CN103920384A - Equipment for absorbing high-concentration nitric oxides by adopting normal-pressure process - Google Patents
Equipment for absorbing high-concentration nitric oxides by adopting normal-pressure process Download PDFInfo
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- CN103920384A CN103920384A CN201410169295.5A CN201410169295A CN103920384A CN 103920384 A CN103920384 A CN 103920384A CN 201410169295 A CN201410169295 A CN 201410169295A CN 103920384 A CN103920384 A CN 103920384A
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Abstract
The invention relates to equipment for absorbing high-concentration nitric oxides by adopting a normal-pressure process. The equipment comprises a first-level absorption tower, a second-level absorption tower and a third-level absorption tower, wherein the top of each absorption tower is connected with an air inlet pipeline and an absorption liquid inlet pipe; an air inlet pipeline of the first-level absorption tower is connected with a treated air source; an air inlet pipeline of the second-level absorption tower is connected with the first-level absorption tower; an air inlet pipeline of the third-level absorption tower is connected with the second-level absorption tower; the absorption liquid inlet pipes of the first-level absorption tower and the second-level absorption tower are connected with an acid liquor storage tank; the absorption liquid inlet pipe of the third-level absorption tower is connected with an alkaline liquor storage tank; a liquid pump is arranged on each absorption liquid inlet pipe; a tower bottom liquid return pipe connected with a corresponding storage tank is arranged at the bottom of each absorption tower; a water cooler is arranged on the tower bottom liquid return pipe. According to the equipment, nitric oxides can be converted into nitric acid and potassium nitrate through second-level acid absorption and first-level acid absorption, and tail gas reaches the national emission standard. The absorption tower adopts a jet absorption form, gas and liquid enter from the top of the tower, the structure is simple, the process flow is short, and wide-range variable working condition requirements are met.
Description
Technical field
The present invention relates to the equipment that a kind of non-pressure process absorbs high concentration nitrogen oxide, nitrogen oxide is absorbed into nitric acid with diluted acid with hydrogen peroxide oxidation, tail gas reaches discharging standards.
Background technology
In nitric acid industry, often can run into high concentration nitrogen oxide (NO
x) the processing problem of tail gas, the discharge of nitrogen oxide, there is strict standard in country, and the processing of high concentration nitrogen oxide, difficulty is very large, and cost is higher.The nitrogen oxide exhaust gas treating method using both at home and abroad is at present divided into dry method and the large class of wet method two.Dry method is taking catalytic reduction as main, under high temperature, with reducing agent by NO
xcatalytic reduction is N
2deng gas, purely from environmental angle, handling object is low concentration of NO
x, for higher concentration NO
x, poor effect, and can not recycle NO
x, can be by NO and absorb
xbe converted into HNO
3, concerning nitric acid industry, economic implications is much larger than dry method.Absorption is the one of wet method, and absorption process makes water, acid or aqueous slkali absorbing NOx, is converted into nitric acid or nitrate.Be absorbed with non-pressure process, synthesis, middle-pressure process, high-pressure process and double pressurized method, the main double pressurized method that adopts at present, other method seldom adopts, because process NO in rear tail gas
xconcentration is higher.Be absorbed in countercurrent absorber and complete, industrial general employing multistage absorption.The net reaction of water absorbing NOx is:
3NO
2?+?H
2O?=?2HNO
3?+?NO?+?Q?(1)
2NO?+?O
2?=?2NO
2?+?Q?(2)
NO?+?NO
2?+?Na
2CO
3?=?2NaNO
2?+?CO
2?(3)
NO
2?+?Na
2CO
3?=?NaNO
3?+?NaNO
2?+?CO
2?(4)
Known 1 mol NO by reaction equation (1), (2)
2become 1/3 mol NO of difficult absorption, make NO absorb, must again be oxidized to NO
2, again absorb, through being repeatedly oxidized absorption, just can reach emission request, in this process, NO
2absorption reaction and the oxidation reaction of NO intersect and carry out, process is very complicated.
The absorption process of nitrogen oxide, also has acid to absorb and alkali absorbs.There are some researches show NO
2while absorption in rare nitric acid, the oxidation of NO is mainly carried out in gas liquid film and liquid phase, the oxidation of NO is a slow process, low temperature and pressurization are conducive to the carrying out of oxidation reaction, therefore adopt at present double pressurized methods more, but the rising of pressure must make equipment cost and operating cost increase, and energy consumption increases; And current normal pressure absorption technique tail gas concentration is higher, seldom adopt.Reduce and absorb temperature, can increase the oxidation rate of NO, improve oxidizability, be beneficial to absorption, make device structure complexity but remove reaction heat.
Current absorption process all adopts the integrated processes that multistage acid absorbs and multistage alkali absorbs, after acid absorbs, there are a large amount of NO to generate, after dry oxidation, the oxidizability of NO is increased to 40%, enter again alkali absorption level, generate nitrite and nitrate, as reaction equation (3), (4), nitrite is strong carcinogen, discharge standard is 0.5 ppm, and the content of nitrite generating in alkali absorbs is higher, the follow-up difficult problem that will run into processing nitrite.
Summary of the invention
The technical problem to be solved in the present invention is the equipment that a kind of non-pressure process of exploitation absorbs high concentration nitrogen oxide; This equipment is atmospheric circulating absorption equipment, at room temperature high concentration nitrogen oxide can be converted into nitric acid, and tail gas reaches discharging standards, and nitric acid nitrite is lower than 0.5ppm, not containing other secondary pollution.
Non-pressure process absorbs an equipment for high concentration nitrogen oxide, it is characterized in that: comprise first grade absorption tower, two-level absorption tower and three grades of absorption towers; Top, absorption tower at different levels is connected with air inlet pipeline and absorption liquid feed tube, the air inlet pipeline of first grade absorption tower connects processed source of the gas, two-level absorption tower air inlet pipeline is connected with first grade absorption tower, three grades of absorption tower air inlet pipelines are connected with two-level absorption tower, the absorption liquid feed tube of one-level, two-level absorption tower connects acid solution storage tank, the absorption liquid feed tube on three grades of absorption towers connects alkali lye storage tank, on each absorption liquid feed tube, liquid pump is installed, bottom, absorption tower at different levels is provided with the tower bottoms recovery tube being connected with corresponding storage tank, on tower bottoms recovery tube, water cooler is installed.
The structure on three absorption towers is identical, it is a kind of jetting type normal pressure absorption tower, comprise tower body, it is characterized in that: tower body top is installed into tracheae and feed tube, liquid distribution trough is installed on tower body top, feed tube outlet is connected with liquid distribution trough, between tower body top and liquid distribution trough, be provided with admission space, packed tower is installed in liquid distribution trough below, space below packed tower is as gas-liquid separator, blast pipe is installed on gas-liquid separator top, and gas-liquid separator outside is provided with liquid level gauge, and gas-liquid separator bottom installs back closed tube.
Non-pressure process of the present invention absorbs the equipment of high concentration nitrogen oxide, and development process is mainly to start with from the following technical issues that need to address:
The one, the selection of absorbing medium, can be in liquid phase Quick Oxidation NO, improve as much as possible oxidizability, make it change as soon as possible NO into
2, make tail gas up to standard with the least possible absorption level;
The 2nd, the structural design on absorption tower, make NO in absorption tower, have enough time of staying, completes oxidation and absorbs, and Liquid Flow form is the key of dealing with problems.
The 3rd, remove the method for heat, the absorption of high concentration nitrogen oxide, there is very large reaction heat to emit, absorption liquid temperature exceedes more than 35 DEG C, assimilation effect is very poor, how removing in time reaction heat is the technical barrier absorbing, and will solve the problem of heat exchange mode, makes absorption equipment structure simple as far as possible.The corresponding scheme that solves above-mentioned three point problem is:
One, absorbing medium
With rare nitric acid and hydrogen peroxide (H
2o
2) as absorbing medium, NO, under the co-oxidation of rare nitric acid and hydrogen peroxide, is converted into rapidly NO in liquid phase
2, as reaction equation (5), reaction speed is fast, and degree of oxidation is high, and being repeatedly oxidized in absorption, the content decay of NO is very fast, just can reach very high degree of absorption with the less order of reaction, after the absorption of hydrogen peroxide acid solution, NO in tail gas
xcontent very low, become KNO with KOH alkali liquor absorption
3with micro-KNO
2, as reaction equation (6), (7), KNO
2by H
2o
2be oxidized to KNO
3, as reaction equation (8).KNO in final absorption liquid
2content is very low, can reach below 0.5ppm.
NO?+?H
2O
2?=?NO
2?+?H
2O?(5)
2NO
2?+2?KOH?=?KNO
3?+?KNO
2?+?H
2O?(6)
NO?+?NO
2?+?2KOH?=?2KNO
2?+?H
2O?(7)
KNO
2?+?H
2O
2?=?KNO
3?+?H
2O?(8)
Two, absorption tower structure
Absorption tower adopts jet to absorb pattern, does not adopt gas, the liquid countercurrent that prior art generally adopts to enter tower.But gas, liquid all enter from top, absorption tower, between tower body top and liquid distribution trough, be provided with admission space, tower top is equipped with liquid distribution trough, absorption liquid from distributor spray and, form jet, produce certain negative pressure, gas can be sucked in tower, even if air pressure is lower, also can overcome packing layer resistance, pass through smoothly packing layer.Gas, from tower top enters, impacts liquid and makes the liquid atomization, and produces spray effect, can effectively promote gas-liquid contact degree, reaches the object of abundant mass transfer.Adopt packed tower, filling ceramic ring filler in tower, to reduce resistance and liquid holdup.Jet and packing layer can make gas-liquid be uniformly distributed along tower section, and the possibility that produces axial short circuit is little, and gas-liquid contact is abundant, and gas is from tower top to tower reactor, and gas circuit is long, long at dwell time in the tower, and NO has the sufficient time to be oxidized to NO
2, gas-liquid is during to tower reactor, in liquid, contained NO amount seldom, is easily overflowed from tower reactor liquid, realizes gas-liquid separation in tower reactor, even in still liquid containing NO, also can be by H
2o
2continue oxidation; And when prior art counter-current absorption, first gas-liquid contacts in tower reactor, carries a large amount of NO in still liquid, when still liquid is discharged, NO can be expelled to absorption liquid storage tank with still liquid, on-the-spot a large amount of acid mists and the tobacco of producing.Absorption tower employing jet absorption pattern of the present invention, jet absorbs and can adapt to the operating mode that liquid-gas ratio, air pressure and flow constantly change, energy intermittence and continued operation, operating flexibility is more much bigger than adverse current, even if large liquid measure is not prone to liquid flooding and leakage yet.Tower reactor is as gas-liquid separator, and tail gas separates from tower reactor with absorption liquid, and tail gas enters after the further precipitation of liquid droplets of cyclone hydraulic separators, enters next stage absorption tower.The certain liquid level of tower reactor control, to realize fluid-tight.
Three, cooling method
Jet absorbs, the initial contact interface of gas-liquid is at tower top packing layer, tower top reaction is the most violent, and heat release is maximum, adopts large liquid spray flux, can take away fast reaction heat, effectively reduce absorption liquid temperature, do not need to arrange cooling device in tower, absorption tower is simple in structure, the water cooler arranging in tower reactor drain line is cooling to absorption liquid, circulates in order to absorption liquid.
Absorption tower of the present invention has adopted jet to absorb pattern, and gas-liquid is uniformly distributed along tower section with the form of spraying, and mass transfer is abundant, and gas residence time is long, and NO has time enough oxidation to absorb.Adopt the mode of large liquid spray flux and cooling reactor liquid to remove absorption heat, absorption liquid temperature is down to below 30 DEG C, absorption tower is simple in structure, and flow process is short, and operating flexibility is large, adapts to variable working condition requirement on a large scale completely.The present invention can be converted into high concentration nitrogen oxide in higher concentration nitric acid, realizes waste reclamation, and tail gas and tail washings can reach discharging standards, environmental protection cost is low, and device structure is simple, and technological process is simple, operating cost is low, and economic benefit and social benefit are obvious.
Brief description of the drawings
Fig. 1 is structural representation of the present invention,
Fig. 2 is absorption tower structural representation.
In figure: 1-acid solution storage tank, 2-H
2o
2storage tank, 3-one-level absorbs liquid pump, 4-one-level absorption liquid feed tube, be called for short feed tube, 5-one-level absorption liquid electromagnetic flowmeter, 6-one-level absorption liquid control valve, 7-first grade absorption tower, 701-air inlet pipe, 702-liquid distribution trough feed liquor supervisor, 703-admission space, 704-pressure type liquid distribution trough, 705-tower body, 706-packing layer, 707-tower reactor, also claim gas-liquid separator, 708-cyclone hydraulic separators, 709-supporting leg, 710-packing support plate, 711-hold-down grid, 8-one-level liquid level gauge, 9-one-level still liquid switch valve, 10-one-level tower bottoms recovery tube, be called for short recovery tube, 11-N
2o
4waste gas source of the gas, 12-waste gas orifice flowmeter, 13-one-level air inlet adjustment valve, 14-one-level offgas duct, also be two-level absorption tower air inlet pipeline, 15-two-level absorption tower, 16-secondary absorbs liquid pump, 17-secondary absorption liquid feed tube, 18-secondary tower bottoms recovery tube, 19-secondary offgas duct, also be three grades of absorption tower air inlet pipelines, 20-three grades of absorption towers, 21-alkali lye storage tank, 22-three grades of absorption liquid pumps, 23-three grades of absorption liquid feed tubes, 24-three grades of tower bottoms recovery tubes, 25-join alkali case, 26-three grades of offgas duct, 27-acid solution discharge line, 28-alkali lye discharge line, 29-one-level water cooler, 30-two-stage water-cooling is device but, 31-tertiary effluent cooler.
Detailed description of the invention
Below in conjunction with accompanying drawing, device structure of the present invention is described in further detail.Non-pressure process absorbs an equipment for high concentration nitrogen oxide, comprises first grade absorption tower 7, two-level absorption tower 15 and three grades of absorption towers 20; Top, absorption tower at different levels is connected with air inlet pipeline and absorption liquid feed tube; Be that first grade absorption tower 7 tops are provided with one-level air inlet pipeline and one-level absorption liquid feed tube 4, it is that secondary air inlet pipe 14 and 20 tops, 17, three grades of absorption towers of secondary absorption liquid feed tube are provided with i.e. three grades of air inlet pipe 19 and the three grades of absorption liquid feed tubes 23 of secondary offgas duct that are connected with two-level absorption tower that two-level absorption tower 15 tops are provided with one-level offgas duct; One-level air inlet pipeline and processed N
2o
4waste gas source of the gas 11 connects, and two-level absorption tower air inlet pipeline 14 is connected with first grade absorption tower 7, and three grades of absorption tower air inlet pipelines 19 are connected with two-level absorption tower 15; Three grades of absorption towers 20 are provided with 26 outlets of 26, three grades of offgas duct of three grades of offgas duct and are directly communicated with atmosphere.
One-level absorption liquid feed tube 4 is connected 1, three grade of absorption liquid feed tube 23 of acid solution storage tank and connects alkali lye storage tank 21 with secondary absorption liquid feed tube 17; On each absorption liquid feed tube, liquid pump is installed, one-level absorption liquid feed tube 4 is installed one-level absorption liquid pump 3, and secondary absorption liquid feed tube 17 is installed 16, three grades of absorption liquid feed tubes 23 of secondary absorption liquid pump three grades of absorption liquid pumps 22 are installed; Bottom, absorption tower at different levels is provided with the tower bottoms recovery tube being connected with corresponding storage tank, on tower bottoms recovery tube, water cooler is installed, be that first grade absorption tower 7 bottoms are provided with the one-level tower bottoms return duct 10 being connected with acid solution storage tank 1, two-level absorption tower 15 is provided with 18, the three grades of absorption towers 20 of secondary tower bottoms return duct that are connected with acid solution storage tank 1 and is provided with three grades of tower bottoms return ducts 24 that are connected with alkali lye storage tank 21; On one-level tower bottoms return duct 10, one-level water cooler 29 is installed, two-stage water-cooling is installed on secondary tower bottoms return duct 18 and but on 30, three grades of tower bottoms return ducts 24 of device, tertiary effluent cooler 31 is installed.
One-level air inlet pipeline is provided with waste gas orifice flowmeter 12 and one-level air inlet adjustment valve 13, is respectively used to measure charge flow rate and regulates charge flow rate; One-level absorbs on the liquid outlet end, one-level absorption liquid feed tube 4 of liquid pump 3 installs one-level absorption liquid electromagnetic flowmeter 5 and one-level absorption liquid control valve 6 successively, is respectively used to measure feed liquor flow and regulates feed liquor flow; One-level still liquid switch valve 9 is installed on one-level tower bottoms return duct 10, and one-level liquid level gauge 8 is electrically connected with one-level still liquid switch valve 9, and in the time that liquid level reaches setting value, one-level still liquid switch valve 9 is opened automatically; Acid solution storage tank 1 is connected with H
2o
2storage tank 2, acid solution discharge line 27 is installed in acid solution storage tank 1 bottom, and alkali lye storage tank 21 is connected with joins alkali case 25, and alkali lye discharge line 28 is installed in alkali lye storage tank 21 bottoms.
When non-pressure process absorbs the equipment of high concentration nitrogen oxide and is used for absorbing high concentration nitrogen oxide, method roughly: taking weight percent concentration as 3%～5% rare nitric acid and 0.1%～2% hydrogen peroxide as main absorption liquid, be placed in acid solution storage tank; With the auxiliary absorption liquid of 16% potassium hydroxide, be placed in alkali lye storage tank; Under normal pressure, under intermittence and continuous operation mode, by concentration 40% ~ 60% (mol%), flow 100 ~ 400 Nm
3/ h, the dinitrogen tetroxide of pressure 0.01 ~ 0.2MPa is or/and nitrogen dioxide gas enters first grade absorption tower, and one-level tail gas enters two-level absorption tower, and secondary tail gas enters three grades of absorption towers again, and three grades of tail gas reach discharge standard and pass through high altitude discharge; Realize dinitrogen tetroxide or/and nitrogen dioxide gas absorbs through secondary acid absorption and one-level alkali, be converted into potassium nitrate, tail gas concentration reaches 100 mg/m
3discharging standards, absorption liquid nitrite is lower than the discharging standards of 0.5 ppm, containing other secondary pollution.
The structure on three absorption towers is identical, be jetting type normal pressure absorption tower, this implementation method is described the structure on jetting type normal pressure absorption tower as an example of first grade absorption tower example: a kind of jetting type normal pressure absorption tower, comprise tower body 705, tower body 705 tops are installed into tracheae 701 and liquid distribution trough feed liquor supervisor 702, liquid distribution trough 704 is installed on tower body 705 tops, feed tube 4 outlets are connected with liquid distribution trough feed liquor supervisor 702, liquid distribution trough feed liquor is responsible for 702 ports of export and is connected liquid distribution trough 704, between tower body 705 tops and liquid distribution trough 704, be provided with admission space 703, packing layer 706 is installed in liquid distribution trough 704 belows, packing layer 706 space is below as gas-liquid separator 707, blast pipe 14 is installed on gas-liquid separator 707 tops, gas-liquid separator 707 outsides are provided with liquid level gauge 8, gas-liquid separator 707 bottoms arrange return duct 10.Blast pipe 14 is connected to cyclone hydraulic separators 708.Tower body 705 bottoms are fixedly connected with supporting leg 709.
Packing layer 706 comprises packing support plate 710 and hold-down grid 711, filler be arranged on packing support plate 710 and and hold-down grid 711 between, filler is selected Dg50 pottery Pall ring.
Oxides of nitrogen gas enters tower head from air inlet pipe, and absorption liquid enters liquid distribution trough from tower head feed tube, and liquid distribution trough is a kind of pressure type comb, absorption liquid can be uniformly distributed on tower body cross section.Tower head is the space of air inlet and feed liquor, and gas-liquid in the contact of tower head part, then enters packing layer at first, and gas-liquid completes oxidation and absorbs in packing layer.Tower reactor is the space of gas-liquid separation, and unabsorbed tail gas, after tower reactor separates, is discharged from blast pipe, enter cyclone hydraulic separators, further separate the drop in tail gas, absorption liquid flows out from return duct, after water cooler is cooling, flow into absorption liquid storage tank, so that circulation absorbs.The liquid level gauge that tower reactor is installed, is convenient to measure control liquid level.
Claims (8)
1. non-pressure process absorbs an equipment for high concentration nitrogen oxide, it is characterized in that: comprise first grade absorption tower (7), two-level absorption tower (15) and three grades of absorption towers (20); First grade absorption tower (7) top is provided with one-level air inlet pipeline and one-level absorption liquid feed tube (4), two-level absorption tower (15) top is provided with one-level offgas duct (14) and secondary absorption liquid feed tube (17), and top, three grades of absorption towers (20) is provided with the secondary offgas duct (19) and the three grades of absorption liquid feed tubes (23) that are connected with two-level absorption tower; One-level air inlet pipeline and processed N
2o
4waste gas source of the gas (11) connects, and two-level absorption tower air inlet pipeline (14) is connected with first grade absorption tower (7), and three grades of absorption tower air inlet pipelines (19) are connected with two-level absorption tower (15); Three grades of absorption towers (20) are provided with three grades of offgas duct (26), and three grades of offgas duct (26) outlet is directly communicated with atmosphere.
2. a kind of non-pressure process as claimed in claim 1 absorbs the equipment of high concentration nitrogen oxide, it is characterized in that: one-level absorption liquid feed tube (4) is connected acid solution storage tank (1) with secondary absorption liquid feed tube (17), three grades of absorption liquid feed tubes (23) connect alkali lye storage tank (21); One-level absorption liquid feed tube (4) is installed one-level and is absorbed liquid pump (3), and secondary absorption liquid feed tube (17) is installed secondary and absorbed liquid pump (16), and secondary absorption liquid feed tube (23) is installed three grades of absorption liquid pumps (22); First grade absorption tower (7) bottom is provided with the one-level tower bottoms recovery tube (10) being connected with acid solution storage tank (1), two-level absorption tower (15) is provided with the secondary tower bottoms recovery tube (18) being connected with acid solution storage tank (1), and three grades of absorption towers (20) are provided with the three grades of tower bottoms recovery tubes (24) that are connected with alkali lye storage tank (21); One-level water cooler (29) is installed on one-level tower bottoms recovery tube (10), but device (30) of two-stage water-cooling is installed on secondary tower bottoms recovery tube (18), tertiary effluent cooler (31) is installed on three grades of tower bottoms recovery tubes (24).
3. a kind of non-pressure process as described in claim 1,2 or 3 absorbs the equipment of high concentration nitrogen oxide, it is characterized in that: one-level air inlet pipeline is provided with waste gas orifice flowmeter (12) and one-level air inlet adjustment valve (13), one-level absorbs on the liquid outlet end, one-level absorption liquid feed tube (4) of liquid pump (3) installs one-level absorption liquid electromagnetic flowmeter (5) and one-level absorption liquid control valve (6) successively.
4. a kind of non-pressure process as claimed in claim 3 absorbs the equipment of high concentration nitrogen oxide, it is characterized in that: the upper one-level still liquid switch valve (9) of installing of one-level tower bottoms return duct (10), and one-level liquid level gauge (8) is connected with one-level still liquid switch valve (9); Acid solution storage tank (1) is connected with H
2o
2storage tank (2), acid solution discharge line (27) is installed in acid solution storage tank (1) bottom, and alkali lye storage tank (21) is connected with joins alkali case (25), and alkali lye discharge line (28) is installed in alkali lye storage tank (21) bottom.
5. a jetting type normal pressure absorption tower, comprise tower body 705, it is characterized in that: tower body (705) top is installed into tracheae (701) and liquid distribution trough feed liquor supervisor (702), liquid distribution trough (704) is installed on tower body (705) top, feed tube (4) outlet is connected with liquid distribution trough feed liquor supervisor (702), liquid distribution trough feed liquor supervisor (702) port of export connects liquid distribution trough (704), between tower body (705) top and liquid distribution trough (704), be provided with admission space (703), packing layer (706) is installed in liquid distribution trough (704) below, packing layer (706) space is below as gas-liquid separator (707), blast pipe (14) is installed on gas-liquid separator (707) top, gas-liquid separator (707) outside is provided with liquid level gauge (8), return duct (10) is installed in gas-liquid separator (707) bottom.
6. a kind of jetting type normal pressure as claimed in claim 5 absorption tower, is characterized in that: blast pipe (14) is installed cyclone hydraulic separators (708).
7. a kind of jetting type normal pressure as claimed in claim 6 absorption tower, is characterized in that: packing layer (706) comprises packing support plate (710) and hold-down grid (711), between packing support plate (710) and hold-down grid (711), filler is installed.
8. a kind of jetting type normal pressure as claimed in claim 7 absorption tower, is characterized in that: filler is selected Dg50 pottery Pall ring.
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| CN108014617A (en) * | 2017-11-12 | 2018-05-11 | 安徽金禾实业股份有限公司 | A kind of method and device of the dense nitre tail gas of low temperature ammonia reduction treatment |
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Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1333079A (en) * | 2001-02-28 | 2002-01-30 | 天津大学 | Nox containing tail gas processing technology and tower equipment for production of oxalic acid by nitric acid oxidation method |
| CN101036851A (en) * | 2007-02-09 | 2007-09-19 | 中北大学 | Method and apparatus for processing waste air including oxynitride |
| CN201023022Y (en) * | 2007-04-23 | 2008-02-20 | 谢建中 | Device for making dilute nitric acid with nitrogen oxide adsorption |
| WO2010036436A1 (en) * | 2008-09-26 | 2010-04-01 | Neumann Systems Group, Inc. | Gas liquid contactor and effluent cleaning system and method |
| CN102266714A (en) * | 2011-06-29 | 2011-12-07 | 天津大学 | Method for desorbing acidic gas by oxidization process |
| CN102407068A (en) * | 2010-09-25 | 2012-04-11 | 潍坊信誉环境工程有限公司 | Acidic water solution for absorbing NOx and method for purifying NOx-containing waste gas by applying same |
| CN102974200A (en) * | 2012-12-05 | 2013-03-20 | 寿光富康制药有限公司 | Oxynitride waste gas treatment device and oxynitride waste gas treatment method |
-
2014
- 2014-04-25 CN CN201410169295.5A patent/CN103920384B/en not_active Expired - Fee Related
Patent Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1333079A (en) * | 2001-02-28 | 2002-01-30 | 天津大学 | Nox containing tail gas processing technology and tower equipment for production of oxalic acid by nitric acid oxidation method |
| CN101036851A (en) * | 2007-02-09 | 2007-09-19 | 中北大学 | Method and apparatus for processing waste air including oxynitride |
| CN201023022Y (en) * | 2007-04-23 | 2008-02-20 | 谢建中 | Device for making dilute nitric acid with nitrogen oxide adsorption |
| WO2010036436A1 (en) * | 2008-09-26 | 2010-04-01 | Neumann Systems Group, Inc. | Gas liquid contactor and effluent cleaning system and method |
| CN102407068A (en) * | 2010-09-25 | 2012-04-11 | 潍坊信誉环境工程有限公司 | Acidic water solution for absorbing NOx and method for purifying NOx-containing waste gas by applying same |
| CN102266714A (en) * | 2011-06-29 | 2011-12-07 | 天津大学 | Method for desorbing acidic gas by oxidization process |
| CN102974200A (en) * | 2012-12-05 | 2013-03-20 | 寿光富康制药有限公司 | Oxynitride waste gas treatment device and oxynitride waste gas treatment method |
Non-Patent Citations (1)
| Title |
|---|
| 谈华应: "新型高效气体吸收器的开发与应用", 《淀粉与淀粉糖》 * |
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