CN102451610B - Treatment method for nitrogen oxide tail gas discharged from industrial production furnace, and apparatus thereof - Google Patents
Treatment method for nitrogen oxide tail gas discharged from industrial production furnace, and apparatus thereof Download PDFInfo
- Publication number
- CN102451610B CN102451610B CN201010514314.5A CN201010514314A CN102451610B CN 102451610 B CN102451610 B CN 102451610B CN 201010514314 A CN201010514314 A CN 201010514314A CN 102451610 B CN102451610 B CN 102451610B
- Authority
- CN
- China
- Prior art keywords
- gas
- liquid
- guide vane
- hollow guide
- hollow
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
Images
Abstract
The present invention discloses a treatment method for nitrogen oxide tail gas discharged from an industrial production furnace, and an apparatus thereof. According to the present invention, gas generated from the furnace is connected to a self-sucking type gas-liquid mixing device through a pipeline to carry out a treatment on the furnace tail gas; the treated gas is discharged by using a gas exhaust tube with the pressure provided by the self-sucking type gas-liquid mixing device. The apparatus of the present invention comprises the self-sucking type gas-liquid mixing device, an absorption liquid cooling system and an absorption liquid settlement system. Compared to the prior art, with the method and the apparatus of the present invention, the nitrogen oxide tail gas discharged from the industrial production furnace can be effectively treated, the cost is low, the process is simple, and the operation can be stably performed for a long period.
Description
Technical field
The present invention relates to a kind of exhaust gas treatment method and device, particularly the improvement method and apparatus of industrial production kiln nitrogen oxide tail gas.
Background technology
The industrial production kiln often can discharge the waste gas that contains in a large number nitrogen oxide, and its composition is mainly nitric oxide (NO), nitrous oxide (N
2o), nitrogen dioxide (NO
2) etc., be one of Air Pollutants of national limiting emission.The waste gas of Catalyst Production kiln discharge particularly, its nitrous oxides concentration is high, and color is brownish red or brown color, and environment and people's health is had to harmfulness.For example, while adopting metal to react with nitric acid (red fuming nitric acid (RFNA) or rare nitric acid) to produce catalyst or use metal nitrate as raw material, at stage kilns such as catalyst drying, calcination activations, all can give off the waste gas of nitrogen-containing oxide.The nitrogen oxide tail gas of Catalyst Production kiln discharge has following characteristics: (1) concentration is high.In the catalyst roasting process, the nitrogen substances such as the nitrate of catalyst soakage, amine are at high temperature concentrated and are decomposed or oxidation generation nitrogen oxide, and nitrous oxides concentration is very high, and the nitrous oxides concentration that the catalyst of some kind produces reaches 10000-30000mg/m
3, gas is reddish brown, is discharged in atmosphere harm very large.(2) the capacity fluctuation is large.Due to catalytic production, some is not continuous process, and the different temperatures stage of roasting, the different time of uniform temp, and all great changes have taken place for the generation of waste gas.Follow-up exhaust-gas treatment is brought to very large problem.When the large and treating capacity hour of emission-control equipment of waste gas generation, kiln tail gas will leak, and the healthy of operating personnel caused damage.When little and treating capacity emission-control equipment of waste gas generation is large, catalyst fines will enter emission-control equipment loss by pipeline, and catalyst production descends, and the normal operating of emission-control equipment is caused to very large harm simultaneously.(3) dust content is high, and dust size is little, is difficult to remove.The dust problem of Catalyst Production waste gas is the difficult point of catalyst exhaust-gas treatment.Because some catalyst are to carry out roasting with pulverulence, the particle diameter of its dust is very little, adopt conventional bag-type dust, cyclone dust removal all to be difficult to complete place to go, a lot of to the harm of emission-control equipment, often within several days, just may block and stop absorption plants such as packed towers.(4) EGT is high.Catalyst kiln outlet EGT is up to 700-800 ℃, even also have 300-400 ℃ after piping is carried, if there is no cooling measure, after processing, the exhaust temperature of discharge is very high, produces serious thermal pollution.
The nitrous oxides exhaust gas treatment technology, can be divided into dry method and wet method two classes.Dry method comprises the ammine selectivity catalytic reduction method (SCR) that the NOx in waste gas is reduced to nitrogen, as ammine selective non-catalytic reduction method, metal carbon-supported catalysts catalytic reduction method etc.; Absorption method (molecular sieve, active carbon, silica gel and containing NN
3mud coal etc.); Plasma-activated method etc.Wet method comprises water absorption method, alkali absorption method, ammonia absorption method, oxidation absorption process, Reduction by Thiosulfate method, urea absorption reducing process and Absorption via Chemical Complexation etc.
In dry method treatment technology, absorption method than little, the reasons such as consumption large, the processing that needs to regenerate, is generally applied less due to the adsorption capacity that has adsorbent now in the NOx exhaust-gas treatment.Ammine selectivity catalytic reduction method and ammine selective non-catalytic reduction method, the current focus that has become denitration of boiler smoke technical research and application.But facts have proved, during the NOx waste gas that produces in administering the Industrial Stoves production process, ammine selectivity catalytic reduction method processing method also is not suitable for, and its main cause is the inhomogeneities due to the NOx discharge, causes operating temperature and throw the ammonia amount to be difficult to control, cause beds and equipment inner member sintering, the side reaction of this reaction is many in addition, can regenerate NOx, and ammonia easily penetrates, discharge frequent visible large tobacco and great Bai cigarette in gas, product is NH
4nO
2, NH
4nO
3, NH
3deng.Therefore, while adopting dry technique to process waste gas of industrial kiln and furnace, reply technological process, catalyst and equipment etc. are furtherd investigate.
In the wet-treating technology, the absorption liquid kind is many, applies comparatively general.As alkali absorption method (comprises NaOH, Na
2cO
3) be widely used at home the vent gas treatment in nitric acid production and use procedure, and by-product sodium nitrate and natrium nitrosum product.Ammoniacal liquor liquid phase absorption process and ammonia spray method also are applied on boiler smoke is processed.Reduction by Thiosulfate method, urea reduction method etc. also are applied gradually in the industry exhaust-gas treatments such as space flight, nitric acid production and use, Catalyst Production.With dry method, compare, wet method has larger operating flexibility, can select different reaction systems, is more suitable in the processing of Industrial Stoves process gas.
The main equipment of wet method nitrogen oxide treatment process is to provide the absorption tower of gas-liquid contact, mass transfer, reaction.Existing absorption tower is divided into two kinds: a kind of is the spray absorber (band filler or void tower) of gas-liquid two-phase counter current contacting, and in this equipment, gas phase is continuous phase, and liquid phase is decentralized photo; Another kind is gas-liquid two-phase bubbling contact reactor, and in running, liquid phase is continuous phase, and gas phase is decentralized photo.All there is limitation in these two kinds of equipment in waste gas treatment process: the spray column pressure drop is little, and power consumption is few, but the gas-liquid contact surface area is low, and device efficiency is lower; Bubbling reactor, for the contact area of larger gas-liquid two-phase is provided, must increase liquid depth, will make like this pressure drop increase, and power consumption increases, and easily results in blockage.
Summary of the invention
For the deficiencies in the prior art, the invention provides a kind of expense cheap, the improvement method and apparatus of the simple industrial production kiln of technique nitrogen oxide tail gas.
The improvement method of industrial production kiln nitrogen oxide tail gas of the present invention comprises following content: kiln is produced to gas and be connected on the self-suction gas-liquid mixing apparatus by pipeline, kiln tail gas is processed, and the pressure that the gas after processing relies on self-suction gas-liquid mixing apparatus self to provide is discharged by aiutage.
In the inventive method, described Self inhaling type gas-liquid mixed equipment is by tank body, motor, and impeller shaft, gas-liquid mixing impeller and transmission seal part etc. partly form.Utilize motor to drive by impeller shaft the negative pressuren zone that under the absorption liquid of gas-liquid mixing impeller in tank body, High Rotation Speed produces, kiln tail gas is drawn to the gas-liquid mixing impeller negative pressuren zone by impeller shaft internal channel or the impeller shaft outer sleeve of Self inhaling type gas-liquid mixed equipment, gas-liquid mixing impeller is provided with qi-emitting hole, by qi-emitting hole, by gas, the form with microbubble is scattered in liquid kiln tail gas, quick mass transfer and chemical reaction occur, pollutant in kiln tail gas is trapped by the absorption liquid in Self inhaling type gas-liquid mixed equipment, absorb and react, after processing, gas floats from absorption liquid, enter the aiutage discharge from the reactor head exhaust outlet.
The gas-liquid mixing impeller structure of described Self inhaling type gas-liquid mixed equipment is as follows: gas-liquid mixing impeller mainly is comprised of hollow connecting shaft joint, hollow disc, hollow guide vane, ring diversion plate.The duct of hollow connecting shaft joint communicates with the inner space of hollow disc; Hollow disc is comprised of upper cover plate, lower cover and cylindrical shell; The hollow disc lower cover downside hollow guide vane that is tightly connected, offer with the lower cover of hollow guide vane correspondence position the passage be communicated with hollow guide vane inner space, hollow guide vane lower end arranges ring diversion plate, and the rear one lateral lobe sheet of hollow guide vane direction of rotation arranges qi-emitting hole.
In above-mentioned gas-liquid mixing impeller, hollow guide vane has an inner space, this inner space upside communicates with hollow disc, and the rear one lateral lobe sheet of hollow guide vane direction of rotation is by qi-emitting hole and hollow guide vane exterior, and remainder is hermetically-sealed construction.
In above-mentioned gas-liquid mixing impeller, the cross section of hollow guide vane can be suitable shape, as suitable shapes such as equilateral del, BI del, irregular del, trapezoidal, irregular, parallelogram.On the hollow disc lower cover with hollow guide vane between channel shape preferably identical with hollow guide vane cross section.Hollow guide vane quantity can arrange according to the scale of gas-liquid mixing impeller 1～50, is preferably 2～30.
In above-mentioned gas-liquid mixing impeller, described qi-emitting hole can arrange along the impeller axis direction a row or multi-row.The number of qi-emitting hole and arrangement mode also can be made any change on the one lateral lobe sheet of hollow guide vane direction of rotation rear.
In above-mentioned gas-liquid mixing impeller, hollow guide vane upper end is connected with the lower cover of hollow disk, and lower end is connected with ring diversion plate, between two adjacent hollow guide vanes, forms water stream channel.
In above-mentioned gas-liquid mixing impeller, there is flat board or the conical plate of circular water inlet (or inlet) centered by ring diversion plate; Its profile can adopt arbitrary shape as required, but the general circle of selecting.Ring diversion plate is connected with hollow guide vane, and the formed annular region area of the inside and outside circle of deflector at least can closed hollow guide vane lower end.Ring diversion plate can prevent current from hollow guide vane upper end or the sliding leakage in lower end, improves the suction water yield and the vacuum of impeller, thereby improves amount of air entrainment and gas-liquid mixed effect; Ring diversion plate can also reduce the towing of water body to hollow guide vane in addition, reduces the power consumption of impeller.
The gettering rate of Self inhaling type gas-liquid mixed equipment is by the rotating speed decision of its motor, and rotating speed is faster, and gettering rate is larger.Discharge capacity according to kiln tail gas during operation is controlled the rotating speed of motor by frequency converter, thereby control the gettering rate of Self inhaling type gas-liquid mixed equipment, the discharge capacity that makes system process tolerance and industrial production kiln is consistent, and take and just makes kiln not yearn for leakage waste gas as best.
Described impeller 200mm at least below the absorption liquid liquid level.Its effect is when this self-suction gas-liquid mixing apparatus does not turn round, and because the qi-emitting hole on impeller is positioned under liquid, makes whole equipment be equivalent to a water seal, guarantees that kiln tail gas can not be leaked to external environment.
Described absorption liquid can be urea liquid, sodium hydroxide solution, ammoniacal liquor, hypo solution or sodium carbonate liquor.Wherein preferred urea liquid, comprising urea 1%-30% (weight), can comprise the catalyst of appropriate routine.Absorption liquid active ingredient concentration can be changed fresh absorption liquid or add active ingredient after reducing.
Temperature and the solid matter content situation of absorption liquid during according to operation, carry out cooling and/or sedimentation separation operation, then recycles.Below general control absorption liquid temperature to 60 ℃, be preferably below 50 ℃, in absorption liquid, solids content general control (weight) below 30%, be preferably below 20%.Cooling and the sedimentation of absorption liquid can be carried out in the tank body of gas-liquid mixed equipment, also so that independently cooling system and sedimenting system to be set.Cooling system and sedimenting system can be arranged in parallel, and absorption liquid enters respectively cooling system and sedimenting system; The setting of also can connecting of cooling system and sedimenting system, absorption liquid successively enters cooling system and sedimenting system, and sequencing can be any, preferably is introduced into sedimenting system and enters cooling system again; Cooling system and sedimenting system can be also systems independently separately.Cooling system and sedimenting system can intermittently be used according to the operational circumstances choice for use, also can use continuously, can use simultaneously, also can use one of them system.
Described cooling system can be comprised of various forms of coolers, its objective is make due to the heat exchange of high temperature kiln tail gas after the temperature of the absorption liquid that heats up descend.
Described sedimenting system can be various forms of filters, sedimentation tower, settling tank etc., preferred overflow-type settling tank, it is characterized in that sedimentation after supernatant flow out settling tank by downflow weir, the mud in absorption liquid is discharged by mud valve at the bottom of being deposited to tank.Its objective is that the dust that will enter absorption liquid removes from absorption liquid, make absorption liquid can continue to recycle.
The controlling device of industrial production kiln nitrogen oxide tail gas of the present invention comprises Self inhaling type gas-liquid mixed equipment, absorption liquid cooling system and absorption liquid sedimenting system.The structure of Self inhaling type gas-liquid mixed equipment, absorption liquid cooling system and absorption liquid sedimenting system and correlation are determined by foregoing of the present invention.Cooling system wherein and sedimenting system are arranged one of as follows: cooling system and sedimenting system are arranged in parallel, and absorption liquid enters respectively cooling system and sedimenting system; Perhaps cooling system and sedimenting system series connection arrange, and absorption liquid successively enters cooling system and sedimenting system, and sequencing is any; Perhaps cooling system and sedimenting system are systems independently separately.Be generally: cooling system and sedimenting system can be arranged in parallel, and the leakage fluid dram of Self inhaling type gas-liquid mixed equipment communicates with the inlet of cooling system and the inlet of sedimenting system respectively; The setting of also can connecting of cooling system and sedimenting system, be Self inhaling type gas-liquid mixed equipment priority and cooling system and sedimenting system UNICOM, sequencing can be any, and preferably Self inhaling type gas-liquid mixed equipment communicates with sedimenting system, and sedimenting system communicates with cooling system.
Advantage of the present invention be can nitrogen oxide to remove efficiency high, can reach more than 90%; Treating capacity can be followed kiln tail gas generation and be changed at any time; There is not blockage problem in device; After processing, exhaust temperature is low, can directly discharge.The Self inhaling type gas-liquid mixed equipment that the inventive method is used has overcome existing Self inhaling type gas-liquid mixed equipment inspiratory capacity deficiency and inspiratory capacity is adjusted inflexible problem, take full advantage of the area of hollow guide vane direction of rotation rear one lateral lobe sheet, can greatly increase the quantity of qi-emitting hole, and can increase arbitrarily by increasing hollow guide vane height the number of qi-emitting hole and change arrangement mode.The negative pressure that in the time of can taking full advantage of vane rotary, the guide vane rear side produces, the negative pressure that between guide vane, the current modified line produces, and the shear action that current produce in disc surfaces is introduced gas, the amount of air entrainment of impeller is large, gas-liquid mixed is effective, not only under slow speed, can introduce a large amount of gas, and the bleed hole is not in the central area of impeller, what the impeller center sucked is only absorption liquid, the vacuum size is not limited by other factors, gas introduction volume and suction liquid measure can improve and increase simultaneously with revolution, the amount of air entrainment size adjustment is convenient, the current shear action can also prevent that qi-emitting hole from stopping up in addition.The characteristics that can effectively adapt to some industrial production kiln nitrogen oxide tail gas.
The accompanying drawing explanation
Fig. 1 is a kind of idiographic flow signal of the present invention and formation picture of device.
Vertical section from the air feeding type gas liquid mixing blade front view of the Self inhaling type gas-liquid mixed equipment that Fig. 2 is the inventive method use.
The A-A direction view that Fig. 3 is Fig. 2.
The drawing in side sectional elevation that Fig. 4 is another kind of hollow guide vane structure.
The drawing in side sectional elevation that Fig. 5 is the third hollow guide vane structure.
Fig. 6 is gas-liquid mixing impeller contour structures stereogram.
The specific embodiment
Further illustrate implementation of the present invention below in conjunction with accompanying drawing.
The pressure that the gas of the tail gas of the nitrogen-containing oxide that as shown in Figure 1, Industrial Stoves 101 produce after piping 102 enters 103 processing of self-suction gas-liquid mixing apparatus relies on self-suction gas-liquid mixing apparatus self to provide is by aiutage 104 qualified discharges.
Self-suction gas-liquid mixing apparatus 103 is comprised of motor 105, tank body 106, impeller shaft 107, impeller 108 and transmission and sealing mechanism.Absorption liquid 109 is housed in tank body.Absorption liquid is delivered in settling tank 111 and cooler 112 and carries out desilt and cooling down operation through pump 10.Downflow weir 113 and mud valve 114 are arranged in settling tank.Settling tank 111 and cooler 112 are positioned at a high position, through sedimentation and cooling after absorption liquid rely on flow by gravity to return in the tank body 106 of self-suction gas-liquid mixing apparatus 103 to recycle.
Further illustrate below in conjunction with Fig. 2～6 structure from air feeding type gas liquid mixing blade and the method for operation that Self inhaling type gas-liquid mixed equipment is used.
As shown in Figure 2, from guided gas gas-liquid mixed blade wheel, by hollow connecting shaft joint 1, upper cover plate 2, cylindrical shell 3, lower cover 5, hollow guide vane 6, ring diversion plate 7 forms; Wherein upper cover plate 2, cylindrical shell 3, lower cover 5 form the cylindrical shape hollow disc of impeller; It is corresponding that lower cover 5 even circumferentials are distributed with some and hollow guide vane 6
the shape opening; Hollow guide vane 6 is on cross section and lower cover 5
the hollow structure of shape opening similar shape, hollow guide vane 6 upper ends
on shape opening and lower cover 5
the shape opening is tightly connected, and with the hollow disc inner space, communicates; Lower end
the shape opening is sealed by ring diversion plate 7.Qi-emitting hole 4 is arranged on the rear one side guide vane of hollow guide vane direction of rotation.
In Fig. 3～Fig. 5 view, therefrom form and the position of visible hollow guide vane 6 and ring diversion plate 7.The direction of arrow is the vane rotary direction, the position of qi-emitting hole 4.Described hollow guide vane can also adopt other forms.
Under the drive of drive motors and impeller shaft, impeller rotates with certain speed in liquid, and in the inner negative pressure that produces of impeller, tail gas enters impeller by hollow connecting shaft joint 1, enter hollow guide vane by the opening on hollow disk lower cover 5, be scattered in liquid with the microbubble form through qi-emitting hole 4.
The water sucking mouth (or liquid sucting port) that the perforate of ring diversion plate 7 centers is impeller, ring diversion plate 7 forms with guide vane 6, lower cover 5 water stream channel (or fluid passage) be sealed, effectively prevent current from the guide vane bottom or the sliding leakage in top, improved water velocity and the vacuum of impeller inside, also reduced water body impeller is pulled simultaneously.After increasing ring diversion plate, the vacuum of the impeller inside vacuum (0.1MPa left and right) that can reach capacity, not only amount of air entrainment obviously improves, and power-dissipation-reduced.
The nitrous oxides concentration of the tail gas that some industrial production kiln produces is high, and temperature is high, and dust content is very large, and tolerance and noxious pollutant change greatly.Adopt the inventive method and device, when the form with microbubble enters absorption liquid, between gas-liquid, through sufficient mass transfer and heat transfer, nitrogen oxide reacts with absorption liquid and generates nitrogen, and clearance reaches more than 90%.Dust enters absorption liquid, makes to process rear waste gas not containing dust, and temperature will be down to below 50 ℃, meets discharging standards.The absorption liquid temperature slightly raises, and after the cooling and sedimenting system desilt of cooler, returns and recycles.The inventive method and device can carry out the stable processing of long period to this tail gas.
Claims (10)
1. the improvement method of an industrial production kiln nitrogen oxide tail gas, comprise following content: kiln is produced to gas and be connected on the self-suction gas-liquid mixing apparatus by pipeline, kiln tail gas is processed, the pressure that gas after processing relies on self-suction gas-liquid mixing apparatus self to provide is discharged by aiutage, it is characterized in that: described Self inhaling type gas-liquid mixed equipment is by tank body, motor, impeller shaft, gas-liquid mixing impeller and transmission seal part form, utilize motor to drive by impeller shaft the negative pressuren zone that under the absorption liquid of gas-liquid mixing impeller in tank body, High Rotation Speed produces, kiln tail gas is drawn to the gas-liquid mixing impeller negative pressuren zone by impeller shaft internal channel or the impeller shaft outer sleeve of Self inhaling type gas-liquid mixed equipment, gas-liquid mixing impeller is provided with qi-emitting hole, by qi-emitting hole, by gas, the form with microbubble is scattered in liquid kiln tail gas, quick mass transfer and chemical reaction occur, pollutant in kiln tail gas is trapped by the absorption liquid in Self inhaling type gas-liquid mixed equipment, absorb and react, after processing, gas floats from absorption liquid, enter the aiutage discharge from the reactor head exhaust outlet, wherein the gas-liquid mixing impeller structure of Self inhaling type gas-liquid mixed equipment is as follows: gas-liquid mixing impeller mainly is comprised of hollow connecting shaft joint, hollow disc, hollow guide vane, ring diversion plate, the duct of hollow connecting shaft joint communicates with the inner space of hollow disc, hollow disc is comprised of upper cover plate, lower cover and cylindrical shell, the hollow disc lower cover downside hollow guide vane that is tightly connected, offer with the lower cover of hollow guide vane correspondence position the passage be communicated with hollow guide vane inner space, hollow guide vane lower end arranges ring diversion plate, and the rear one lateral lobe sheet of hollow guide vane direction of rotation arranges qi-emitting hole.
2. in accordance with the method for claim 1, it is characterized in that: in gas-liquid mixing impeller, hollow guide vane has an inner space, this inner space upside communicates with hollow disc, the rear one lateral lobe sheet of hollow guide vane direction of rotation is by qi-emitting hole and hollow guide vane exterior, and remainder is hermetically-sealed construction.
3. in accordance with the method for claim 1, it is characterized in that: in gas-liquid mixing impeller, on the hollow disc lower cover with hollow guide vane between channel shape identical with hollow guide vane cross section.
4. it is characterized in that in accordance with the method for claim 1: hollow guide vane quantity is 1～50.
5. in accordance with the method for claim 1, it is characterized in that: in gas-liquid mixing impeller, hollow guide vane upper end is connected with the lower cover of hollow disk, and lower end is connected with ring diversion plate, between two adjacent hollow guide vanes, forms water stream channel.
6. in accordance with the method for claim 1, it is characterized in that: in gas-liquid mixing impeller, there is flat board or the conical plate of circular water inlet centered by ring diversion plate; Ring diversion plate is connected with hollow guide vane, and the formed annular region area of the inside and outside circle of deflector at least can closed hollow guide vane lower end.
7. in accordance with the method for claim 1, it is characterized in that: absorption liquid is urea liquid, sodium hydroxide solution, ammoniacal liquor, hypo solution or sodium carbonate liquor.
8. in accordance with the method for claim 1, it is characterized in that: control below absorption liquid temperature to 60 ℃, in absorption liquid, solids content is controlled below 30%.
9. in accordance with the method for claim 8, it is characterized in that: control below absorption liquid temperature to 50 ℃, in absorption liquid, solids content is controlled below 20%.
10. the controlling device of an industrial production kiln nitrogen oxide tail gas, is characterized in that: comprise Self inhaling type gas-liquid mixed equipment, absorption liquid cooling system and absorption liquid sedimenting system; Self inhaling type gas-liquid mixed equipment is the Self inhaling type gas-liquid mixed equipment related in the arbitrary claim of claim 1～6; Cooling system wherein and sedimenting system are arranged one of as follows: cooling system and sedimenting system are arranged in parallel, and absorption liquid enters respectively cooling system and sedimenting system; Perhaps cooling system and sedimenting system series connection arrange, and absorption liquid successively enters cooling system and sedimenting system, and sequencing is any; Perhaps cooling system and sedimenting system are systems independently separately.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201010514314.5A CN102451610B (en) | 2010-10-15 | 2010-10-15 | Treatment method for nitrogen oxide tail gas discharged from industrial production furnace, and apparatus thereof |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201010514314.5A CN102451610B (en) | 2010-10-15 | 2010-10-15 | Treatment method for nitrogen oxide tail gas discharged from industrial production furnace, and apparatus thereof |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN102451610A CN102451610A (en) | 2012-05-16 |
| CN102451610B true CN102451610B (en) | 2014-01-01 |
Family
ID=46035540
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201010514314.5A Active CN102451610B (en) | 2010-10-15 | 2010-10-15 | Treatment method for nitrogen oxide tail gas discharged from industrial production furnace, and apparatus thereof |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN102451610B (en) |
Families Citing this family (15)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| KR101344658B1 (en) * | 2013-06-11 | 2013-12-24 | 김웅회 | Eliminaing device for removing poisonous substance of noxious gases and method therof |
| CN103409632B (en) * | 2013-07-18 | 2016-01-13 | 山东国大黄金股份有限公司 | A kind of method of gold mud wet processing tail gas comprehensive reutilization |
| CN103449388B (en) * | 2013-09-10 | 2016-03-30 | 安徽淮化股份有限公司 | A kind of dust technology recovery method and specific equipment thereof |
| CN105921013A (en) * | 2016-05-10 | 2016-09-07 | 南宁市夏阳化工科技有限责任公司 | Adblue solution with lubricating and anti-freezing functions |
| CN108224552A (en) * | 2016-12-22 | 2018-06-29 | 王支业 | A kind of air purifier |
| CN106823618A (en) * | 2017-02-16 | 2017-06-13 | 江西稀有稀土金属钨业集团有限公司 | A kind of dust arrester installation |
| CN107367177B (en) * | 2017-07-31 | 2019-02-26 | 贵州宜化化工有限责任公司 | A kind of exhaust gas cooling device of carbamide production system |
| CN107930322A (en) * | 2017-11-29 | 2018-04-20 | 宁夏三和日升化工有限公司 | A kind of furnace flue gas desulfurization dust-removal system and method |
| CN108325354A (en) * | 2018-01-11 | 2018-07-27 | 孙江天 | Seawater spiral desulfurizer |
| CN108771934B (en) * | 2018-07-05 | 2020-11-10 | 安徽顺达环保科技股份有限公司 | Desulfurization and dust removal process for ore smelting |
| CN110227328B (en) * | 2019-07-16 | 2022-05-27 | 湖北东方化工有限公司 | Nitric acid flue gas absorption treatment method with high recovery rate |
| CN111773850B (en) * | 2020-06-08 | 2021-10-29 | 河南科技学院 | Industrial waste gas treatment device |
| CN111715004B (en) * | 2020-06-16 | 2022-06-24 | 上海建工四建集团有限公司 | Method for purifying air with dust |
| CN114433365A (en) * | 2020-10-31 | 2022-05-06 | 中国石油化工股份有限公司 | Separation device and separation method for large-particle-size solids in oil sludge sand |
| CN116966724B (en) * | 2023-09-19 | 2023-12-12 | 山西诺成制药有限公司 | Solvent circulation type efficient absorption spray tower |
Citations (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| BE861495R (en) * | 1976-12-06 | 1978-03-31 | Soaf | IMPROVEMENTS TO LIQUID AERATION TURBINES |
| US4193949A (en) * | 1977-06-23 | 1980-03-18 | Makoto Naito | Apparatus for generating finely divided particulate bubbles |
| US5318360A (en) * | 1991-06-03 | 1994-06-07 | Stelzer Ruhrtechnik Gmbh | Gas dispersion stirrer with flow-inducing blades |
| CN2405925Y (en) * | 1999-12-10 | 2000-11-15 | 魏刚 | Eddy air-floating machine |
| CN2613482Y (en) * | 2003-04-03 | 2004-04-28 | 西安交通大学 | Aeration stirring device |
| CN1907869A (en) * | 2006-07-28 | 2007-02-07 | 沈福昌 | No pollution treatment technique for residue of refined terephthalic acid thin-film evaporator |
| CN101172216A (en) * | 2006-11-01 | 2008-05-07 | 中国石油化工股份有限公司 | Self-suction gas-liquid mixing impeller |
| CN101172217A (en) * | 2006-11-01 | 2008-05-07 | 中国石油化工股份有限公司 | Self-suction gas-liquid mixing impeller |
| CN201342344Y (en) * | 2008-12-02 | 2009-11-11 | 中昊晨光化工研究院 | Device for gas-liquid reactions/gas-liquid-solid reactions |
-
2010
- 2010-10-15 CN CN201010514314.5A patent/CN102451610B/en active Active
Patent Citations (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| BE861495R (en) * | 1976-12-06 | 1978-03-31 | Soaf | IMPROVEMENTS TO LIQUID AERATION TURBINES |
| US4193949A (en) * | 1977-06-23 | 1980-03-18 | Makoto Naito | Apparatus for generating finely divided particulate bubbles |
| US5318360A (en) * | 1991-06-03 | 1994-06-07 | Stelzer Ruhrtechnik Gmbh | Gas dispersion stirrer with flow-inducing blades |
| CN2405925Y (en) * | 1999-12-10 | 2000-11-15 | 魏刚 | Eddy air-floating machine |
| CN2613482Y (en) * | 2003-04-03 | 2004-04-28 | 西安交通大学 | Aeration stirring device |
| CN1907869A (en) * | 2006-07-28 | 2007-02-07 | 沈福昌 | No pollution treatment technique for residue of refined terephthalic acid thin-film evaporator |
| CN101172216A (en) * | 2006-11-01 | 2008-05-07 | 中国石油化工股份有限公司 | Self-suction gas-liquid mixing impeller |
| CN101172217A (en) * | 2006-11-01 | 2008-05-07 | 中国石油化工股份有限公司 | Self-suction gas-liquid mixing impeller |
| CN201342344Y (en) * | 2008-12-02 | 2009-11-11 | 中昊晨光化工研究院 | Device for gas-liquid reactions/gas-liquid-solid reactions |
Also Published As
| Publication number | Publication date |
|---|---|
| CN102451610A (en) | 2012-05-16 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN102451610B (en) | Treatment method for nitrogen oxide tail gas discharged from industrial production furnace, and apparatus thereof | |
| WO2016192273A1 (en) | Ozone-based flue gas treatment system and method | |
| CN102772986B (en) | Flue gas desulfurization and denitration integrated process | |
| CN106268270B (en) | Chain grate-rotary kiln denitration system | |
| CN102772990B (en) | Denitration process and device of gas-phase oxidation and wet-process absorption | |
| CN105080332A (en) | Resource utilization system for pellet sintering waste gas and method | |
| CN103111173A (en) | Flue gas purification system and method thereof | |
| CN103752151A (en) | Technology for flue gas denitration by magnesium sulfite | |
| JP2019531881A (en) | Flue gas denitration method | |
| CN105536467A (en) | Flue gas purification device and method combining photo-catalytic oxidization and double cyclic absorption | |
| CN105126567A (en) | Method and device for removing nitric oxide and sulfur oxide from gas flow | |
| US3574562A (en) | Apparatus for removal of sulfur dioxide from waste gases | |
| CN105833692B (en) | Industrial smoke dry type low temperature cooperates with dust-removal and desulfurizing denitration removal of mercury integrated apparatus and technique | |
| CN111318154A (en) | Integration low temperature denitrification facility | |
| CN208642272U (en) | A kind of high temperature desulfurizing denitration purification integrated device | |
| CN202844865U (en) | Denitration process system by high-temperature atomization wet method | |
| CN204768225U (en) | Hypergravity multiple -effect flue gas is retrieved and gas cleaning device | |
| CN102309916B (en) | Bead-collecting fogging desulfuration and dust collect tower | |
| CN211753815U (en) | Microwave-induced activated carbon adsorption steam desorption hydrogen sulfide removal device | |
| CN108114591A (en) | A kind of flue gas processing method | |
| CN104984651B (en) | Hypergravity multiple-effect off-gas recovery and flue gas purifying method and device | |
| CN204429082U (en) | Dust-removal and desulfurizing denitrification integrated device | |
| CN208145708U (en) | A kind of low-temperature dry active coke desulphurizing denitration collaboration integrated treatment unit | |
| CN110893314A (en) | Wet process low temperature deNOx systems | |
| CN207871902U (en) | A kind of flue gas processing device |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant |