CN205815447U - The double ammonia process integration desulfurization denitration system of coking flue gas two-part - Google Patents
The double ammonia process integration desulfurization denitration system of coking flue gas two-part Download PDFInfo
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- CN205815447U CN205815447U CN201620400716.5U CN201620400716U CN205815447U CN 205815447 U CN205815447 U CN 205815447U CN 201620400716 U CN201620400716 U CN 201620400716U CN 205815447 U CN205815447 U CN 205815447U
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- flue gas
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- 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
nullThe utility model discloses the double ammonia process integration desulfurization denitration system of coking flue gas two-part，Including denitration in the stove system、Chimney，Denitration in the stove system is connected with coke oven，Coke oven is logical to be connected with chimney，Chimney is connected with waste heat boiler，Waste heat boiler is connected with smoke re-heater，Smoke re-heater is connected with flue gas blower fan，Flue gas blower and pipeline is connected with scrubber，Scrubber is connected with cleaning circulation pump，Cleaning circulation pump is connected with cleaning dust cooler，Cleaning dust cooler is connected with scrubber upper entrance pipeline，Scrubber is connected with pipeline reactor，Pipeline reactor is connected with ozonator，Pipeline reactor is connected with desulphurization denitration integrated tower，Desulphurization denitration integrated tower top is connected with smoke re-heater，Smoke re-heater is connected with chimney，The purifying smoke discharging desulphurization denitration integrated tower enters return chimney high altitude discharge after smoke re-heater heat temperature raising.This utility model denitration low cost, efficiency are high.
Description
Technical field
This utility model relates to coking stack gases purification technology field, particularly relates to a kind of coking flue gas two sections
Double ammonia (ammonium) the method integration desulfurization denitration system of formula.
Background technology
The desulphurization denitration of coking flue gas of the prior art processes and the process of ammonia-containing water has various ways, to reach energy
Source recycling, reduction energy consumption, reduce environmental pollution and the purpose of destruction, but these method and apparatus of the prior art deposited
Defect be: the flue gas desulfurization and denitration method cost that has in prior art is high, high temperature method the most of the prior art and catalysis
Method method of denitration cost is high；Some desulfurization off sulfide effect are poor, residual quantity big, and clean-up effect is bad, and vapour phase amount of ammonia slip is many simultaneously,
Environment and air are polluted.
This utility model be applicant on the basis of original applying number is 201510690115.2 utility model patents, pass through
Continuous technological innovation, reduces technological equipment investment and the operating cost of desulphurization denitration further.
Utility model content
The purpose of this utility model is exactly for solving existing flue gases of cock oven desulphurization denitration high expensive, investing bigger than normal asking
Topic, it is provided that double ammonia (ammonium) the method integration desulfurization denitration system of a kind of coking flue gas two-part.This utility model utilizes coking certainly
The ammonia produced, as alkali source, carries out desulphurization denitration purification to flue gas, forms callable ammonium sulfate and ammonium nitrate is incorporated to coking
The ammonium sulfate workshop section of flow process, is can value-added side-product by the element sulphur in stack gases and nitrogen cycling of elements；This utility model fills
Divide and combine denitration in the stove and the outer denitration technology of stove, significantly reduce denitration cost；This utility model uses the ammonia of variable concentrations
Desulphurization denitration, strong aqua ammonia can form resource product, and weak ammonia reduces the vapour phase dividing potential drop of ammonia, reduces the escaping of ammonia；This practicality is new
Type uses integration apparatus, simultaneous SO_2 and NO removal, significantly reduces desulphurization denitration investment；This utility model utilizes outside ozone stove
Hydrogen peroxide denitration in denitration, tower, realizes the removing of NOx at a lower temperature, significantly reduces denitration cost；This utility model
Utilize coking flow process internal resource ammonium sulfate liquor to wash flue gas, further avoid ammonia process of desulfurization denitration and would generally produce free ammonia
The phenomenon that vapour phase is escaped, does not only increase cost, and improves the inside networking degree of coking flow process, efficiently solves desulfurization and takes off
The escaping of ammonia phenomenon of nitre process.
This utility model solves the technical scheme of technical problem:
The double ammonia process integration desulfurization denitration system of a kind of coking flue gas two-part, including denitration in the stove system, chimney, remaining
Heat boiler, smoke re-heater, coke oven, also include flue gas blower fan, scrubber, cleaning dust circulating pump, cleaning dust cooling
Device, ozonator, pipeline reactor, desulphurization denitration integrated tower, circulation oxidator, described denitration in the stove system is empty by dilution
Feed channel or dilution nitrogen pipeline are connected with coke oven, and coke oven is connected with chimney by coke oven flue gas pipeline, and chimney passes through coke oven cigarette
Feed channel is connected with waste heat boiler, and waste heat boiler is connected with smoke re-heater by flue after recovered flue gas high-temperature residual heat,
Smoke re-heater is connected with flue gas blower fan by flue after reclaiming low temperature exhaust heat, flue gas blower and pipeline and cleaning dust
Device connects, and scrubber bottom is connected with cleaning circulation pump by liquid pipe, and cleaning circulation pump is exported by lower liquid phase
Pipeline is connected with cleaning dust cooler, and cleaning dust cooler is connected with scrubber upper entrance pipeline, cleaning dust
Device is connected with pipeline reactor by pipeline after cleaning dust, and pipeline reactor is connected with ozonator by ozone pipeline,
Pipeline reactor by reaction after flue is connected with desulphurization denitration integrated tower, through washing lower the temperature after flue gas and from
The ozone of ozonator is sufficiently mixed reaction in pipeline reactor, by part or all of for the nitric oxide in flue gases of cock oven
After oxidation, send into desulphurization denitration integrated tower and carry out desulphurization denitration process；Desulphurization denitration integrated tower top is by fume pipe after purifying
Road is connected with smoke re-heater, and smoke re-heater is connected with chimney by purifying smoke pipeline, discharges desulphurization denitration integrated tower
Purifying smoke enters smoke re-heater, and before utilizing desulphurization denitration, the low temperature exhaust heat heating of flue gas is increased to 100-150 DEG C of return
Chimney, high altitude discharge.
Described desulphurization denitration integrated tower includes the two-stage nitration desulphurization denitration section at one section of desulphurization denitration section of bottom, middle part, two-stage nitration
The top of desulphurization denitration section is provided with catches ammonia section, catches ammonia section top and is provided with physical property demister.Described one section of desulphurization denitration section with
The scrubbing ammonia waterpipe of strong aqua ammonia pipeline or raw coke oven gas desulfurization regeneration tail gas connects, described strong aqua ammonia pipeline and coking ammonia still process
The strong aqua ammonia pipeline of workshop section connects, and described scrubbing ammonia waterpipe connects with the scrubbing ammonia waterpipe of raw coke oven gas desulfurization regeneration tail gas
Connect, from the washing ammonia of the strong aqua ammonia of coking ammonia still process workshop section or raw coke oven gas desulfurization regeneration tail gas as the alkali of desulphurization denitration
Source adds one section of desulphurization denitration section.One section of circulating pump is connected with desulphurization denitration integrated tower by one section of circulation ammonium liquid pipeline, one section
Cooler is connected by one section of circulation ammonium liquid pipeline and one section of circulating pump, and one-step cooling device circulates ammonium liquid pipeline with de-by one section
Sulfur denitration integrated tower connects, and one section of desulphurization denitration section of desulphurization denitration integrated tower is by ammonium liquid side line pipeline with circulation oxidator even
Connecing, circulation cycle delivery side of pump is connected with circulation oxidator top by circulation cycle conduit upper, described circulation cycle pipeline
Top is provided with ejector near the position on circulation oxidator top, the import of circulation cycle pump by circulation cycle pipeline bottom with
Connect bottom circulation oxidator, the ammonium sulfate after oxidation and ammonium nitrate being mixed by spur outlet and pipeline of circulation cycle pump
Ammonium salt solution is sent to the ammonium sulfate workshop section Resource recovery product of coking or for complex acid；
Described two-stage nitration desulphurization denitration section is connected by pipeline with the remained ammonia from coking ammonia still process workshop section, steams from coking
The remained ammonia of ammonia workshop section passes through the pipeline diluent addition two-stage nitration desulphurization denitration section as ammonia concentration, described two-stage nitration desulfurization
The bottom of denitration section is connected with two-stage nitration pump inlet by two-stage nitration circulation fluid pipeline, and two-stage nitration circulating-pump outlet is circulated by two-stage nitration
Liquid pipeline is connected with two-step cooling device, and two-step cooling device is connected by the top of two-stage nitration circulation fluid pipeline with two-stage nitration desulphurization denitration section
Connect.Remained ammonia is sent to the ammonia still of the ammonia still process workshop section of coking by the spur outlet of two-stage nitration circulating pump by pipeline.
Described ammonia section of catching is connected with ammonium sulfate liquor pipeline, the flue gas after two-stage nitration desulphurization denitration, enters desulphurization denitration
Integrated tower top catch ammonia section, utilize sulphuric acid workshop section acid mother liquid washing flue gas, sulfur ammonium acid mother liquid washing flue gas catch
Returning ammonium sulfate workshop section after residue ammonia, the control temperature catching ammonia section is 50-70 DEG C.
After described physical property demister intercepts power elimination flue gas acid mist by centrifugal force and inertia, flue gas is from desulfurization
Denitration integrated tower top is discharged；Flue gas after catching ammonia section enters the physical property at desulphurization denitration integrated tower top except mist dress
Putting, after intercepting power elimination flue gas acid mist by centrifugal force and inertia, flue gas is discharged from desulphurization denitration integrated tower top；Catch mist
The temperature of section controls as 50-60 DEG C.
Ejector uses venturi tube structure, and ejector is connected with external air duct, utilizes the ejector of venturi tube structure
Circulation injection suction is incorporated herein the air oxidant as circulation oxidator, sprays generation by the circulation of circulation cycle pump
Suction introduces air, and the oxygen in air is fully and ammonium liquid is sufficiently mixed reaction, ammonium sulfite therein generates ammonium sulfate, so
After the mixed salt solution containing ammonium sulfate and ammonium nitrate is sent to the ammonium sulfate workshop section of coking, Resource recovery product, described circulation oxygen
Controlling temperature in changing device and be 50-80 DEG C, pH controls as 6.0-6.8.
Flue gas after described dilution air line waste heat recovery or the flue gas after purification are dilution air, or
Air is mixed into the 0-50% that mixed volume is air capacity of noble gas, flue gas or noble gas；Heating gas mixes
Entering low-heat value gas, low-heat value gas mixed volume is the 0-70% of heating gas amount, reduces the nitrogen oxidation that coke oven is discharged in flue gas
Thing content, the amount of nitrogen oxides making coke oven discharge in flue gas is 250-550mg/m3。
Coke oven flue temperature after denitration in the stove system denitration processes is 220-350 DEG C, and flue gases of cock oven is sent into
Waste heat boiler reclaims flue gas high-temperature residual heat, and the waste heat that waste heat boiler reclaims is used as to produce steam, or is directly used in ammonia still process heating
Distilled ammonia wastewater, or heating conduction oil, after reclaiming high-temperature residual heat, effluent gas temperature is down to 150-200 DEG C；Reclaim through waste heat boiler
Flue gas after high-temperature residual heat is sent into smoke re-heater and is reclaimed flue gases at low waste heat, the purification discharged by desulphurization denitration integrated tower
Flue gas is heated to 100-150 DEG C from 50-80 DEG C, and own temperature is down to 90-130 DEG C；Flue after reclaiming low temperature exhaust heat
Gas sends into scrubber by flue gas blower fan, utilizes cleaning circulation pump by cycles of washing liquid from washing in scrubber
Cleaner unit top sprays into, with fed from below into flue gas counter current contacting, washing removing flue gas in dust impurity, flue gas
It is cooled to 60-80 DEG C further.
Flue gas after washing cooling is sufficiently mixed instead with the ozone from ozonator in pipeline reactor
Should, after the nitric oxide in flue gases of cock oven is partly or entirely aoxidized, send into desulphurization denitration integrated tower and carry out at desulphurization denitration
Reason.
Add hydrogen peroxide carry out oxidation in one section of described desulphurization denitration section, two-stage nitration desulphurization denitration section.Strengthening denitration
Efficiency, reduces ozone-depleting, reduces operating cost.
The beneficial effects of the utility model:
1. this utility model utilizes the self-produced ammonia of coking as alkali source, and flue gas carries out desulphurization denitration purification, is formed
Callable ammonium sulfate and ammonium nitrate are incorporated to the ammonium sulfate workshop section of coking flow process, by the element sulphur in stack gases and nitrogen cycling of elements
For can value-added side-product；Do not produce solid waste and pollution transportation.
2. this utility model fully combines denitration in the stove and the outer denitration technology of stove, and denitration in the stove uses dilution air and dilution
The measure of coal gas combines, and significantly reduces denitration cost.
3. this utility model uses the ammonia desulphurization denitration of variable concentrations, and strong aqua ammonia can form resource product, dilute ammonia
Water reduces the vapour phase dividing potential drop of ammonia, reduces the escaping of ammonia, and the close Rhizoma Nelumbinis of ammonium sulfate workshop section existing with coking and ammonia still process workshop section is closed and is connected simultaneously,
Make full use of and excavated automatically cleaning and the self-purification function of coking flow process；Construction investment and operating cost are greatly reduced.
4. this utility model uses integration apparatus, simultaneous SO_2 and NO removal, generates production by recycling by one section of desulphurization denitration
Product, two-stage nitration desulphurization denitration and ammonium sulfate liquor are caught ammonia section and are eliminated the escaping of ammonia, mist catching section elimination acid mist, not only complete several functions
Integrated, enhance desulphurization and denitration, catch ammonia, except fog effect, also significantly reduce desulphurization denitration investment；Improve coke oven
Stack gas cleaning degree and environmental quality.
5. this utility model patent uses oxidizing process to utilize the outer denitration of ozone stove, can fully recycle flue gases of cock oven
Waste heat, and realize the removing of nitrogen oxides at a lower temperature, can effectively reduce denitration cost；By one section of desulphurization denitration
Section, two-stage nitration desulphurization denitration section add hydrogen peroxide and carry out oxidation, strengthen denitration efficiency, reduce ozone-depleting, reduce and run into
This.
6. this utility model has fully reclaimed the UTILIZATION OF VESIDUAL HEAT IN of flue gas.Waste heat boiler is utilized to reclaim high-temperature residual heat, by-product
Steam, or directly heat distilled ammonia wastewater, or heating conduction oil；Flue gas after utilizing low temperature exhaust heat heating desulphurization denitration to purify,
Effectively eliminate the dew point corrosion of flue gas, take full advantage of the high altitude discharge advantage of original chimney.Coking stream is utilized by profit
Journey internal resource ammonium sulfate liquor washing flue gas, further avoid ammonia process of desulfurization denitration and would generally produce what free ammonia vapour phase was escaped
Phenomenon, does not only increase cost, and improves the inside networking degree of coking flow process, efficiently solve the ammonia of desulphurization denitration process
Escape phenomenon.
7. this utility model develops circulation oxidator, effectively improves sulfite oxidation effect.
Accompanying drawing explanation
Fig. 1 is the structural representation of utility model.
Detailed description of the invention
In order to be more fully understood that this utility model, explain in detail embodiment of the present utility model below in conjunction with the accompanying drawings.
As it is shown in figure 1, the double ammonia process integration desulfurization denitration system of a kind of coking flue gas two-part, including denitration in the stove system
System 1, chimney 2, waste heat boiler 3, smoke re-heater 4, flue gas blower fan 5, scrubber 6, cleaning dust circulating pump 7, washing remove
Dirt cooler 8, ozonator 9, pipeline reactor 10, desulphurization denitration integrated tower 11, one section of circulating pump 12, one-step cooling device
13, two-stage nitration circulating pump 14, two-step cooling device 15, circulation oxidator 16, circulation cycle pump 17, penetrate haustorium 18, coke oven 19.Described stove
Interior denitrating system 1 is connected with coke oven 19 by dilution air line 29 and dilution gas piping 28, and coke oven 19 passes through coke oven flue gas
Pipeline is connected with chimney 2, and chimney 2 is connected with waste heat boiler 3 by coke oven flue gas pipeline, and waste heat boiler 3 is high by recovered flue gas
After temperature waste heat, flue is connected with smoke re-heater 4, and smoke re-heater 4 is by flue and flue gas after recovery low temperature exhaust heat
Blower fan 5 connects, and flue gas blower fan 5 is connected with scrubber 6 by pipeline, and scrubber 6 bottom is passed through liquid pipe and washed
Washing circulating pump 7 to connect, cleaning circulation pump 7 is connected with cleaning dust cooler 8 by lower liquid phase outlet conduit, and cleaning dust is cold
But device 8 is connected with scrubber 6 upper entrance pipeline, and scrubber 6 is by pipeline and pipeline reactor after cleaning dust
10 connect, and pipeline reactor 10 is connected with ozonator 9 by ozone pipeline, and pipeline reactor 10 is by fume pipe after reaction
Road is connected with desulphurization denitration integrated tower 11.Desulphurization denitration integrated tower 11 top is by flue after purifying and smoke re-heater 4
Connecting, smoke re-heater 4 is connected with chimney 2 by purifying smoke pipeline.The purifying smoke discharging desulphurization denitration integrated tower enters
Smoke re-heater, before utilizing desulphurization denitration, the low temperature exhaust heat heating of flue gas is increased to 100-150 DEG C, returns chimney, high idle discharge
Put.
Described desulphurization denitration integrated tower includes the two-stage nitration desulphurization denitration section at one section of desulphurization denitration section of bottom, middle part, two-stage nitration
The top of desulphurization denitration section is provided with catches ammonia section, catches ammonia section top and is provided with physical property demister.Described one section of desulphurization denitration section with
The scrubbing ammonia waterpipe 20 of strong aqua ammonia pipeline 21 or raw coke oven gas desulfurization regeneration tail gas connects, described strong aqua ammonia pipeline and coking
The strong aqua ammonia pipeline of ammonia still process workshop section connects, described scrubbing ammonia waterpipe and the scrubbing ammonia waterpipe of raw coke oven gas desulfurization regeneration tail gas
Connect, take off as desulfurization from the strong aqua ammonia of coking ammonia still process workshop section or the washing ammonia of coal oven dithio-gas desulfurization regeneration tail gas
The alkali source of nitre adds one section of desulphurization denitration section.One section of circulating pump 12 is by one section of circulation ammonium liquid pipeline and desulphurization denitration integrated tower 11
Connecting, one-step cooling device 13 is connected by one section of circulation ammonium liquid pipeline and one section of circulating pump 12, and one-step cooling device 13 is by one section
Circulation ammonium liquid pipeline is connected with desulphurization denitration integrated tower 11, and one section of desulphurization denitration section of desulphurization denitration integrated tower 11 passes through ammonium liquid side
Spool road is connected with circulation oxidator 16, and the outlet of circulation cycle pump 17 is by circulation cycle pipeline 30 top and circulation oxidator
16 tops connect, and described circulation cycle pipeline 30 top is provided with ejector 18, circulation near the position on circulation oxidator 16 top
The import of circulating pump 17 is connected bottom circulation oxidator 16 by circulation cycle pipeline bottom, and circulation cycle pump 17 passes through branch line
Ammonium sulfate after oxidation and ammonium nitrate mixed-ammonium salt solution are sent to ammonium sulfate workshop section 27 Resource recovery of coking by outlet and pipeline
Product or for complex acid.
Described two-stage nitration desulphurization denitration section is connected, from coking by pipeline 22 with the remained ammonia from coking ammonia still process workshop section
The remained ammonia of ammonia still process workshop section passes through the pipeline 22 diluent addition two-stage nitration desulphurization denitration section as ammonia concentration, described two-stage nitration
The bottom of desulphurization denitration section is connected with two-stage nitration circulating pump 14 import by two-stage nitration circulation fluid pipeline, and two-stage nitration circulating pump 14 outlet is passed through
Two-stage nitration circulation fluid pipeline is connected with two-step cooling device 15, and two-step cooling device 15 is by two-stage nitration circulation fluid pipeline and two-stage nitration desulphurization denitration
The top of section connects.Remained ammonia is sent to the ammonia still process of the ammonia still process workshop section of coking by the spur outlet of two-stage nitration circulating pump 14 by pipeline
Tower 25.
In two-stage nitration desulphurization denitration section, add two-stage nitration desulphurization denitration from the remained ammonia before coking ammonia still process workshop section ammonia still
Section, dilution is from ammonia vapour phase concentration in the flue gas after one section of desulphurization denitration section.Most of surplus ammonia passes through two-stage nitration circulating pump
Send into two-stage nitration recirculation cooler, after one section of recirculation cooler controls temperature, add two from the top of one section of desulphurization denitration tower
Section desulphurization denitration section, connects with the flue gases of cock oven adverse current from the entrance of two-stage nitration desulphurization denitration pars infrasegmentalis, from one section of desulphurization denitration section
Touch, on the one hand complete the removing of remaining sulfur dioxide and nitrogen oxides, on the other hand reduce the ammonia dividing potential drop in gas phase, control ammonia and escape
Ease.According to the principle of material balance, small part circulation fluid returns the ammonia still of coking ammonia still process workshop section.The control of one section of desulphurization denitration section
Temperature processed is 50-80 DEG C, and pH controls as 5.5-6.2.
Add hydrogen peroxide carry out oxidation in one section of described desulphurization denitration section, two-stage nitration desulphurization denitration section.At Ta Neijia
Enter hydrogen peroxide oxidation effect, improve denitration efficiency, it is possible to reduce ozone usage, reduce operating cost.
Described ammonia section of catching is connected with ammonium sulfate liquor pipeline 23, and the ammonium sulfate liquor washing two-stage desulfurization utilizing sulphuric acid workshop section is clean
Flue gas after change, ammonium sulfate liquor washing flue gas returns ammonium sulfate workshop section 24 by pipeline after catching residue ammonia.Through two-stage nitration desulfurization
Flue gas after denitration, enter desulphurization denitration integrated tower top catches ammonia section, utilizes the acid mother liquid washing flue of ammonium sulfate workshop section
Gas, acid mother liquid washing flue gas returns ammonium sulfate workshop section after catching residue ammonia.The control temperature catching ammonia section is 50-70 DEG C.If it is logical
After crossing two-stage nitration desulphurization denitration, the ammonia content in flue gas is up to standard, and this catches ammonia section and can not put into operation as standby measure.
After described physical property demister intercepts power elimination flue gas acid mist by centrifugal force and inertia, flue gas is from desulfurization
Denitration integrated tower 11 top is discharged.Flue gas after catching ammonia section enters the demister at desulphurization denitration integrated tower top, logical
After crossing centrifugal force and inertia interception power elimination flue gas acid mist, flue gas is discharged from desulphurization denitration integrated tower top, enters flue gas
Reheater, after the low temperature exhaust heat of flue gas heats before utilizing desulphurization denitration, returns chimney, high altitude discharge.The temperature control of mist catching section
It is made as 50-60 DEG C.
Ejector 18 uses venturi tube structure, ejector 18 to be connected with external air duct 26, utilize venturi tube structure
Ejector 18 circulation injection suction is incorporated herein the air oxidant as circulation oxidator.In circulation oxidator, pass through ring
The suction that the circulation injection of stream circulating pump produces introduces air, and abundant and ammonium liquid is sufficiently mixed reaction, by ammonium sulfite therein
Generating ammonium sulfate, the mixed salt solution containing ammonium sulfate and ammonium nitrate the most at last is sent to the ammonium sulfate workshop section of coking, and Resource recoveryization is produced
Product.Controlling temperature in circulation oxidator and be 50-100 DEG C, pH controls as 6.0-6.8.
Described dilution air line 29 is dilution air by the flue gas after the flue gas after waste heat recovery or purification, or
Being mixed into noble gas in atmosphere, the mixed volume of described flue gas or noble gas is the 0-50% of air capacity；Adding hot coal
Being mixed into low-heat value gas in gas, such as dilution coal gas measures such as blast furnace gas, vaporization coal gas and water coal gas, mixed volume is heating gas
The 0-70% of amount, reduces coke oven and discharges the amount of nitrogen oxides in flue gas, and the amount of nitrogen oxides making coke oven discharge in flue gas is
250-550mg/M3。
Coke oven flue temperature after denitration in the stove system 1 denitration processes is 220-350 DEG C, coke oven flue pneumatic transmission
Entering waste heat boiler and reclaim flue gas high-temperature residual heat, the waste heat that waste heat boiler reclaims is used as to produce steam, or is directly used in ammonia still process and adds
Hot distilled ammonia wastewater, or heating conduction oil, after reclaiming high-temperature residual heat, effluent gas temperature is down to 150-200 DEG C；Return through waste heat boiler
Receiving the flue gas after high-temperature residual heat and send into smoke re-heater recovery flue gases at low waste heat, that is discharged by desulphurization denitration integrated tower is clean
Changing flue gas and be heated to 100-150 DEG C from 50-80 DEG C, own temperature is down to 90-130 DEG C；Cigarette after reclaiming low temperature exhaust heat
Road gas sends into scrubber by flue gas blower fan, utilizes cleaning circulation pump by cycles of washing liquid from washing in scrubber
Cleaner unit top sprays into, with fed from below into flue gas counter current contacting, washing removing flue gas in dust impurity, flue gas
It is cooled to 60-80 DEG C further.The dust obtained after spray is enriched with at scrubber bottom precipitation, periodically discharges it, and makees
For fixed-end forces.Cycles of washing liquid can use clear water, the outer draining of available cycles, it is also possible to give up after waste water or biochemical treatment after ammonia still process
Water.
Flue gas after washing cooling is sufficiently mixed instead with the ozone from ozonator in pipeline reactor
Should, after the nitric oxide in flue gases of cock oven is partly or entirely aoxidized, send into desulphurization denitration integrated tower and carry out at desulphurization denitration
Reason.According to technique needs, this oxidation reactor realizes oxidation reaction function in may also placed in desulphurization denitration integrated tower.
One section of desulphurization denitration section, from strong aqua ammonia or the washing of coke oven gas desulfurization regenerator top of coking ammonia still process workshop section
Liquid adds one section of desulphurization denitration section, anti-with sending into sulfur dioxide and nitrogen oxides in flue gases of cock oven from one section of desulphurization denitration section
Should, generating ammonium sulfite and the solution of ammonium nitrate, major part ammonium salt solution sends into one section of recirculation cooler by one section of circulating pump,
After one section of recirculation cooler controls temperature, add one section of desulphurization denitration section from the top of one section of desulphurization denitration tower, and from one
The flue gases of cock oven counter current contacting of section desulphurization denitration pars infrasegmentalis, completes desulphurization denitration process.According to the principle of material balance, few portion
Divide ammonium liquid to send into circulation oxidator to aoxidize further.The control temperature of one section of desulphurization denitration section is 50-80 DEG C, and pH controls as 5.8-
6.5。
In circulation oxidator, sprayed the suction produced by the circulation of circulation cycle pump, introduce air, abundant and ammonium
Liquid is sufficiently mixed reaction, ammonium sulfite therein is generated ammonium sulfate, contains the mixed salt solution of ammonium sulfate and ammonium nitrate the most at last
It is sent to the ammonium sulfate workshop section of coking, Resource recovery product.Controlling temperature in circulation oxidator and be 50-80 DEG C, pH controls as 6.0-
6.8。
Technical specification after this utility model processes is as follows:
Index after gas cleaning
SO2:≤50mg/Nm3；
NOX:≤100mg/Nm3；
NH3:≤1mg/Nm3；
Dust content :≤5mg/Nm3；
Sulphuric acid mist content :≤5mg/Nm3。
Although the detailed description of the invention of utility model is described by the above-mentioned accompanying drawing that combines, but not to this utility model
The restriction of protection domain, on the basis of the technical solution of the utility model, those skilled in the art need not pay creativeness
Various amendments that work can be made or deformation are still within protection domain of the present utility model.
Claims (6)
1. the double ammonia process integration desulfurization denitration system of coking flue gas two-part, including denitration in the stove system, chimney, waste heat
Boiler, smoke re-heater, coke oven, is characterized in that, also includes that flue gas blower fan, scrubber, cleaning dust circulating pump, washing remove
Dirt cooler, ozonator, pipeline reactor, desulphurization denitration integrated tower, circulation oxidator, described denitration in the stove system is passed through
Dilution air line and dilution gas piping are connected with coke oven, and coke oven is connected with chimney by coke oven flue gas pipeline, and chimney passes through
Coke oven flue gas pipeline is connected with waste heat boiler, and waste heat boiler is by flue and smoke re-heater after recovered flue gas high-temperature residual heat
Connecting, smoke re-heater is connected with flue gas blower fan by reclaiming flue after low temperature exhaust heat, flue gas blower and pipeline with wash
Washing cleaner unit to connect, scrubber bottom is connected with cleaning circulation pump by liquid pipe, and cleaning circulation pump passes through bottom liquid
Phase outlet conduit is connected with cleaning dust cooler, and cleaning dust cooler is connected with scrubber upper entrance pipeline, washes
Washing cleaner unit to be connected with pipeline reactor by pipeline after cleaning dust, pipeline reactor passes through ozone pipeline and ozonator
Connecting, pipeline reactor is connected with desulphurization denitration integrated tower by flue after reaction, the flue gas after washing cooling
In pipeline reactor, reaction it is sufficiently mixed, by the nitric oxide part in flue gases of cock oven with the ozone from ozonator
Or after all aoxidizing, send into desulphurization denitration integrated tower and carry out desulphurization denitration process；After desulphurization denitration integrated tower top is by purifying
Flue is connected with smoke re-heater, and smoke re-heater is connected with chimney by purifying smoke pipeline, discharges desulphurization denitration one
The purifying smoke of body tower enters smoke re-heater, and before utilizing desulphurization denitration, the low temperature exhaust heat heating of flue gas is increased to 100-150
DEG C return chimney, high altitude discharge.
2. the double ammonia process integration desulfurization denitration system of coking flue gas two-part as claimed in claim 1, is characterized in that, described
Desulphurization denitration integrated tower includes the two-stage nitration desulphurization denitration section at one section of desulphurization denitration section of bottom, middle part, two-stage nitration desulphurization denitration section
Top is provided with catches ammonia section, catches ammonia section top and is provided with physical property demister, described one section of desulphurization denitration section and strong aqua ammonia pipeline or
The scrubbing ammonia waterpipe of person's raw coke oven gas desulfurization regeneration tail gas connects, the strong aqua ammonia of described strong aqua ammonia pipeline and coking ammonia still process workshop section
Pipeline connects, and described scrubbing ammonia waterpipe is connected with the scrubbing ammonia waterpipe of raw coke oven gas desulfurization regeneration tail gas, steams from coking
The strong aqua ammonia of ammonia workshop section or the washing ammonia of raw coke oven gas desulfurization regeneration tail gas are de-as the alkali source addition one section of desulphurization denitration
Sulfur denitration section, one section of circulating pump is connected with desulphurization denitration integrated tower by one section of circulation ammonium liquid pipeline, and one-step cooling device passes through one
Duan Xunhuan ammonium liquid pipeline and one section of circulating pump connect, and one-step cooling device is by one section of circulation ammonium liquid pipeline and desulphurization denitration integrated tower
Connecting, one section of desulphurization denitration section of desulphurization denitration integrated tower is connected with circulation oxidator by ammonium liquid side line pipeline, circulation cycle
Delivery side of pump is connected with circulation oxidator top by circulation cycle conduit upper, and described circulation cycle conduit upper is near circulation
The position on oxidator top is provided with ejector, and the import of circulation cycle pump is at the bottom of by circulation cycle pipeline bottom and circulation oxidator
Portion connects, and the ammonium sulfate after oxidation and ammonium nitrate mixed-ammonium salt solution are sent to Jiao by spur outlet and pipeline by circulation cycle pump
The ammonium sulfate workshop section Resource recovery product changed or for complex acid；
Described two-stage nitration desulphurization denitration section is connected by pipeline, from coking ammonia still process work with the remained ammonia from coking ammonia still process workshop section
The remained ammonia of section passes through the pipeline diluent addition two-stage nitration desulphurization denitration section as ammonia concentration, described two-stage nitration desulphurization denitration
The bottom of section is connected with two-stage nitration pump inlet by two-stage nitration circulation fluid pipeline, and two-stage nitration circulating-pump outlet passes through two-stage nitration circulation fluid pipe
Road is connected with two-step cooling device, and two-step cooling device is connected with the top of two-stage nitration desulphurization denitration section by two-stage nitration circulation fluid pipeline, and two
Remained ammonia is sent to the ammonia still of the ammonia still process workshop section of coking by the spur outlet of section circulating pump by pipeline；
Described ammonia section of catching is connected with ammonium sulfate liquor pipeline, the flue gas after two-stage nitration desulphurization denitration, enters desulphurization denitration one
Tower top catch ammonia section, utilize sulphuric acid workshop section acid mother liquid washing flue gas, sulfur ammonium acid mother liquid washing flue gas catch residue
Returning ammonium sulfate workshop section after ammonia, the control temperature catching ammonia section is 50-70 DEG C；
After described physical property demister intercepts power elimination flue gas acid mist by centrifugal force and inertia, flue gas is from desulphurization denitration
Integrated tower top is discharged；Flue gas after catching ammonia section enters the physical property demister at desulphurization denitration integrated tower top, logical
After crossing centrifugal force and inertia interception power elimination flue gas acid mist, flue gas is discharged from desulphurization denitration integrated tower top, enters flue gas
Reheater, after the low temperature exhaust heat of flue gas heats before utilizing desulphurization denitration, returns chimney, high altitude discharge；The temperature control of mist catching section
It is made as 50-60 DEG C.
3. the double ammonia process integration desulfurization denitration system of coking flue gas two-part as claimed in claim 1, is characterized in that, injection
Device uses venturi tube structure, and ejector is connected with external air duct, utilizes the ejector circulation injection suction of venturi tube structure
Air oxidant as circulation oxidator is incorporated herein, is sprayed the suction produced by the circulation of circulation cycle pump and introduce sky
Gas, the oxygen in air is fully and ammonium liquid is sufficiently mixed reaction, and ammonium sulfite therein is generated ammonium sulfate, then will be containing sulfur
The mixed salt solution of acid ammonium and ammonium nitrate controls in being sent to the ammonium sulfate workshop section of coking, Resource recovery product, described circulation oxidator
Temperature is 50-80 DEG C, and pH controls as 6.0-6.8.
4. the double ammonia process integration desulfurization denitration system of coking flue gas two-part as claimed in claim 1, is characterized in that, described
Flue gas after dilution air line waste heat recovery or the flue gas after purification are dilution air, or are mixed into lazy in atmosphere
Property gas, the mixed volume of flue gas or noble gas is the 0-50% of air capacity；Low-heat value gas it is mixed in heating gas,
Low-heat value gas mixed volume is the 0-70% of heating gas amount, reduces coke oven and discharges the amount of nitrogen oxides in flue gas, makes coke oven
The amount of nitrogen oxides discharged in flue gas is 250-550mg/m3。
5. the double ammonia process integration desulfurization denitration system of coking flue gas two-part as described in claim 1 or 2, its feature
Being that the coke oven flue temperature after denitration in the stove system denitration processes is 220-350 DEG C, flue gases of cock oven sends into waste heat pot
Stove recovery flue gas high-temperature residual heat, the waste heat that waste heat boiler reclaims is used as to produce steam, or it is useless to be directly used in ammonia still process heating ammonia still process
Water, or heating conduction oil, reclaim high-temperature residual heat rear pass temperature and be down to 150-200 DEG C；More than waste heat boiler recovery high temperature
Flue gas after heat is sent into smoke re-heater and is reclaimed flue gases at low waste heat, the purification flue gas discharged by desulphurization denitration integrated tower
Being heated to 100-150 DEG C from 50-80 DEG C, own temperature is down to 90-130 DEG C；Flue gas after reclaiming low temperature exhaust heat is passed through
Scrubber sent into by flue gas blower fan, utilizes cleaning circulation pump by cycles of washing liquid in scrubber from scrubber
Portion sprays into, with fed from below into flue gas counter current contacting, washing removing flue gas in dust impurity, flue gas drops further
Temperature is to 60-80 DEG C.
6. the double ammonia process integration desulfurization denitration system of coking flue gas two-part as claimed in claim 2, is characterized in that, in institute
One section of desulphurization denitration section, the two-stage nitration desulphurization denitration section stated add hydrogen peroxide and carry out oxidation.
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| CN201620400716.5U CN205815447U (en) | 2016-05-05 | 2016-05-05 | The double ammonia process integration desulfurization denitration system of coking flue gas two-part |
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| CN201620400716.5U CN205815447U (en) | 2016-05-05 | 2016-05-05 | The double ammonia process integration desulfurization denitration system of coking flue gas two-part |
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Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN105797562A (en) * | 2016-05-05 | 2016-07-27 | 济南冶金化工设备有限公司 | Two-section type double-ammonia-process integrated desulfurization and denitration system for coking flue gas |
| CN107213785A (en) * | 2017-05-25 | 2017-09-29 | 江苏新世纪江南环保股份有限公司 | A kind of method and device of FCC tail gas by ammonia method denitration desulfurization and dedusting |
| CN107388847A (en) * | 2017-07-12 | 2017-11-24 | 天津大学 | Heat reclaim unit and technique in flue gas desulfurization and denitration technique |
| CN108744930A (en) * | 2018-06-13 | 2018-11-06 | 哈尔滨工程大学 | A kind of system of the high efficiente callback gas fired-boiler fume afterheat based on injector |
| CN112370952A (en) * | 2020-09-16 | 2021-02-19 | 江苏汇能环境工程有限公司 | Factory-used waste gas desulfurization and denitrification treatment device |
| CN115006977A (en) * | 2022-06-28 | 2022-09-06 | 常州工学院 | Comprehensive treatment device for coke oven flue gas |
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2016
- 2016-05-05 CN CN201620400716.5U patent/CN205815447U/en not_active Withdrawn - After Issue
Cited By (12)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN105797562A (en) * | 2016-05-05 | 2016-07-27 | 济南冶金化工设备有限公司 | Two-section type double-ammonia-process integrated desulfurization and denitration system for coking flue gas |
| CN105797562B (en) * | 2016-05-05 | 2018-05-15 | 济南冶金化工设备有限公司 | The double ammonia process integration desulfurization denitration systems of coking flue gas two-part |
| CN107213785A (en) * | 2017-05-25 | 2017-09-29 | 江苏新世纪江南环保股份有限公司 | A kind of method and device of FCC tail gas by ammonia method denitration desulfurization and dedusting |
| EP3406320A1 (en) * | 2017-05-25 | 2018-11-28 | Jiangnan Environmental Protection Group Inc. | Method and apparatus for denitration and desulfurization of and dust removal from fcc tail gas by ammonia-based process |
| KR20180129588A (en) * | 2017-05-25 | 2018-12-05 | 지앙난 엔바이론멘탈 프로텍션 그룹, 인크. | Method and apparatus for denitration and desulfurization of and dust removal from FCC tail gas by ammonia-based process |
| US10343110B2 (en) | 2017-05-25 | 2019-07-09 | Jiangnan Environmental Protection Group Inc. | Dust removal and desulfurization of FCC exhaust gas |
| KR102022305B1 (en) * | 2017-05-25 | 2019-09-18 | 지앙난 엔바이론멘탈 프로텍션 그룹, 인크. | Method and apparatus for denitration and desulfurization of and dust removal from FCC tail gas by ammonia-based process |
| US10471383B2 (en) | 2017-05-25 | 2019-11-12 | Jiangnan Environmental Protection Group Inc. | Dust removal and desulfurization of FCC exhaust gas |
| CN107388847A (en) * | 2017-07-12 | 2017-11-24 | 天津大学 | Heat reclaim unit and technique in flue gas desulfurization and denitration technique |
| CN108744930A (en) * | 2018-06-13 | 2018-11-06 | 哈尔滨工程大学 | A kind of system of the high efficiente callback gas fired-boiler fume afterheat based on injector |
| CN112370952A (en) * | 2020-09-16 | 2021-02-19 | 江苏汇能环境工程有限公司 | Factory-used waste gas desulfurization and denitrification treatment device |
| CN115006977A (en) * | 2022-06-28 | 2022-09-06 | 常州工学院 | Comprehensive treatment device for coke oven flue gas |
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