CN204261549U - The purifying equipment of a kind of low temperature coke oven stack gases - Google Patents
The purifying equipment of a kind of low temperature coke oven stack gases Download PDFInfo
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- CN204261549U CN204261549U CN201420725611.8U CN201420725611U CN204261549U CN 204261549 U CN204261549 U CN 204261549U CN 201420725611 U CN201420725611 U CN 201420725611U CN 204261549 U CN204261549 U CN 204261549U
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Abstract
The utility model relates to the purifying equipment of a kind of low temperature coke oven stack gases, mainly comprises the cigarette wind unit, low temperature SCR denitration unit, ammonia process of desulfurization unit, the ammonia that are connected by main line and prepares unit; Pipeline between cigarette wind unit and low temperature SCR denitration unit is connected with spray ammonia unit; Coke-oven plant's remained ammonia recycling, low temperature SCR denitration technology, ammonia-process desulfurization technique combine by this equipment, realizing high-efficiency desulfurization denitration simultaneously, reduce the escaping of ammonia rate, by-product (NH
4)
2sO
4product, while reaching the relevant environmental protection policy requirements of country, reduces the operating cost of coal chemical enterprise desulphurization denitration.
Description
Technical field
The utility model relates to the purifying equipment of a kind of low temperature coke oven stack gases, and particularly the low temperature coke oven stack gases of a kind of temperature between 170 DEG C-250 DEG C removes the equipment of nitrogen oxide, oxysulfide, belongs to coking of coal industry prevention and control of air pollution field.
Background technology
Coke oven flue waste gas is the waste gas produced after destructive distillation cleaned coal produces the burning of coke coke-stove gas, mainly containing SO
2, NO
xdeng pollutant.Only 2013, the SO in China's domestic coke-oven plant coke oven flue waste gas
2discharge capacity is about 75.86 ten thousand tons, accounts for SO then
24% of total emission volumn; NO
xdischarge capacity is about 606.88 ten thousand tons, accounts for domestic NO then
x27% of total emission volumn.
In June, 2012; Environmental Protection Department and national quality supervision and inspection Quarantine Bureau combine and have issued " coking chemistry emission of industrial pollutants standard GB16171-2012 "; the clear stipulaties atmosphere pollutants emission standards of coking industry: on October 1st, 2012 to rise newly-built enterprise and January 1 in 2015 Qi existing enterprise, coke oven chimney SO
2concentration of emission is by ≯ 100mg/Nm
3become ≯ 50mg/Nm
3, NO
xconcentration of emission is by ≯ 800mg/Nm
3become ≯ 500mg/Nm
3; Special limit value is coke oven chimney SO
2concentration of emission ≯ 30mg/Nm
3, NO
xconcentration of emission ≯ 150mg/Nm
3.Therefore how carrying out desulphurization denitration to coke oven stack gases makes it reach the environmental protection standard of country, become coking industry must and need the problem of solution badly.
The application of coke oven flue exhuast gas desulfurization denitration in coking industry still belongs to blank, because of industry characteristic, can not indiscriminately imitate the desulfurizing and denitrifying process of the industries such as former power plant, steel sintering flue gas, boiler, cement.Main application crux has the following aspects:
SCR (SCR) technology is current NO
xthe mainstream technology reduced discharging, but the catalyst requirement flue-gas temperature of SCR technological core just can complete catalytic reduction reaction more than 350 DEG C, and current coke oven flue EGT is generally between 170-250 DEG C, especially through the coke oven flue waste gas of waste heat recovery, temperature is low to less than 170 DEG C, belongs to the category of low-temperature denitration of flue gas.And under cryogenic for reaching desirable denitration effect, nearly all denitration technology all needs smoke treatment to be heated to more than 350 DEG C, and follow-up desulphurization system needs gas approach temperature to be reduced to less than 100 DEG C, so just waste a large amount of heat energy, and do not meet the energy-saving and cost-reducing thought of country's promotion instantly.Therefore, research and development one can the SCR technology of denitration under low temperature (170-250 DEG C) condition, becomes SCR technology in low-temperature denitration of flue gas field, especially coke oven flue exhaust gas denitration field problem demanding prompt solution.
The sulfur removal technology of the industry main flows such as current domestic electrical, iron and steel is limestone-gypsum method, but due to its cost of investment and operating cost higher, and there is the problems such as secondary residue pollution, along with continuous innovation, the progress of desulfur technology, more and more show not science, the diseconomy of its application.Coal chemical enterprise remained ammonia is more, and when coke oven flue exhuast gas desulfurization, introducing " ammonia process of desulfurization " that more can embody circular economy concept has been trend in industry.But due to coke oven flue EGT, SO
2, NO
xand the parameter such as smoke content is all different from the ammonia process of desulfurization and has other industry compared with extensive use, therefore, design the ammonia desulfurizing process which kind of is reasonably applicable to coking industry, reduce the escaping of ammonia phenomenon, become one of key factor of this Technique Popularizing of restriction application.
Summary of the invention
For the above-mentioned defect, the crux that exist when in existing other industry, flue gas desulfurization and denitrification technology is applied in coking industry, the utility model provides the purifying equipment of a kind of low temperature coke oven stack gases, make full use of the remained ammonia that coal chemical enterprise is more than needed, adopt the technique that low-temperature SCR catalytic denitration combines with the ammonia process of desulfurization, denitration efficiency > 88%, desulfuration efficiency > 95%, simultaneously by-product goes out ammonium sulfate and makes chemical fertilizer, industrial chemicals, significantly reduces the operating cost of coal chemical enterprise desulphurization denitration.
For achieving the above object, the utility model realizes by the following technical solutions:
The purifying equipment of a kind of low temperature coke oven stack gases, coke-oven plant's remained ammonia recycling, low temperature SCR denitration technology, ammonia-process desulfurization technique combine by this equipment, and the ammonia that the remained ammonia adopting ammonia still process workshop section of coke-oven plant to produce is evaporated is as denitrification reducing agent; Adopt low-temperature denitration catalyst, utilize selective catalytic reduction to carry out denitration, denitrating catalyst adopts honeycomb coaly structure; Adopt the SO in ammonia desulfurizing process removal coke oven exhaust gas
2, by-product (NH
4)
2sO
4.The equipment be made up of each unit is realizing high-efficiency desulfurization denitration simultaneously, and the escaping of ammonia rate is low, by-product (NH
4)
2sO
4product, while reaching the relevant environmental protection policy requirements of country, reduces the operating cost of coal chemical enterprise desulphurization denitration.
This equipment is mainly comprised the cigarette wind unit, low temperature SCR denitration unit, ammonia process of desulfurization unit, the ammonia that are connected by main line and prepares unit; Pipeline between cigarette wind unit and low temperature SCR denitration unit is connected with spray ammonia unit;
Described cigarette wind unit comprises gas approach I, exhanst gas outlet I and air-introduced machine, and air-introduced machine is arranged on the pipeline of SCR reactor exhanst gas outlet II;
Described low temperature SCR denitration unit comprises SCR reactor, and SCR reactor top is gas approach II, and bottom is exhanst gas outlet II; SCR inside reactor is provided with rectifier and three layers of catalyst layer from top to bottom successively; SCR reactor is provided with the blow device adapted with catalyst layer;
Described spray ammonia unit comprises the blower fan, air heating apparatus, ammonia/air mixer, ammonia-spraying grid, the flue gas blender that are connected by pipeline; Ammonia-spraying grid and flue gas blender are located on the pipeline of SCR reactor gas approach II;
Described ammonia process of desulfurization unit comprises desulfurizing tower, is provided with gas approach III and gas approach III is connected by the air-introduced machine of pipeline with cigarette wind unit below desulfurizing tower; Desulfurizing tower inside is provided with secondary cycle liquid bath, the secondary cycle spray equipment be communicated with secondary cycle liquid bath, separating plate, primary cycle spray equipment and demister from bottom to up successively; Desulfurizing tower outside is provided with the primary cycle liquid bath be communicated with primary cycle spray equipment; The exhanst gas outlet III at desulfurizing tower top is communicated with by the exhanst gas outlet I of pipeline with cigarette wind unit;
Primary cycle spray equipment is divided into three grades, upper, middle and lower shower from top to bottom, and higher level's shower and primary cycle liquid bath lower floor pipeline connection, subordinate's shower and primary cycle liquid bath upper strata pipeline connection;
Described ammonia prepare unit comprise connected by pipeline unload ammonia pump, ammonia storage tank, ammonium hydroxide delivery pump, ammonia evaporator, ammonia surge tank, desulfurization unit ammonium hydroxide delivery pump;
Primary cycle liquid bath is communicated with desulfurization unit ammonium hydroxide delivery pump by pipeline;
Ammonia surge tank is communicated with ammonia/air mixer by pipeline;
Aerator is respectively equipped with bottom secondary cycle liquid bath and primary cycle liquid bath;
Separating plate is provided with overfall, and overfall is communicated with primary cycle liquid bath by pipeline.
First, the concentration from ammonia still process workshop section of coke-oven plant is that the remained ammonia of 10%-19% pumps into ammonia storage tank by unloading ammonia pump, and the ammoniacal liquor stored in ammonia storage tank can simultaneously for spray ammonia unit and ammonia process of desulfurization unit two unit.Ammoniacal liquor for spray ammonia unit is delivered to ammonia evaporator through ammonium hydroxide delivery pump, and the heat needed for ammonia evaporation is provided by low-pressure saturated steam.Ammonia evaporator is equipped with pressure-control valve, ammonia pressure is controlled in certain limit, when outlet pressure is more than 0.3MPa, then close ammonium hydroxide delivery pump.Ammonia outlet pipeline is equipped with temperature detector, closes ammonium hydroxide delivery pump when the temperature is too low, make ammonia surge tank holding temperature be no more than 80 DEG C and pressure is no more than 0.3MPa, avoid because ammonia temperature and hypertonia cause security incident.Ammonia evaporator is also equipped with safety valve, equipment pressure anomaly can be prevented too high.Flow to ammonia surge tank from the ammonia of ammonia evaporator evaporation, then delivered to by ammonia transfer pipeline in the ammonia/air mixer of spray ammonia unit.
Meanwhile, low-pressure saturated steam is at air heating apparatus place, and by the air heat from blower fan to 180-250 DEG C, the hot-air after heating is mixed to form ammonia air gas mixture at ammonia/air mixer place with the ammonia entered from ammonia surge tank.For preventing when in ammonia and coke oven exhaust gas mist, ammonia volume ratio is more than 15%, the explosion danger that can occur, the volume ratio therefore controlling ammonia and hot-air is 3:97 ~ 5:95.Simultaneously, the temperature controlling ammonia air gas mixture is 170-250 DEG C, close to coke oven flue EGT, if mist temperature is too low, reduce the temperature of mixed flue gas after mixing with coke oven exhaust gas, the catalytic activity of follow-up low-temperature SCR catalyst can be affected and then reduce the denitration rate of flue gas; If mist temperature is too high, although low-temperature SCR catalyst adaptive temperature scope is 160 DEG C-300 DEG C, and temperature its denitration rate higher is relatively higher, and too high temperature can waste vapour source, and uneconomical.
Low-pressure saturated steam described in the utility model is vapour source ready-made in 1.0MPa, 184 DEG C of low-pressure saturated steams or other coke-oven plants.
Meanwhile, low temperature coke oven stack gases, under the effect of cigarette wind unit air-introduced machine, enters the pipeline be connected with the SCR reactor of low temperature SCR denitration unit through gas approach I.Ammonia air gas mixture evenly sprays the pipeline entering and be connected with the SCR reactor of low temperature SCR denitration unit through ammonia-spraying grid, mix further through flue gas blender after tentatively mixing with low temperature coke oven stack gases, the SCR reactor entering low temperature SCR denitration unit carries out denitration again.Wherein, the volume ratio of coke oven flue waste gas and ammonia air gas mixture is 35:1 ~ 45:1, if volume ratio is excessive, then and the mist NO that cannot reduce thoroughly in coke oven exhaust gas
xif both volume ratios are too small, then can cause NH unnecessary in mist
3with the SO in coke oven exhaust gas
2react, form ammonium sulfurous particle, particle is attached on low-temperature SCR catalyst, and catalyst poisoning can be made to lose efficacy; Coke oven flue EGT is 170-250 DEG C, SO2 content is 200-300mg/Nm
3, NO
xcontent is 800-1000mg/Nm
3.
Enter the ammonia of SCR reactor, air, coke oven flue waste gas mist through rectifier layout evenly, enter SCR reactor three layers of catalyst layer, ensure that flue gas is without bias current, makes the catalytic reduction of catalyst layer point position farthest be utilized.The concrete preparation method of catalyst described in the utility model is with reference to Chinese patent application 200810224495.0.Every one deck catalyst layer is V
2o
5-MoO
3-TiO
2the compound of component, TiO
2as active material V
2o
5and MoO
3carrier, and V
2o
5as main active material, to NO
xreduction there is catalytic action, control its mass percent 3%-10%, can guarantee that it is in effective Reduction of NO
xprerequisite under, can not SO be caused
2oxidation and N
2the generation of O; MoO
3then can reduce the initial temperature of catalytic reduction reaction, improve heat endurance and the mechanical performance of catalyst, control its mass fraction 10%-15%, this catalyst can be low to moderate the NO at the temperature of 160 DEG C-170 DEG C in effective catalytic reduction coke oven flue waste gas
x.Denitrating catalyst adopts cellular structure, and compare plate-type denitration catalyst, honeycomb fashion has the larger feature of specific area, can be NH
3with NO
xmore catalytic reduction point position is provided, more effectively promotes NH
3reductive NO
xfor N
2reaction.Reaction equation is:
4NH
3+4NO+O
2→4N
2+6H
2O (1)
4NH
3+2NO
2+O
2→3N
2+6H
2O (2)
The wherein NO of 95%
xfor NO, equation (1) is key reaction.The utility model, by the volume ratio by controlling ammonia air gas mixture and coke oven exhaust gas, ensures the NO of ammonia all for reducing in coke oven exhaust gas
x, at about 170 DEG C, ammonia and SO
2reaction can not preferentially occur.
After low temperature SCR denitration unit runs a period of time, deposit in low-temperature catalyzed oxidant layer for preventing the flying dust in flue gas and other impurity, blocking catalyst duct, must according to catalyst layer pressure loss situation when running, timely startup blow device, blow away dust and other impurity, to maintain the catalytic activity of catalyst layer.
After low temperature SCR denitration cell processing, NO in low temperature coke oven stack gases
xcontent can by 800-1000mg/Nm
3be down to 150-190mg/Nm
3, NO
xclearance > 80%.
Coke oven flue waste gas after denitration, under the effect of air-introduced machine, through pipeline, at gas approach III place, enters in the desulfurizing tower of ammonia process of desulfurization unit.Coke oven flue waste gas enters after in desulfurizing tower, and flow from bottom to top, first with the sulphur ammonium secondary cycle liquid heat exchange be atomized through secondary cycle spray equipment, flue-gas temperature is down to less than 60 DEG C, the SO at this temperature in flue gas
2reaction efficiency with ammonia and ammonium sulfurous is the highest, and meanwhile, ammoniacal liquor more than needed in sulphur ammonium secondary cycle liquid can with the SO in flue gas
2there is initial reaction, generate ammonium sulfurous; Flue gas after cooling is through separating plate, and continue to rise, contact with the sulphur ammonium primary cycle liquid be atomized through primary cycle liquid spray equipment, ammoniacal liquor more than needed in sulphur ammonium primary cycle liquid can with the SO in flue gas
2react further, generate ammonium sulfurous.Generate ammonium sulfurous reaction equation as follows:
SO
2+H
2O+xNH
3→(NH
4)
xH
2-xSO
3
Under the effect of separating plate, flue gas upflow velocity is low, ensures the SO in flue gas
2by efficient absorption.Primary cycle spray equipment is divided into three grades, upper, middle and lower shower from top to bottom, and higher level's shower and primary cycle liquid bath lower floor pipeline connection, subordinate's shower and primary cycle liquid bath upper strata pipeline connection; When adopting the sulphur ammonium primary cycle liquid of atomization to carry out desulphurization reaction, the coke oven flue waste gas after denitration adopts the upper, middle and lower layer of sulphur ammonium primary cycle liquid to spray successively; The upper strata pH value of sulphur ammonium primary cycle liquid is 5-6, and middle level pH value is 4-5, and lower floor's pH value is 3-4.By controlling the pH value of sulphur ammonium primary cycle liquid, can ensure that the ammonia content in whole desulfurizing tower in ammonium sulfate solution can not be much excessive relative to the sulfur dioxide in flue gas and nitrogen oxide, greatly reducing the escape of unnecessary ammonia.In desulfurizing tower, ammonium sulfate solution is carried out two stage cycle, to ensure that ammoniacal liquor can with the SO in coke oven flue waste gas
2sufficient reaction, improves the utilization rate of ammoniacal liquor, reduces the amount of ammonia slip of flue gas.And respectively from primary cycle liquid bath upper strata, middle level, lower floor extract sulphur ammonium primary cycle liquid, and upper strata extract sulphur ammonium primary cycle liquid first with smoke contacts, because the sulphur ammonium primary cycle liquid in primary cycle liquid bath is because the mass-transfer efficiency problem of ammonia, the pH of each layer is not identical, and first circulating slot top because of contacting with the ammoniacal liquor added, and pH is the highest, ammonia content is the highest, by itself and smoke contacts, can more be beneficial to SO in flue gas
2absorption, improve the utilization rate of ammoniacal liquor simultaneously, reduce its escapement ratio.
Demister and backwash spray equipment supporting is with it provided with above described primary cycle spray equipment.Containing a small amount of SO
2(lower than 50mg/Nm
3) and escape ammonia (lower than 5mg/Nm
3) coke oven flue waste gas continue to rise, catch the H in flue gas through demister
2o, prevents the conditions of streaking produced because flue gas water content is too high, and the water droplet simultaneously on demister also further can catch the escape ammonia in flue gas, and the amount of desulfurizing tower escape ammonia is met the requirements.Demister backwash spray equipment is set below demister, in order to periodic flushing demister.
Sulphur ammonium secondary cycle liquid bottom desulfurizing tower through secondary cycle spray equipment constantly with the coke oven exhaust gas heat exchange from gas approach III, portion of water can along with flue gas upwards, sulphur ammonium secondary cycle liquid can be constantly concentrated, for ensureing that it keeps certain liquid level bottom desulfurizing tower, simultaneously for preventing flue dust from depositing at separating plate place, the reverse spray equipment of primary cycle is provided with below separating plate, this device is communicated with the higher level's shower in primary cycle liquid spray equipment, when in primary cycle liquid bath, sulphur ammonium primary cycle liquor ratio is heavily more than 1.1kg/L, open the reverse spray equipment of primary cycle, extract the sulphur ammonium primary cycle liquid in primary cycle liquid bath, to desulfurizing tower fluid infusion, the separating plate of backwash simultaneously.
Respectively by the aerator be positioned at bottom secondary cycle liquid bath and primary cycle liquid bath, aeration is carried out to sulphur ammonium one-level, secondary cycle liquid, occurs to react as follows:
(NH
4)
xH
2-xSO
3+1/2O
2+(2-x)NH
3→(NH
4)
2SO
4
For ensureing oxidation effectiveness, oxidation air compartment system adopts jet tube, and oxidation air is distributed pipe and injects, and is separated into tiny bubble and is distributed in sulphur ammonium one-level, secondary cycle liquid, HSO
3 -oxidized air complete oxidation.
Equipment described in the utility model also comprises fresh water (FW) unit and sulphur ammonium prepares unit;
Described fresh water (FW) unit comprises the technique water tank and technique water pump that are connected by pipeline; Technique water pump is communicated with the backwash spray equipment in desulfurizing tower by pipeline;
Described sulphur ammonium is prepared unit and is comprised the cyclone, centrifuge, drying machine, the packing machine that are connected by pipeline; Cyclone is communicated with secondary cycle liquid bath.
Sulphur ammonium secondary cycle liquor ratio bottom desulfurizing tower in secondary cycle liquid bath is heavily generally 1.1kg/L-1.2kg/L, along with the continuous circulation of secondary sulphur ammonium circulation fluid, moisture runs off gradually, the proportion of secondary sulphur ammonium circulation fluid increases gradually, after sulphur ammonium secondary cycle liquor ratio is heavily more than 1.2kg/L, be delivered to sulphur ammonium through over cure ammonium excavationg pump and prepare unit, preparing finished articles sulphur ammonium.
Primary cycle liquid bath top is provided with overfall, by pipeline connection in desulfurizing tower, maintains the unlikely spilling of certain liquid level to make the sulphur ammonium primary cycle liquid in primary cycle liquid bath; Primary cycle liquid bath top is provided with ammoniacal liquor and adds mouth, and ammoniacal liquor is carried by desulfurization unit ammonium hydroxide delivery pump, and pump adopts VFC, as the SO in coke oven exhaust gas
2when content changes, in primary cycle liquid bath, the pH of each layer sulphur ammonium primary cycle liquid can change, controlling primary cycle liquid bath top pH value of solution is between 5-6, middle part pH is between 4-5, bottom pH is between 3-4, once each several part pH changes, then and VFC ammoniacal liquor dosage, if pH raises, then reduce the frequency of desulfurization unit ammonium hydroxide delivery pump to reduce ammoniacal liquor dosage; If pH reduces, then increase the frequency of desulfurization unit ammonium hydroxide delivery pump to promote ammoniacal liquor dosage; Guarantee the desulfuration efficiency of ammonia process of desulfurization unit be not less than 95% and the escaping of ammonia rate be no more than 5mg/Nm
3.
In addition, sulphur ammonium secondary cycle liquid is after the atomization of secondary cycle spray equipment, and after being the coke oven flue exhaust gas contact of 170 DEG C-250 DEG C with temperature, coke oven flue EGT reduces to 50-60 DEG C, when both contact heat-exchangings, the ammonia in sulphur ammonium secondary cycle liquid and ammonium sulfurous are to the NO in flue gas
xstill old reduction, can reduce NO in flue gas further
xcontent, clearance is about about 40%.
After ammonia process of desulfurization cell processing, SO in coke oven flue waste gas
2content is about 10-30mg/Nm
3, NOx content is about 90-110mg/Nm
3, indices all meets the atmosphere pollutants emission standards of " coking chemistry emission of industrial pollutants standard GB16171-2012 " enforcement from 1 day January in 2015, meanwhile, and water droplet carrying amount ≯ 75mg/Nm
3, the escaping of ammonia rate ≯ 5mg/Nm
3, the coke oven flue waste gas after process after desulphurization denitration flue gas through the exhanst gas outlet I qualified discharge of cigarette wind unit.
The utility model fresh water (FW) unit comprises the technique water tank and technique water pump that are connected by pipeline; Technique water pump is communicated with the backwash spray equipment in desulfurizing tower by pipeline, and fresh water (FW), is atomized through device, back flush demister to demister backwash spray equipment by fresh water (FW) transport pump.Use water place by fresh water (FW) transport pump to other, the inwall of flushable flue and desulfurizing tower, deposit throughout to prevent the dust in flue gas.
Sulphur ammonium is prepared unit and is comprised the cyclone, centrifuge, drying machine, the packing machine that are connected by pipeline; Cyclone is communicated with secondary cycle liquid bath.The ammonium sulfate solution reaching corresponding proportion sends into cyclone by sulphur ammonium excavationg pump, slurries gravity flow after concentrated enters centrifuge, after further dehydration, dried by drying machine, reach the sulphur ammonium after standard by packing machine bagging and packaging, cyclone and the isolated ammonium sulfate liquor of centrifuge are back in desulfurizing tower.The sulphur ammonium product encapsulated by packing machine is taken out, and reduces coal chemical enterprise desulphurization denitration cost.
In sum, compared with prior art, the beneficial effects of the utility model are:
1, desulfurization and denitrification integral
Low temperature flue gases of cock oven (170 DEG C-250 DEG C), under the vacuum suction of air-introduced machine, first enters SCR denitration unit, under the catalytic action of catalyst, with NH
3there is oxygen reduction reaction and generate N
2and H
2o, removes the NO of about 80%
x, SCR reactor outlet temperature 160 DEG C-240 DEG C, enters in desulfurizing tower, utilizes ammonia process to remove the SO of more than 95%
2after, enter coke oven chimney, enter air.
This technique is while ensureing waste gas qualified discharge to the denitration of coke oven flue gas desulfurization systems, and the valuable ammonium sulfate products of by-product, effectively reduces process operation cost.
2, the treatment of wastes with processes of wastes against one another, turns waste into wealth
The remained ammonia that coal chemical enterprise ammonia still process workshop section produces there is no other ways of dissolving, can only as wastewater treatment, and the ammoniacal liquor that ammonia process of desulfurization denitration can effectively utilize coal chemical enterprise unnecessary, the deposed ammonia of the sulfur dioxide in waste gas and coke-oven plant is converted into chemical fertilizer, do not produce any waste water, waste liquid and waste residue, there is no secondary pollution, both the problem that remained ammonia is dissolved nowhere had been solved, create economic benefit again, reduce the operating cost of coal chemical enterprise desulfurizing and denitrifying process, be one truly by whole for pollutant resource, meet the desulfur technology that recycling economy requires.
3, ammonia process of desulfurization equipment volume is little, take up an area less, energy consumption is low and equipment is less scaling
Ammonia is a kind of good alkaline absorbent, and the ammonia process of desulfurization belongs to gas-liquid reaction, and reaction speed is fast, and react completely, absorbent utilization rate is high, decreases volume and the energy consumption of equipment.And there is very high reactivity due to ammonia, and ammonium sulfate has very soluble chemical characteristic, therefore ammonia method desulfurizing system not easily produces scale formation.In addition, primary cycle liquid bath is arranged separately, interior Sheng sulphur ammonium primary cycle liquid, both desulfurizing tower height had been reduced, corresponding pump lift reduces, save equipment investment, sulphur ammonium primary cycle liquid with the sulphur ammonium secondary cycle liquid bottom desulfurizing tower separately simultaneously, sulphur ammonium primary cycle liquor ratio is heavily generally 1.0kg/L-1.1kg/L, sulphur ammonium secondary cycle liquor ratio is heavily generally 1.1kg/L-1.2kg/L, by two kinds of circulation fluids separately, be more beneficial to the control of sulphur ammonium crystallization inside tower, the preparation cost of sulphur ammonium product is lower, technique is more reasonable.
4, not only desulfurization but also denitration
At ammonia process of desulfurization unit, ammonia is to NO
xhave absorption equally, the ammonium sulfurous formed in sweetening process is in addition to NO
xalso there is reduction, so the object of a part of denitration also can be realized while the ammonia process of desulfurization, the NO of about 40% can be removed
x, the denitration efficiency making the utility model final, more than 88%, can meet stricter NOx emission requirement, adapts to higher environmental requirement.
5, the escape amount of ammonia is greatly reduced
In traditional handicraft, be generally adopt the ammoniacal liquor through spray equipment atomization to contact with flue gas is reverse, while flue-gas temperature being down to below 60 DEG C, the SO in ammoniacal liquor and flue gas
2there is initial reaction, remove a part of SO
2but the drawback of spraying ammoniacal liquor is, when the ammoniacal liquor of atomization and temperature are the coke oven flue waste gas instant contact of more than 160 DEG C, the ammoniacal liquor of quite a few can preferentially be decomposed into ammonia and water, and ammonia is relative to SO
2be excessive far away, thus cause the escape of ammonia; And in the application, by setting the pH value of sulphur ammonium primary cycle liquid and adopting the means such as multiple stage circulation, guarantee that the desulfuration efficiency of ammonia process of desulfurization unit does not reduce and the escaping of ammonia rate is no more than 5mg/Nm
3.
Accompanying drawing explanation
Fig. 1 is structural representation of the present utility model.
In figure: 1. cigarette wind unit, 1a. coke oven chimney, 1b. gas approach I, 1c. exhanst gas outlet I, 1d. air-introduced machine, 1e coke oven flue.2. low temperature SCR denitration unit, 2a. expansion joint, 2b. rectifier, 2c. catalyst layer, 2d. blow device, 2e.SCR reactor, 2f. gas approach II, 2g. exhanst gas outlet II.3. spray ammonia unit, 3a. low-pressure steam, 3b. blower fan, 3c. air heating apparatus, 3d. ammonia/air mixer, 3e. ammonia-spraying grid, 3f. flue gas blender.4. ammonia prepares unit, and 4a. unloads ammonia pump, 4b. ammonia storage tank, 4c. ammonium hydroxide delivery pump, 4d. ammonia evaporator, 4e. ammonia surge tank, 4f. desulfurization unit ammonium hydroxide delivery pump.5. ammonia process of desulfurization unit, 5a. gas approach III, 5b. sulphur ammonium excavationg pump, 5c. secondary sulphur ammonium circulating pump, 5d. accident pump, 5e. aerator, 5f. secondary cycle spray equipment, the reverse spray equipment of 5g. primary cycle, 5h. overfall, 5i. separating plate, 5j. primary cycle spray equipment, 5k. demister, 5l. aerator, 5m. primary cycle pump, 5n. primary cycle liquid bath overfall, 5o. primary cycle liquid bath, 5p. desulfurizing tower, 5q. ammoniacal liquor adds mouth, 5r. exhanst gas outlet III, 5s. secondary cycle liquid bath.6. fresh water (FW) unit, 6a. technique water tank, 6b. technique water pump, 6c. backwash spray equipment, 6d. other use water place.7. sulphur ammonium prepares unit, 7a. cyclone separator, 7b. centrifuge, 7c. drying machine, 7d. packing machine, 7e. sulphur ammonium product, and 7f. ammonium sulfate liquor refluxes.
Detailed description of the invention
Below by non-limiting embodiment and by reference to the accompanying drawings to the utility model further instruction:
Embodiment 1
The purifying equipment of a kind of low temperature coke oven stack gases, is mainly comprised the cigarette wind unit 1, low temperature SCR denitration unit 2, ammonia process of desulfurization unit 5, the ammonia that are connected by main line and prepares unit 4; Pipeline between cigarette wind unit 1 and low temperature SCR denitration unit 2 is connected with spray ammonia unit 3;
Described cigarette wind unit 1 comprises gas approach I1b, exhanst gas outlet I1c and air-introduced machine 1d, and air-introduced machine 1d is arranged on the pipeline of SCR reactor 2e exhanst gas outlet II2g;
Described low temperature SCR denitration unit 2 comprises SCR reactor 2e, and SCR reactor 2e top is gas approach II2f, and bottom is exhanst gas outlet II2g; SCR reactor 2e inside is provided with rectifier 2b and three layer of catalyst layer 2c from top to bottom successively; SCR reactor is provided with the blow device 2d adapted with catalyst layer;
Described spray ammonia unit 3 comprise connected by pipeline blower fan 3b, air heating apparatus 3c, ammonia/air mixer 3d, ammonia-spraying grid 3e, flue gas blender 3f; Ammonia-spraying grid 3e and flue gas blender 3f is located on the pipeline of SCR reactor 2e exhanst gas outlet II2g;
Described ammonia process of desulfurization unit 5 comprises desulfurizing tower 5p, is provided with gas approach III5a and gas approach III5a is connected by the air-introduced machine 1d of pipeline with cigarette wind unit 1 below desulfurizing tower 5p; Secondary cycle spray equipment 5f, separating plate 5i, primary cycle spray equipment 5j and demister 5k that desulfurizing tower 5p inside is provided with secondary cycle liquid bath 5s from bottom to up successively, is communicated with secondary cycle liquid bath 5s; Desulfurizing tower 5p outside is provided with the primary cycle liquid bath 5o be communicated with primary cycle spray equipment 5j; The exhanst gas outlet III5a at desulfurizing tower 5p top is communicated with by the exhanst gas outlet I1c of pipeline with cigarette wind unit 1;
Primary cycle spray equipment 5j is divided into three grades, upper, middle and lower shower from top to bottom, and higher level's shower and primary cycle liquid bath lower floor pipeline connection, subordinate's shower and primary cycle liquid bath upper strata pipeline connection;
Described ammonia prepare unit 4 comprise connected by pipeline unload ammonia pump 4a, ammonia storage tank 4b, ammonium hydroxide delivery pump 4c, ammonia evaporator 4d, ammonia surge tank 4e, desulfurization unit ammonium hydroxide delivery pump 4f;
Primary cycle liquid bath 5o is communicated with desulfurization unit ammonium hydroxide delivery pump 4f by pipeline;
Ammonia surge tank 4e is communicated with ammonia/air mixer 3d by pipeline;
Aerator 5e, 5l is respectively equipped with bottom secondary cycle liquid bath 5s and primary cycle liquid bath 5o;
Separating plate 5i is provided with overfall 5h, and overfall 5h is communicated with primary cycle liquid bath 5o by pipeline.
Demister 5k and demister backwash spray equipment 6c supporting is with it provided with above described primary cycle spray equipment 5j.
The reverse spray equipment 5g of primary cycle be communicated with the higher level's shower in primary cycle spray equipment 5j is provided with below separating plate 5i.
This equipment also comprises fresh water (FW) unit 6 and sulphur ammonium prepares unit 7;
Described fresh water (FW) unit 6 comprises the technique water tank 6a and technique water pump 6b that are connected by pipeline; Technique water pump 6b is communicated with the demister backwash spray equipment 6c in desulfurizing tower 5p by pipeline;
Described sulphur ammonium is prepared unit 7 and is comprised the cyclone 7a, centrifuge 7b, drying machine 7c, the packing machine 7d that are connected by pipeline; Cyclone 7a is communicated with secondary cycle liquid bath 5s.
Cigarette wind unit comprises gas approach I1b, exhanst gas outlet I1c and air-introduced machine 1d, air-introduced machine 1d is arranged on the pipeline of SCR reactor exhanst gas outlet II, for sucking the coke oven flue waste gas from coke oven flue 1f, and coke oven flue waste gas is delivered to coke oven chimney 1a, every pollutant discharge in compliance with the standard enters air.
Pending coke oven flue waste gas SO
2content is generally 200-300mg/Nm
3, NO
xcontent is generally 800-1000mg/Nm
3, when process system runs, flue gas is introduced in process system by air-introduced machine 1e by coke oven flue 1f.
Concentration from ammonia still process workshop section of coke-oven plant is that the remained ammonia of 10%-19% pumps into ammonia storage tank 4b by unloading ammonia pump 4a, and the ammoniacal liquor stored in ammonia storage tank 4b can simultaneously for spray ammonia unit 3 and ammonia process of desulfurization unit 5 two unit.Ammoniacal liquor for spray ammonia unit 3 is delivered to ammonia evaporator 4d through ammonium hydroxide delivery pump 4c, heat needed for ammonia evaporation is provided by low-pressure saturated steam 3a, ammonia evaporator 4d being equipped with pressure-control valve controls in certain limit by ammonia pressure, when outlet pressure is more than 0.3MPa, then close ammonium hydroxide delivery pump 4c.Ammonia outlet pipeline is equipped with temperature detector, closes ammonium hydroxide delivery pump 4c when the temperature is too low, make ammonia surge tank 4e maintain proper temperature and pressure, ammonia evaporator 4d is also equipped with safety valve, and equipment pressure anomaly can be prevented too high.The ammonia evaporated from ammonia evaporator 4d flows to ammonia surge tank 4e, then delivers to spray ammonia unit 3 by ammonia feed-line.
Low-pressure saturated steam 3a is at air heating apparatus 3c place, by the air heat from blower fan 3b, add hot-air ammonia/air mixer 3d place with enter and mix from the ammonia of ammonia surge tank 4e after, evenly spray through ammonia-spraying grid 3e and enter coke oven exhaust gas pipeline, after mixing with the low temperature coke oven stack gases from flue, make it mix further through flue gas blender 3f, enter low temperature SCR denitration unit 2.
Coke oven flue waste gas is introduced by cigarette wind unit 1, carry through flue, tentatively mix with the ammonia/air gas mixture carrying out blowing ammonia unit 3 at ammonia-spraying grid 3e place, after flue gas blender 3f mixes further, enter the expansion joint 2a of low temperature SCR denitration unit 2, after compensating by expansion joint 2a the additional stress caused because of temperature difference and mechanical oscillation, through rectifier 2b by ammonia, air, coke oven flue waste gas mist is arranged evenly, enter the SCR catalyst layer 2c of SCR reactor 2e, ensure that flue gas is without bias current, the catalytic reduction of SCR catalyst layer 2c point position is farthest utilized.
Be filled with three layers of low temperature SCR denitration catalyst 2c (ground floor is as spare level) in SCR reactor 2e, can be low to moderate 170 DEG C of still old higher catalytic activitys in temperature, its main component is the V of certain mass proportioning
2o
5-MoO
3-TiO
2the compound of component, TiO
2as active material V
2o
5and MoO
3carrier, and V
2o
5as main active material, to NO
xreduction there is catalytic action, control its mass percent 3%-10%, can guarantee that it is in effective Reduction of NO
xprerequisite under, can not SO be caused
2oxidation and N
2the generation of O; MoO
3then can reduce the initial temperature of catalytic reduction reaction, improve heat endurance and the mechanical performance of catalyst, controlling its mass fraction is 10%-15%, and this catalyst can be low to moderate the NO at the temperature of 160 DEG C-170 DEG C in effective catalytic reduction coke oven flue waste gas
x.Denitrating catalyst adopts cellular structure, and compare plate-type denitration catalyst, honeycomb fashion has the larger feature of specific area, can be NH
3with NO
xmore catalytic reduction point position is provided, more effectively promotes NH
3reductive NO
xfor N
2reaction.Reaction equation is:
4NH
3+4NO+O
2→4N
2+6H
2O (1)
4NH
3+2NO
2+O
2→3N
2+6H
2O (2)
The wherein NO of 95%
xfor NO, equation (1) is key reaction.
After low temperature SCR denitration unit 2 runs a period of time, deposit on low-temperature SCR catalyst 2c for preventing the flying dust in flue gas and other impurity, blocking catalyst duct, must according to low-temperature SCR catalyst 2c pressure loss situation when running, timely startup blow device 2d, blow away dust and other impurity, to maintain the catalytic activity of low-temperature SCR catalyst 2c.
After low temperature SCR denitration unit 2 processes, NO in low temperature coke oven stack gases
xcontent can by 800-1000mg/Nm
3be down to 150-190mg/Nm
3, NOx clearance > 80%.
Low temperature SCR denitration unit 2 processes the coke oven flue waste gas after denitration under the effect of air-introduced machine 1e, through flue, at gas approach III5a place, enters in the desulfurizing tower 5p of ammonia process of desulfurization unit 5.Flue gas enters after in desulfurizing tower 5p, and flow from bottom to top, first with the sulphur ammonium secondary cycle liquid heat exchange be atomized through secondary cycle spray equipment 5f, flue-gas temperature is down to 50 DEG C-60 DEG C, and meanwhile, ammoniacal liquor more than needed in sulphur ammonium secondary cycle liquid can with the SO in flue gas
2there is initial reaction, generate ammonium sulfurous; Flue gas after cooling is through separating plate 5i, and continue to rise, contact respectively with the sulphur ammonium primary cycle liquid be atomized through primary cycle liquid spray equipment 5j, ammoniacal liquor more than needed in sulphur ammonium primary cycle liquid can with the SO in flue gas
2react further, generate ammonium sulfurous.Generate ammonium sulfurous reaction equation as follows:
SO
2+H
2O+xNH
3→(NH
4)
xH
2-xSO
3
Sulphur ammonium primary cycle liquid from the upper strata of primary cycle liquid bath 5o, middle level, bottom, is delivered to primary cycle liquid spray equipment A/B/C5j through primary cycle pump A/B/C5m respectively.Sulphur ammonium primary cycle liquid under spray, after separating plate 5i collects, enters primary cycle liquid bath 5o by separating plate overfall 5h overflow.
In desulfurizing tower 5p, ammonium sulfate solution is carried out two stage cycle, to ensure that ammoniacal liquor can with the SO in coke oven flue waste gas
2sufficient reaction, improves the utilization rate of ammonia, reduces the amount of ammonia slip in coke oven exhaust gas.Containing a small amount of SO
2(lower than 50mg/Nm
3) and escape ammonia (lower than 5mg/Nm
3) coke oven flue waste gas continue to rise, catch the H in flue gas through demister A/B5k
2o, prevents the conditions of streaking produced because flue gas water content is too high, and the water droplet simultaneously on demister A/B5k also further can catch the escape ammonia in flue gas, and the amount of desulfurizing tower escape ammonia is met the requirements.Demister backwash spray equipment 6c is set below demister A/B5k, in order to periodic flushing demister A/B5k.
Sulphur ammonium secondary cycle liquid bottom desulfurizing tower 5p through secondary cycle spray equipment 5f constantly with the coke oven exhaust gas heat exchange from gas approach 5a, portion of water can along with flue gas upwards, sulphur ammonium secondary cycle liquid can be constantly concentrated, for ensureing that it keeps certain liquid level bottom desulfurizing tower 5p, simultaneously for preventing flue dust from depositing at separating plate 5i place, be provided with the reverse spray equipment 5g of primary cycle, maintain sulphur ammonium secondary cycle liquid liquid level bottom desulfurizing tower 5p with regular backwash separating plate 5i.
Aeration is carried out to sulphur ammonium one-level, secondary cycle liquid, the ammonium sulfate solution in forced oxidation I and II circulation liquid bath respectively by the aerator B5l be positioned at bottom primary cycle liquid bath 5o and the aerator A5e be positioned at bottom desulfurizing tower 5p, occurs to react as follows:
(NH
4)
xH
2-xSO
3+1/2O
2+(2-x)NH
3→(NH
4)
2SO
4
Along with the continuous circulation of the sulphur ammonium secondary cycle liquid bottom desulfurizing tower 5p, moisture runs off gradually, and the proportion of sulphur ammonium secondary cycle liquid increases gradually, after increase proportion is greater than 1.2kg/L, is delivered to sulphur ammonium and prepares unit 7, preparing finished articles sulphur ammonium through over cure ammonium excavationg pump 5b.
Be provided with accident pump 5d bottom desulfurizing tower 5p, when sulphur ammonium secondary cycle liquid occurs abnormal, by accident pump 5d, circulation fluid can be drained into accident pool.
Primary cycle liquid bath 5o top is provided with overfall 5n, by pipeline communication in desulfurizing tower 5p, maintains the unlikely spilling of certain liquid level to make the sulphur ammonium primary cycle liquid in circulating slot 5o; Circulating slot 5o top is provided with ammoniacal liquor and adds a mouthful 5q, and remained ammonia is carried by desulfurization unit ammonium hydroxide delivery pump 4f, and pump adopts VFC, as SO in flue gas
2content and desulfurizing tower in pH change time, VFC ammoniacal liquor dosage, guarantee the desulfuration efficiency of ammonia process of desulfurization unit 5 be greater than 95% and the escaping of ammonia rate be no more than 5mg/Nm
3.
In addition, sulphur ammonium secondary cycle liquid is after secondary cycle spray equipment 5f is atomized, and when with temperature being the coke oven flue exhaust gas contact of 170 DEG C-250 DEG C, at this temperature, the ammoniacal liquor in sulphur ammonium secondary cycle liquid and ammonium sulfurous are to the NO in flue gas
xstill old reduction, can reduce NO in flue gas further
xcontent, clearance is about about 40%.
After ammonia process of desulfurization unit 5 processes, in coke oven flue waste gas, SO2 content is about 10-30mg/Nm
3, NOx content is about 90-110mg/Nm
3, indices all meets the atmosphere pollutants emission standards of " coking chemistry emission of industrial pollutants standard GB16171-2012 " enforcement from 1 day January in 2015, meanwhile, and water droplet carrying amount ≯ 75mg/Nm
3, the escaping of ammonia rate ≯ 5mg/Nm
3, the flue gas after desulphurization denitration of the coke oven flue waste gas after process, through exhanst gas outlet I1c, enters coke oven chimney 1a, qualified discharge.
Fresh water (FW) unit 6 comprises technique water tank 6a, technique water pump 6b, and fresh water (FW) is delivered to demister backwash spray equipment 6c by technique water pump 6b, through device atomization, and back flush demister 5k.Be delivered to other with water place 6d by technique water pump 6b, the inwall of flushable flue and desulfurizing tower 5p, deposits throughout to prevent the dust in flue gas.
Sulphur ammonium is prepared unit 7 and is comprised cyclone 7a, centrifuge 7b, drying machine 7c, packing machine 7d.The ammonium sulfate solution reaching design concentration sends into cyclone 7a by sulphur ammonium excavationg pump 5b, slurries gravity flow after concentrated enters centrifuge 7b, after further dehydration, dried by drying machine 7c, reach the sulphur ammonium after standard by packing machine 7d bagging and packaging, the isolated ammonium sulfate liquor 7f of cyclone 7a and centrifuge 7b is back in desulfurizing tower 5p.The sulphur ammonium product 7e encapsulated by packing machine 7d takes out, and reduces coal chemical enterprise desulphurization denitration cost.
Claims (4)
1. the purifying equipment of low temperature coke oven stack gases, is characterized in that: this equipment is mainly comprised the cigarette wind unit, low temperature SCR denitration unit, ammonia process of desulfurization unit, the ammonia that are connected by main line and prepares unit; Pipeline between cigarette wind unit and low temperature SCR denitration unit is connected with spray ammonia unit;
Described cigarette wind unit comprises gas approach I, exhanst gas outlet I and air-introduced machine, and air-introduced machine is arranged on the pipeline of SCR reactor exhanst gas outlet II;
Described low temperature SCR denitration unit comprises SCR reactor, and SCR reactor top is gas approach II, and bottom is exhanst gas outlet II; SCR inside reactor is provided with rectifier and three layers of catalyst layer from top to bottom successively; SCR reactor is provided with the blow device adapted with catalyst layer;
Described spray ammonia unit comprises the blower fan, air heating apparatus, ammonia/air mixer, ammonia-spraying grid, the flue gas blender that are connected by pipeline; Ammonia-spraying grid and flue gas blender are located on the pipeline of SCR reactor gas approach II;
Described ammonia process of desulfurization unit comprises desulfurizing tower, is provided with gas approach III and gas approach III is connected by the air-introduced machine of pipeline with cigarette wind unit below desulfurizing tower; Desulfurizing tower inside is provided with secondary cycle liquid bath, the secondary cycle spray equipment be communicated with secondary cycle liquid bath, separating plate, primary cycle spray equipment and demister from bottom to up successively; Desulfurizing tower outside is provided with the primary cycle liquid bath be communicated with primary cycle spray equipment; The exhanst gas outlet III at desulfurizing tower top is communicated with by the exhanst gas outlet I of pipeline with cigarette wind unit;
Primary cycle spray equipment is divided into three grades, upper, middle and lower shower from top to bottom, and higher level's shower and primary cycle liquid bath lower floor pipeline connection, subordinate's shower and primary cycle liquid bath upper strata pipeline connection;
Described ammonia prepare unit comprise connected by pipeline unload ammonia pump, ammonia storage tank, ammonium hydroxide delivery pump, ammonia evaporator, ammonia surge tank, desulfurization unit ammonium hydroxide delivery pump;
Primary cycle liquid bath is communicated with desulfurization unit ammonium hydroxide delivery pump by pipeline;
Ammonia surge tank is communicated with ammonia/air mixer by pipeline;
Aerator is respectively equipped with bottom secondary cycle liquid bath and primary cycle liquid bath;
Separating plate is provided with overfall, and overfall is communicated with primary cycle liquid bath by pipeline.
2. the purifying equipment of a kind of low temperature coke oven stack gases according to claim 1, is characterized in that: be provided with demister and backwash spray equipment supporting with it above described primary cycle spray equipment.
3. the purifying equipment of a kind of low temperature coke oven stack gases according to claim 1, is characterized in that: be provided with the reverse spray equipment of primary cycle be communicated with the higher level's shower in primary cycle spray equipment below separating plate.
4. the purifying equipment of a kind of low temperature coke oven stack gases according to claim 1, is characterized in that: this equipment also comprises fresh water (FW) unit and sulphur ammonium prepares unit;
Described fresh water (FW) unit comprises the technique water tank and technique water pump that are connected by pipeline; Technique water pump is communicated with the backwash spray equipment in desulfurizing tower by pipeline;
Described sulphur ammonium is prepared unit and is comprised the cyclone, centrifuge, drying machine, the packing machine that are connected by pipeline; Cyclone is communicated with secondary cycle liquid bath.
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|---|---|---|---|
| CN201420725611.8U CN204261549U (en) | 2014-11-27 | 2014-11-27 | The purifying equipment of a kind of low temperature coke oven stack gases |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201420725611.8U CN204261549U (en) | 2014-11-27 | 2014-11-27 | The purifying equipment of a kind of low temperature coke oven stack gases |
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| CN204261549U true CN204261549U (en) | 2015-04-15 |
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ID=52796449
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Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104353336A (en) * | 2014-11-27 | 2015-02-18 | 山东同源和环境工程有限公司 | Low-temperature coke oven flue waste gas cleaning technology and equipment thereof |
| CN105194991A (en) * | 2015-10-26 | 2015-12-30 | 北京神雾环境能源科技集团股份有限公司 | Glass furnace flue gas desulfurization and denitrification system and process |
| CN107575882A (en) * | 2017-09-26 | 2018-01-12 | 广州智光节能有限公司 | A kind of waste heat boiler SCR denitrating flue gas efficiency-adjusted apparatus and method |
| CN109107356A (en) * | 2018-08-20 | 2019-01-01 | 彩虹集团（邵阳）特种玻璃有限公司咸阳分公司 | A kind of cover-plate glass tank furnace smoke processing system |
| CN116510509A (en) * | 2023-04-24 | 2023-08-01 | 华能淮阴第二发电有限公司 | Denitration device capable of effectively reducing ammonia escape |
-
2014
- 2014-11-27 CN CN201420725611.8U patent/CN204261549U/en not_active Withdrawn - After Issue
Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104353336A (en) * | 2014-11-27 | 2015-02-18 | 山东同源和环境工程有限公司 | Low-temperature coke oven flue waste gas cleaning technology and equipment thereof |
| CN104353336B (en) * | 2014-11-27 | 2016-08-24 | 山东同源和环境工程有限公司 | A kind of low temperature purifying technique of coke oven stack gases and equipment thereof |
| CN105194991A (en) * | 2015-10-26 | 2015-12-30 | 北京神雾环境能源科技集团股份有限公司 | Glass furnace flue gas desulfurization and denitrification system and process |
| CN105194991B (en) * | 2015-10-26 | 2018-06-08 | 神雾科技集团股份有限公司 | Glass kiln flue gas desulfurization and denitrification system and technique |
| CN107575882A (en) * | 2017-09-26 | 2018-01-12 | 广州智光节能有限公司 | A kind of waste heat boiler SCR denitrating flue gas efficiency-adjusted apparatus and method |
| CN109107356A (en) * | 2018-08-20 | 2019-01-01 | 彩虹集团（邵阳）特种玻璃有限公司咸阳分公司 | A kind of cover-plate glass tank furnace smoke processing system |
| CN116510509A (en) * | 2023-04-24 | 2023-08-01 | 华能淮阴第二发电有限公司 | Denitration device capable of effectively reducing ammonia escape |
| CN116510509B (en) * | 2023-04-24 | 2024-01-23 | 华能淮阴第二发电有限公司 | Denitration device capable of effectively reducing ammonia escape |
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