CN103285717A - Simultaneous desulfurization and denitrification method using aqueous ammonia - Google Patents
Simultaneous desulfurization and denitrification method using aqueous ammonia Download PDFInfo
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- CN103285717A CN103285717A CN2012100525142A CN201210052514A CN103285717A CN 103285717 A CN103285717 A CN 103285717A CN 2012100525142 A CN2012100525142 A CN 2012100525142A CN 201210052514 A CN201210052514 A CN 201210052514A CN 103285717 A CN103285717 A CN 103285717A
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- tower
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- flue gas
- desulfurization
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
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Abstract
The invention relates to a method for simultaneously removing sulfur oxides and nitrogen oxides in flue gas by using aqueous ammonia. According to the method, the (NH4)2SO3, which is obtained from a desulfurization reaction for absorbing SO2 by aqueous ammonia, is used as an absorption solution for a denitrification reaction; and the (NH4)2SO3 has reducibility for reducing NOx in the flue gas to N2 to achieve the denitrification purpose. The method provided by the invention comprises the following steps that: the flue gas firstly enters into a denitrification spraying layer of a contraction segment in a venturi tower and is subjected to a downstream contact reaction with a circulating liquid from an oxidation pond on the tower bottom, an aqueous ammonia spraying layer is arranged at the throat part of the venturi tower to carry out the desulfurization reaction, the concentration of the (NH4)2SO3 is instantly increased due to the desulfurization reaction, the denitrification reaction is further carried out, the liquid after reaction and the flue gas transversely enter into the middle lower part of a cylindrical tower along the lower part of the venturi tower, the liquid flows downwards to the bottom of the cylindrical tower, the flue gas moves upwards after passing through a tower plate and is countercurrent contact with the circulating liquid to further generate a desulfurization reaction and a denitrification reaction, fine liquid drops and aerosol of the purified flue gas are captured when the purified flue gas passes through the water spraying layer and a folded plate type defroster, the purified flue gas is then directly exhausted from a direct exhaust chimney connected to the tower top, and simultaneously, a by-product of the system is ammonium sulfate, which is a raw material of an agricultural nitrogenous fertilizer or a compound fertilizer.
Description
Technical field
The present invention relates to a kind ofly remove SO in the flue gas with ammoniacal liquor
2, NOx method, belong to the flue gases purification field.
Background technology
SOx, NOx are the main sources of atmosphere pollution, have caused huge harm to environment.Along with the increasingly stringent of national environmental protection rules, in conjunction with existing flue gas treatment technology, develop a kind of reliable, investment operating cost lower flue gas desulfurization, denitrating technique and tally with the national condition, have application promise in clinical practice.
At present, the flue gas desulfurization technique comparative maturity, wet processing occuping market share maximum wherein, technical process is simple, desulfurized effect good, adoptable absorbent is also a lot; But the still selective catalytic reduction (SCR) of flue-gas denitration process overwhelming majority employing at present, this method utilizes ammonia under the effect of catalyst NOx to be reduced to N as reducing agent
2, process system and equipment more complicated, the catalyst dependence on import, price is very expensive.
Summary of the invention
The invention provides and a kind ofly remove SO in the flue gas with ammoniacal liquor
2, NOx method, this method technological process is simple, workable, the investment and economic operating cost.
Characteristics of the present invention are that flue gas need not to carry out heat exchange and enters in the tower, under higher temperature, and SO
2Can with ammoniacal liquor NH
3H
2The O reaction generates (NH
4)
2SO
3, (NH
4)
2SO
3React as the NOx in reducing agent and the flue gas.Its chemical principle is:
1, high temperature desulfurizing reaction: SO
2+ 2NH
3H
2O=(NH
4)
2SO
3+ H
2O (a)
2, denitration reaction: 2 (NH
4)
2SO
3+ 2NOx=2x (NH
4)
2SO
4+ N
2(b)
Method of the present invention realizes that in the desulphurization denitration tower described desulphurization denitration tower is " U " type structure that venturi tower, cylinder tower two towers communicate.Venturi tower is terminal to be connected with cylinder tower middle and lower part, and venturi tower arranges the denitration desulfurization section, and the cylinder tower is provided with desulphurization denitration section, anti-section and the demist section of escaping of washing.
Flue gas at first enters venturi tower, under 100 ℃～150 ℃ temperature conditions NOx with from tower at the bottom of (NH in the circulation fluid of oxidation pond
4)
2SO
3Reduction reaction takes place by chemical equation (b) in contact, and the ammoniacal liquor with ammonia spray layer spray contacts afterwards, and desulphurization reaction takes place fast (a) by chemical equation, generates (NH
4)
2SO
3, make (NH
4)
2SO
3Concentration moment change is conducive to the further generation of denitration reaction greatly.
Reacted flue gas carry liquid along the venturi tower bottom 90 ° of bends through cylinder tower middle and lower part, liquid flows into downwards at the bottom of the cylinder tower, flue gas is uniform upwards operation behind column plate, desulphurization denitration further takes place under 80 ℃～100 ℃ conditions of temperature with from the circulation fluid counter current contacting in tower outer circulation pond, the pH value control in tower outer circulation pond is beneficial to the generation of desulfurization and denitrification reaction between 5.5～6.5.
After flue gas after being purified rises gas by the riser column plate, after water spraying layer and folded plate type demister are removed fine drop and aerosol, by the in line smoke stack emission of cat head.
Doctor solution enters tower outer circulation pond through the oxidation aeration, after filtering at the bottom of by tower, advances evaporation and concentration in the tower, returns tower and carries out crystallization outward, enters ammonium sulfate dry packing system after the cyclone separator Separation of Solid and Liquid, prepares the ammonium sulfate that meets the agrochemical standard.
Description of drawings
Fig. 1 is process flow diagram of the present invention
The specific embodiment
As shown in Figure 1, flue gas need not heat exchange, under 100 ℃～150 ℃ conditions of higher temperature, at first enter venturi tower (1), venturi tower (1) arranges denitration spraying layer (2), ammonia spray layer (3) respectively by the flue gas inflow direction, the denitration spraying layer is connected with oxidation pond (5) at the bottom of cylinder tower (4) tower by thin liquid circulating pump (6), and 2 (NH take place denitration spraying layer (2)
4)
2SO
3+ 2NOx=2x (NH
4)
2SO
4+ N
2Denitration reaction, SO takes place in the ammoniacal liquor of the flue gas after the denitration and ammonia spray layer (3)
2+ 2NH
3H
2O=(NH
4)
2SO
3+ H
2The desulphurization reaction of O makes (NH in the liquid phase
4)
2SO
3Concentration moment increase is conducive to 2 (NH
4)
2SO
3+ 2NOx=2x (NH
4)
2SO
4+ N
2Denitration reaction further takes place in the carrying out of reaction.Flue gas after the denitration desulfurization is entered by cylinder tower (4) middle and lower part, behind column plate (7) upwards with the circulation fluid counter current contacting of spraying layer (10) spray, the described desulfurization and denitrification reaction of above-mentioned reaction equation further takes place, spraying layer (10) solution is collected through column plate (7) and is entered tower outer circulation pond (8), enter spraying layer (10) from pipeline separately respectively by two dope circulating pumps (9), have 1 bye-pass to be connected with oxidation pond at the bottom of the tower (5) by valve on column plate (7) outlet line.Dope circulating pump (9) outlet line is provided with ammoniacal liquor and replenishes mouth, and the ammoniacal liquor that replenishes advances spraying layer (10) spray.Flue gas after being purified rises gas by water spraying layer (14) by riser column plate (11) and two-layer folded plate type demister (15) is removed fine drop and aerosol discharges by in line chimney (17).Water lotion flows back to recirculated water jar (12) certainly from major loop, pressurize by booster water pump (13), part water lotion water inlet spraying layer (14), part water lotion carries out spray Cleaning for High Capacity to folded plate type demister (15) in demist shower (16) enters cylinder tower (4), another part water lotion advances venturi tower (1) and carries out spray in the tower; Another branch road of water lotion is by valve oxidation pond (5) at the bottom of flowing to tower.Oxidation pond at the bottom of the tower (5) liquid is discharged at the bottom of by cylinder tower (4) tower, enters dust treatment system (18) processing such as separation of dewatering; Solution is after filtering used at the bottom of pumped back cylinder tower (4) tower again, and the oxidation wind with oxidation fan (21) stirs oxidation to solution in the tower, and the clean liquid part after the filtration is sent tower outer circulation pond (8) fluid infusion to.When reaching, tower outer circulation pond (8) solution concentration extracts when requiring, be evacuated to cyclone separator by the pump of sulphur ammonium extraction system (19) and carry out Separation of Solid and Liquid, liquid returns tower outer circulation pond (8), and the crystalline particle thing of separation enters dry packing fortune system (20), prepares ammonium sulfate product.
Claims (9)
1. the method for ammoniacal liquor desulfurization denitration simultaneously, it is characterized in that: this method realizes that in the desulphurization denitration tower desulphurization denitration was divided equally for two steps and carried out.Described desulphurization denitration tower is " U " type structure that venturi tower (1), cylinder tower (4) two towers communicate, and venturi tower (1) is established denitration, desulfurization section, and denitration is main; Cylinder tower (4) is established denitration, desulfurization section, and desulfurization is main; Cylinder tower (4) top set up defences escape, demist section.Flue gas enters venturi tower (1), with denitration spraying layer (2), the denitration desulphurization reaction takes place in the spray liquid contact of ammonia spray layer (3), oxidation pond (5) was connected at the bottom of denitration spraying layer (2) passed through the tower of thin liquid circulating pump (6) bottom cylinder tower (4), reacted flue gas is entered by cylinder tower (4) middle and lower part, behind column plate (7) upwards with the circulation fluid counter current contacting of spraying layer (10) spray desulfurization and denitrification reaction takes place further, spraying layer (10) solution is collected by column plate (7) and is refluxed into tower outer circulation pond (8) from major loop, and another branch road is by valve oxidation pond (5) at the bottom of flowing to tower; Flue gas after being purified is discharged by in line chimney (17) after being risen gas and removed fine drop and aerosol by water spraying layer (14) and two-layer folded plate type demister (15) by riser column plate (11); Water lotion flows back to recirculated water jar (12) certainly from major loop, pressurize by booster water pump (13), part water lotion water inlet spraying layer (14), part water lotion carries out spray Cleaning for High Capacity to folded plate type demister (15) in demist shower (16) enters cylinder tower (4), another part water lotion advances venturi tower (1) and carries out spray in the tower; Another branch road of water lotion is by valve oxidation pond (5) at the bottom of flowing to tower.Oxidation pond at the bottom of the tower (5) liquid is discharged at the bottom of by tower, enters dust treatment system (18) processing such as separation of dewatering; The pumped back tower bottom of solution after filtering stirs oxidation with the oxidation wind of oxidation fan (21) to solution in the tower, and the clean liquid part after the filtration is sent tower outer circulation pond (8) fluid infusion to.Tower outer circulation pond (8) solution concentration reaches to be extracted when requiring, be evacuated to cyclone separator by the pump of sulphur ammonium extraction system (19) and carry out Separation of Solid and Liquid, liquid goes back to tower outer circulation pond (8), and the crystalline particle thing enters dry packing system (20), prepares the product that meets agrochemical ammonium sulfate standard.
2. desulphurization denitration tower according to claim 1 is characterized in that: venturi tower (1) is terminal to be connected with cylinder tower (4) middle and lower part, and venturi tower (1) is provided with the denitration desulfurization section, and cylinder tower (4) is provided with desulphurization denitration section, anti-escape section and demist section.
3. cylinder tower according to claim 1 (4), it is characterized in that: be provided with a layer column plate (7) and riser column plate (11) in the tower, be used for collecting spray liquid, inject tower outer circulation pond (8) and circulation water pot (12) respectively, and all have branch road to be connected with oxidation pond at the bottom of the tower (5) by by-pass valve control.
4. the method for a kind of ammoniacal liquor desulfurization according to claim 1 denitration simultaneously, it is characterized in that: venturi tower (1) desulphurization denitration section reaction temperature is 150 ℃～100 ℃.
5. the method for a kind of ammoniacal liquor desulfurization according to claim 1 denitration simultaneously, it is characterized in that: cylinder tower (4) denitration desulfurization section reaction temperature is 70 ℃～100 ℃.
6. the method for a kind of ammoniacal liquor desulfurization according to claim 1 denitration simultaneously, it is characterized in that: venturi tower (1) is U-shaped fabricated structure with cylinder tower (4).
7. the method for a kind of ammoniacal liquor desulfurization according to claim 1 denitration simultaneously, it is characterized in that: oxidation pond at the bottom of the tower (5) pH value scope is controlled between 5.0～6.0, and tower outer circulation pond (8) pH value scope is controlled between 5.5～6.5.
8. the method for a kind of ammoniacal liquor desulfurization according to claim 1 denitration simultaneously, it is characterized in that: the control of ammonium sulfate concentration range is less than 15% in the oxidation pond at the bottom of the tower (5), and the concentration of tower outer circulation pond (8) ammonium sulfate is controlled between 25%～35%.
9. the method for a kind of ammoniacal liquor desulfurization according to claim 1 denitration simultaneously is characterized in that: water spraying layer (14) is for two-layer, be located at respectively riser column plate (11) about, lower floor's demist is held concurrently and is replenished system for desulfuration and denitration loss water.
Priority Applications (1)
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|---|---|---|---|
| CN2012100525142A CN103285717A (en) | 2012-03-02 | 2012-03-02 | Simultaneous desulfurization and denitrification method using aqueous ammonia |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2012100525142A CN103285717A (en) | 2012-03-02 | 2012-03-02 | Simultaneous desulfurization and denitrification method using aqueous ammonia |
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| Publication Number | Publication Date |
|---|---|
| CN103285717A true CN103285717A (en) | 2013-09-11 |
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ID=49087560
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|---|---|---|---|
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Cited By (17)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104061580A (en) * | 2014-06-16 | 2014-09-24 | 河南心连心化肥有限公司 | Ammonia desulphurization device for treating flue gas desulphurization and process thereof |
| CN104437051A (en) * | 2014-11-17 | 2015-03-25 | 傅明冲 | Wet desulphurization and denitrification system and method |
| CN105597534A (en) * | 2016-03-17 | 2016-05-25 | 盐城东博环保科技有限公司 | Device and method for ammonia process-outer-tower oxidation desulfurization and denitrification |
| CN106178904A (en) * | 2016-09-09 | 2016-12-07 | 成都九十度工业产品设计有限公司 | A kind of emission-control equipment and waste gas processing method |
| CN106334427A (en) * | 2015-07-13 | 2017-01-18 | 中国石化工程建设有限公司 | Ammonia method flue gas dedusting-desulphurization-denitration integrated purification system and method |
| CN106334426A (en) * | 2015-07-13 | 2017-01-18 | 中国石化工程建设有限公司 | Ammonia method flue gas dedusting-desulphurization-denitration integrated purification system and method |
| CN106345248A (en) * | 2015-07-13 | 2017-01-25 | 中国石化工程建设有限公司 | Ammonia process fume dust collection desulfurization and denitrification integral purification system and method |
| CN108686492A (en) * | 2017-04-12 | 2018-10-23 | 中国石油化工股份有限公司 | Flue-gas dust-removing and desulfurization tower and dust-collecting sulfur-removing method |
| CN108686491A (en) * | 2017-04-12 | 2018-10-23 | 中国石油化工股份有限公司 | A kind of flue-gas dust-removing and desulfurization tower and dust-collecting sulfur-removing method |
| CN111151106A (en) * | 2018-11-07 | 2020-05-15 | 洛阳德明石化设备有限公司 | System for improving gas-liquid separation effect of WGS (WGS) desulfurizing tower and application of system |
| CN111924808A (en) * | 2020-09-09 | 2020-11-13 | 胡光雄 | Equipment for concentrating high-temperature flue gas waste acid in titanium dioxide production by sulfuric acid method and use method |
| CN112044245A (en) * | 2020-09-24 | 2020-12-08 | 浙江大学 | Sectional temperature self-adaptive accurate regulation and control reinforced SO2Absorption-oxidation ship tail gas purification device and process |
| CN115055034A (en) * | 2022-07-26 | 2022-09-16 | 北京清新环境技术股份有限公司 | Semi-dry treatment method and system for flue gas purification |
| CN115055035A (en) * | 2022-07-26 | 2022-09-16 | 北京清新环境技术股份有限公司 | Semi-dry treatment method and system for flue gas desulfurization and denitrification |
| CN115350548A (en) * | 2022-08-25 | 2022-11-18 | 广东兴荣环保科技有限公司 | Dust removal and odor removal device for dust-containing waste gas and treatment method |
| CN117357999A (en) * | 2023-12-04 | 2024-01-09 | 长春黄金研究院有限公司 | Instantaneous high-concentration nitrogen oxide flue gas treatment method |
| CN117398812A (en) * | 2023-12-15 | 2024-01-16 | 万华化学集团股份有限公司 | Quenching absorption method for aromatic hydrocarbon ammoxidation reaction gas |
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| CN201578985U (en) * | 2010-01-29 | 2010-09-15 | 东南大学 | Double-shaft collision flow smoke gas synchronous desulfuration and denitration device |
| CN102188889A (en) * | 2011-04-14 | 2011-09-21 | 中国环境科学研究院 | Device and method for combined removal of sulphur dioxide (SO2), nitrogen oxide (NOX) and mercury from fume |
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| CN201578985U (en) * | 2010-01-29 | 2010-09-15 | 东南大学 | Double-shaft collision flow smoke gas synchronous desulfuration and denitration device |
| CN101785965A (en) * | 2010-03-02 | 2010-07-28 | 浙江菲达环保科技股份有限公司 | Complex absorption cycle semi-dry desulfurization and denitrification integral process and device |
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Cited By (21)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104061580A (en) * | 2014-06-16 | 2014-09-24 | 河南心连心化肥有限公司 | Ammonia desulphurization device for treating flue gas desulphurization and process thereof |
| CN104061580B (en) * | 2014-06-16 | 2016-11-23 | 河南心连心化肥有限公司 | Process ammonia desulfuration equipment and the technique thereof of flue gas desulfurization band liquid |
| CN104437051A (en) * | 2014-11-17 | 2015-03-25 | 傅明冲 | Wet desulphurization and denitrification system and method |
| CN104437051B (en) * | 2014-11-17 | 2017-06-20 | 傅明冲 | A kind of wet desulphurization denitrating system and method |
| CN106334427A (en) * | 2015-07-13 | 2017-01-18 | 中国石化工程建设有限公司 | Ammonia method flue gas dedusting-desulphurization-denitration integrated purification system and method |
| CN106334426A (en) * | 2015-07-13 | 2017-01-18 | 中国石化工程建设有限公司 | Ammonia method flue gas dedusting-desulphurization-denitration integrated purification system and method |
| CN106345248A (en) * | 2015-07-13 | 2017-01-25 | 中国石化工程建设有限公司 | Ammonia process fume dust collection desulfurization and denitrification integral purification system and method |
| CN105597534A (en) * | 2016-03-17 | 2016-05-25 | 盐城东博环保科技有限公司 | Device and method for ammonia process-outer-tower oxidation desulfurization and denitrification |
| CN106178904A (en) * | 2016-09-09 | 2016-12-07 | 成都九十度工业产品设计有限公司 | A kind of emission-control equipment and waste gas processing method |
| CN108686491A (en) * | 2017-04-12 | 2018-10-23 | 中国石油化工股份有限公司 | A kind of flue-gas dust-removing and desulfurization tower and dust-collecting sulfur-removing method |
| CN108686492A (en) * | 2017-04-12 | 2018-10-23 | 中国石油化工股份有限公司 | Flue-gas dust-removing and desulfurization tower and dust-collecting sulfur-removing method |
| CN111151106A (en) * | 2018-11-07 | 2020-05-15 | 洛阳德明石化设备有限公司 | System for improving gas-liquid separation effect of WGS (WGS) desulfurizing tower and application of system |
| CN111924808A (en) * | 2020-09-09 | 2020-11-13 | 胡光雄 | Equipment for concentrating high-temperature flue gas waste acid in titanium dioxide production by sulfuric acid method and use method |
| CN112044245A (en) * | 2020-09-24 | 2020-12-08 | 浙江大学 | Sectional temperature self-adaptive accurate regulation and control reinforced SO2Absorption-oxidation ship tail gas purification device and process |
| CN115055034A (en) * | 2022-07-26 | 2022-09-16 | 北京清新环境技术股份有限公司 | Semi-dry treatment method and system for flue gas purification |
| CN115055035A (en) * | 2022-07-26 | 2022-09-16 | 北京清新环境技术股份有限公司 | Semi-dry treatment method and system for flue gas desulfurization and denitrification |
| CN115350548A (en) * | 2022-08-25 | 2022-11-18 | 广东兴荣环保科技有限公司 | Dust removal and odor removal device for dust-containing waste gas and treatment method |
| CN117357999A (en) * | 2023-12-04 | 2024-01-09 | 长春黄金研究院有限公司 | Instantaneous high-concentration nitrogen oxide flue gas treatment method |
| CN117357999B (en) * | 2023-12-04 | 2024-03-01 | 长春黄金研究院有限公司 | Instantaneous high-concentration nitrogen oxide flue gas treatment method |
| CN117398812A (en) * | 2023-12-15 | 2024-01-16 | 万华化学集团股份有限公司 | Quenching absorption method for aromatic hydrocarbon ammoxidation reaction gas |
| CN117398812B (en) * | 2023-12-15 | 2024-02-13 | 万华化学集团股份有限公司 | Quenching absorption method for aromatic hydrocarbon ammoxidation reaction gas |
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Application publication date: 20130911 |