CN105797581A - System and process for utilizing coke oven flue gas desulfurization and denitrification waste heat - Google Patents
System and process for utilizing coke oven flue gas desulfurization and denitrification waste heat Download PDFInfo
- Publication number
- CN105797581A CN105797581A CN201610391156.6A CN201610391156A CN105797581A CN 105797581 A CN105797581 A CN 105797581A CN 201610391156 A CN201610391156 A CN 201610391156A CN 105797581 A CN105797581 A CN 105797581A
- Authority
- CN
- China
- Prior art keywords
- flue gas
- waste heat
- coke oven
- module
- scr denitration
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Pending
Links
Classifications
-
- 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
- B01D53/8637—Simultaneously removing sulfur oxides and nitrogen oxides
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/46—Removing components of defined structure
- B01D53/60—Simultaneously removing sulfur oxides and nitrogen oxides
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
- B01D53/81—Solid phase processes
- B01D53/82—Solid phase processes with stationary reactants
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
- C10B57/00—Other carbonising or coking processes; Features of destructive distillation processes in general
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2257/00—Components to be removed
- B01D2257/30—Sulfur compounds
- B01D2257/302—Sulfur oxides
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2257/00—Components to be removed
- B01D2257/40—Nitrogen compounds
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2258/00—Sources of waste gases
- B01D2258/02—Other waste gases
- B01D2258/0283—Flue gases
-
- 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
- Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
- Y02A50/00—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE in human health protection, e.g. against extreme weather
- Y02A50/20—Air quality improvement or preservation, e.g. vehicle emission control or emission reduction by using catalytic converters
-
- 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
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
- Y02P20/129—Energy recovery, e.g. by cogeneration, H2recovery or pressure recovery turbines
Abstract
The invention provides a system and process for utilizing coke oven flue gas desulfurization and denitrification waste heat. The process includes: allowing flue gas to enter an SCR denitrification reactor to react with the reducing agent, allowing the flue gas after the reaction to enter a waste heat boiler module for heat exchanging, controlling the module to allow the temperature of the flue gas to be 160-180 DEG C, allowing the flue gas to enter a magnesium desulfurization module for desulfurization, and discharging, wherein the SCR denitrification reactor is connected with an inlet flue, a guide plate is arranged at the turning part of the flue, a rectifying grating is arranged on the upper portion in an SCR denitrification reactor shell, a catalyst layer is arranged below the rectifying grating, and a steam soot blower is arranged between the rectifying grating and the catalyst layer; the catalyst is a vanadium-titanium-based catalyst and/or a rare-earth-system low-temperature catalyst; volume velocity is controlled to be 5000-8000m<3>/m<3>. H, and flue gas speed is controlled to be 3-10m/s; the waste heat boiler module is a heat pipe waste heat boiler. The process has the advantages that the nitrogen oxide and sulfide in the coke oven flue gas are removed successfully, the flue gas waste heat is utilized to the maximum extent, and the economy of the system is increased.
Description
Technical field
The present invention relates to flue gas desulfurization and denitrification UTILIZATION OF VESIDUAL HEAT IN technique and system, particular for coke oven flue gas desulphurization denitration UTILIZATION OF VESIDUAL HEAT IN technique and system.
Background technology
Many ground, north severe haze weather that especially Beijing-tianjin-hebei Region often occurs in recent years, this atmospheric pollution growed in intensity has had been subjected to the extensive concern of country and the whole society, and effective control atmosphere pollution has become as common recognition and the expectation of all circles.
During ten two five to ten three five, China puts into effect and have modified substantial amounts of existing environmental regulation so that each field air pollution emission standard is all increasingly strict.Under this overall background, the coking industry being before substantially in unordered emissions status has been also affected by concerns many especially.Chinese Ministry of Environmental Protection promulgated new " coking chemistry industrial pollution discharge standard " (GB16171-2012) in 2012, specified in new standard, and from 1 day January in 2015, all enterprises all should perform according to new atmospheric emission standard.This just requires that the new desulphurization denitration facility of each coal chemical enterprise construction is to ensure the qualified discharge of flue gas.But the system for desulfuration and denitration that in prior art, a kind of maturation is not energy-efficient and technique to solve this technical problem perfectly.
CN104923046A discloses a kind of coke oven flue gas desulphurization and denitration and waste heat recovery integral method, and the system that the method adopts includes heating furnace, denitrification apparatus, waste-heat recovery device, supplies ammonia system, desulfurizer, thiamine recovery device etc..Flue gas from coke oven initially enters heating furnace and is heated to 300～400 DEG C, enters back into denitrification apparatus, utilizes the nitrogen oxides in denitrification reducing agent and denitrating catalyst elimination flue gas；Denitrification reducing agent is ammonia；Denitrification apparatus flue gas out reclaims heat through waste-heat recovery device and is cooled to 100～150 DEG C, enters back into the sulfur dioxide in ammonia desulfuration equipment elimination flue gas.This technology has to use for heating furnace by flue gas to 300～400 DEG C, and this process needs to consume the substantial amounts of energy, not only needs substantial amounts of actual motion cost, simultaneously whether increase electric consumption or gas consumption, itself is namely again create pollution course.Additionally, the ammonia process of desulfurization by-product recovery efficiency in this technique is low, economic worth is low, causes the wasting of resources and economic rationality not good enough.Further, this technique is not provided with the system that can cross pressure match to ensure original flue negative pressure state, it is difficult to reply coke oven is for the rigors of flue gas system pressure and high security requirement.
CN203816509U discloses a kind of coalitenessity furnace exhaust system for desulfuration and denitration, this system includes arranging the heater with coke oven flue outlet, described heater outlet connects with SCR reactor, and is provided with ammonia-spraying grid between described heater and SCR reactor；Described SCR reactor outlet connects with desulfurizing tower through heat recovery boiler, and the exiting flue gas of described desulfurizing tower introduces smoke stack emission through air-introduced machine.Identical with CN104923046A, this case there is also the technical problem needing mass energy to add hot waste gas so that system energy consumption is high, operation cost is significantly increased while causing secondary environmental pollution.Additionally, this technique is also not provided with the system that can cross pressure match to ensure original flue negative pressure state, it is difficult to reply coke oven is for the rigors of flue gas system pressure and high security requirement.
Enterprise has or intends in system and the technique of employing at home, owing to being subject to the restriction of process or catalysts conditions, it is common to there are four problems: one is that denitrating technique efficiency is low, it is impossible to adapt to the needs that coke oven produces completely；Two is generally need flue gas is heated, and produces substantial amounts of energy resource consumption, causes the waste of the energy；Three is that technological process is not reasonable smooth and easy, is not consistent with reacting the optimal case carrying out principle；Four is cannot the safety of effective guarantee coke oven flue gas system.Therefore, develop and a kind of can either ensure that coke oven production safety can complete again the technique of desulphurization denitration waste heat recovery and system is that those skilled in the art need badly and one of solve the technical problem that energy-efficiently.
Summary of the invention
Present invention is primarily targeted at a kind of method providing coke oven flue gas desulphurization denitration and waste heat recovery, the method can complete desulphurization denitration waste heat recovery and by-product utilized energy-efficiently, makes the discharge of coke oven flue gas reach the requirement of GB16171-2012.
Another object of the present invention is to provide the system of a kind of coke oven flue gas desulphurization denitration and waste heat recovery, the inventive method adopts this system can while the production safety of effective guarantee denitration sulfur removal technology, complete desulphurization denitration waste heat recovery and by-product utilized energy-efficiently, make the discharge of coke oven flue gas reach the requirement of GB16171-2012.
For achieving the above object, on the one hand, the present invention provides a kind of method of coke oven flue gas desulphurization denitration and waste heat recovery, and described method includes: make 180～300 DEG C and SO2Concentration is lower than 1500mg/Nm3Coke oven flue gas enter SCR denitration reactor and reducing agent and react elimination nitrogen oxides, after reaction, flue gas entrance waste heat boiler module carries out heat exchange, controlling the temperature of flue gas after waste heat boiler module makes heat exchange is 160～180 DEG C, discharges after making it into magnesium processes desulfurizer scrubbing CO_2 subsequently；
The entrance of described SCR denitration reactor connects inlet flue duct, this inlet flue duct turning arranges deflector, described SCR denitration reactor includes housing, this housing internal upper part arranges flow straightening grid, this flow straightening grid is arranged below catalyst layer, arranges steam sootblower between described flow straightening grid and described catalyst layer；
The catalyst used in described SCR denitration reactor is vanadium Ti-base catalyst and/or rare-earth system low temperature catalyst；This catalyst can make SO2Conversion ratio is not more than 1%, and makes the denitration efficiency of the coke oven flue gas of 180～300 DEG C be not less than 70%；
It is 5000～8000m that described method controls volume space velocity in SCR denitration reactor3/m3.h；And the speed controlling to enter the coke oven flue gas of described SCR denitration reactor is 3～10m/s；
Described waste heat boiler module is can heat the heat pipe waste heat boiler of water and air with heat smoke for thermal source simultaneously；Controlling the flow of water and air makes after heat exchange the temperature of flue gas at 160～180 DEG C.
The present invention is by selecting existing catalyst, SCR denitration reactor increases deflector and strengthens the mixing of coke oven flue gas and reducing agent, flow straightening grid is set, adopt steam sootblower to substitute the acoustic wave ash ejector used in prior art and avoid the impurity such as the tar impact on system entrained in flue gases of cock oven, the temperature of flue gas after adopting heat pipe waste heat boiler to replace shell-and-tube exhaust-heat boiler of the prior art and utilize its control heat exchange, control the volume space velocity in technique and the speed of coke oven flue gas entrance, it is reasonable that final present invention process arranges, not only successfully remove the nitrogen oxides in coke oven flue gas and sulfide, discharge reaches the requirement of GB16171-2012, utilize fume waste heat to greatest extent simultaneously, the economy of raising system.
Heat pipe waste heat boiler of the present invention is to adopt the heat smoke after denitration as thermal source, adds hot water and air simultaneously.The temperature of the flue gas after denitration, generally at about 170～290 DEG C, uses this heat pipe waste heat boiler WATER AS FLOW MEDIUM heating can be produced saturated vapor, and this WATER AS FLOW MEDIUM can be industrial soft water, utilizes this flue gas can be heated by air for thermal source simultaneously.Adopt this heat pipe waste heat boiler can the heat of heat smoke after efficient recovery denitration, make the energy effectively utilize, and also can make recovered after denitration flue gas be content with very little the requirement of sulfur removal technology.
In the method for the invention one detailed description of the invention, controlling to enter the flow velocity of flue gas in magnesium processes desulfurization module is 2～9m/s, and the liquid-gas ratio of spray slurry and this flue gas is 2～8L:1m3, make smog discharge temperature more than 80 DEG C；Described spray slurry is MgO aqueous solution.By controlling the desulfurization degree of the magnesium processes desulfurizer that this technological parameter makes up to more than 98%.
In the method for the invention one detailed description of the invention, the temperature of described coke oven flue gas is 200～250 DEG C, comprises 1～1500mg/nm in this coke oven flue gas3SO2And 1～1000mg/nm3NOx。
In the method for the invention one detailed description of the invention, described reducing agent is liquefied ammonia, and its consumption is 50～200kg/h.
In the method for the invention one detailed description of the invention, controlling the water after heat pipe waste heat boiler makes heating and be changed into the saturated vapor of 0.8MPa, the air after heating is changed into the air that temperature is 140 DEG C.Gained saturated vapor can directly send user to use, and gained hot-air can as the hot standby thermal source of chimney, and air at such a temperature makes chimney have the draft of about 500Pa.Steam production is depending on amount of flue gas emission, and hot-air expense is about 10000～50000Nm according to field condition difference3/h。
On the other hand, the present invention provides this system of system being applied to the method for the invention to include coke oven flue gas desulphurization denitration waste heat recovery module, denitration protection module and coke oven flue gas safety dumping module；
Described coke oven flue gas desulphurization denitration waste heat recovery module includes the described SCR denitration reactor being sequentially connected with, described waste heat boiler module and magnesium processes desulfurizer；
Described waste heat boiler module is provided with water inlet and corresponding steam outlet；Cool air inlet and corresponding hot air outlet；
Described coke oven flue gas safety dumping module includes safe flue and chimney；
The fume emission mouth of coke oven is connected to the entrance of described SCR denitration reactor and one end of described safe flue by pipeline and three-way switch valve, the other end of described safe flue is connected to the bottom of described chimney, and the bottom of described chimney is connected with the hot air outlet of described waste heat boiler module by pipeline；
Described SCR denitration protection module includes valve and heater; one end of described valve is connected with the hot air outlet of described waste heat boiler module by pipeline; the other end is connected with the entrance of described heater, and the outlet of described heater is connected by the entrance of pipeline with described SCR denitration reactor.
The method of the invention adopts as above system to be possible not only to meet the requirement of desulphurization denitration and waste heat recovery, also can fully ensure the safety in art production process and avoid SCR catalyst to be subject to the injury of low temperature instability coke oven flue gas.Additionally, due to described hot air outlet and described chimney bottom are directly connected to, hot-air without consuming additional energy source, is effectively saved energy resource consumption as hot standby chimney thermal source.
Specifically, when in the state of accident, enabling coke oven flue gas to discharge from safe flue and chimney in time by switch valve.This is directly connected to described chimney bottom mainly due to the hot air outlet of waste heat boiler module described in said system, and the hot-air produced in production process makes chimney be in hot standby state, and the discharge of coke oven flue gas does not send blocking.
180～300 DEG C of temperature and SO is met when flue gas2Concentration is lower than 1500mg/Nm3Time, flue gas can be directly entered said system and carry out denitration, waste heat recovery, desulfurization.When coke oven flue gas temperature lower than 180 DEG C and/or SO2Concentration is higher than 1500mg/Nm3Time, open the described valve in described denitration protection module, the hot-air coming from described hot air outlet is heated to 600～700 DEG C by described heater, delivers to described SCR denitration reactor inlet and improves coke oven flue gas temperature and/or dilution SO2Concentration.Adopt this set to make system avoid low temperature to corrode and/or catalyst poisoning, guarantee denitration efficiency simultaneously.The fuel of described heater is blast furnace gas and/or coke-stove gas.
In the method for the invention one detailed description of the invention, described system also includes magnesium sulfate retracting device, and this device is connected to described magnesium processes desulfurizer, and the magnesium sulfate in desulfurization slurry and other impurity can be completely converted into solid crystals.This solid crystals is utilized can directly to prepare commodity Magnesium sulfate heptahydrate, it is achieved no effuent discharge.
In a detailed description of the invention of system of the present invention, described system is additionally provided with the device providing reducing agent into described SCR denitration reactor；Preferably, described reducing agent is liquefied ammonia.
Unless otherwise indicated, if do not conflicted, technical characteristic involved in the present invention can be mutually combined.
In summary, technique of the present invention and system at least possess following three points beneficial effect:
(1) at utmost rationalize arrangement technological process, make whole technological process simple, optimize the device in technique and condition so that desulfurization off sulfide effect can fully ensure that.By adopting SCR denitration reactor and protecting module with denitration, make whole flow process smooth, and cope with extreme case.
(2) economy of this technique is protected.In this technique under nominal situation (more than the 95% of the year-round operation time), flue gas need not be heated by this technique, saves mass energy.Originally, utilizing waste heat boiler to produce steam and hot-air, the production of hot-air makes security module draft keep not needing to consume additional energy source.And under extreme operating condition (less than the 5% of the year-round operation time), add the heat loss energy minimum.
(3) security guarantee maximizes.Utilize safe flue module, make system keep safe draft at any time, can immediately switch in the state of accident, be absent from incuring loss through delay and cold start-up wait.
(4) no effuent discharge is realized.By magnesium sulfate recycling module, the magnesium sulfate in desulfurization wastewater and impurity are all evaporated to crystal state, magnesium sulfate and carnallite and all can realize commercialization recycling.
Accompanying drawing explanation
Fig. 1 is the coke oven flue gas desulphurization denitration residual neat recovering system schematic diagram described in embodiment 1；Label in Fig. 1 has following meaning:
1: coke oven；2: three-way switch valve；3:SCR denitrification apparatus；4: heat pipe waste heat boiler；41: water inlet；42: steam outlet；43: cool air inlet；44: hot air outlet；5: magnesium processes desulfurizer；6: magnesium sulfate retracting device 7: heater；71: ball valve；8: the device of reducing agent is provided；9: safe flue；10: chimney.
Fig. 2 is the structural representation of SCR denitration device in embodiment 1 system for use in carrying；In Fig. 2, label has following meaning:
21: inlet flue duct；22: deflector；23: flow straightening grid；24: steam sootblower；25: catalyst layer.
Detailed description of the invention
In order to the technical characteristic of the present invention, purpose and beneficial effect are more clearly understood from, in conjunction with instantiation and accompanying drawing, technical scheme is carried out described further below, it should be understood that these examples are merely to illustrate the present invention rather than restriction the scope of the present invention.
Embodiment 1
The coke oven flue gas desulphurization denitration residual neat recovering system schematic diagram that the present embodiment uses is as it is shown in figure 1, this system includes coke oven flue gas desulphurization denitration waste heat recovery module, denitration protection module and coke oven flue gas safety dumping module；
Described coke oven flue gas desulphurization denitration waste heat recovery module includes the SCR denitration reactor 3, waste heat boiler module 4, magnesium processes desulfurizer 5 and the magnesium sulfate retracting device that are sequentially connected with；
Described waste heat boiler module 4 is provided with water inlet 41, and this water inlet can be technique soft water entrance, and corresponding steam outlet 42；Cool air inlet 43 and corresponding hot air outlet 44；
Described coke oven flue gas safety dumping module includes safe flue 9 and chimney 10；
The fume emission mouth of coke oven is connected to the entrance of described SCR denitration reactor 3 and one end of described safe flue 9 by pipeline and three-way switch valve 2, the other end of described safe flue 9 is connected to the bottom of described chimney 10, and the bottom of described chimney 10 is connected with the hot air outlet 44 of described waste heat boiler module by pipeline；
Described denitration protection module includes ball valve 71 and heater 7; one end of described ball valve 71 is connected with the hot air outlet 44 of described waste heat boiler module by pipeline; the other end is connected with the entrance of described heater 7, and the outlet of described heater 7 is connected by the entrance of pipeline with described SCR denitration reactor 3；
This system is additionally provided with the device 8 providing reducing agent for described SCR denitration reactor 3；Described reducing agent is liquefied ammonia.
The structure of SCR denitration reactor described in Fig. 1 is as shown in Figure 2, the entrance of described SCR denitration reactor 3 connects inlet flue duct 21, this inlet flue duct 21 turning arranges deflector 22, described SCR denitration reactor includes housing, this housing internal upper part arranges flow straightening grid 23, this flow straightening grid is arranged below catalyst layer 24, arranges steam sootblower 24 between described flow straightening grid 23 and described catalyst layer 25；Also set up 2 layers of catalyst layer 25 in described SCR denitration reactor, between every two catalyst layers 25, steam sootblower 24 is set.
The coke oven flue gas desulphurization denitration exhaust heat recovering method that the present embodiment provides adopts as above system, and when being embodied as, from coke oven flue opening, (mean concentration of this nitrogen oxides in effluent is 1000mg/Nm to take the whole flue gas of coke oven 13, the mean concentration of sulfide is 800mg/Nm3, temperature is 200～250 DEG C, and flow is 250000Nm3/ h), pass into described SCR denitration device 3, to provide the liquefied ammonia that the device 8 of reducing agent provides to spray in SCR denitration device 3 as reducing agent to described low temperature SCR denitration device, hour liquefied ammonia consumption 120～150kg, flue gas flow rate 3～5m/s, under the effect of low temperature sulfur resistive rare-earth system catalyst, with the nitric oxide (NO) in flue gas, nitrogen dioxide NO2Nitrogen (N is generated Deng reaction2), thus the nitrogen oxides removed in flue gas；Flue gas after denitration enters heat pipe waste heat boiler 4, utilize existing 190～240 DEG C of temperature of flue gas, heat a certain amount of industrial soft water entering heat pipe waste heat boiler 4 from technique soft water entrance 41, produce the saturated vapor of 0.8MPa, discharge from the steam outlet 42 of heat pipe waste heat boiler 4, for other techniques of factory, heat pipe waste heat boiler 4 heats the cold air entered from cool air inlet 43 simultaneously, and flue gas is by 20000m3Left and right (per hour) cold air is from ambient temperature to about 150 DEG C, and these hot-airs directly pass into chimney 10 from hot air outlet 44, make chimney 10 keep about 500Pa draft；Coke oven flue gas temperature through heat exchange is down to 160～180 DEG C, and this flue gas finally enters magnesium processes desulfurizer 5, the sulfur dioxide (SO in flue gas2) and sulfur trioxide (SO3) with the absorbent MgO reactant aqueous solution in magnesium processes desulfurizer 5, set in tower liquid-gas ratio as 3～6L/m3, flue gas flow rate about 3m/s in tower, thus removing sulfur oxide.The chimney that flue gas after desulfurization eventually passes through on magnesium processes desulfurizer is drained in air.In flue gas after desulfurization, the mean concentration of nitrogen oxides is≤150mg/Nm3, the mean concentration of sulfide is≤30mg/Nm3.Under normal condition, the valve in denitration protection module, namely ball valve 71 is normally closed, does not work.
The part in magnesium processes desulfurizer 5 serosity containing magnesium sulfite and magnesium sulfate is discharged into magnesium sulfate retracting device 6, clarifies through filter pressing, the multiple-effect evaporation unit in this retracting device flashes to the Magnesium sulfate heptahydrate crystal (MgSO of commerical grade4·7H2O).Magnesium sulfate heptahydrate crystal can be sold after packaging.
When accident condition, flue gas is directly discharged to chimney 10 through bypassing safe flue 9, and the chimney negative pressure that hot-air provides enables flue gas to discharge from chimney rapidly, in case coke oven smoke evacuation is freely not accidents caused.Under accident condition, the ball valve 71 in denitration protection module is opened, and heater 7 heats hot-air and passes in SCR denitration device 3 to 650 DEG C, and protection reactor and catalyst do not suffer damage under low temperature state.
In summary, coke oven flue gas desulphurization denitration UTILIZATION OF VESIDUAL HEAT IN of the present invention and by-product utilized system can ensure denitrification efficiency, safe and feasible, it is possible to reduce, for coking industry, the SO that total amount is huge every year in engineering practice2、NOxDischarge.The heat energy simultaneously reclaimed is utilized effectively, and can save substantial amounts of electric energy and other fuel.The production safety of coke oven can be sufficiently ensured, and makes coke oven will not cause danger because of situations such as the fault of desulphurization denitration facility or power-off.
The present invention at least can bring following beneficial effect:
The technological process utilizing system of the present invention takes full advantage of the energy that coke oven flue gas itself contains, each device or module according to flue-gas temperature reasonable Arrangement, make use of coke oven flue gas heat to greatest extent, from without flue gas link, it is to avoid substantial amounts of energy resource consumption produced by flue gas link；Meanwhile, can by used heat commercialization to greatest extent, becoming can by the saturated vapor of the specified pressure of industrial utilization.
The present invention devises denitrification apparatus protection module and negative pressure keeps module, and denitrification apparatus protection module can be effectively ensured low temperature SCR denitration system and run safety, it is prevented that denitrification apparatus and catalyst suffer damage under special cryogenic conditions；Negative pressure keeps module to can adapt to coke oven production safety requirement, and the moment keeps accident emergency smoke evacuation system unimpeded.
Desulfurizing byproduct in the present invention can direct preparing magnesium sulfate, it is possible to effectively accomplish Matter Transfer, allows the by-product creation of value simultaneously；By-product can do industrial chemicals after purifying, and does not produce secondary pollution, and the benefit created can balance portion operation cost, be coking flue gas desulfurization and denitrification more economically.
Finally illustrate: above example is merely to illustrate implementation process and the feature of the present invention; and unrestricted technical scheme; although the present invention being described in detail with reference to above-described embodiment; it will be understood by those within the art that: still the present invention can be modified or equivalent replacement; without deviating from any modification or partial replacement of the spirit and scope of the present invention, all should be encompassed in the middle of protection scope of the present invention.
Claims (9)
1. the method for coke oven flue gas desulphurization denitration and waste heat recovery, described method includes: make 180～300 DEG C and SO2Concentration is lower than 1500mg/Nm3Coke oven flue gas enter SCR denitration reactor and reducing agent and react elimination nitrogen oxides, after reaction, flue gas entrance waste heat boiler module carries out heat exchange, controlling the temperature of flue gas after waste heat boiler module makes heat exchange is 160～180 DEG C, discharges after making it into magnesium processes desulfurizer scrubbing CO_2 subsequently；
The entrance of described SCR denitration reactor connects inlet flue duct (21), this inlet flue duct (21) turning arranges deflector (22), described SCR denitration reactor includes housing, this housing internal upper part arranges flow straightening grid (23), this flow straightening grid is arranged below catalyst layer (25), arranges steam sootblower (24) between described flow straightening grid (23) and described catalyst layer (25)；
The catalyst used in described SCR denitration reactor is vanadium Ti-base catalyst and/or rare-earth system low temperature catalyst；This catalyst can make SO2Conversion ratio is not more than 1%, and makes the denitration efficiency of the coke oven flue gas of 180～300 DEG C be not less than 70%；
It is 5000～8000m that described method controls volume space velocity in SCR denitration reactor3/m3.h；And the speed controlling to enter the coke oven flue gas of described SCR denitration reactor is 3～10m/s；
Described waste heat boiler module is can heat the heat pipe waste heat boiler of water and air with heat smoke for thermal source simultaneously；Controlling the flow of water and air makes after heat exchange the temperature of flue gas at 160～180 DEG C.
2. method according to claim 1, wherein, also sets up multi-layer catalyst layer (25), arranges steam sootblower (24) between every two catalyst layers (25) in described SCR denitration reactor.
3. method according to claim 1, wherein, controlling to enter the flow velocity of flue gas in magnesium processes desulfurization module is 2～9m/s, and the liquid-gas ratio of spray slurry and this flue gas is 2～8L:1m3, make smog discharge temperature more than 80 DEG C；Described spray slurry is MgO aqueous solution.
4. method according to claim 1, wherein, the temperature of described coke oven flue gas is 200～250 DEG C, comprises 1～1500mg/nm in this coke oven flue gas3SO2And 1～1000mg/nm3NOx。
5. method according to claim 1, wherein, described reducing agent is liquefied ammonia, and its consumption is 50～200kg/h.
6. method according to claim 1, wherein, controls the water after heat pipe waste heat boiler makes heating and is changed into the saturated vapor of 0.8MPa, and the air after heating is changed into the air that temperature is 140 DEG C.
7. being applied to a system for method according to any one of claim 1～6, wherein, this system includes coke oven flue gas desulphurization denitration waste heat recovery module, denitration protection module and coke oven flue gas safety dumping module；
Described coke oven flue gas desulphurization denitration waste heat recovery module includes the described SCR denitration reactor (3), described waste heat boiler module (4) and the magnesium processes desulfurizer (5) that are sequentially connected with；
Described waste heat boiler module (4) is provided with water inlet (41) and corresponding steam outlet (42)；Cool air inlet (43) and corresponding hot air outlet (44)；
Described coke oven flue gas safety dumping module includes safe flue (9) and chimney (10)；
The fume emission mouth of coke oven is connected to the entrance of described SCR denitration reactor (3) and one end of described safe flue (9) by pipeline and three-way switch valve (2), the other end of described safe flue is connected to the bottom of described chimney (10), and the bottom of described chimney (10) is connected with the hot air outlet (44) of described waste heat boiler module by pipeline；
Described SCR denitration protection module includes valve (71) and heater (7); one end of described valve (71) is connected with the hot air outlet (44) of described waste heat boiler module by pipeline; the other end is connected with the entrance of described heater (7), and the outlet of described heater (7) is connected by the entrance of pipeline with described SCR denitration reactor (3).
8. system according to claim 7, wherein, this system also includes magnesium sulfate retracting device, and this device is connected to described magnesium processes desulfurizer, and the magnesium sulfate in desulfurization slurry and other impurity can be completely converted into solid crystals.
9. the system according to claim 7 or 8, wherein, described system is additionally provided with the device providing reducing agent into described SCR denitration reactor；Preferably, described reducing agent is liquefied ammonia.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201610391156.6A CN105797581A (en) | 2016-06-03 | 2016-06-03 | System and process for utilizing coke oven flue gas desulfurization and denitrification waste heat |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201610391156.6A CN105797581A (en) | 2016-06-03 | 2016-06-03 | System and process for utilizing coke oven flue gas desulfurization and denitrification waste heat |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN105797581A true CN105797581A (en) | 2016-07-27 |
Family
ID=56427863
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201610391156.6A Pending CN105797581A (en) | 2016-06-03 | 2016-06-03 | System and process for utilizing coke oven flue gas desulfurization and denitrification waste heat |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN105797581A (en) |
Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106244175A (en) * | 2016-08-19 | 2016-12-21 | 肖爱国 | The reduction denitration of fume high-temperature carbon and heat-energy recovering apparatus |
| CN106422702A (en) * | 2016-10-31 | 2017-02-22 | 中钢集团鞍山热能研究院有限公司 | Desulfuration, denitration and energy conservation integrated purification system for coke oven flue gas and control method of system |
| CN107325827A (en) * | 2017-07-11 | 2017-11-07 | 南京华电节能环保设备有限公司 | A kind of coke oven flue waste gas afterheat recovery unit of simultaneous SO_2 and NO removal |
| CN108126492A (en) * | 2018-02-01 | 2018-06-08 | 北京国能中电节能环保技术股份有限公司 | Flue gas desulfurization and denitrification device |
| CN108507364A (en) * | 2018-04-12 | 2018-09-07 | 深圳市凯盛科技工程有限公司 | A kind of spare heat-exchange system of waste heat boiler of glass furnace |
| CN108579369A (en) * | 2018-03-21 | 2018-09-28 | 中冶京诚工程技术有限公司 | A kind of coke oven flue gas multi-pollutant collaboration governing system and method |
| CN109173709A (en) * | 2018-09-18 | 2019-01-11 | 内蒙古中谷矿业有限责任公司 | A kind of novel molten salt furnace rare earth catalyst flue gas denitrification system |
| CN113477279A (en) * | 2021-07-27 | 2021-10-08 | 苏州西热节能环保技术有限公司 | Waste heat utilization method and device in denitration catalyst regeneration process |
Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP1316352A1 (en) * | 2001-07-18 | 2003-06-04 | Mitsubishi Heavy Industries, Ltd. | Method for treating mercury in exhaust gas and exhaust gas treating system |
| US20110268638A1 (en) * | 2009-12-14 | 2011-11-03 | Babcock-Hitach Kabushiki Kaisha | Method of mercury removal from combustion exhaust gas and combustion exhaust gas purification apparatus |
| CN103480272A (en) * | 2013-10-01 | 2014-01-01 | 王脯胜 | Dust-removing, denitration and desulfurization process and device for flue gas of glass kiln |
| CN103752171A (en) * | 2014-01-18 | 2014-04-30 | 浙江诸暨泓泰环境科技有限公司 | Catalytic reduction flue gas denitration equipment |
| CN104556157A (en) * | 2014-12-03 | 2015-04-29 | 北京中晶佳镁环境科技股份有限公司 | Magnesium sulfate production device and method by flue gas desulfurization |
| CN205164504U (en) * | 2015-12-10 | 2016-04-20 | 中冶京诚工程技术有限公司 | Denitration of coke oven flue gas desulfurization and waste heat utilization system |
-
2016
- 2016-06-03 CN CN201610391156.6A patent/CN105797581A/en active Pending
Patent Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP1316352A1 (en) * | 2001-07-18 | 2003-06-04 | Mitsubishi Heavy Industries, Ltd. | Method for treating mercury in exhaust gas and exhaust gas treating system |
| US20110268638A1 (en) * | 2009-12-14 | 2011-11-03 | Babcock-Hitach Kabushiki Kaisha | Method of mercury removal from combustion exhaust gas and combustion exhaust gas purification apparatus |
| CN103480272A (en) * | 2013-10-01 | 2014-01-01 | 王脯胜 | Dust-removing, denitration and desulfurization process and device for flue gas of glass kiln |
| CN103752171A (en) * | 2014-01-18 | 2014-04-30 | 浙江诸暨泓泰环境科技有限公司 | Catalytic reduction flue gas denitration equipment |
| CN104556157A (en) * | 2014-12-03 | 2015-04-29 | 北京中晶佳镁环境科技股份有限公司 | Magnesium sulfate production device and method by flue gas desulfurization |
| CN205164504U (en) * | 2015-12-10 | 2016-04-20 | 中冶京诚工程技术有限公司 | Denitration of coke oven flue gas desulfurization and waste heat utilization system |
Non-Patent Citations (3)
| Title |
|---|
| 吕天宝: "《工业脱硫及综合利用技术》", 30 April 2011, 国防工业出版社 * |
| 杨飏: "《氮氧化物减排技术与烟气脱硝工程》", 31 January 2007, 冶金工业出版社 * |
| 王振峰: "《材料传输工程基础》", 31 December 2008, 冶金工业出版社 * |
Cited By (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106244175A (en) * | 2016-08-19 | 2016-12-21 | 肖爱国 | The reduction denitration of fume high-temperature carbon and heat-energy recovering apparatus |
| CN106422702A (en) * | 2016-10-31 | 2017-02-22 | 中钢集团鞍山热能研究院有限公司 | Desulfuration, denitration and energy conservation integrated purification system for coke oven flue gas and control method of system |
| CN107325827A (en) * | 2017-07-11 | 2017-11-07 | 南京华电节能环保设备有限公司 | A kind of coke oven flue waste gas afterheat recovery unit of simultaneous SO_2 and NO removal |
| CN107325827B (en) * | 2017-07-11 | 2023-09-26 | 南京华电节能环保股份有限公司 | Coke oven flue waste gas waste heat recovery device capable of simultaneously desulfurizing and denitrating |
| CN108126492A (en) * | 2018-02-01 | 2018-06-08 | 北京国能中电节能环保技术股份有限公司 | Flue gas desulfurization and denitrification device |
| CN108579369A (en) * | 2018-03-21 | 2018-09-28 | 中冶京诚工程技术有限公司 | A kind of coke oven flue gas multi-pollutant collaboration governing system and method |
| CN108579369B (en) * | 2018-03-21 | 2023-06-27 | 中冶京诚工程技术有限公司 | Coke oven flue gas multi-pollutant cooperative treatment system and method |
| CN108507364A (en) * | 2018-04-12 | 2018-09-07 | 深圳市凯盛科技工程有限公司 | A kind of spare heat-exchange system of waste heat boiler of glass furnace |
| CN109173709A (en) * | 2018-09-18 | 2019-01-11 | 内蒙古中谷矿业有限责任公司 | A kind of novel molten salt furnace rare earth catalyst flue gas denitrification system |
| CN113477279A (en) * | 2021-07-27 | 2021-10-08 | 苏州西热节能环保技术有限公司 | Waste heat utilization method and device in denitration catalyst regeneration process |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN105797581A (en) | System and process for utilizing coke oven flue gas desulfurization and denitrification waste heat | |
| CN108579369B (en) | Coke oven flue gas multi-pollutant cooperative treatment system and method | |
| CN105944564A (en) | Coke oven flue gas waste heat recycling, desulfuration and denitration integrated system and method | |
| CN205164504U (en) | Denitration of coke oven flue gas desulfurization and waste heat utilization system | |
| CN210035516U (en) | Hazardous waste incineration flue gas treatment device | |
| CN105214478A (en) | The integral process of a kind of coke oven flue exhuast gas desulfurization denitration and waste heat recovery | |
| CN105457486A (en) | Coke oven flue gas integrated treatment method | |
| CN109482049B (en) | Dry desulfurization, denitrification and purification integrated process for coke oven flue gas | |
| CN106984169A (en) | The denitrating system and method for a kind of direct utilization sintering deposit heat | |
| CN105797562A (en) | Two-section type double-ammonia-process integrated desulfurization and denitration system for coking flue gas | |
| CN207287090U (en) | A kind of purifying processing device of production of carbon black exhaust gas | |
| CN109731472B (en) | Energy-saving boiler flue gas purification system and method | |
| CN210021683U (en) | Flue gas treatment device of rotary kiln | |
| CN110484283B (en) | Comprehensive recovery process and system for coking waste heat | |
| CN113776061A (en) | Hazardous waste incineration flue gas purification and waste heat recovery device and method thereof | |
| CN103611417B (en) | A kind of coke oven exhaust gas wet denitration method | |
| CN108654363A (en) | Couple waste heat of coke-oven flue gas and amounts of sulphur contaminants acid-making process | |
| CN105485701A (en) | Coal-fired power generation system deeply and integrally provided with system for desulfurizing and decarburizing calcium-based sorbent in sequence | |
| CN206139011U (en) | System for desulfurization simultaneously of sintering flue gas is out of stock | |
| CN111135698A (en) | Sintering flue gas desulfurization, white removal and denitration comprehensive treatment system and process | |
| CN201754034U (en) | Comprehensive treatment system for glass furnace flue gas | |
| CN205659559U (en) | Coke oven smoke SOx/NOx control waste heat recovery system | |
| CN206463781U (en) | A kind of desulfuring and denitrifying apparatus of coke oven flue gas | |
| CN206778183U (en) | A kind of denitrating system for directly utilizing sintering deposit heat | |
| CN212262910U (en) | Ultra-clean discharge system for desulfurization, denitrification and waste heat recovery of coke oven flue gas |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| WD01 | Invention patent application deemed withdrawn after publication |
Application publication date: 20160727 |
|
| WD01 | Invention patent application deemed withdrawn after publication |