CN105169943A - Integrated system for coke oven flue gas desulfurization and denitrification and waste heat recovery - Google Patents

Integrated system for coke oven flue gas desulfurization and denitrification and waste heat recovery Download PDF

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Publication number
CN105169943A
CN105169943A CN201510630517.3A CN201510630517A CN105169943A CN 105169943 A CN105169943 A CN 105169943A CN 201510630517 A CN201510630517 A CN 201510630517A CN 105169943 A CN105169943 A CN 105169943A
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China
Prior art keywords
flue
waste heat
coke oven
flour mill
denitration
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任毅
李东林
周礼
唐茂辉
陈洪会
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CHENGDU HUAXITANG INVESTMENT Co Ltd
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CHENGDU HUAXITANG INVESTMENT Co Ltd
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Abstract

The invention provides an integrated system for coke oven flue gas desulfurization and denitrification and waste heat recovery. The integrated system comprises a coke oven, a low-temperature SCR denitrification system, a waste heat boiler, a flue, a pulverizer, a filtering system and a chimney. The coke oven, the low-temperature SCR denitrification system, the waste heat boiler, the filtering system and the chimney are sequentially connected through the flue, a dry powder absorbent inlet is formed in the portion, between the waste heat boiler and the filtering system, of the flue and is connected with an outlet of the pulverizer through a pipeline, and an absorbent inlet is formed in the pulverizer. The system is free from waste water and gas emission and capable of directly carrying out denitrification without heating, absorbent can be used circularly, investment can be reduced, and energy can be saved.

Description

The integral system of a kind of coke oven flue exhuast gas desulfurization denitration and waste heat recovery
Technical field
The present invention relates to coke oven flue exhaust emission to control and heat recovery technology field, be specifically related to the integral system of a kind of coke oven flue exhuast gas desulfurization denitration and waste heat recovery.
Background technology
The pollutant of coke oven smoke stack emission, mainly containing SO 2, NO xand dust granules thing.Research shows, gas phase SO 2, NO xbe the presoma of PM2.5, dust granules thing is the main component of PM10, by SO 2, NO x, more than the amount of PM2.5 that changes of the presoma such as VOCs directly discharges, SO 2, NO xthe main matter forming haze and acid rain with dust granules thing.China SO in recent years 2, NO xdischarge capacity occupy first place in the world repeatly, atmosphere pollution and acid rain problem cause serious harm to human health and the ecosystem, become the key factor of restriction China sustainable development of socio-economy, government and society also reaches unprecedented height to its attention.
The SO of coke oven smoke stack emission 2be that in coke oven heating coal gas, contained sulphides burn produces, mainly comprise H in coke oven heating coke-stove gas 2s burns the SO generated 2; In coke oven heating coke-stove gas, organic sulfur burns the SO generated 2; Because coking furnace shaft blowby causes raw coke oven gas to enter combustion system, the SO that wherein contained sulphides burn generates 2.The SO discharged in coke oven flue waste gas 2according to the degree of each factory gas purification and the managerial skills of coke oven, generally at 100 ~ 600mg/m 3.
Combustion gas, when coke oven vertical flame path burns, can produce nitrogen oxide (NO x), nitrogen oxide refers to NO and NO usually 2mixture, the nitrogen oxide in air damages the ozone layer, and causes acid rain, contaminated environment.Research shows, at the NO that burning generates xin, NO accounts for 95%, NO 2be about 5%, NO is slowly converted into NO in an atmosphere 2.The NO of coke oven chimney exhaust gas discharge xconcentration is generally at 800 ~ 1200mg/m 3.
Soot particulate matter in coke-stove gas forms carbon black when heating, hydrocarbon pyrolysis in coke-stove gas also forms carbon black, the raw gas (containing tar and finely divided coal dust in raw gas) of coke furnace carbonization chamber effusion enters into combustion chamber, and the carbon granule concentration in the waste gas of formation can reach 100mg/m 3above.
On June 27th, 2012 national environmental protection portion and State Administration for Quality Supervision and Inspection and Quarantine jointly issued " coking chemistry emission of industrial pollutants standard " (GB16171-2012), require from 1 day January in 2015, existing enterprise perform " table 5 " regulation; From 1 day January in 2012, newly-built enterprise performed " table 5 " regulation; Area performs " table 6 " stricter regulation especially, and in GB16171-2012, " table 5 ", " table 6 " concrete regulation see the following form.
" table 5 ", " table 6 " coke oven chimney Air Pollutant Emission concentration limit in table 1GB16171-2012
Compared with the other industry stack gases such as power plant, flue gases of cock oven denitration has following characteristics:
1) flue gases of cock oven temperature is lower.By the impact of the factors such as the coke oven type of furnace, fuel type, operating duty, field management level, different coke-oven plants flue gases of cock oven temperature difference is very large, generally between 220-290 DEG C.Compare the flue-gas temperature of power plant 300-400 DEG C, flue gases of cock oven temperature is relatively low, if directly adopt power-plant flue gas denitration catalyst used to carry out denitration, denitration efficiency is low, is difficult to meet discharging standards requirement.
2) coke oven chimney must be in hot standby state all the time.Compared with power-plant flue gas, flue gases of cock oven must get back to coke oven smoke stack emission to air after desulphurization denitration, makes coke oven chimney be in hot standby state all the time.Effluent gas temperature after desulphurization denitration must higher than flue gas dew point temperature, and must not lower than 130 DEG C, otherwise cannot directly adopt the conventional Wet Flue Gas Desulfurization Technique of power plant to carry out flue gas desulfurization.
3) NO xcontent is higher.NO in coke-oven plant's flue gases of cock oven of current operation xcontent is 800-1200mg/Nm 3.
4) NH 3the control of escapement ratio is a difficult point.If adopt the NH that power plant is conventional 3-SCR method carries out denitration to flue gases of cock oven, because low-temperature denitration efficiency is lower, so the NH after denitration 3escape amount is difficult to meet discharging standards requirement.
5) independent coke-oven plant's employing coke-stove gas heating coke oven flue waste gas is moisture is about 20%.Adopt conventional wet lay sulfur removal technology to produce a large amount of waste water and form secondary pollution, adopt conventional lime dry desulfurization, form a large amount of solid secondary pollutions.
At present, the industries such as electric power, cement, glass are quite ripe to the treatment process of oxynitrides, but due to the coke oven flue EGT of coke-oven plant's discharge relatively low, NO xthe relatively high and SO of content 2content is relatively low, if adopt traditional denitrating technique, by the restriction of the factors such as stack gases temperature is low, must cannot meet coking industry NO xdischarge standard requirement.
As 201410088231.2, name is called the patent of invention of " a kind of low temperature coke oven flue gas desulfurization systems denitrating technique ", disclose low temperature coke oven flue gas desulfurization systems denitrating technique, this technique is prepared unit, denitration by air inducing unit, desulfurization unit, ammonia and is formed, by spraying into fluidised NaHCO in flue gas conveyance conduit except ammonia unit, compressed air unit, particle supply unit 3fine powder, the SO of the overwhelming majority in dry removal flue gas 2, denitrating catalyst structure sheaf is combined with except ammonia catalyst structure layer, the NO in efficient removal flue gases of cock oven simultaneously x, denitrating catalyst adopts filter bag shaped structure, except ammonia catalyst adopts V-shape structure.The first desulfurization of this patent, the soda powder that desulfurization produces will take low-temperature SCR device to coke oven flue waste gas, soda has strong toxic action to low-temperature SCR catalyst, and use residual coking ammonia water denitration, because residual coking ammonia water concentration is low, ammonia only containing 3g/L, also has the impurity such as oil, hydrogen sulfide, hydrogen cyanide, does not therefore reach the technological requirement that denitration uses ammonia.
201420259668.3, name is called the utility model patent of " coalitenessity furnace exhaust system for desulfuration and denitration ", disclose a kind of coalitenessity furnace exhaust system for desulfuration and denitration, heater with coke oven flue outlet is set, described heater outlet is communicated with SCR reactor, and is provided with ammonia-spraying grid between described heater and SCR reactor; Described SCR reactor outlet is communicated with desulfurizing tower through heat recovery boiler, and the exiting flue gas of described desulfurizing tower introduces smoke stack emission through air-introduced machine.This patent needs through operations such as heating, denitration, waste heat recovery, desulfurization, and desulfurization adopts conventional wet desulfurizing process, and system flow is complicated, and energy consumption is high, forms a large amount of waste water after wet desulphurization, produces secondary pollution.
201410087513.0, the patent of invention that name is called " a kind of low-temperature flue gas desulphurization denitration is except ammonia integral system ", discloses a kind of low-temperature flue gas desulphurization denitration except ammonia integral system, is applicable to flue-gas temperature and is greater than 180 DEG C, SO 2content is less than 150mg/Nm 3coke oven flue exhuast gas desulfurization denitration, according to fluidization principle first dry desulfurization before denitration, the ammonia that the remained ammonia adopting ammonia still process workshop section of coke-oven plant to produce is evaporated is as reducing agent, utilize cloth bag-except ammonia catalyst composite structure is as dedusting and denitration means, while high-efficiency desulfurization denitration, amount of ammonia slip can be controlled lower than discharging standards value.The first dry desulfurization of this patent, then denitration, by filter bag trapped particles thing, dry-desulphurizer alkaline matter residual in flue gas enters denitration section, denitrating catalyst can be caused poisoning, and there is denitration temperature low, reaction speed is slow simultaneously, catalyst amount is many, invests high, the problem that the escaping of ammonia rate is high.
201410119747.9, name is called the patent of invention of " a kind of method of coke oven flue waste gas heat utilization and purification ", its concrete operation step is as follows: 1) stack gases is first through waste gas residual heat recovery unit, the waste heat of stack gases is recovered, temperature is reduced to 100 DEG C ~ 150 DEG C, enter in low-temperature SCR desulphurization denitration unit subsequently, SO2 in flue gas is by coke adsorbing and removing, flue gas through desulfurization mixes with ammonia, take coke as the catalyst of SCR method, there is denitration reduction reaction, complete removing of NOx; 2) the coke supply in low-temperature SCR desulphurization denitration unit comes from the coke feed unit be made up of elevator and grader leveling blade conveyer, and the coke after denitration reduction reaction is expelled in coke basin, and timing is sent outside by outer row's vehicle; 3) flue gas that low-temperature SCR desulphurization denitration unit is discharged delivers to chimney after the whole clean unit udst separation of flue gas, realizes the qualified discharge of stack gases.This patent adopts activated coke/active carbon denitration efficiency low, bulky, and activated coke/regenerating active carbon amount is large, the high concentration SO of generation 2flue gas needs process further, and regeneration needs to reach 400 DEG C, needs to consume a large amount of energy (electricity or coal gas, fuel oil etc.), and energy consumption is high.
201410785779.2, name is called the patent of invention of " a kind of coke oven flue exhuast gas desulfurization denitrating technique ", disclose a kind of coke oven flue exhuast gas desulfurization denitrating technique, the dry desulfurizing process that the coke-stove gas used by coke oven heating first adopts desulfurizing tower to connect with adsorption tower removes sulfur-containing compound and impurity, under the effect of the coke oven flue waste gas that coke-stove gas after being purified produces in coke oven combustion at low temperature SCR denitration catalyst, then reclaim after heat through superheater tube waste heat circulation boiler removed the nitrogen oxide in stack gases by SCR reaction after and discharge.This patent when there is a large amount of blowby in coke oven, the SO in the coke oven flue waste gas of discharge 2the emission limit requirement that " coking chemistry emission of industrial pollutants standard " (GB16171-2012) specifies will do not reached.
In sum, coking industry also do not have in production application a kind of economy, reliably can disposable solution desulphurization and denitration, dedusting and waste heat recovery process system, therefore, technique and the device of developing a kind of desulfur denitrate dust collecting waste heat recovery for coke oven flue waste gas are very necessary.
Summary of the invention
The present invention in order to solve existing coke oven flue exhuast gas desulfurization denitration technology exist secondary pollution, operating cost is high, energy consumption is high, coke oven blowby SO 2the problem of discharge beyond standards, provides the integral system of a kind of coke oven flue exhuast gas desulfurization denitration and waste heat recovery.Coke oven flue waste gas, under the effect of low temperature SCR denitration system, reacts the nitrogen oxide removed in stack gases through SCR, reduce after coke oven flue gas temperature, by the SO in absorbent dry removal coke oven flue waste gas through waste heat boiler 2, then the particle of coke oven flue waste gas is removed by filtration system, finally reach the emission limit requirement that " coking chemistry emission of industrial pollutants standard " (GB16171-2012) specifies.
In order to realize foregoing invention object, the present invention adopts following technical scheme:
An integral system for coke oven flue exhuast gas desulfurization denitration and waste heat recovery, is characterized in that: comprise coke oven, low temperature SCR denitration system, waste heat boiler, flue, flour mill, filtration system, chimney; Described coke oven, low temperature SCR denitration system, waste heat boiler, filtration system are connected by flue successively with chimney, flue between described waste heat boiler and filtration system is provided with the import of dry powder absorbent, the import of dry powder absorbent is connected with the outlet of flour mill by pipeline, and described flour mill is provided with absorbent entrance.
Coke oven flue waste gas is under the effect of low temperature SCR denitration catalyst, there is SCR and react the nitrogen oxide removed in stack gases, after waste heat boiler recovery waste heat, by spraying the desulfurization of sodium backbone powder absorbent to stack gases, the emission limit requirement that stack gases after desulfurization after filter dedusting, finally reaches again " coking chemistry emission of industrial pollutants standard " (GB16171-2012) specifies.
The stack gases temperature that the present invention reclaims after heat through waste heat boiler is 140-160 DEG C, makes recovery waste heat many, and evaporation capacity is large, and exhaust gas temperature is low; Make follow-up dry desulfurization carry out at low temperatures simultaneously, contribute to improving desulfuration efficiency.
Integral system of the present invention is applicable to the content of sulfur dioxide≤500mg/Nm of coke oven flue gas 3.The too high performance that can affect catalyst of content of sulfur dioxide, reduces the denitration efficiency of SCR.
Low temperature SCR denitration system of the present invention to be temperature range the be SCR denitration system of 160 DEG C ~ 290 DEG C.Meet the feature that coke oven flue EGT is lower, do not need heating, energy consumption is low.Coke oven flue waste gas, by after recuperation of heat, sprays into the SO in absorbent powder absorption coke oven flue waste gas 2, finally by qualified discharge after the particle of filter removing coke oven flue waste gas.
Because flue gases of cock oven temperature is 220 ~ 290 DEG C, under this temperature conditions, carry out denitration reaction, the SCR catalyst at selecting 160 DEG C ~ 290 DEG C has very high denitration efficiency, and the escaping of ammonia rate is very low, can effectively by the NO in coke oven flue gas xbe converted into N 2, denitration efficiency is high.
Filtration system of the present invention is sack cleaner.
The concrete steps of dry desulfurization of the present invention are: sodium acid carbonate is pulverized through pulverizer, and sodium hydrogen carbonate powder excessive after pulverizing decomposes in high-temperature flue gas generates sodium carbonate, and sodium carbonate absorbs the SO in coke oven flue waste gas 2and SO 3, surface reaction generates Na 2sO 4and Na 2sO 3, flue gas carries the sodium sulphate of unreacted sodium carbonate and reaction generation by delivering to chimney qualified discharge through air-introduced machine after sack cleaner.
The product in flue gas after desulfurization is separated by sack cleaner, certain thickness filter course is formed on filter bag surface, this filter course is the mixed powder collected, and comprises sodium sulphate, sodium nitrate, sodium sulfite, natrium nitrosum, niter cake, sodium hydrogensulfite and dust etc.Na in filter course 2cO 3continue to react, by SO in coke oven flue waste gas with acidic gaseous pollutant in flue gas 2be reduced to and be less than 30mg/Nm 3.
Preferably, the product sent for regeneration absorbent that the dry desulfurization that sack cleaner is collected obtains or power plant desulfurization carry out secondary utilization.The product Na that dry method produces is comprised in powder 2sO 4and Na 2sO 3powder, delivers to recycling centre regeneration and obtains NaHCO3, recycles not outer row, does not form secondary pollution; Or product dry method produced is containing Na 2sO 4, Na 2sO 3powder delivers to lime desulfurization device, carries out secondary utilization for desulfurization.Meanwhile, the unreacted Na of part in desulfurization reaction product 2cO 3, again spray in coke oven flue waste gas by circulation, improve Na 2cO 3utilization ratio.
SCR of the present invention is reacted coking concentrated ammonia liquor that the reducing agent that uses produces for residual coking ammonia water ammonia still process and is obtained by refining.
Ammoniacal liquor after refining contains ammonia 16 ~ 26%, containing H 2s is less than 5mg/l, hydrogen cyanide is less than 5mg/l.
In the reducing agent of SCR of the present invention reaction, the amount of ammonia is 0.8 ~ 1.2 times with the mol ratio removing nitrogen oxide, can ensure that denitration efficiency can reduce the escaping of ammonia again.
Waste heat boiler of the present invention is heat pipe-type Natural Circulation HRSG.Amount of steam withdrawn can reach 100kg/t coke, realizes energy-conservation object; On the other hand, the design of outlet cigarette temperature is lower, and the design of economizer caloric receptivity is comparatively large, and make recovery waste heat many, evaporation capacity is large, and exhaust gas temperature can lower than 160 DEG C.
Sodium backbone powder absorbent of the present invention is sodium acid carbonate, utilizes the SO in Dry sodium bicarbonate removing coke oven flue waste gas 2.
Flue between waste heat boiler of the present invention and the import of dry powder absorbent is provided with exhanst gas outlet, and exhanst gas outlet is communicated with the import of dry powder absorbent by auxiliary flue, and described flour mill is arranged in auxiliary flue.
Part of smoke enters auxiliary flue through exhanst gas outlet, is called air-supply flue gas, and another part flue gas continues to stay flue.Dry powder absorbent enters flue through auxiliary flue with flue gas of blowing for carrier.Absorbent is pulverized while, and carry out reacting and obtaining primary mixture with air-supply flue gas, the absorbent in this primary mixture has activity because of reaction, and after being sent to flue, its denitrification efficiency is also improved, and practical effect is good.
Flour mill of the present invention is airflow milling, and airflow milling disposal ability is large, dry powder absorbent particle diameter can be milled to and be less than 1 μm, be beneficial to raising denitrification efficiency; Connect grader after flour mill, the front end of flour mill or the rear end of grader are provided with high-pressure suction fan, ensure the particle diameter of dry powder absorbent; Flour mill is provided with air duct.The spatial dispersion utilizing air-flow to drive absorbent in flour mill and turbulence, can realize the pulverizing of absorbent equally, operate very flexible.
Preferably, in described flue, be provided with static mixer, make dry powder absorbent and flue gas mix evenly, the abundant mixing improving primary mixture and flue gas with contact.Described static mixer form is venturi type, diffusion tubular type, spiral, grating type, baffle-type etc.
Preferably, described exhanst gas outlet is provided with booster fan.
The front end of chimney of the present invention is provided with air-introduced machine.
Compared with prior art, the invention has the beneficial effects as follows:
1, the present invention is by SCR denitration system and dry method desulfuration system coupling, and the simple superposition of non-traditional systems, and after SCR denitration, the sulphur nitrogen ratio in flue gas increases considerably, improve greatly dry powder jet segment denitration efficiency; And be separated the product in flue gas after desulfurization by sack cleaner, the time of staying of prolong smoke, form certain thickness filter course, unreacted Na in filter course on filter bag surface 2cO 3continue to react with acidic gaseous pollutant in flue gas, define the desulfurized effect of fixed bed, achieve further desulfurization, by SO in coke oven flue waste gas 2be reduced to and be less than 30mg/Nm 3.
2, the prior art of coke oven flue exhuast gas desulfurization denitration generally uses power plant's High-temperature scr catalyst, and efficiency is low, and the complete ammonia of unreacted is high; The present invention is 220 ~ 290 DEG C according to flue gases of cock oven temperature, and the low temperature SCR denitration system at selecting 160 DEG C ~ 290 DEG C, meets the feature that coke oven flue EGT is lower, and do not need heating, energy consumption is low.Not only directly can carry out denitration reaction to flue gases of cock oven, also have very high denitration efficiency, the escaping of ammonia rate is very low, can effectively by the NO in coke oven flue gas xbe converted into N 2, denitration efficiency is high.Coke oven flue waste gas, by after recuperation of heat, sprays into the SO in absorbent powder absorption coke oven flue waste gas 2, finally by qualified discharge after the particle of filter removing coke oven flue waste gas.
3, adopt concentration that in coke-oven plant gas purification ammonia still process workshop section, remained ammonia ammonia still process produces be about 16% ~ 20% coking concentrated ammonia liquor or liquefied ammonia as the raw materials of reducing agent, coking ammonia water is refined the requirement reaching the reducing agent that SCR catalytic reduction uses, utilize the ammoniacal liquor of self, storage, transport are just very simple, achieve and reduce denitration expense, reduce investment, the coke-oven plant of 1,000,000 tons/year saves about 1,400,000.
4, the present invention adopts heat pipe-type Natural Circulation HRSG to reclaim heat after SCR denitration, alleviates the corrosion of boiler.On the one hand, heat pipe waste heat circulation boiler is except drum belongs to pressure vessel, and remaining part does not belong to pressure vessel, when heat pipe equipment goes wrong, water can not go to stack gases side, does not affect the normal operation that coking is produced, for coking system, security is high; On the other hand, while pollutant catabolic gene, reclaim the heat of flue gases of cock oven, make enterprise's some income while pollution administration thing, while obtaining environmental benefit, obtain economic benefit, reduce the expense that enterprise governance is polluted; In addition, the design of natural-circulation evaporator outlet cigarette temperature is lower, and the design of economizer caloric receptivity is comparatively large, and make recovery waste heat many, evaporation capacity is large, and exhaust gas temperature, lower than 160 DEG C, contributes to improving dry desulfurization efficiency.
5, coke oven flue exhuast gas desulfurization generally uses wet desulfurization system at present, and the general flow process of system is complicated, and energy consumption is high, forms a large amount of waste water after wet desulphurization, produces secondary pollution.The present invention adopts dry method desulfuration system to be removed by the sulfide in coke oven flue waste gas, sodium base absorbant significant desulfurization effect, and desulfurization product obtains sodium acid carbonate by regeneration recycles outer row, do not form secondary pollution, or desulfurization product is delivered to lime desulfurization device and carry out secondary utilization; Flue gas does not need heating, and directly can carry out desulfurization, desulfuration efficiency can reach highest standard (table 6) SO that GB16171-2012 specifies 2<30mg/m 3, both reduced investment, in turn saved the energy.
6, the powder collected by filtration system after inventive desulfurization is siccative, is convenient to collect, transport and focus on, and there is not secondary pollution, full technique is without waste water, toxic emission.Traditional wet desulphurization needs spray cooling to be humidified, and outlet purifying smoke is saturated flue gas, and in former flue gas, water content is usually not enough, thus needs to consume a large amount of water resources for technique moisturizing.Native system is pure dry method, does not have the process that spray cooling is humidified, and does not need additionally to supplement fresh water (FW), not water consumption, reduces the risk of equipment corrosion.Waste desulfurizing agent can utilize by secondary, renewable process after discarded SCR catalyst reclaims.
Accompanying drawing explanation
Fig. 1 is the structure chart of the integral system of coke oven flue exhuast gas desulfurization denitration of the present invention and waste heat recovery.
Fig. 2 is the structure chart of embodiment of the present invention 8-12.
Be labeled as in figure: 1, coke oven, 2, low temperature SCR denitration system, 3, waste heat boiler, 4, filtration system, 5, air-introduced machine, 6, chimney, 7, flour mill, 8, static mixer, 9, auxiliary flue, 10, flue.
Detailed description of the invention
Below in conjunction with detailed description of the invention, essentiality content of the present invention is described in further detail.
Embodiment 1
An integral system for coke oven flue exhuast gas desulfurization denitration and waste heat recovery, comprises coke oven 1, low temperature SCR denitration system 2, waste heat boiler 3, flue 10, flour mill 7, filtration system 4, chimney 6; Described coke oven 1, low temperature SCR denitration system 2, waste heat boiler 3, filtration system 4 are connected by flue 10 successively with chimney 6, flue 10 between described waste heat boiler 3 and filtration system 4 is provided with the import of dry powder absorbent, the import of dry powder absorbent is connected by the outlet of pipeline with flour mill 7, and described flour mill 7 is provided with absorbent entrance.
The present invention adopts coke oven flue gas low temperature SCR denitration+dry method desulfuration system, and prior art generally adopts coke oven flue gas semi-dry desulphurization+low temperature SCR denitration system, specifically compares in table 1:
The integral system situation compared with the prior art of the denitration of table 1. inventive desulfurization and waste heat recovery
Embodiment 2
An integral system for coke oven flue exhuast gas desulfurization denitration and waste heat recovery, comprises coke oven 1, low temperature SCR denitration system 2, waste heat boiler 3, flue 10, flour mill 7, filtration system 4, chimney 6; Described coke oven 1, low temperature SCR denitration system 2, waste heat boiler 3, filtration system 4 are connected by flue 10 successively with chimney 6, flue 10 between described waste heat boiler 3 and filtration system 4 is provided with the import of dry powder absorbent, the import of dry powder absorbent is connected by the outlet of pipeline with flour mill 7, and described flour mill 7 is provided with absorbent entrance.
Described waste heat boiler 3 is heat pipe Natural Circulation HRSG, and prior art generally adopts chimney flue type water pipe Natural Circulation HRSG, specifically compares in table 2:
Table 2. heat pipe Natural Circulation and chimney flue type water pipe Natural Circulation HRSG comparable situation
Embodiment 3
An integral system for coke oven flue exhuast gas desulfurization denitration and waste heat recovery, comprises coke oven 1, low temperature SCR denitration system 2, waste heat boiler 3, flue 10, flour mill 7, filtration system 4, chimney 6; Described coke oven 1, low temperature SCR denitration system 2, waste heat boiler 3, filtration system 4 are connected by flue 10 successively with chimney 6, flue 10 between described waste heat boiler 3 and filtration system 4 is provided with the import of dry powder absorbent, the import of dry powder absorbent is connected by the outlet of pipeline with flour mill 7, and described flour mill 7 is provided with absorbent entrance.
Described low temperature SCR denitration system 2 for temperature range be the SCR denitration system of 160 DEG C ~ 290 DEG C.
Embodiment 4
An integral system for coke oven flue exhuast gas desulfurization denitration and waste heat recovery, comprises coke oven 1, low temperature SCR denitration system 2, waste heat boiler 3, flue 10, flour mill 7, filtration system 4, chimney 6; Described coke oven 1, low temperature SCR denitration system 2, waste heat boiler 3, filtration system 4 are connected by flue 10 successively with chimney 6, flue 10 between described waste heat boiler 3 and filtration system 4 is provided with the import of dry powder absorbent, the import of dry powder absorbent is connected by the outlet of pipeline with flour mill 7, and described flour mill 7 is provided with absorbent entrance.
Described low temperature SCR denitration system 2 for temperature range be the SCR denitration system of 160 DEG C ~ 290 DEG C.
Described filtration system 4 is sack cleaner.
Embodiment 5
An integral system for coke oven flue exhuast gas desulfurization denitration and waste heat recovery, comprises coke oven 1, low temperature SCR denitration system 2, waste heat boiler 3, flue 10, flour mill 7, filtration system 4, chimney 6; Described coke oven 1, low temperature SCR denitration system 2, waste heat boiler 3, filtration system 4 are connected by flue 10 successively with chimney 6, flue 10 between described waste heat boiler 3 and filtration system 4 is provided with the import of dry powder absorbent, the import of dry powder absorbent is connected by the outlet of pipeline with flour mill 7, and described flour mill 7 is provided with absorbent entrance.
Described low temperature SCR denitration system 2 for temperature range be the SCR denitration system of 160 DEG C ~ 290 DEG C.
Described filtration system 4 is sack cleaner.
Content of sulfur dioxide≤the 500mg/Nm of coke oven flue waste gas of the present invention 3.
Embodiment 6
An integral system for coke oven flue exhuast gas desulfurization denitration and waste heat recovery, comprises coke oven 1, low temperature SCR denitration system 2, waste heat boiler 3, flue 10, flour mill 7, filtration system 4, chimney 6; Described coke oven 1, low temperature SCR denitration system 2, waste heat boiler 3, filtration system 4 are connected by flue 10 successively with chimney 6, flue 10 between described waste heat boiler 3 and filtration system 4 is provided with the import of dry powder absorbent, the import of dry powder absorbent is connected by the outlet of pipeline with flour mill 7, and described flour mill 7 is provided with absorbent entrance.
Described low temperature SCR denitration system 2 for temperature range be the SCR denitration system of 160 DEG C ~ 290 DEG C.
Described filtration system 4 is sack cleaner.
Content of sulfur dioxide≤the 500mg/Nm of coke oven flue waste gas of the present invention 3.
The stack gases temperature reclaimed after heat through waste heat boiler is 140-160 DEG C.
Embodiment 7
An integral system for coke oven flue exhuast gas desulfurization denitration and waste heat recovery, comprises coke oven 1, low temperature SCR denitration system 2, waste heat boiler 3, flue 10, flour mill 7, filtration system 4, chimney 6; Described coke oven 1, low temperature SCR denitration system 2, waste heat boiler 3, filtration system 4 are connected by flue 10 successively with chimney 6, flue 10 between described waste heat boiler 3 and filtration system 4 is provided with the import of dry powder absorbent, the import of dry powder absorbent is connected by the outlet of pipeline with flour mill 7, and described flour mill 7 is provided with absorbent entrance.
Described low temperature SCR denitration system 2 for temperature range be the SCR denitration system of 160 DEG C ~ 290 DEG C.
Described filtration system 4 is sack cleaner.
Content of sulfur dioxide≤the 500mg/Nm of coke oven flue waste gas of the present invention 3.
The stack gases temperature reclaimed after heat through waste heat boiler is 140-160 DEG C.
Described waste heat boiler 3 is heat pipe-type Natural Circulation HRSG.
Embodiment 8
An integral system for coke oven flue exhuast gas desulfurization denitration and waste heat recovery, comprises coke oven 1, low temperature SCR denitration system 2, waste heat boiler 3, flue 10, flour mill 7, filtration system 4, chimney 6; Described coke oven 1, low temperature SCR denitration system 2, waste heat boiler 3, filtration system 4 are connected by flue 10 successively with chimney 6, flue 10 between described waste heat boiler 3 and filtration system 4 is provided with the import of dry powder absorbent, the import of dry powder absorbent is connected by the outlet of pipeline with flour mill 7, and described flour mill 7 is provided with absorbent entrance.
Described low temperature SCR denitration system 2 for temperature range be the SCR denitration system of 160 DEG C ~ 290 DEG C.
Described filtration system 4 is sack cleaner.
Content of sulfur dioxide≤the 500mg/Nm of coke oven flue waste gas of the present invention 3.
The stack gases temperature reclaimed after heat through waste heat boiler is 140-160 DEG C.
Described waste heat boiler 3 is heat pipe-type Natural Circulation HRSG.
Flue 10 between described waste heat boiler 3 and the import of dry powder absorbent is provided with exhanst gas outlet, and exhanst gas outlet is communicated with the import of dry powder absorbent by auxiliary flue 9, and described flour mill 7 is arranged in auxiliary flue 9.
The front end of described chimney 6 is provided with air-introduced machine 5.
Embodiment 9
An integral system for coke oven flue exhuast gas desulfurization denitration and waste heat recovery, comprises coke oven 1, low temperature SCR denitration system 2, waste heat boiler 3, flue 10, flour mill 7, filtration system 4, chimney 6; Described coke oven 1, low temperature SCR denitration system 2, waste heat boiler 3, filtration system 4 are connected by flue 10 successively with chimney 6, flue 10 between described waste heat boiler 3 and filtration system 4 is provided with the import of dry powder absorbent, the import of dry powder absorbent is connected by the outlet of pipeline with flour mill 7, and described flour mill 7 is provided with absorbent entrance.
Described low temperature SCR denitration system 2 for temperature range be the SCR denitration system of 160 DEG C ~ 290 DEG C.
Described filtration system 4 is sack cleaner.
Content of sulfur dioxide≤the 500mg/Nm of coke oven flue waste gas of the present invention 3.
The stack gases temperature reclaimed after heat through waste heat boiler is 140-160 DEG C.
Described waste heat boiler 3 is heat pipe-type Natural Circulation HRSG.
Flue 10 between described waste heat boiler 3 and the import of dry powder absorbent is provided with exhanst gas outlet, and exhanst gas outlet is communicated with the import of dry powder absorbent by auxiliary flue 9, and described flour mill 7 is arranged in auxiliary flue 9.
The front end of described chimney 6 is provided with air-introduced machine 5.
Connect grader after described flour mill 7, the front end of flour mill 7 or the rear end of grader are provided with high-pressure suction fan.
Embodiment 10
An integral system for coke oven flue exhuast gas desulfurization denitration and waste heat recovery, comprises coke oven 1, low temperature SCR denitration system 2, waste heat boiler 3, flue 10, flour mill 7, filtration system 4, chimney 6; Described coke oven 1, low temperature SCR denitration system 2, waste heat boiler 3, filtration system 4 are connected by flue 10 successively with chimney 6, flue 10 between described waste heat boiler 3 and filtration system 4 is provided with the import of dry powder absorbent, the import of dry powder absorbent is connected by the outlet of pipeline with flour mill 7, and described flour mill 7 is provided with absorbent entrance.
Described low temperature SCR denitration system 2 for temperature range be the SCR denitration system of 160 DEG C ~ 290 DEG C.
Described filtration system 4 is sack cleaner.
Content of sulfur dioxide≤the 500mg/Nm of coke oven flue waste gas of the present invention 3.
The stack gases temperature reclaimed after heat through waste heat boiler is 140-160 DEG C.
Described waste heat boiler 3 is heat pipe-type Natural Circulation HRSG.
Flue 10 between described waste heat boiler 3 and the import of dry powder absorbent is provided with exhanst gas outlet, and exhanst gas outlet is communicated with the import of dry powder absorbent by auxiliary flue 9, and described flour mill 7 is arranged in auxiliary flue 9.
Connect grader after described flour mill 7, the front end of flour mill 7 or the rear end of grader are provided with high-pressure suction fan.
The front end of described chimney 6 is provided with air-introduced machine 5.
Described exhanst gas outlet is provided with booster fan; Described dry powder absorbent import department is provided with static mixer 3.
Embodiment 11
An integral system for coke oven flue exhuast gas desulfurization denitration and waste heat recovery, comprises coke oven 1, low temperature SCR denitration system 2, waste heat boiler 3, flue 10, flour mill 7, filtration system 4, chimney 6; Described coke oven 1, low temperature SCR denitration system 2, waste heat boiler 3, filtration system 4 are connected by flue 10 successively with chimney 6, flue 10 between described waste heat boiler 3 and filtration system 4 is provided with the import of dry powder absorbent, the import of dry powder absorbent is connected by the outlet of pipeline with flour mill 7, and described flour mill 7 is provided with absorbent entrance.
Described low temperature SCR denitration system 2 for temperature range be the SCR denitration system of 160 DEG C ~ 290 DEG C.
Described filtration system 4 is sack cleaner.
Content of sulfur dioxide≤the 500mg/Nm of coke oven flue waste gas of the present invention 3.
The stack gases temperature reclaimed after heat through waste heat boiler is 140-160 DEG C.
Described waste heat boiler 3 is heat pipe-type Natural Circulation HRSG.
Flue 10 between described waste heat boiler 3 and the import of dry powder absorbent is provided with exhanst gas outlet, and exhanst gas outlet is communicated with the import of dry powder absorbent by auxiliary flue 9, and described flour mill 7 is arranged in auxiliary flue 9.
The front end of described chimney 6 is provided with air-introduced machine 5.
Connect grader after described flour mill 7, the front end of flour mill 7 or the rear end of grader are provided with high-pressure suction fan.
Described exhanst gas outlet is provided with booster fan; Described dry powder absorbent import department is provided with static mixer 3.
Described flour mill 7 is airflow milling, and is provided with air duct.
Sodium backbone powder absorbent of the present invention is sodium acid carbonate, utilizes the SO in Dry sodium bicarbonate removing coke oven flue waste gas 2.
Dry-desulphurizer after the use that described sack cleaner is collected, after pulverizing, spray into flue continue to participate in desulfurization, returning charge and virgin material ratio are 5 ~ 50:1.
Embodiment 12
An integral system for coke oven flue exhuast gas desulfurization denitration and waste heat recovery, comprises coke oven 1, low temperature SCR denitration system 2, waste heat boiler 3, flue 10, flour mill 7, filtration system 4, chimney 6; Described coke oven 1, low temperature SCR denitration system 2, waste heat boiler 3, filtration system 4 are connected by flue 10 successively with chimney 6, flue 10 between described waste heat boiler 3 and filtration system 4 is provided with the import of dry powder absorbent, the import of dry powder absorbent is connected by the outlet of pipeline with flour mill 7, and described flour mill 7 is provided with absorbent entrance.
Described low temperature SCR denitration system 2 for temperature range be the SCR denitration system of 160 DEG C ~ 290 DEG C.
Described filtration system 4 is sack cleaner.
Content of sulfur dioxide≤the 500mg/Nm of coke oven flue waste gas of the present invention 3.
The front end of described chimney 6 is provided with air-introduced machine 5.
Described waste heat boiler 3 is heat pipe-type Natural Circulation HRSG.
Flue 10 between described waste heat boiler 3 and the import of dry powder absorbent is provided with exhanst gas outlet, and exhanst gas outlet is communicated with the import of dry powder absorbent by auxiliary flue 9, and described flour mill 7 is arranged in auxiliary flue 9.
Described flour mill 7 is airflow milling, and is provided with air duct; Connect grader after flour mill 7, the front end of flour mill 7 or the rear end of grader are provided with high-pressure suction fan.
Described exhanst gas outlet is provided with booster fan; Described dry powder absorbent import department is provided with static mixer 3.
Sodium backbone powder absorbent of the present invention is sodium acid carbonate, utilizes the SO in Dry sodium bicarbonate removing coke oven flue waste gas 2.
Dry-desulphurizer after the use that described sack cleaner is collected, after pulverizing, spray into flue continue to participate in desulfurization, returning charge and virgin material ratio are 5 ~ 50:1.

Claims (10)

1. an integral system for coke oven flue exhuast gas desulfurization denitration and waste heat recovery, is characterized in that: comprise coke oven (1), low temperature SCR denitration system (2), waste heat boiler (3), flue (10), flour mill (7), filtration system (4), chimney (6); Described coke oven (1), low temperature SCR denitration system (2), waste heat boiler (3), filtration system (4) are connected by flue (10) successively with chimney (6), flue (10) between described waste heat boiler (3) and filtration system (4) is provided with the import of dry powder absorbent, the import of dry powder absorbent is connected by the outlet of pipeline with flour mill (7), and described flour mill (7) is provided with absorbent entrance.
2. the integral system of a kind of coke oven flue exhuast gas desulfurization denitration according to claim 1 and waste heat recovery, is characterized in that: described low temperature SCR denitration system (2) for temperature range be the SCR denitration system of 160 DEG C ~ 290 DEG C.
3. the integral system of a kind of coke oven flue exhuast gas desulfurization denitration according to claim 1 and waste heat recovery, is characterized in that: described filtration system (4) is sack cleaner.
4. the integral system of a kind of coke oven flue exhuast gas desulfurization denitration according to claim 1 and waste heat recovery, is characterized in that: described integral system is applicable to the content of sulfur dioxide≤500mg/Nm of coke oven flue gas 3.
5. the integral system of a kind of coke oven flue exhuast gas desulfurization denitration according to claim 1 and waste heat recovery, is characterized in that: the stack gases temperature reclaimed after heat through waste heat boiler is 140-160 DEG C.
6. the integral system of a kind of coke oven flue exhuast gas desulfurization denitration according to claim 1 and waste heat recovery, is characterized in that: described waste heat boiler (3) is heat pipe-type Natural Circulation HRSG.
7. the integral system of a kind of coke oven flue exhuast gas desulfurization denitration according to claim 1 and waste heat recovery, it is characterized in that: the flue (10) between described waste heat boiler (3) and the import of dry powder absorbent is provided with exhanst gas outlet, exhanst gas outlet is communicated with the import of dry powder absorbent by auxiliary flue (9), and described flour mill (7) is arranged in auxiliary flue (9).
8. the integral system of a kind of coke oven flue exhuast gas desulfurization denitration according to claim 1 and waste heat recovery, is characterized in that: the front end of described chimney (6) is provided with air-introduced machine (5).
9. the integral system of a kind of coke oven flue exhuast gas desulfurization denitration according to claim 1 and waste heat recovery, is characterized in that: described exhanst gas outlet is provided with booster fan; Described dry powder absorbent import department is provided with static mixer (3).
10. a kind of dry type flue gas desulfurizing denitration dust collecting integral cleaning system according to claim 1, is characterized in that: described flour mill (7) is airflow milling, and is provided with air duct; Connect grader after flour mill (7), the front end of flour mill (7) or the rear end of grader are provided with high-pressure suction fan.
CN201510630517.3A 2015-09-29 2015-09-29 Integrated system for coke oven flue gas desulfurization and denitrification and waste heat recovery Pending CN105169943A (en)

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