CN1883767A - Process for realizing medium temperature dry-method direct denitration of flue gas by using ethanol - Google Patents
Process for realizing medium temperature dry-method direct denitration of flue gas by using ethanol Download PDFInfo
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- CN1883767A CN1883767A CN 200610026665 CN200610026665A CN1883767A CN 1883767 A CN1883767 A CN 1883767A CN 200610026665 CN200610026665 CN 200610026665 CN 200610026665 A CN200610026665 A CN 200610026665A CN 1883767 A CN1883767 A CN 1883767A
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- flue gas
- ethanol
- denitration
- flue
- nitric oxide
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- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 title claims abstract description 79
- 239000003546 flue gas Substances 0.000 title claims abstract description 73
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 title claims abstract description 72
- 238000000034 method Methods 0.000 title claims abstract description 32
- MWUXSHHQAYIFBG-UHFFFAOYSA-N Nitric oxide Chemical compound O=[N] MWUXSHHQAYIFBG-UHFFFAOYSA-N 0.000 claims abstract description 40
- 238000002485 combustion reaction Methods 0.000 claims abstract description 27
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims abstract description 18
- 239000000446 fuel Substances 0.000 claims abstract description 17
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims abstract description 9
- 229910052757 nitrogen Inorganic materials 0.000 claims abstract description 9
- 239000001301 oxygen Substances 0.000 claims abstract description 9
- 229910052760 oxygen Inorganic materials 0.000 claims abstract description 9
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 claims abstract description 6
- 229910002092 carbon dioxide Inorganic materials 0.000 claims abstract description 3
- 239000001569 carbon dioxide Substances 0.000 claims abstract description 3
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Chemical compound O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 3
- 238000006243 chemical reaction Methods 0.000 claims description 10
- 239000003517 fume Substances 0.000 claims description 4
- 239000002028 Biomass Substances 0.000 claims 1
- 239000002803 fossil fuel Substances 0.000 claims 1
- 238000005516 engineering process Methods 0.000 abstract description 22
- 239000003054 catalyst Substances 0.000 abstract description 4
- 239000006227 byproduct Substances 0.000 abstract description 2
- 230000007613 environmental effect Effects 0.000 abstract description 2
- 238000000926 separation method Methods 0.000 abstract description 2
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 description 9
- 238000010531 catalytic reduction reaction Methods 0.000 description 8
- 239000007789 gas Substances 0.000 description 7
- MHAJPDPJQMAIIY-UHFFFAOYSA-N Hydrogen peroxide Chemical compound OO MHAJPDPJQMAIIY-UHFFFAOYSA-N 0.000 description 6
- 239000000654 additive Substances 0.000 description 5
- 230000000996 additive effect Effects 0.000 description 5
- 239000000126 substance Substances 0.000 description 5
- MGWGWNFMUOTEHG-UHFFFAOYSA-N 4-(3,5-dimethylphenyl)-1,3-thiazol-2-amine Chemical compound CC1=CC(C)=CC(C=2N=C(N)SC=2)=C1 MGWGWNFMUOTEHG-UHFFFAOYSA-N 0.000 description 3
- XSQUKJJJFZCRTK-UHFFFAOYSA-N Urea Chemical compound NC(N)=O XSQUKJJJFZCRTK-UHFFFAOYSA-N 0.000 description 3
- 235000011114 ammonium hydroxide Nutrition 0.000 description 3
- 239000004202 carbamide Substances 0.000 description 3
- JCXJVPUVTGWSNB-UHFFFAOYSA-N nitrogen dioxide Inorganic materials O=[N]=O JCXJVPUVTGWSNB-UHFFFAOYSA-N 0.000 description 3
- PRORZGWHZXZQMV-UHFFFAOYSA-N azane;nitric acid Chemical compound N.O[N+]([O-])=O PRORZGWHZXZQMV-UHFFFAOYSA-N 0.000 description 2
- 238000004140 cleaning Methods 0.000 description 2
- 238000006477 desulfuration reaction Methods 0.000 description 2
- 230000023556 desulfurization Effects 0.000 description 2
- 238000002347 injection Methods 0.000 description 2
- 239000007924 injection Substances 0.000 description 2
- 239000007921 spray Substances 0.000 description 2
- 235000009470 Theobroma cacao Nutrition 0.000 description 1
- 244000240602 cacao Species 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000009826 distribution Methods 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 229910052739 hydrogen Inorganic materials 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 239000000047 product Substances 0.000 description 1
- 230000005855 radiation Effects 0.000 description 1
- 238000006722 reduction reaction Methods 0.000 description 1
- 239000000243 solution Substances 0.000 description 1
- 239000002341 toxic gas Substances 0.000 description 1
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Abstract
一种环保技术领域的利用乙醇实现烟气中温干法直接脱硝的方法。本发明利用乙醇与烟气中的一氧化氮、氧气发生化学反应生成氮气、水蒸汽和二氧化碳从而实现烟气干法直接脱硝，乙醇射入时，烟气温度为750℃－1100℃。本发明的优点在于：第一、射入燃料燃烧过程结束后烟气中温区域的乙醇直接与烟气中的一氧化氮反应生成氮气。第二、由于乙醇被射入燃烧设备中烟气温度为中温区域的烟道内与烟气中的一氧化氮直接迅速反应而生成氮气，因此不需另外布置脱硝反应器、脱硝副产物分离装置及催化剂，具有实施容易的特点。第三、由于是在燃料燃烧过程完成后的烟气中温区域通过乙醇实现烟气干法直接脱硝，因此不受具体燃烧设备和燃料特性限制，有着广阔的应用前景。
The invention relates to a method in the field of environmental protection technology for realizing direct denitrification of flue gas by using ethanol at medium temperature and dry method. The invention uses ethanol to react with nitric oxide and oxygen in flue gas to generate nitrogen, water vapor and carbon dioxide to realize direct denitrification of flue gas by dry method. When ethanol is injected, the flue gas temperature is 750°C-1100°C. The advantages of the present invention are as follows: firstly, the ethanol injected into the middle-temperature area of the flue gas after the fuel combustion process is completed directly reacts with the nitric oxide in the flue gas to generate nitrogen. Second, since ethanol is injected into the flue of the combustion equipment where the temperature of the flue gas is in the middle temperature area, it reacts directly and rapidly with the nitric oxide in the flue gas to generate nitrogen, so there is no need to arrange additional denitrification reactors, denitrification by-product separation devices and Catalyst has the characteristics of easy implementation. Third, since the flue gas dry method directly denitrates the flue gas through ethanol in the middle-temperature area of the flue gas after the completion of the fuel combustion process, it is not limited by specific combustion equipment and fuel characteristics, and has broad application prospects.
Description
Technical field
The present invention relates to the method for environmental technology field, specifically is a kind of method of utilizing ethanol to realize the direct denitration of warm dry method in the flue gas.
Background technology
In the fuel combustion process, owing to itself contain the nitrogen element, the high temperature of combustion process contains high concentration nitric oxide toxic gas in the gas of feasible burning back in addition, and environment is polluted.In the existing dry fume denitration technology, mainly comprise the air classification combustion technology taked in the high-temp combustion process, fuel staging combustion technology and SNCR technology again, afterbody low-temperature selective catalytic reduction and non-selective catalytic-reduction denitrified technology after combustion process finishes.Outside the deacration fractional combustion denitration technology, fuel staging denitration by refueling technology, SNCR denitration technology, selective-catalytic-reduction denitrified technology and non-selective catalytic-reduction denitrified technology all need the denitration additive.Wherein, fuel staging denitration by refueling technology is to add the denitration additive in high temperature reduction atmosphere zone, the SNCR denitration technology is to add the denitration additive in fuel high temperature after-flame zone, selective-catalytic-reduction denitrified technology and non-selective catalytic-reduction denitrified technology are that the lower temperature region after fuel combustion finishes adds the denitration additive, realize the denitration purpose of flue gas in high temperature and lower temperature region.Can realize the direct denitration of dry method at the middle temperature area between the low temperature after high temperature in combustion process and the burning end, it is a difficult problem to be solved always, because the high temperature denitration in the combustion process always contradicts with the raising efficiency of combustion, low-temperature selective catalytic reduction and special denitrification apparatus and the catalyst of non-selective catalytic-reduction denitrified Technology Need after burning finishes, investment and operating cost height.The direct denitration of warm dry method in the flue gas both can solve the contradiction of fuel combustion and denitrating flue gas, did not need special denitrification apparatus and catalyst again.
Find by prior art documents, Chinese patent application number: CN03125332.6, patent name is: the dry method flue gas cleaning technology and the system thereof of while desulphurization denitration, this patent readme is: the dry method flue gas cleaning technology and the system thereof that the invention discloses a kind of while desulphurization denitration, disclosed flue-gas denitration process is for adopting hydrogen peroxide or methyl alcohol as additive, it is ejected into the temperature that gives off from combustion apparatus is 350～700 ℃ of flue gases, make nitric oxide gas and hydrogen peroxide or methyl alcohol generation chemical reaction generation nitrogen dioxide gas in the flue gas, adopt ammoniacal liquor or urea as denitrfying agent, it is ejected into carries out denitration in the flue gas of handling through desulfurization and handle, make nitrogen dioxide gas and ammoniacal liquor or urea generation chemical reaction generation denitration accessory substance nitric acid ammonia in the flue gas.Foregoing invention fails to realize the direct denitration of flue gas, but flue gas through the lower temperature region after the desulfurization by add ammoniacal liquor or urea with before rely on and add the nitrogen dioxide gas that hydrogen peroxide or methyl alcohol generates and generate denitration accessory substance nitric acid ammonia realization denitrating flue gas purpose.Simultaneously, owing to increased denitration reaction tower and denitration product separator, cause SR increase, energy consumption to rise.
Summary of the invention
The objective of the invention is to overcome the deficiency that existing dry fume denitration technology exists, a kind of method of utilizing ethanol to realize the direct denitration of warm dry method in the flue gas is provided, make it utilize ethanol to realize the direct denitration purpose of warm dry method in the flue gas, have the characteristics that are easy to of implementing.
The present invention is achieved by the following technical solutions, temperature area in the flue gas after fuel combustion process finishes, ethanol is sprayed in the flue gas that contains nitric oxide gas, thereby make nitric oxide, oxygen and ethanol generation chemical reaction in the flue gas generate the direct denitration of warm dry method in nitrogen, water vapour and the carbon dioxide realization flue gas.
The present invention utilizes ethanol to realize that the chemical equation of the direct denitration of warm dry method in the flue gas is as follows:
In addition, the chemical equation that remaining oxygen takes place after the fuel combustion in ethanol and the flue gas is as follows:
By above-mentioned chemical equation as can be known, spray into the ethanol in the flue gas, except that with flue gas in nitric oxide produce the chemical reaction, also with flue gas in remaining oxygen generation chemical reaction after the fuel combustion, the amount of alcohol that sprays into like this is just relevant with nitric oxide and amount of oxygen in the flue gas.Under nitric oxide in flue gas and the amount of oxygen certain condition, denitration efficiency reduces and increases with nitric oxide and ethanol molar percentage value.
Compare with existing dry method denitration technology, the invention has the advantages that: the first, inject ethanol that fuel combustion process finishes temperature area in the flue gas of back directly with flue gas in nitric oxide reaction generation nitrogen.The second, owing to ethanol be launched into flue-gas temperature in the combustion apparatus in the flue of middle temperature area with flue gas in the nitric oxide direct prompt reaction generate nitrogen, therefore do not need to arrange Benitration reactor, denitration separation of by-products device and catalyst in addition to have the characteristics that are easy to of implementing.Three, because the present invention is that temperature area is realized the direct denitration of dry fume by ethanol in the flue gas after fuel combustion process is finished, so the present invention do not limit by concrete combustion apparatus and fuel characteristic, and wide application prospect is arranged.
Description of drawings
The device schematic diagram that Fig. 1 adopts for the embodiment of the invention
Fig. 2 is an A-A cutaway view shown in Figure 1
The specific embodiment
Be example with a coal-fired power station boiler below, utilize ethanol to realize that the direct denitration of warm dry method is described in detail in the flue gas to the present invention in conjunction with Fig. 1 and Fig. 2.
Coal-fired contain nitric oxide production high-temperature flue gas what furnace of power-plant boilers 1 internal combustion generated, finish with burner hearth around behind the radiation heat transfer of water-cooling wall, flow into horizontal flue 2 successively, discharge tail vertical well gas flue 4 backs.Table 1 is for each component in the flue gas and inject the molar percentage of ethanol, and table 2 is injected the denitration efficiency of ethanol under different flue-gas temperatures under table 1 condition.
Each component and inject the molar percentage of ethanol in table 1 flue gas
| Flue gas composition % | H 2O | CO 2 | N 2 | O 2 | NO | C 2H 5OH |
| Molar percentage % | 7.68 | 14.80 | 73.98 | 2.56 | 0.14 | 0.83 |
The denitration efficiency of table 2 ethanol under different flue-gas temperatures
| Flue-gas temperature ℃ | 750 | 760 | 770 | 780 | 790 | 800 | 810 | 820 | 830 | 840 |
| Denitration efficiency % | 44.5 | 79.8 | 78.9 | 77.4 | 75.8 | 74.1 | 72.3 | 70.4 | 68.5 | 66.5 |
| Flue-gas temperature ℃ | 850 | 860 | 870 | 880 | 890 | 900 | 910 | 920 | 930 | 940 |
| Denitration efficiency % | 64.5 | 62.4 | 60.3 | 58.2 | 56.1 | 54.0 | 51.8 | 49.8 | 47.7 | 45.7 |
| Flue-gas temperature ℃ | 950 | 960 | 970 | 980 | 990 | 1000 | 1010 | 1100 |
| Denitration efficiency % | 43.7 | 41.7 | 39.8 | 38.0 | 36.2 | 34.5 | 32.8 | 21.5 |
As shown in Table 2, be between 760～870 ℃ in flue-gas temperature, the ethanol of injecting has higher relatively denitration efficiency.Calculate and The actual running results according to coal-fired power station boiler heating power, flue-gas temperature is that the middle temperature area between 760～870 ℃ is the rear portion of horizontal flue 2, therefore utilizing ethanol injection apparatus 3 that ethanol is injected horizontal flue 2 flue-gas temperatures is middle temperature area between 760～870 ℃, generate nitrogen and realize the direct denitration of dry method with the nitric oxide reaction in the flue gas, have higher relatively denitration efficiency.
In addition, under nitric oxide in flue gas and the amount of oxygen certain condition, denitration efficiency reduces and raises with the ethanol molar percentage value of nitric oxide in the flue gas and adding.For guaranteeing the even distribution of ethanol in flue gas, ethanol injection apparatus 3 both cocoa is arranged on top, bottom and the left and right sides wall of horizontal flue 2, also can be arranged in the horizontal flue 2.
Claims (4)
1. method of utilizing ethanol to realize the direct denitration of warm dry method in the flue gas, it is characterized in that: thus utilize nitric oxide, oxygen generation chemical reaction in ethanol and the flue gas to generate nitrogen, water vapour and the direct denitration of carbon dioxide realization dry fume, when ethanol was injected, flue-gas temperature was between 750 ℃-1100 ℃.
2. the method for utilizing ethanol to realize the direct denitration of warm dry method in the flue gas according to claim 1 is characterized in that, under nitric oxide in flue gas and the amount of oxygen rigid condition, denitration efficiency reduces and increases with nitric oxide and ethanol molar percentage value.
3. according to claim 1 or the 2 described methods of utilizing ethanol to realize the direct denitration of warm dry method in the flue gas, it is characterized in that described flue gas, the flue gas that generates for combustion of fossil fuel or be the flue gas of biomass fuel combustion generation.
4. the method for utilizing ethanol to realize the direct denitration of warm dry method in the flue gas according to claim 1 is characterized in that when ethanol was injected, flue-gas temperature was 760～870 ℃.
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| Application Number | Priority Date | Filing Date | Title |
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| CNB2006100266655A CN100434142C (en) | 2006-05-18 | 2006-05-18 | The method of using ethanol to realize the direct denitrification of flue gas dry method |
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| CNB2006100266655A CN100434142C (en) | 2006-05-18 | 2006-05-18 | The method of using ethanol to realize the direct denitrification of flue gas dry method |
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| CN1883767A true CN1883767A (en) | 2006-12-27 |
| CN100434142C CN100434142C (en) | 2008-11-19 |
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Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102302893A (en) * | 2011-06-20 | 2012-01-04 | 中国华能集团清洁能源技术研究院有限公司 | Selective non-catalytic reduction and denitration method for circulating fluidized bed boiler |
| CN111514726A (en) * | 2019-02-02 | 2020-08-11 | 广东万引科技发展有限公司 | Novel composite biomass denitration agent for dry-process cement kiln, use method of denitration agent and denitration system |
| CN111514738A (en) * | 2019-02-02 | 2020-08-11 | 广东万引科技发展有限公司 | A new type of composite biomass denitrification water agent for dry process cement kiln, its use method and denitration system |
| CN112742205A (en) * | 2019-10-31 | 2021-05-04 | 广东万引科技发展有限公司 | Novel biomass denitration agent for dry-process cement kiln, use method of novel biomass denitration agent and denitration system |
Family Cites Families (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4844878A (en) * | 1985-10-04 | 1989-07-04 | Fuel Tech, Inc. | Process for the reduction of nitrogen oxides in an effluent |
| JPS63205140A (en) * | 1987-02-19 | 1988-08-24 | Hidefumi Hirai | Adsorbent for nitrogen monoxide and method for separating and removing nitrogen monoxide |
| CN1084098A (en) * | 1992-09-12 | 1994-03-23 | 中国科学院福建物质结构研究所 | Eliminate the new method of nitrogen oxide gas contaminated environment |
| CN1239235C (en) * | 2003-08-26 | 2006-02-01 | 武汉凯迪电力股份有限公司 | Dry smoke cleaning process for desulfurizing and denitrating simultaneously and its system |
| US7090811B2 (en) * | 2003-12-11 | 2006-08-15 | General Motors Corporation | Method of reducing NOx in diesel engine exhaust |
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2006
- 2006-05-18 CN CNB2006100266655A patent/CN100434142C/en not_active Expired - Fee Related
Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102302893A (en) * | 2011-06-20 | 2012-01-04 | 中国华能集团清洁能源技术研究院有限公司 | Selective non-catalytic reduction and denitration method for circulating fluidized bed boiler |
| CN102302893B (en) * | 2011-06-20 | 2014-10-29 | 中国华能集团清洁能源技术研究院有限公司 | Selective non-catalytic reduction and denitration method for circulating fluidized bed boiler |
| CN111514726A (en) * | 2019-02-02 | 2020-08-11 | 广东万引科技发展有限公司 | Novel composite biomass denitration agent for dry-process cement kiln, use method of denitration agent and denitration system |
| CN111514738A (en) * | 2019-02-02 | 2020-08-11 | 广东万引科技发展有限公司 | A new type of composite biomass denitrification water agent for dry process cement kiln, its use method and denitration system |
| CN111514726B (en) * | 2019-02-02 | 2024-01-26 | 广东万引科技发展有限公司 | Novel composite biomass denitration agent for dry-method cement kiln, application method of novel composite biomass denitration agent and denitration system |
| CN112742205A (en) * | 2019-10-31 | 2021-05-04 | 广东万引科技发展有限公司 | Novel biomass denitration agent for dry-process cement kiln, use method of novel biomass denitration agent and denitration system |
| CN112742205B (en) * | 2019-10-31 | 2024-01-23 | 广东万引科技发展有限公司 | Novel biomass denitration agent for dry-method cement kiln, application method of novel biomass denitration agent and denitration system |
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