CN103752151B - A kind of magnesium sulfite flue-gas denitration process - Google Patents
A kind of magnesium sulfite flue-gas denitration process Download PDFInfo
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- CN103752151B CN103752151B CN201310754094.7A CN201310754094A CN103752151B CN 103752151 B CN103752151 B CN 103752151B CN 201310754094 A CN201310754094 A CN 201310754094A CN 103752151 B CN103752151 B CN 103752151B
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- denitration
- magnesium sulfite
- absorption tower
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- ozone
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Abstract
The invention discloses a kind of magnesium sulfite flue-gas denitration process, comprise the steps: (1) boiler smoke through dust removal process laggard enter static mixer, simultaneously in static mixer, spray into ozone, ozone and smoke reaction obtain mist; (2) described mist is sent into denitration absorption tower bottom absorption tower, in the tower reactor on denitration absorption tower, add magnesium sulfite slurries, and magnesium sulfite slurries are squeezed into top, denitration absorption tower by circulating pump, carry out Sprayer Circulation absorption, carry out denitration to mist; (3) neat stress after denitration is discharged through chimney.The method that the present invention utilizes inferior sulfate radical to absorb, ensure that the denitration performance of integrated artistic maintains a higher level, realizes the high efficiency of the nitrogen oxide in flue gas.
Description
Technical field
The invention belongs to environmental protection technical field, relate to the treatment process of the flue gases such as coal-burning boiler, be specifically related to a kind of magnesium sulfite flue-gas denitration process.
Background technology
The selective catalytic reduction technique of main method (SCR), SNCR technology (SNCR), wet process complex absorption techniques, oxidation-absorption technology etc. of denitrating flue gas.SCR is method of denitration the most frequently used at present, although this technology denitration efficiency is high, infrastructure investment, operating cost are expensive.In addition, the bad adaptability of this technology centering, sulphur coal, the sulphur component in flue gas can reduce catalyst life, and the coal sulfur content that China produces is general higher.Therefore, from the national conditions that China is current, SCR technology is difficult to widely popularize at home.
In order to the gas denitrifying technology that exploiting economy is feasible, various oxidation-absorption denitration technology is suggested in succession.They utilize gas phase or liquid-phase oxidation by flue gas nitrogen oxide NO
xthe nitric oxide NO that middle solubility is less is oxidized to nitrogen dioxide NO
2, dinitrogen pentoxide N
2o
5deng, and then absorbed with the absorbing liquid of alkalescence, oxidisability or reproducibility.Compared with SCR technology, investment, the operating cost of oxidation-absorption denitration technology are lower, and denitration efficiency is high, better to the adaptability of coal, can be applicable to the boiler of various scale.
Publication number is that the Chinese invention patent description of CN1768902 individually discloses a kind of ozone oxidation and denitration method of boiler flue gas.Alkali lye as absorbent, is absorbed the nitrogen oxide through being to a certain degree oxidized by it, and main thought utilizes ozone O
3, liquid phase strong oxidizer or catalytic oxidation means are when being partly or entirely oxidized to nitrogen dioxide by nitric oxide, alkali lye is not high to the efficiency of nox adsorption; And when utilizing ozone nitric oxide to be all oxidized to dinitrogen pentoxide, denitration efficiency can be greatly improved, but due to the unstability of dinitrogen pentoxide, and ozone produces the Problems existing such as cost and ozone escape, therefore application is still subject to certain restrictions.
Publication number be 101053750 Chinese invention patent description disclose a kind of method of flue gas combined desulfurization and denitration, utilize photo catalysis reactor, under the effect of ultraviolet light and catalyst, the NO in flue gas is oxidized to NO
2, rear end utilizes Dual alkali absorption reactor thermally to absorb, and points out the Na in reaction product
2sO
3with the NO in flue gas
2reaction, can by NO
2be reduced to N
2discharge.But in this technique, photochemical catalytic oxidation NO technology is still immature, current application can be restricted, and the wear rate of inferior sulfate radical is very fast, according to the absorbent of sodium sulfite as commercial Application, the problem of high cost can be caused, by contrast, the cost of magnesium sulfite is lower, is adapted at promoting in commercial Application.
Summary of the invention
The invention provides a kind of magnesium sulfite flue-gas denitration process, utilize the method that inferior sulfate radical absorbs, ensure that the denitration performance of integrated artistic maintains a higher level, realize and the high efficiency of denitration simultaneously.
A kind of magnesium sulfite flue-gas denitration process, comprises the steps:
(1) boiler smoke through dust removal process laggard enter static mixer, simultaneously in static mixer, spray into ozone, ozone and smoke reaction obtain the mist after complete oxidation;
(2) described mist is sent into denitration absorption tower bottom absorption tower, in the tower reactor on denitration absorption tower, add magnesium sulfite slurries, and magnesium sulfite slurries are squeezed into top, denitration absorption tower by circulating pump, carry out Sprayer Circulation absorption, carry out denitration to mist;
(3) neat stress after denitration is discharged through chimney.
Realize denitrification apparatus of the present invention comprise connect successively boiler flue, deduster, denitration absorption tower and chimney, also comprise: be arranged on the static mixer between deduster and denitration absorption tower; The ozone generator be connected with described static mixer; The magnesium sulfite dosing chamber be communicated with described denitration absorption tower.
For the boiler smoke after dedusting, in static mixing device, spray into ozone, make flue gas and ozone Homogeneous phase mixing, the nitric oxide in flue gas is oxidized to easy absorbed high-valence state nitrogen oxide (comprising nitrogen dioxide and dinitrogen pentoxide etc.).Then flue gas is led to into denitration absorption tower, on the top on denitration absorption tower, adopt magnesium sulfite slurries to carry out spray-absorption.
Meanwhile, in the magnesium sulfite solution bottom denitration absorption tower, add oxidation retarder, the oxidizing process of inferior sulfate radical is suppressed, ensure that the inferior sulfate radical content in slurries maintains in the concentration needed for technique, thus obtain higher denitration efficiency.
The present invention is directed to the denitrating technique of boiler smoke, require that flue gas is through dust removal process, preferred control temperature 80-200 degree Celsius, dustiness is lower than 100mg/m
3.
As preferably, the mass concentration of described magnesium sulfite slurries is 1% ~ 15%, and further preferred concentration is 5% ~ 10%.
As preferably, the liquid-gas ratio in described absorption tower is 1-30L/m
3, more preferably 3 ~ 10L/m
3, be more preferably 5L/m
3; PH scope is 3 ~ 11, and more preferably, pH is 4 ~ 5, most preferably is 5.
As preferably, the addition of ozone is 0.5 ~ 2.5 times of NO mole coefficient, and being more preferably is 1.1 ~ 1.2, most preferably is 1.2.
Most preferably, the mass concentration of described magnesium sulfite slurries is 10%, and the liquid-gas ratio in described absorption tower is 5L/m
3, pH value is 5, and the addition of ozone is 1.2 times of NO mole coefficient, and absorption tower is spray absorber, and the spray number of plies in tower is 6 layers.
As preferably, in described magnesium sulfite slurries, also add oxidation retarder.
As preferably, described oxidation retarder is at least one in sodium sulfite, sodium pyrosulfite, dibutylphenol, sodium hydrogensulfite, sodium thiosulfate and butylated hydroxyarisol.
Further preferably, in described magnesium sulfite slurries, the concentration of oxidation retarder is 2 ~ 10000ppm.
As preferably, described static mixer is venturi mixer, grating type blender or spiral-flow plate-type blender.
As preferably, the main tower on described denitration absorption tower is spray column or packed tower.When selecting spray absorber, the spray number of plies in spray absorber is 3 ~ 6 layers.
Most preferably, specifically process successively by following processing step:
1) in magnesium sulfite dosing chamber, configure required magnesium sulfite slurries and pass into denitration absorption tower, the solid concentration of magnesium sulfite slurries is 1% ~ 15%;
2) boiler exhaust gas is after dedusting, enters denitration absorption tower from bottom, sprays in tower by circulating pump by the magnesium sulfite slurries at the bottom of tower from top;
3) ozone from ozone generator blasts static mixer by blower fan, after mixing, directly enters denitration absorption tower with flue gas;
4) in the bottom slurry on denitration absorption tower, oxidation retarder is added;
5) controlling liquid-gas ratio is 1-30L/m
3, pH scope is 4 ~ 11, and purifying smoke is discharged by chimney.
Present invention process has following technique effect: for the boiler smoke that nitrogen oxide in tail gas content is higher, provide a kind of denitrating technique based on wet absorption technology, compared to general wet absorption denitrating technique, this technique has higher absorption efficiency for nitrogen oxide, and absorption product is nitrogen, can realize the harmless treatment of absorption product.
Accompanying drawing explanation
Fig. 1 is apparatus of the present invention structural representations.
Shown in figure, Reference numeral is as follows:
1-coal-burning boiler 2-boiler flue 3-deduster
4-static mixer 5-ozone generator 6-denitration absorption tower
7-circulating pump 8-chimney 9-magnesium sulfite dosing chamber.
Detailed description of the invention
As shown in Figure 1, a kind of flue gas processing device of magnesium sulfite denitration, comprises deduster, static mixer, absorption tower and chimney.
Coal-burning boiler 1 is connected to deduster 3 by flue, deduster 3 is connected to static mixer 4, ozone generator 5 is connected to this static mixer 4, static mixer 4 connects the smoke inlet on absorption tower 6 by flue, absorption tower is wet absorption tower, be specially spray absorber in this example, the spray number of plies in spray absorber is 3 ~ 6 layers, realizes by circulating pump 7 circulated sprinkling absorbing slurries in absorption tower.
Arrange magnesium sulfite dosing chamber 9 outside absorption tower 6, magnesium sulfite dosing chamber 9 is communicated with the tower reactor in absorption tower 6; Top, absorption tower 6 is with exhanst gas outlet, and exhanst gas outlet connects chimney 8 by flue.
Static mixer adopts in venturi mixer, grating type blender or spiral-flow plate-type blender a kind of.
Technological process of the present invention is as follows:
1) in magnesium sulfite dosing chamber, configure required magnesium sulfite slurries and pass into denitration absorption tower, the solid concentration of magnesium sulfite slurries is 1% ~ 15%;
2) boiler exhaust gas is after dedusting, enters denitration absorption tower from bottom, sprays in tower by circulating pump by the magnesia slurry at the bottom of tower from top;
3) ozone from ozone generator blasts static mixer by blower fan, after mixing, directly enters denitration absorption tower with flue gas;
4) in the bottom slurry on denitration absorption tower, oxidation retarder is added;
5) controlling liquid-gas ratio is 1-30L/m
3, pH scope is 4 ~ 11, and purifying smoke is discharged by chimney
Embodiment 1
By device of the present invention and technique, at 5m
3the experimental simulation device of/h scale is simulated denitrating flue gas process.Exhaust gas volumn 5m
3/ h, flue gas composition is as follows: O
2be 5%, NO be 200ppm, all the other are nitrogen, flue-gas temperature 150 degrees Celsius, pressure 1 atmospheric pressure.
Employing spray equipment absorbs, and the spray number of plies is six layers, and liquid-gas ratio is 5L/m
3, pH controls 5.Adopt 10% gypsum slurries to absorb, then denitration rate is 10 ~ 15%.If by ozone according to mol ratio O
3: the ratio of NO=1.1 sprays into, and after abundant mixed oxidization, the oxygenation efficiency of exit NO can reach 90%, rear employing 5%MgSO
3slurries absorb, and add the Na of 0.1%
2s
2o
3as oxidation retarder, denitration efficiency can reach more than 85%.
Embodiment 2
By device of the present invention and technique, at 5m
3the experimental simulation device of/h scale is simulated denitrating flue gas process.Exhaust gas volumn 5m
3/ h, flue gas composition is as follows: O
2be 10%, NO be 230ppm, all the other are nitrogen, flue-gas temperature 100 degrees Celsius, pressure 1 atmospheric pressure.Employing spray equipment absorbs, and the spray number of plies is six layers, and liquid-gas ratio is 5L/m
3, pH controls 5.Ozone is according to mol ratio O
3: the ratio of NO=1.2 sprays into, and the oxygenation efficiency of exit NO can reach 95%.Absorb according to 10% gypsum slurries, then denitration rate is 40%; According to 5%MgSO
3slurries absorb, and add the Na of 0.5%
2s
2o
3as oxidation retarder, denitration efficiency can reach more than 85%.
Embodiment 3
By device of the present invention and technique, flue gas flow is 6000Nm
3/ h, flue gas composition is as follows: O
2be 9%, NO be 250ppm, all the other are nitrogen, flue-gas temperature 100 degrees Celsius, pressure 1 atmospheric pressure.Employing spray equipment absorbs, and the spray number of plies is six layers, and liquid-gas ratio is 5L/m
3, pH controls 6.Ozone is according to mol ratio O
3: the ratio of NO=1.2 sprays into, and the oxygenation efficiency of exit NO can reach 95%, and absorb according to 10% gypsum slurries, then denitration rate is 45%; According to 10%MgSO
3slurries absorb, and add the dibutylphenol of 0.5% as oxidation retarder, denitration efficiency can reach more than 85%.
Embodiment 4
By device of the present invention and technique, flue gas flow is 4500Nm
3/ h, flue gas composition is as follows: O
2be 8%, NO be 350ppm, all the other are nitrogen, flue-gas temperature 120 degrees Celsius, pressure 1 atmospheric pressure.Employing spray equipment absorbs, and the spray number of plies is six layers, and liquid-gas ratio is 5L/m
3, pH controls 7.Ozone is according to mol ratio O
3: the ratio of NO=1.2 sprays into, and the oxygenation efficiency of exit NO can reach 95%, and absorb according to 10% gypsum slurries, then denitration rate is 45%; According to 10%MgSO
3slurries absorb, and add the Na of 0.5%
2s
2o
3as oxidation retarder, in conjunction with spray-absorption device, denitration efficiency can reach more than 85%.
Embodiment 5
By device of the present invention and technique, flue gas flow is 4500Nm
3/ h, flue gas composition is as follows: O
2be 10%, NO be 150ppm, all the other are nitrogen, flue-gas temperature 120 degrees Celsius, pressure 1 atmospheric pressure.Employing spray equipment absorbs, and the spray number of plies is four layers, and liquid-gas ratio is 5L/m
3, pH controls 6.Ozone is according to mol ratio O
3: the ratio of NO=1.2 sprays into, and the oxygenation efficiency of exit NO can reach 95%, and absorb according to 10% gypsum slurries, then denitration rate is 45%; According to 10%MgSO
3slurries absorb, and add the Na of 0.4%
2s
2o
3as oxidation retarder, in conjunction with spray-absorption device, denitration efficiency can reach more than 80%.
Claims (4)
1. a magnesium sulfite flue-gas denitration process, is characterized in that, comprises the steps:
(1) boiler smoke through dust removal process laggard enter static mixer, simultaneously in static mixer, spray into ozone, ozone and smoke reaction obtain the mist after complete oxidation;
(2) described mist is sent into denitration absorption tower bottom out of stock absorption tower, magnesium sulfite slurries are added in the tower reactor on denitration absorption tower, magnesium sulfite slurries are squeezed into top, denitration absorption tower by circulating pump, carry out Sprayer Circulation absorption, carry out denitration to mist;
(3) neat stress after denitration is discharged through chimney;
The mass concentration of described magnesium sulfite slurries is 1% ~ 15%; Also oxidation retarder is added in described magnesium sulfite slurries;
Described oxidation retarder is at least one in dibutylphenol and butylated hydroxyarisol;
In described magnesium sulfite slurries, the concentration of oxidation retarder is 2 ~ 10000ppm.
2. magnesium sulfite flue-gas denitration process according to claim 1, it is characterized in that, the liquid-gas ratio in described absorption tower is 1-30L/m
3, pH scope is 4 ~ 11.
3. magnesium sulfite flue-gas denitration process according to claim 1, it is characterized in that, the addition of ozone is 0.5 ~ 2.5 times of NO mole coefficient.
4. magnesium sulfite flue-gas denitration process according to claim 1, it is characterized in that, described static mixer is venturi mixer, grating type blender or spiral-flow plate-type blender.
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|---|---|---|---|
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| CN201310754094.7A CN103752151B (en) | 2013-12-31 | 2013-12-31 | A kind of magnesium sulfite flue-gas denitration process |
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| CN103752151B true CN103752151B (en) | 2016-01-06 |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108970351A (en) * | 2018-06-19 | 2018-12-11 | 山东师范大学 | A kind of flue gas low-temperature denitration method |
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| CN104888591B (en) * | 2015-06-04 | 2017-01-25 | 南京龙源环保有限公司 | Boiler flue gas denitration purification system and boiler flue gas denitration purification method |
| GB2545760A (en) * | 2015-12-21 | 2017-06-28 | Linde Ag | Methods for removing contaminants from gas streams |
| US10065151B2 (en) | 2015-12-21 | 2018-09-04 | Linde Aktiengesellschaft | Methods for removing contaminants from gas streams |
| CN106474898A (en) * | 2016-11-22 | 2017-03-08 | 凯天环保科技股份有限公司 | A kind of low-temperature denitration and the method and system of nitrogen Sulphur ressourceization utilization |
| CN109092017B (en) * | 2018-09-19 | 2021-11-26 | 上海交通大学 | Method for controlling generation of nitrate in absorption liquid by flue gas oxidation denitration |
| CN109224820A (en) * | 2018-11-12 | 2019-01-18 | 实友化工（扬州）有限公司 | A kind of ozone oxidation and denitration method of boiler flue gas |
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| CN111995213A (en) * | 2020-07-16 | 2020-11-27 | 株洲时代新材料科技股份有限公司 | Sludge treatment process |
| CN114289072A (en) * | 2022-01-11 | 2022-04-08 | 云南民族大学 | Preparation method and application of magnesium sulfite catalytic oxidant |
Citations (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP0301272A2 (en) * | 1987-07-29 | 1989-02-01 | Waagner-Biro Aktiengesellschaft | Process and device for purifying off-gas or waste gas |
| WO1999022847A1 (en) * | 1997-10-30 | 1999-05-14 | Alliedsignal Inc. | Process for abating nitrogen oxide emissions from a manufacturing stream |
| WO2006113997A1 (en) * | 2005-04-27 | 2006-11-02 | Clean World Strategies Corp. | A process for removal of pollutants |
| CN1990089A (en) * | 2005-12-28 | 2007-07-04 | 浙江大学 | Wet process complex denitration technique enhancing Fe*EDTA by using sulfite reducing agent |
| CN101254932A (en) * | 2007-02-28 | 2008-09-03 | 张家港市新中环保设备有限公司 | Technique for preparing magnesium sulfite during magnesium method desulfurization process |
| CN101352645A (en) * | 2008-08-29 | 2009-01-28 | 浙江大学 | Flue gas catalytic oxidation denitration technique and catalyst thereof |
| CN101879404A (en) * | 2010-07-12 | 2010-11-10 | 华东理工大学 | Recycled flue gas desulfurization and denitration method |
| CN102716648A (en) * | 2012-05-16 | 2012-10-10 | 北京航空航天大学 | Method for automatically controlling desulphurization and denitration by flue gas based on pH value and ORP value and apparatus thereof |
| CN202823136U (en) * | 2012-08-02 | 2013-03-27 | 浙江天蓝环保技术股份有限公司 | Denitration device combining gas phase oxidation and wet method absorption |
| CN103212281A (en) * | 2013-03-29 | 2013-07-24 | 江苏中显集团有限公司 | Smoke desulfurization and denitrification integration method and special device thereof |
-
2013
- 2013-12-31 CN CN201310754094.7A patent/CN103752151B/en not_active Expired - Fee Related
Patent Citations (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP0301272A2 (en) * | 1987-07-29 | 1989-02-01 | Waagner-Biro Aktiengesellschaft | Process and device for purifying off-gas or waste gas |
| WO1999022847A1 (en) * | 1997-10-30 | 1999-05-14 | Alliedsignal Inc. | Process for abating nitrogen oxide emissions from a manufacturing stream |
| WO2006113997A1 (en) * | 2005-04-27 | 2006-11-02 | Clean World Strategies Corp. | A process for removal of pollutants |
| CN1990089A (en) * | 2005-12-28 | 2007-07-04 | 浙江大学 | Wet process complex denitration technique enhancing Fe*EDTA by using sulfite reducing agent |
| CN101254932A (en) * | 2007-02-28 | 2008-09-03 | 张家港市新中环保设备有限公司 | Technique for preparing magnesium sulfite during magnesium method desulfurization process |
| CN101352645A (en) * | 2008-08-29 | 2009-01-28 | 浙江大学 | Flue gas catalytic oxidation denitration technique and catalyst thereof |
| CN101879404A (en) * | 2010-07-12 | 2010-11-10 | 华东理工大学 | Recycled flue gas desulfurization and denitration method |
| CN102716648A (en) * | 2012-05-16 | 2012-10-10 | 北京航空航天大学 | Method for automatically controlling desulphurization and denitration by flue gas based on pH value and ORP value and apparatus thereof |
| CN202823136U (en) * | 2012-08-02 | 2013-03-27 | 浙江天蓝环保技术股份有限公司 | Denitration device combining gas phase oxidation and wet method absorption |
| CN103212281A (en) * | 2013-03-29 | 2013-07-24 | 江苏中显集团有限公司 | Smoke desulfurization and denitrification integration method and special device thereof |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108970351A (en) * | 2018-06-19 | 2018-12-11 | 山东师范大学 | A kind of flue gas low-temperature denitration method |
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