secondary heat exchange room
Flue gas converge after cigarette temperature T1-3Meet 300～400 DEG C, SCR denitration device may be selected tradition vanadium Titanium series catalyst.
Alternatively, by adjusting flue gas sendout, blast furnace slag granulation amount and enhanced heat exchange efficiency, optimization improves first heat exchange
The heat-exchange temperature T of flue gas1-1With the heat-exchange temperature T of secondary heat exchange flue gas1-2, it is ensured that through first Heat Room and secondary heat exchange room
Flue gas converge after cigarette temperature T1-3Meet 250～350 DEG C, SCR denitration device may be selected middle low temperature catalyst.
The above-mentioned technical proposal of the present invention has the beneficial effect that：
In such scheme, steel industry typical case multi-pollutant (NOx, SO can be realized2, CO, bioxin, dirt etc.) collaboration
Remove, flue gas is heated using blast-furnace cement sensible heat directly contact and the heat release of CO oxidizing fires, solve cigarette temperature low and cannot adopt
The problem of SCR technique denitrations, while realizing CO He the direct oxidation of the pollutant such as bioxin purification, process avoids existing
The utilization rate of waste heat of blast furnace water quenching cooling method is low, flushing cinder water resource waste and secondary pollution problem.
Description of the drawings
Fig. 1 is the flue gas multiple pollutant synergistic purification apparatus structure schematic diagram that the blast-furnace cement sensible heat of the present invention is utilized.
Wherein：1-1：Air-introduced machine；1-2：Secondary air-introduced machine；2-1：Slag lead-in groove；2-2：Quantitative diverter；2-3：
Liquid slag pelletizer；2-4：Solid slag conveyer device；3-1：First Heat Room；3-2：Secondary heat exchange room；4：Cleaner unit；5：SCR
Denitrification apparatus；6：Heat exchange boiler；7：Desulfurizer；8- chimneys.
Specific embodiment
To make the technical problem to be solved in the present invention, technical scheme and advantage clearer, below in conjunction with accompanying drawing and tool
Body embodiment is described in detail.
The present invention provides the flue gas multiple pollutant synergistic purification technique that a kind of blast-furnace cement sensible heat is utilized.
As shown in figure 1, before in the technique equipment therefor, an air-introduced machine 1-1 is arranged on first Heat Room 3-1, slag is led
Enter groove 2-1 and slag is imported into quantitative diverter 2-2, quantitative diverter 2-2 is followed by liquid slag pelletizer 2-3, liquid slag pelletizer
2-3 is located at first Heat Room 3-1 tops, and first Heat Room 3-1 bottoms arrange solid slag conveyer device 2-4, solid slag conveying dress
Put the 2-4 other ends and access secondary heat exchange room 3-2, first Heat Room 3-1 and secondary heat exchange room 3-2 flue gas out enters cleaner unit
4, cleaner unit 4 is followed by SCR denitration device 5, and SCR denitration device 5 is followed by heat exchange boiler 6, and heat exchange boiler 6 passes through secondary air-introduced machine 1-
2 are connected with desulfurizer 7, and desulfurizer 7 is followed by chimney 8.
Wherein, secondary heat exchange room 3-2 could be arranged to multi-stage heat exchanger room.SCR denitration device 5 adopts wide temperate zone SCR technology,
The operating temperature of catalyst is controlled at 250～450 DEG C.
Present invention process is specific as follows：
Process flue gas (Q1, m3/ h) through an air-introduced machine 1-1 by partial fume (Q1-1, m3/ h) deliver to first Heat Room 3-
1, the molten blast furnace slag imported by slag lead-in groove 2-1 is delivered to liquid slag pelletizer 2-3 through quantitative diverter 2-2 and is broken into liquid
Drop；First Heat Room 3-1's processes flue gas by the directly contact with granulated blast-furnace drop slag, realizes the intensification of flue gas；Through
The blast furnace slag Jing solid slag conveyer devices 2-4 of first cooling enters secondary heat exchange room 3-2, for being introduced into first Heat Room 3-1
Remaining flue gas (Q1-2, m3/ h) Direct Contact Heating；In the hot height of high temperature of first Heat Room 3-1 and secondary heat exchange room 3-2
Under the directly contact of slag, CO in flue gas is He the direct oxidation of the gaseous contaminant such as bioxin is CO2, realize oxidation, purification, and oxygen
The heat for changing combustion process release further lifts flue-gas temperature；By first Heat Room 3-1 and secondary heat exchange room 3-2 out
Heating flue gas realizes NO in flue gas by cleaner unit 4 into SCR denitration device 5xRemoving；Flue gas after denitration is by heat exchange
Boiler 6 realizes the recycling of fume afterheat, and then flue gas is delivered to desulfurizer 7 by secondary air-introduced machine 1-2, further real
SO in existing flue gas2Removing, with after, Jing chimneys 8 are emitted into atmospheric environment.
Embodiment 1
Existing Q1=100 ten thousand m3The sintering flue gas of/h, CO contents 1% (volume fraction) not yet carry out flue gas desulfurization, flue gas
Mean temperature T1=150 DEG C, flue gas mean specific heat c1=1.077KJ/kg/ DEG C, flue gas average density ρ1=0.9kg/m3.Enter
Enter exhaust gas volumn Q of first Heat Room1-1Ten thousand m of=X3/ h, remainder (100-X) ten thousand m3/ h flue gases enter secondary heat exchange room.
Molten blast furnace slag temperature T2=1500 DEG C, mean specific heat is c2=1.05KJ/kg/ DEG C, liquid slag granulation amount m2
(kg), mean temperature T after first heat exchange2-1=600 DEG C, the sensible heat utilization efficiency eta of first Heat Room1=80%, first Heat Room
CO oxidizing fire efficiency etas3=90%, unit interval t are 1h.
First Heat Room：
(Q1-1×t×ρ1)×c1×(T1-1–T1)=m2×c2×(T2–T2-1)×η1+Q1-1× x% × 103×t×q/
[22.4×(273+T1-1)/273]×η3
That is,
Q1-1×0.9×1.077×(T1-1- 150)=m2× 1.05 × (1500-600) × 80%+Q1-1× 1% × 103×
283 × 90% × 273/ (273+T1-1)/22.4 (formula 1)
The mean specific heat c of 600 DEG C of blast furnace slag2-1=1.05KJ/kg/ DEG C, the slag temperature after secondary heat exchange
T2-2=200 DEG C.Secondary heat exchange exhaust gas volumn Q1-2=100-Q1-1Ten thousand m of=(100-X)3/ h, cigarette temperature T after secondary heat exchange1-2℃。
The sensible heat utilization efficiency eta of secondary heat exchange room2=70%, secondary heat exchange room CO oxidizing fire efficiency etas4=80%, the unit interval, t was
1h。。
Secondary heat exchange room：
[(Q1–Q1-1)×t×ρ1]×c1×(T1-2–T1)=m2×c2-1×(T2-1–T2-2)×η2+(Q1–Q1-1) × x% ×
103×t×q/[22.4×(273+T1-1)/273]×η4
That is,
(Q1–Q1-1)×0.9×1.077×(T1-2- 150)=m2× 1.05 × (600-200) × 70%+ (Q1–Q1-1)×
1% × 103× 283 × 80% × 273/ (273+T1-1)/22.4 (formula 2)
Preferably, T1-1=T1-2When=300 DEG C, calculated with formula (2) according to formula (1), exhaust gas volumn X=of first Heat Room
73.4 ten thousand m3/ h, into 26.6 ten thousand m of secondary heat exchange room exhaust gas volumn3/ h, theoretical required unit interval (1h) granulated bf slag quality m2
=79392kg ≈ 79.4t.
Embodiment 2
Existing Q1=100 ten thousand m3The sintering flue gas of/h, CO contents 1% (volume fraction) have completed flue gas desulfurization, and flue gas is put down
Equal temperature T1=100 DEG C, flue gas mean specific heat c1=1.077KJ/kg/ DEG C, flue gas average density ρ1=0.9kg/m3.Into
Exhaust gas volumn Q of first Heat Room1-1Ten thousand m of=X3/ h, remainder (100-X) ten thousand m3/ h flue gases enter secondary heat exchange room.
Molten blast furnace slag temperature T2=1500 DEG C, mean specific heat is c2=1.05KJ/kg/ DEG C, liquid slag granulation amount m2
(kg), mean temperature T after first heat exchange2-1=600 DEG C, the sensible heat utilization efficiency eta of first Heat Room1=80%, first Heat Room
CO oxidizing fire efficiency etas3=90%, unit interval t are 1h.
First Heat Room：
(Q1-1×t×ρ1)×c1×(T1-1–T1)=m2×c2×(T2–T2-1)×η1+Q1-1× x% × 103×t×q/
[22.4×(273+T1-1)/273]×η3
That is,
Q1-1×0.9×1.077×(T1-1- 100)=m2× 1.05 × (1500-600) × 80%+Q1-1× 1% × 103×
283 × 90% × 273/ (273+T1-1)/22.4 (formula 1)
The mean specific heat c of 600 DEG C of blast furnace slag2-1=1.05KJ/kg/ DEG C, the slag temperature after secondary heat exchange
T2-2=200 DEG C.Secondary heat exchange exhaust gas volumn Q1-2=100-Q1-1Ten thousand m of=(100-X)3/ h, cigarette temperature T after secondary heat exchange1-2℃。
The sensible heat utilization efficiency eta of secondary heat exchange room2=70%, secondary heat exchange room CO oxidizing fire efficiency etas4=80%, the unit interval, t was
1h。。
Secondary heat exchange room：
[(Q1–Q1-1)×t×ρ1]×c1×(T1-2–T1)=m2×c2-1×(T2-1–T2-2)×η2+(Q1–Q1-1) × x% ×
103×t×q/[22.4×(273+T1-1)/273]×η4
That is,
(Q1–Q1-1)×0.9×1.077×(T1-2- 100)=m2× 1.05 × (600-200) × 70%+ (Q1–Q1-1)×
1% × 103× 283 × 80% × 273/ (273+T1-1)/22.4 (formula 2)
Preferably, T1-1=T1-2When=300 DEG C, calculated with formula (2) according to formula (1), exhaust gas volumn X=of first Heat Room
72.8 ten thousand m3/ h, into 27.2 ten thousand m of secondary heat exchange room exhaust gas volumn3/ h, theoretical required unit interval (1h) granulated bf slag quality m2
=134516kg ≈ 134.6t.
Embodiment 3
Existing Q1=100 ten thousand m3The sintering flue gas of/h, CO contents 1% (volume fraction) not yet carry out flue gas desulfurization, flue gas
Mean temperature T1=150 DEG C, flue gas mean specific heat c1=1.077KJ/kg/ DEG C, flue gas average density ρ1=0.9kg/m3.Enter
Enter exhaust gas volumn Q of first Heat Room1-1=100 ten thousand m3/ h, does not adopt secondary heat exchange room.
Molten blast furnace slag temperature T2=1500 DEG C, mean specific heat is c2=1.05KJ/kg/ DEG C, liquid slag granulation amount m2
(kg), mean temperature T after first heat exchange2-1=600 DEG C, the sensible heat utilization efficiency eta of first Heat Room1=80%, first Heat Room
CO oxidizing fire efficiency etas3=90%, unit interval t are 1h.
First Heat Room：
(Q1-1×t×ρ1)×c1×(T1-1–T1)=m2×c2×(T2–T2-1)×η1+Q1-1× x% × 103×t×q/
[22.4×(273+T1-1)/273]×η3
That is,
Q1-1×0.9×1.077×(T1-1- 150)=m2× 1.05 × (1500-600) × 80%+Q1-1× 1% × 103×
283 × 90% × 273/ (273+T1-1)/22.4 (formula 1)
Preferably, T1-1When=300 DEG C, calculated according to formula (1), ten thousand m of exhaust gas volumn X=100 of first Heat Room3/ h, does not adopt
Use secondary heat exchange room, theoretical required unit interval (1h) granulated bf slag quality m2=120668kg ≈ 120.7t.
Embodiment 4
Existing Q1=40 ten thousand m3The coking flue gas of/h, not yet carries out flue gas desulfurization, flue gas mean temperature T1=200 DEG C, flue gas
Mean specific heat c1=1.22KJ/kg/ DEG C, flue gas average density ρ1=1.86kg/m3.Into exhaust gas volumn Q of first Heat Room1-1
Ten thousand m of=X3/h。
Molten blast furnace slag temperature T2=1500 DEG C, mean specific heat is c2=1.05KJ/kg/ DEG C, liquid slag granulation amount m2
(kg), mean temperature T after first heat exchange2-1=600 DEG C, the sensible heat utilization efficiency eta of first Heat Room1=80%, first Heat Room
CO oxidizing fire efficiency etas3=90%, unit interval t are 1h.
First Heat Room：
(Q1-1×t×ρ1)×c1×(T1-1–T1)=m2×c2×(T2–T2-1)×η1+Q1-1× x% × 103×t×q/
[22.4×(273+T1-1)/273]×η3
That is,
Q1-1×1.86×1.22×(T1-1- 200)=m2× 1.05 × (1500-600) × 80%+Q1-1× 1% × 103×
283 × 90% × 273/ (273+T1-1)/22.4 (formula 1)
The mean specific heat c of 600 DEG C of blast furnace slag2-1=1.05KJ/kg/ DEG C, the slag temperature after secondary heat exchange
T2-2=200 DEG C.Secondary heat exchange exhaust gas volumn Q1-2=100-Q1-1Ten thousand m of=(100-X)3/ h, cigarette temperature T after secondary heat exchange1-2℃。
The sensible heat utilization efficiency eta of secondary heat exchange room2=70%, secondary heat exchange room CO oxidizing fire efficiency etas4=80%, the unit interval, t was
1h。。
Secondary heat exchange room：
[(Q1–Q1-1)×t×ρ1]×c1×(T1-2–T1)=m2×c2-1×(T2-1–T2-2)×η2+(Q1–Q1-1) × x% ×
103×t×q/[22.4×(273+T1-1)/273]×η4
That is,
(Q1–Q1-1)×1.86×1.22×(T1-2- 200)=m2× 1.05 × (600-200) × 70%+ (Q1–Q1-1)×
1% × 103× 283 × 80% × 273/ (273+T1-1)/22.4 (formula 2)
Preferably, T1-1=T1-2When=300 DEG C, calculated with formula (2) according to formula (1), exhaust gas volumn X=of first Heat Room
29.1 ten thousand m3/ h, into 10.9 ten thousand m of secondary heat exchange room exhaust gas volumn3/ h, theoretical required unit interval (1h) granulated bf slag quality m2
=66110kg ≈ 66.2t.
Embodiment 5
Existing Q1=20 ten thousand m3The coking flue gas of/h, not yet carries out flue gas desulfurization, flue gas mean temperature T1=200 DEG C, flue gas
Mean specific heat c1=1.22KJ/kg/ DEG C, flue gas average density ρ1=1.86kg/m3.Into exhaust gas volumn Q of first Heat Room1-1
Ten thousand m of=X3/h。
Molten blast furnace slag temperature T2=1500 DEG C, mean specific heat is c2=1.05KJ/kg/ DEG C, liquid slag granulation amount m2
(kg), mean temperature T after first heat exchange2-1=600 DEG C, the sensible heat utilization efficiency eta of first Heat Room1=80%, first Heat Room
CO oxidizing fire efficiency etas3=90%, unit interval t are 1h.
First Heat Room：
(Q1-1×t×ρ1)×c1×(T1-1–T1)=m2×c2×(T2–T2-1)×η1+Q1-1× x% × 103×t×q/
[22.4×(273+T1-1)/273]×η3
That is,
Q1-1×1.86×1.22×(T1-1- 200)=m2× 1.05 × (1500-600) × 80%+Q1-1× 1% × 103×
283 × 90% × 273/ (273+T1-1)/22.4 (formula 1)
The mean specific heat c of 600 DEG C of blast furnace slag2-1=1.05KJ/kg/ DEG C, the slag temperature after secondary heat exchange
T2-2=200 DEG C.Secondary heat exchange exhaust gas volumn Q1-2=100-Q1-1Ten thousand m of=(100-X)3/ h, cigarette temperature T after secondary heat exchange1-2℃。
The sensible heat utilization efficiency eta of secondary heat exchange room2=70%, secondary heat exchange room CO oxidizing fire efficiency etas4=80%, the unit interval, t was
1h。。
Secondary heat exchange room：
[(Q1–Q1-1)×t×ρ1]×c1×(T1-2–T1)=m2×c2-1×(T2-1–T2-2)×η2+(Q1–Q1-1) × x% ×
103×t×q/[22.4×(273+T1-1)/273]×η4
That is,
(Q1–Q1-1)×1.86×1.22×(T1-2- 200)=m2× 1.05 × (600-200) × 70%+ (Q1–Q1-1)×
1% × 103× 283 × 80% × 273/ (273+T1-1)/22.4 (formula 2)
Preferably, T1-1=T1-2When=350 DEG C, calculated with formula (2) according to formula (1), exhaust gas volumn X=of first Heat Room
14.5 ten thousand m3/ h, into 5.5 ten thousand m of secondary heat exchange room exhaust gas volumn3/ h, theoretical required unit interval (1h) granulated bf slag quality m2
=55635kg ≈ 55.7t.
The above is the preferred embodiment of the present invention, it is noted that for those skilled in the art
For, on the premise of without departing from principle of the present invention, some improvements and modifications can also be made, these improvements and modifications
Should be regarded as protection scope of the present invention.
Claims (4)
1. the flue gas multiple pollutant synergistic purification technique that a kind of blast-furnace cement sensible heat is utilized, it is characterised in that：The technique equipment therefor
Including air-introduced machine (1-1), secondary air-introduced machine (1-2), slag lead-in groove (2-1), quantitative diverter (2-2), a melting slag particle
Change device (2-3), solid slag conveyer device (2-4), first Heat Room (3-1), secondary heat exchange room (3-2), cleaner unit (4), SCR take off
Nitre device (5), heat exchange boiler (6), desulfurizer (7) and chimney (8), pending flue gas is through an air-introduced machine (1-1) by portion
Point flue gas delivers to first Heat Room (3-1), and the molten blast furnace slag imported by slag lead-in groove (2-1) is through quantitative diverter (2-
2) deliver to liquid slag pelletizer (2-3) and be broken into drop；Flue gas into first Heat Room (3-1) is directly connect with blast furnace drop slag
Touch, realize the intensification of flue gas；Subsequently, the blast furnace slag lowered the temperature for the first time is through solid slag conveyer device (2-4) into secondary heat exchange room
(3-2), for the remaining flue gas Direct Contact Heating for being introduced into first Heat Room (3-1)；In first Heat Room (3-1) and two
Under the directly contact of the high temperature thermal-state blast furnace slag of secondary Heat Room (3-2), CO in flue gas is He bioxin gaseous contaminant direct oxidation
For CO2, oxidation, purification is realized, and the heat of combustion process release further lifts flue-gas temperature；First Heat Room (3-1) and two
Secondary Heat Room (3-2) flue gas out carries out dedusting by cleaner unit (4)；SCR denitration device (5) is entered back into, in realizing flue gas
NOxRemoving；Flue gas after denitration realizes the recycling of fume afterheat by heat exchange boiler (6), and then passes through secondary air inducing
Flue gas is delivered to desulfurizer (7) by machine (1-2), further realizes SO in flue gas2Removing, the discharge of subsequent flue gas Jing chimneys (8)
To atmospheric environment.
2. the flue gas multiple pollutant synergistic purification technique that blast-furnace cement sensible heat according to claim 1 is utilized, it is characterised in that：
The SCR denitration device (5) is controlled at 250～450 DEG C using wide temperate zone SCR technology, the operating temperature of catalyst.
3. the flue gas multiple pollutant synergistic purification technique that blast-furnace cement sensible heat according to claim 1 is utilized, it is characterised in that：
The liquid slag pelletizer (2-3) is placed in first Heat Room (3-1) top, and secondary heat exchange room (3-2) is set to multi-stage heat exchanger room.
4. the flue gas multiple pollutant synergistic purification technique that blast-furnace cement sensible heat according to claim 1 is utilized, it is characterised in that：
The flue gas that the first Heat Room (3-1) and secondary heat exchange room (3-2) are heated is realized converging by secondary air-introduced machine (1-2).
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| CN108607341A (en) * | 2018-04-19 | 2018-10-02 | 杨清海 | A kind of collaboration treatment process of sintering flue gas pollutant removing and Btu utilization |
| CN111603913A (en) * | 2020-06-09 | 2020-09-01 | 周昊 | System and method for treating liquid slag discharging boiler waste gas of ozone denitration coal-fired power plant |
| CN111603931A (en) * | 2020-06-09 | 2020-09-01 | 周昊 | SCR denitration coal-fired power plant liquid slag discharge boiler waste gas treatment system and method |
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