CN105797562B - The double ammonia process integration desulfurization denitration systems of coking flue gas two-part - Google Patents
The double ammonia process integration desulfurization denitration systems of coking flue gas two-part Download PDFInfo
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- CN105797562B CN105797562B CN201610293501.2A CN201610293501A CN105797562B CN 105797562 B CN105797562 B CN 105797562B CN 201610293501 A CN201610293501 A CN 201610293501A CN 105797562 B CN105797562 B CN 105797562B
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Abstract
The invention discloses the double ammonia process integration desulfurization denitration systems 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 leads 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 wind turbine,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 ozone generator,Pipeline reactor is connected with desulphurization denitration integrated tower,It is connected at the top of desulphurization denitration integrated tower with smoke re-heater,Smoke re-heater is connected with chimney,The purifying smoke for discharging desulphurization denitration integrated tower enters return chimney high altitude discharge after smoke re-heater heat temperature raising.Denitration cost of the present invention is low, efficient.
Description
Technical field
The present invention relates to coking stack gases purification technology field, more particularly to a kind of coking flue gas two-part are double
Ammonia（Ammonium）Method integration desulfurization denitration system.
Background technology
The desulphurization denitration processing and the processing of ammonia-containing water of coking flue gas of the prior art have various ways, to reach energy
Source recycling, reduce energy consumption, the purpose for reducing environmental pollution and destroying, but these method and apparatus of the prior art are deposited
The defects of be：The flue gas desulfurization and denitration method having in the prior art is of high cost, such as high temperature method of the prior art and catalysis
Method method of denitration is of high cost；Some desulfurization off sulfide effect are poor, residual quantity is big, and clean-up effect is bad, while vapour phase amount of ammonia slip is more,
Environment and air are polluted.
The present invention is applicant on the basis of original applying number is 201510690115.2 patents of invention, passes through persistence techniques
Innovation, further reduces technological equipment investment and the operating cost of desulphurization denitration.
The content of the invention
It is to solve the problems, such as that existing flue gases of cock oven desulphurization denitration high expensive, investment are bigger than normal that the purpose of the present invention, which is exactly,
There is provided a kind of coking flue gas two-part double ammonia（Ammonium）Method integration desulfurization denitration system.The present invention utilizes the self-produced ammonium hydroxide of coking
As alkali source, desulphurization denitration purification is carried out to flue gas, recyclable ammonium sulfate is formed and ammonium nitrate is incorporated to the sulphur of coking flow
Ammonium workshop section, the element sulphur in stack gases and nitrogen are converted into can value-added byproduct；Of the invention fully combine in stove takes off
Nitre and the outer denitration technology of stove, significantly reduce denitration cost；The present invention uses the ammonium hydroxide desulphurization denitration of various concentrations, and concentrated ammonia liquor can
To form resource product, weak aqua ammonia reduces the vapour phase partial pressure of ammonia, reduces the escaping of ammonia；The present invention uses integration apparatus, at the same time
Desulphurization denitration, significantly reduces desulphurization denitration investment；The present invention is using hydrogen peroxide denitration in the outer denitration of ozone stove, tower, relatively low
At a temperature of realize the removing of NOx, significantly reduce denitration cost；The present invention is washed using coking flow internal resource ammonium sulfate liquor
Flue gas is washed, further avoid ammonia process of desulfurization denitration would generally produce the phenomenon of free ammonia vapour phase escape, not increase cost not only,
And the inside networking degree of coking flow is improved, efficiently solve the escaping of ammonia phenomenon of desulphurization denitration process.
The present invention solve technical problem technical solution be：
A kind of double ammonia process integration desulfurization denitration systems of coking flue gas two-part, including it is denitration in the stove system, chimney, remaining
Heat boiler, smoke re-heater, coke oven, further include flue gas wind turbine, scrubber, cleaning dust circulating pump, cleaning dust cooling
Device, ozone generator, pipeline reactor, desulphurization denitration integrated tower, circulation oxidator, the denitration in the stove system are empty by dilution
Feed channel or dilution nitrogen pipeline are connected with coke oven, and coke oven is connected by coke oven flue gas pipeline with chimney, and chimney passes through coke oven cigarette
Feed channel is connected with waste heat boiler, and waste heat boiler is connected by flue after recovered flue gas high-temperature residual heat with smoke re-heater,
Smoke re-heater is connected by flue after recycling low temperature exhaust heat with flue gas wind turbine, flue gas blower and pipeline and cleaning dust
Device connects, and scrubber lower part is connected by liquid pipe with cleaning circulation pump, 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 by pipeline after cleaning dust with pipeline reactor, and pipeline reactor is connected by ozone pipeline with ozone generator,
Pipeline reactor is connected by flue after reaction with desulphurization denitration integrated tower, and the flue gas after washing cools down is with coming from
The ozone of ozone generator is sufficiently mixed reaction in pipeline reactor, and the nitric oxide in flue gases of cock oven is part or all of
After oxidation, it is sent into desulphurization denitration integrated tower and carries out desulphurization denitration processing；Pass through fume pipe after purification at the top of desulphurization denitration integrated tower
Road is connected with smoke re-heater, and smoke re-heater is connected by purifying smoke pipeline with chimney, discharge desulphurization denitration integrated tower
Purifying smoke enters smoke re-heater, and 100-150 °C of return is increased to using the low temperature exhaust heat heating of flue gas before desulphurization denitration
Chimney, high altitude discharge.
The desulphurization denitration integrated tower includes one section of desulphurization denitration section, the two sections of desulphurization denitration sections at middle part of lower part, two sections
The top of desulphurization denitration section is equipped with and catches ammonia section, catches ammonia section top and is equipped with physical demister.One section of desulphurization denitration section with
The scrubbing ammonia waterpipe of concentrated ammonia liquor pipeline or raw coke oven gas desulfurization regeneration tail gas connects, the concentrated ammonia liquor pipeline and coking ammonia still process
The concentrated ammonia liquor pipeline connection of workshop section, the scrubbing ammonia waterpipe of the scrubbing ammonia waterpipe and raw coke oven gas desulfurization regeneration tail gas connect
Connect, the alkali of the washing ammonium hydroxide of concentrated ammonia liquor or raw coke oven gas desulfurization regeneration tail gas from coking ammonia still process workshop section as desulphurization denitration
Source adds one section of desulphurization denitration section.One section of circulating pump is connected by one section of circulation ammonium liquid pipe road with desulphurization denitration integrated tower, one section
Cooler is connected by one section of circulation ammonium liquid pipe road with one section of circulating pump, and one-step cooling device is by one section of circulation ammonium liquid pipe road with taking off
Sulphur denitration integrated tower connects, and one section of desulphurization denitration section of desulphurization denitration integrated tower is connected by ammonium liquid side line pipeline and circulation oxidator
Connect, the outlet of circulation cycle pump is connected by circulation cycle conduit upper with circulation oxidator top, the circulation cycle pipeline
Top is equipped with injector close to the position on circulation oxidator top, the import of circulation cycle pump by circulation cycle pipeline lower part with
Circulation oxidator bottom connects, and circulation cycle pump is mixed the ammonium sulfate after oxidation and ammonium nitrate by spur outlet and pipeline
Ammonium salt solution is sent to the ammonium sulfate workshop section Resource recovery product of coking or for complex acid；
Two sections of desulphurization denitration sections are connected with the remained ammonia from coking ammonia still process workshop section by pipeline, are steamed from coking
The diluent that the remained ammonia of ammonia workshop section is used as vapour phase ammonia density by pipeline adds two sections of desulphurization denitration sections, two sections of desulfurization
The bottom of denitration section is connected by two sections of circulation fluid pipelines with two sections of pump inlets, and two sections of circulating-pump outlets pass through two sections of circulations
Liquid pipe road is connected with two-step cooling device, and two-step cooling device is connected by the top of two sections of circulation fluid pipelines and two sections of desulphurization denitration sections
Connect.Remained ammonia is sent to the ammonia still of the ammonia still process workshop section of coking by pipeline by the spur outlet of two sections of circulating pumps.
The ammonia section of catching is connected with ammonium sulfate liquor pipeline, the flue gas after two sections of desulphurization denitrations, into desulphurization denitration
Ammonia section is caught on integrated tower top, washs flue gas using the acid mother liquid of sulfuric acid workshop section, sulphur ammonium acid mother liquid washing flue gas is caught
Return to ammonium sulfate workshop section after remaining ammonia, catch ammonia section controlled at 50-70 °C.
The physical demister is intercepted after power eliminates flue gas acid mist by centrifugal force and inertia, and flue gas is from desulfurization
Discharge on denitration integrated tower top；Flue gas after catching ammonia section enters the physical demisting dress at the top of desulphurization denitration integrated tower
Put, after intercepting power elimination flue gas acid mist by centrifugal force and inertia, flue gas is discharged at the top of desulphurization denitration integrated tower；It is described
The temperature control of physical demister is 50-60 °C.
The injector uses venturi tube structure, and injector is connected with external air duct, utilizes the spray of venturi tube structure
Oxidant of the air as circulation oxidator is incorporated herein in emitter circulation injection suction, and the circulation pumped by circulation cycle sprays production
Raw suction introduces air, and the oxygen in air is fully sufficiently mixed reaction with ammonium liquid, by ammonium sulfite therein generation sulfuric acid
Mixed salt solution containing ammonium sulfate and ammonium nitrate, is then sent to the ammonium sulfate workshop section of coking, Resource recovery product, the ring by ammonium
Flow controlled at 50-80 °C in oxidator, pH controls are 6.0-6.8.
The dilution air pipeline is dilution air with the flue gas after waste heat recovery or purified flue gas, Huo Zhe
It is mixed into inert gas in air, the mixed volume of flue gas or inert gas is the 0-50% of air capacity；It is mixed into heating gas
Low-heat value gas, low-heat value gas mixed volume are the 0-70% of heating gas amount, and the nitrogen oxides reduced in coke oven discharge flue gas contains
Amount, it is 250-550mg/m3 to make the amount of nitrogen oxides in coke oven discharge flue gas.
Flue gases of cock oven temperature after denitration in the stove system denitration process is 220-350 °C, and flue gases of cock oven is sent into
Waste heat boiler recycles flue gas high-temperature residual heat, and the waste heat of waste heat boiler recycling is used as producing steam, or is directly used in ammonia still process heating
Distilled ammonia wastewater, or heating conduction oil, after recycling high-temperature residual heat, effluent gas temperature is down to 150-200 °C；Recycled by waste heat boiler
Flue gas after high-temperature residual heat is sent into smoke re-heater recycling flue gases at low waste heat, the purification that desulphurization denitration integrated tower is discharged
Flue gas is heated to 100-150 °C from 50-80 °C, and own temperature is down to 90-130 °C；Flue after recycling low temperature exhaust heat
Gas is sent into scrubber by flue gas wind turbine, is removed wash cycle liquid from washing using cleaning circulation pump in scrubber
Dirt device top spray into, with fed from below into flue gas counter current contacting, washing removing flue gas in dust impurity, flue gas into
One step is cooled to 60-80 °C.
Flue gas after washing cools down is sufficiently mixed instead with the ozone from ozone generator in pipeline reactor
Should, after the nitric oxide in flue gases of cock oven partly or entirely oxidation, it is sent into desulphurization denitration integrated tower and carries out at desulphurization denitration
Reason.
Hydrogen peroxide, which is added, in one section of desulphurization denitration section, two sections of desulphurization denitration sections carries out oxidation.Strengthen denitration
Efficiency, reduces ozone-depleting, reduces operating cost.
Beneficial effects of the present invention：
1. the present invention carries out desulphurization denitration purification, formation can be returned by the use of the self-produced ammonium hydroxide of coking as alkali source to flue gas
The ammonium sulfate and ammonium nitrate of receipts are incorporated to the ammonium sulfate workshop section of coking flow, and the element sulphur in stack gases and nitrogen are converted into can
Value-added byproduct；Solid waste and pollution transportation are not produced.
2. of the invention fully combine denitration in the stove and the outer denitration technology of stove, denitration in the stove is using dilution air and dilution coal gas
Measure be combined, significantly reduce denitration cost.
3. the present invention uses the ammonium hydroxide desulphurization denitration of various concentrations, concentrated ammonia liquor can form resource product, weak aqua ammonia drop
The vapour phase partial pressure of low ammonia, reduces the escaping of ammonia, while the close lotus root of ammonium sulfate workshop section existing with coking and ammonia still process workshop section closes and is connected, fully
Using and excavated the automatically cleaning and self-purification function of coking flow；Construction investment and operating cost is greatly reduced.
4. the present invention uses integration apparatus, simultaneous SO_2 and NO removal, resource product, two are generated by one section of desulphurization denitration
Section desulphurization denitration and ammonium sulfate liquor catch ammonia section and eliminate the escaping of ammonia, physical demister elimination acid mist, not only complete a variety of work(
Can it is integrated, enhance desulphurization and denitration, catch ammonia, defogging effect, also significantly reduce desulphurization denitration investment；Improve
Flue gases of cock oven degree of purification and environmental quality.
5. patent of the present invention, using the outer denitration of ozone stove, can be recycled fully more than flue gases of cock oven using oxidizing process
Heat, and the removing of nitrogen oxides is realized at a lower temperature, it can effectively reduce denitration cost；By one section of desulphurization denitration section,
Two sections of desulphurization denitration sections add hydrogen peroxide and carry out oxidation, strengthen denitration efficiency, reduce ozone-depleting, reduce operating cost.
6. the present invention has fully recycled the UTILIZATION OF VESIDUAL HEAT IN of flue gas.Using waste heat boiler recycle high-temperature residual heat, byproduct steam,
Or distilled ammonia wastewater is directly heated, or heating conduction oil；The purified flue gas of desulphurization denitration is heated using low temperature exhaust heat, is effectively disappeared
Except the dew point corrosion of flue gas, the high altitude discharge advantage of original chimney is taken full advantage of.By profit using inside coking flow
Resource ammonium sulfate liquor washs flue gas, and further avoid ammonia process of desulfurization denitration would generally produce the phenomenon of free ammonia vapour phase escape,
Do not increase cost not only, and improve the inside networking degree of coking flow, efficiently solve the escaping of ammonia of desulphurization denitration process
Phenomenon.
7. the present invention develops circulation oxidator, sulfite oxidation effect is effectively improved.
Brief description of the drawings
Fig. 1 is the structure diagram of invention.
Embodiment
For a better understanding of the present invention, embodiments of the present invention are explained in detail below in conjunction with the accompanying drawings.
As shown in Figure 1, a kind of double ammonia process integration desulfurization denitration systems 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 wind turbine 5, scrubber 6, cleaning dust circulating pump 7, washing remove
Dirt cooler 8, ozone generator 9, pipeline reactor 10, desulphurization denitration integrated tower 11, one sections of circulating pumps 12, one-step cooling devices
13rd, two sections of circulating pumps 14, two-step cooling device 15, circulation oxidator 16, circulation cycle pump 17, injector 18, coke oven 19.The stove
Interior denitrating system 1 is connected by dilution air pipeline 29 and dilution gas piping 28 with coke oven 19, and coke oven 19 passes through coke oven flue gas
Pipeline is connected with chimney 2, and chimney 2 is connected by coke oven flue gas pipeline with waste heat boiler 3, and waste heat boiler 3 passes through recovered flue gas height
Flue is connected with smoke re-heater 4 after warm waste heat, and smoke re-heater 4 is by recycling flue and flue gas after low temperature exhaust heat
Wind turbine 5 connects, and flue gas wind turbine 5 is connected by pipeline with scrubber 6, and 6 lower part of scrubber is by liquid pipe with washing
Wash circulating pump 7 to connect, cleaning circulation pump 7 is connected by lower liquid phase outlet conduit with cleaning dust cooler 8, and cleaning dust is cold
But device 8 is connected with 6 upper entrance pipeline of scrubber, and scrubber 6 passes through pipeline after cleaning dust and pipeline reactor
10 connections, pipeline reactor 10 are connected by ozone pipeline with ozone generator 9, and pipeline reactor 10 passes through fume pipe after reaction
Road is connected with desulphurization denitration integrated tower 11.The top of desulphurization denitration integrated tower 11 passes through flue after purification and smoke re-heater 4
Connection, smoke re-heater 4 are connected by purifying smoke pipeline with chimney 2.The purifying smoke for discharging desulphurization denitration integrated tower enters
Smoke re-heater, is increased to 100-150 °C using the low temperature exhaust heat heating of flue gas before desulphurization denitration, returns to chimney, high idle discharge
Put.
The desulphurization denitration integrated tower includes one section of desulphurization denitration section, the two sections of desulphurization denitration sections at middle part of lower part, two sections
The top of desulphurization denitration section is equipped with and catches ammonia section, catches ammonia section top and is equipped with physical demister.One section of desulphurization denitration section with
The scrubbing ammonia waterpipe 20 of concentrated ammonia liquor pipeline 21 or raw coke oven gas desulfurization regeneration tail gas connects, the concentrated ammonia liquor pipeline and coking
The concentrated ammonia liquor pipeline connection of ammonia still process workshop section, the scrubbing ammonia waterpipe of the scrubbing ammonia waterpipe and raw coke oven gas desulfurization regeneration tail gas
Connection, the washing ammonium hydroxide of concentrated ammonia liquor or coal oven dithio-gas desulfurization regeneration tail gas from coking ammonia still process workshop section take off as desulfurization
The alkali source of nitre adds one section of desulphurization denitration section.One section of circulating pump 12 passes through one section of circulation ammonium liquid pipe road and desulphurization denitration integrated tower 11
Connection, one-step cooling device 13 are connected by one section of circulation ammonium liquid pipe road with one section of circulating pump 12, and one-step cooling device 13 passes through one section
Circulation ammonium liquid pipe road 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 passes through 30 top of circulation cycle pipeline and circulation oxidator
16 tops connect, and 30 top of circulation cycle pipeline is equipped with injector 18, circulation close to the position on 16 top of circulation oxidator
The import of circulating pump 17 is connected by circulation cycle pipeline lower part with 16 bottom of circulation oxidator, and circulation cycle pump 17 passes through branch line
Ammonium sulfate after oxidation and ammonium nitrate mixed-ammonium salt solution are sent to 27 Resource recovery of ammonium sulfate workshop section of coking by outlet and pipeline
Product or for complex acid.
Two sections of desulphurization denitration sections are connected with the remained ammonia from coking ammonia still process workshop section by pipeline 22, from coking
The remained ammonia of ammonia still process workshop section by pipeline 22 be used as vapour phase ammonia density diluent add two sections of desulphurization denitration sections, described two sections
The bottom of desulphurization denitration section is connected by two sections of circulation fluid pipelines with two sections of 14 imports of circulating pump, and two sections of outlets of circulating pump 14 pass through
Two sections of circulation fluid pipelines are connected with two-step cooling device 15, and two-step cooling device 15 passes through two sections of circulation fluid pipelines and two sections of desulphurization denitrations
The top connection of section.Remained ammonia is sent to the ammonia still process of the ammonia still process workshop section of coking by pipeline by the spur outlet of two sections of circulating pumps 14
Tower 25.
In two sections of desulphurization denitration sections, the remained ammonia before coking ammonia still process workshop section ammonia still adds two sections of desulphurization denitrations
Section, dilutes ammonia vapour phase concentration in the flue gas after one section of desulphurization denitration section.Most of remained ammonia passes through two sections of circulating pumps
Two sections of recirculation coolers are sent into, after one section of recirculation cooler controls temperature, two are added from the top of one section of desulphurization denitration tower
Section desulphurization denitration section, with entering from two sections of desulphurization denitration pars infrasegmentalises, the flue gases of cock oven from one section of desulphurization denitration section countercurrently connects
Touch, on the one hand complete the removing of remaining sulfur dioxide and nitrogen oxides, on the other hand reduce the ammonia partial pressure in gas phase, control ammonia is escaped
Ease.According to the principle of material balance, small part circulation fluid returns to the ammonia still of coking ammonia still process workshop section.The control of one section of desulphurization denitration section
Temperature processed is 50-80 °C, and pH controls are 5.5-6.2.
Hydrogen peroxide, which is added, in one section of desulphurization denitration section, two sections of desulphurization denitration sections carries out oxidation.In Ta Neijia
Enter hydrogen peroxide oxidation effect, improve denitration efficiency, can also reduce ozone usage, reduce operating cost.
The ammonia section of catching is connected with ammonium sulfate liquor pipeline 23, utilizes the ammonium sulfate liquor washing two-stage desulfurization purification of sulfuric acid workshop section
Flue gas afterwards, ammonium sulfate liquor, which is washed after flue gas catches remaining ammonia, passes through pipeline return ammonium sulfate workshop section 24.Taken off by two sections of desulfurization
Flue gas after nitre, ammonia section is caught into desulphurization denitration integrated tower top, and flue gas is washed using the acid mother liquid of ammonium sulfate workshop section,
Acid mother liquid washing flue gas returns to ammonium sulfate workshop section after catching remaining ammonia.Catch ammonia section controlled at 50-70 °C.If pass through two
After section desulphurization denitration, the ammonia content in flue gas is up to standard, this, which catches ammonia section, can be used as spare measure, not put into operation.
The physical demister is intercepted after power eliminates flue gas acid mist by centrifugal force and inertia, and flue gas is from desulfurization
Discharge on 11 top of denitration integrated tower.Flue gas after catching ammonia section enters the demister at the top of desulphurization denitration integrated tower, leads to
After crossing centrifugal force and inertia interception power elimination flue gas acid mist, flue gas is discharged at the top of desulphurization denitration integrated tower, into flue gas
Reheater, after the low temperature exhaust heat heating using flue gas before desulphurization denitration, returns to chimney, high altitude discharge.Physical demister
Temperature control be 50-60 °C.
The injector 18 uses venturi tube structure, and injector 18 is connected with external air duct 26, utilizes Venturi tube knot
Oxidant of the air as circulation oxidator is incorporated herein in 18 circulation of the injector injection suction of structure.In circulation oxidator, lead to
The suction introducing air that the circulation injection of circulation cycle pump produces is crossed, fully reaction is sufficiently mixed with ammonium liquid, by sulfurous therein
Sour ammonium generates ammonium sulfate, and the mixed salt solution most at last containing ammonium sulfate and ammonium nitrate is sent to the ammonium sulfate workshop section of coking, Resource recovery
Change product.Controlled at 50-100 °C in circulation oxidator, pH controls are 6.0-6.8.
The dilution air pipeline 29 is dilution air with the flue gas after waste heat recovery or purified flue gas, or
It is mixed into inert gas in atmosphere, the mixed volume of the flue gas or inert gas is the 0-50% of air capacity；In heating gas
In be mixed into low-heat value gas, such as blast furnace gas, vaporization coal gas and water coal gas dilution coal gas measure, mixed volume is heating gas amount
0-70%, reduce coke oven discharge flue gas in amount of nitrogen oxides, make coke oven discharge flue gas in amount of nitrogen oxides be 250-
550mg/M3。
Flue gases of cock oven temperature after 1 denitration process of denitration in the stove system is 220-350 °C, and flue gases of cock oven is sent into
Waste heat boiler recycles flue gas high-temperature residual heat, and the waste heat of waste heat boiler recycling is used as producing steam, or is directly used in ammonia still process heating
Distilled ammonia wastewater, or heating conduction oil, after recycling high-temperature residual heat, effluent gas temperature is down to 150-200 °C；Recycled by waste heat boiler
Flue gas after high-temperature residual heat is sent into smoke re-heater recycling flue gases at low waste heat, the purification that desulphurization denitration integrated tower is discharged
Flue gas is heated to 100-150 °C from 50-80 °C, and own temperature is down to 90-130 °C；Flue after recycling low temperature exhaust heat
Gas is sent into scrubber by flue gas wind turbine, is removed wash cycle liquid from washing using cleaning circulation pump in scrubber
Dirt device top spray into, with fed from below into flue gas counter current contacting, washing removing flue gas in dust impurity, flue gas into
One step is cooled to 60-80 °C.The dust obtained after spray is enriched with scrubber bottom precipitation, is periodically discharged it, as
Fixed-end forces.Wash cycle liquid can use clear water, the outer draining of available cycles, it is also possible to waste water after waste water or biochemical treatment after ammonia still process.
Flue gas after washing cools down is sufficiently mixed instead with the ozone from ozone generator in pipeline reactor
Should, after the nitric oxide in flue gases of cock oven partly or entirely oxidation, it is sent into desulphurization denitration integrated tower and carries out at desulphurization denitration
Reason.According to technique needs, this oxidation reactor, which may also placed in desulphurization denitration integrated tower, realizes oxidation reaction function.
The washing at the top of one section of desulphurization denitration section, concentrated ammonia liquor or coke oven gas desulfurization regenerator from coking ammonia still process workshop section
Liquid adds one section of desulphurization denitration section, anti-with being sent into sulfur dioxide and nitrogen oxides in flue gases of cock oven from one section of desulphurization denitration section
Should, the solution of generation ammonium sulfite and ammonium nitrate, most of ammonium salt solution is pumped into one section of recirculation cooler by one section of circulation,
After one section of recirculation cooler controls temperature, one section of desulphurization denitration section is added 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 be sent into circulation oxidator further to aoxidize.One section of desulphurization denitration section controlled at 50-80 °C, pH controls are 5.8-
6.5。
In circulation oxidator, by circulation cycle pump circulation injection produce suction, introduce air, fully with ammonium liquid
Reaction is sufficiently mixed, ammonium sulfite therein is generated into ammonium sulfate, the mixed salt solution most at last containing ammonium sulfate and ammonium nitrate is sent
Toward the ammonium sulfate workshop section of coking, Resource recovery product.Controlled at 50-80 °C in circulation oxidator, pH controls are 6.0-
6.8。
Technical indicator after present invention processing 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 above-mentioned be described the embodiment of invention with reference to attached drawing, not to the scope of the present invention
Limitation, on the basis of technical scheme, those skilled in the art, which need not make the creative labor, to be made
Various modifications or deformation still within protection scope of the present invention.
Claims (5)
1. a kind of double ammonia process integration desulfurization denitration systems of coking flue gas two-part, including denitration in the stove system, chimney, waste heat
Boiler, smoke re-heater, coke oven, it is characterized in that, further include flue gas wind turbine, scrubber, cleaning dust circulating pump, washing remove
Dirt cooler, ozone generator, pipeline reactor, desulphurization denitration integrated tower, circulation oxidator, the denitration in the stove system pass through
Dilution air pipeline and dilution gas piping are connected with coke oven, and coke oven is connected by coke oven flue gas pipeline with chimney, and chimney passes through
Coke oven flue gas pipeline is connected with waste heat boiler, and waste heat boiler passes through flue and smoke re-heater after recovered flue gas high-temperature residual heat
Connection, smoke re-heater are connected by flue after recycling low temperature exhaust heat with flue gas wind turbine, and flue gas blower and pipeline is with washing
Deduster connection is washed, scrubber lower part is connected by liquid pipe with cleaning circulation pump, and cleaning circulation pump passes through lower part liquid
Phase outlet conduit is connected with cleaning dust cooler, and cleaning dust cooler is connected with scrubber upper entrance pipeline, is washed
Wash deduster to be connected with pipeline reactor by pipeline after cleaning dust, pipeline reactor passes through ozone pipeline and ozone generator
Connection, pipeline reactor are connected by flue after reaction with desulphurization denitration integrated tower, the flue gas after washing cools down
Reaction is sufficiently mixed in pipeline reactor with the ozone from ozone generator, by the nitric oxide part in flue gases of cock oven
Or all after oxidation, it is sent into desulphurization denitration integrated tower and carries out desulphurization denitration processing；After desulphurization denitration integrated tower top is by purification
Flue is connected with smoke re-heater, and smoke re-heater is connected by purifying smoke pipeline with chimney, discharges desulphurization denitration one
The purifying smoke of body tower enters smoke re-heater, and 100-150 ° is increased to using the low temperature exhaust heat heating of flue gas before desulphurization denitration
C returns to chimney, high altitude discharge；
The desulphurization denitration integrated tower includes one section of desulphurization denitration section, the two sections of desulphurization denitration sections at middle part of lower part, two sections of desulfurization
The top of denitration section is equipped with and catches ammonia section, catches ammonia section top and is equipped with physical demister, one section of desulphurization denitration Duan Yunong ammonia
The scrubbing ammonia waterpipe of waterpipe or raw coke oven gas desulfurization regeneration tail gas connects, the concentrated ammonia liquor pipeline and coking ammonia still process workshop section
The connection of concentrated ammonia liquor pipeline, the scrubbing ammonia waterpipe is connected with the scrubbing ammonia waterpipe of raw coke oven gas desulfurization regeneration tail gas,
The washing ammonium hydroxide of concentrated ammonia liquor or raw coke oven gas desulfurization regeneration tail gas from coking ammonia still process workshop section adds as the alkali source of desulphurization denitration
Enter one section of desulphurization denitration section, one section of circulating pump is connected by one section of circulation ammonium liquid pipe road with desulphurization denitration integrated tower, one-step cooling
Device is connected by one section of circulation ammonium liquid pipe road with one section of circulating pump, and one-step cooling device is taken off by one section of circulation ammonium liquid pipe road with desulfurization
Nitre integrated tower connects, and one section of desulphurization denitration section of desulphurization denitration integrated tower is connected by ammonium liquid side line pipeline with circulation oxidator,
The outlet of circulation cycle pump is connected by circulation cycle conduit upper with circulation oxidator top, the circulation cycle conduit upper
Injector is equipped with close to the position on circulation oxidator top, the import of circulation cycle pump passes through circulation cycle pipeline lower part and circulation
Oxidator bottom connects, and circulation cycle pump is molten by the ammonium sulfate after oxidation and ammonium nitrate mixed-ammonium salt by spur outlet and pipeline
Liquid is sent to the ammonium sulfate workshop section Resource recovery product of coking or for complex acid；
Two sections of desulphurization denitration sections are connected with the remained ammonia from coking ammonia still process workshop section by pipeline, from coking ammonia still process work
The diluent that the remained ammonia of section is used as vapour phase ammonia density by pipeline adds two sections of desulphurization denitration sections, two sections of desulphurization denitrations
The bottom of section is connected by two sections of circulation fluid pipelines with two sections of pump inlets, and two sections of circulating-pump outlets pass through two sections of circulation liquid pipes
Road is connected with two-step cooling device, and two-step cooling device is connected by two sections of circulation fluid pipelines with the top of two sections of desulphurization denitration sections, and two
Remained ammonia is sent to the ammonia still of the ammonia still process workshop section of coking by pipeline by the spur outlet of section circulating pump；
The ammonia section of catching is connected with ammonium sulfate liquor pipeline, the flue gas after two sections of desulphurization denitrations, into desulphurization denitration one
Ammonia section is caught on tower top, washs flue gas using the acid mother liquid of sulfuric acid workshop section, sulphur ammonium acid mother liquid washing flue gas catches remaining
Ammonium sulfate workshop section is returned after ammonia, catch ammonia section controlled at 50-70 °C；
The physical demister is intercepted after power eliminates flue gas acid mist by centrifugal force and inertia, and flue gas is from desulphurization denitration
Discharge on integrated tower top；Flue gas after catching ammonia section enters the physical demister at the top of desulphurization denitration integrated tower, leads to
After crossing centrifugal force and inertia interception power elimination flue gas acid mist, flue gas is discharged at the top of desulphurization denitration integrated tower, into flue gas
Reheater, after the low temperature exhaust heat heating using flue gas before desulphurization denitration, returns to chimney, high altitude discharge；The physical demisting
The temperature control of device is 50-60 °C.
2. the double ammonia process integration desulfurization denitration systems of coking flue gas two-part as claimed in claim 1, it is characterized in that, it is described
Injector uses venturi tube structure, and injector is connected with external air duct, is sprayed using the injector circulation of venturi tube structure
Oxidant of the air as circulation oxidator is incorporated herein in suction, and the suction that the circulation injection pumped by circulation cycle produces introduces
Air, the oxygen in air are fully sufficiently mixed reaction with ammonium liquid, and ammonium sulfite therein is generated ammonium sulfate, then will be contained
The mixed salt solution of ammonium sulfate and ammonium nitrate is sent to the ammonium sulfate workshop section of coking, Resource recovery product, the circulation oxidator internal control
Temperature processed is 50-80 °C, and pH controls are 6.0-6.8.
3. the double ammonia process integration desulfurization denitration systems of coking flue gas two-part as claimed in claim 1, it is characterized in that, it is described
Dilution air pipeline is dilution air with the flue gas after waste heat recovery or purified flue gas, or is mixed into atmosphere lazy
Property gas, the mixed volume of flue gas or inert gas is the 0-50% of air capacity；Low-heat value gas is mixed into heating gas,
Low-heat value gas mixed volume is the 0-70% of heating gas amount, reduces the amount of nitrogen oxides in coke oven discharge flue gas, arranges coke oven
The amount of nitrogen oxides gone out in flue gas is 250-550mg/m3.
4. the double ammonia process integration desulfurization denitration systems of coking flue gas two-part as claimed in claim 1, it is characterized in that, pass through
Flue gases of cock oven temperature after denitration in the stove system denitration process is 220-350 °C, and flue gases of cock oven is sent into waste heat boiler recycling
Flue gas high-temperature residual heat, the waste heat of waste heat boiler recycling are used as producing steam, or are directly used in ammonia still process heating distilled ammonia wastewater, or add
Thermal conductivity deep fat, recycling high-temperature residual heat rear pass temperature degree are down to 150-200 °C；Cigarette after waste heat boiler recycles high-temperature residual heat
Road pneumatic transmission enters smoke re-heater recycling flue gases at low waste heat, and the purification flue gas that desulphurization denitration integrated tower is discharged is from 50-80 °
C is heated to 100-150 °C, and own temperature is down to 90-130 °C；Flue gas after recycling low temperature exhaust heat passes through flue gas wind turbine
Scrubber is sent into, is sprayed into wash cycle liquid from scrubber top using cleaning circulation pump in scrubber,
With fed from below into flue gas counter current contacting, the dust impurity in washing removing flue gas, flue gas is further cooled to 60-
80°C。
5. the double ammonia process integration desulfurization denitration systems of coking flue gas two-part as claimed in claim 1, it is characterized in that, in institute
One section of desulphurization denitration section, the two sections of desulphurization denitration sections stated add hydrogen peroxide and carry out oxidation.
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| CN106268230A (en) * | 2016-08-18 | 2017-01-04 | 山东铁雄冶金科技有限公司 | A kind of waste heat of coke-oven flue gas reclaim and purify system and technique |
| 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 |
| CN106621768A (en) * | 2016-12-20 | 2017-05-10 | 亚太环保股份有限公司 | Ammonia process of desulfurization integral purification device and method for acid gas sulfur recovery tail gas |
| US10919016B2 (en) * | 2017-02-15 | 2021-02-16 | General Electric Technology Gmbh | Oxidation control for improved flue gas desulfurization performance |
| CN108970352A (en) * | 2018-06-19 | 2018-12-11 | 山东师范大学 | A kind of flue gas low-temperature denitration method |
| CN111068492B (en) * | 2018-10-18 | 2022-12-02 | 中国石油化工股份有限公司 | Coking tail gas treatment process and device |
| CN109210955B (en) * | 2018-10-19 | 2024-03-26 | 上海孚旺炉业有限公司 | Industrial furnace low temperature flue gas waste heat utilization and SOx/NOx removal white smoke integrated system |
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Denomination of invention: Integrated desulfurization and denitrification system for coking flue gas using two-stage double ammonia process Effective date of registration: 20230317 Granted publication date: 20180515 Pledgee: Postal Savings Bank of China Limited Jinan Changqing District sub branch Pledgor: JINAN METALLURGY CHEMICAL EQUIPMENT CO.,LTD. Registration number: Y2023980035136 |
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