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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Abstract
A environment-friendly process for mesothermal dry method direct denitration for flue gas by using ethanol is provided, wherein ethanol reacts with nitrogen monoxide and oxygen to produce nitrogen gas, water vapour, and carbon dioxide in flue gas to realizing dry method direct denitration of flue gas with flue gas temperature of 750 to 1100 DEG C at ethanol infusion. The invention is characterized in that: firstly, ethanol in mesothermal zone directly reacts with nitrogen monoxide in flue gas to give nitrogen gas after combustion process of injection fuel; secondly, because ethanol is injected into the mesothermal zone of flue and directly reacts with nitrogen monoxide to give nitrogen gas, additional denitration reactor, denitration byproduct separator, and catalyst are not demanded; thirdly, there is no limit to burning equipment and fuel characteristic, and as a result, the process in the invention can be used extensively.
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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| 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 |
| CN111514738A (en) * | 2019-02-02 | 2020-08-11 | 广东万引科技发展有限公司 | Novel composite biomass denitration water agent for dry-process cement kiln, use method of composite biomass denitration water agent and denitration system |
| 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 |
| 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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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 |
| CN111514738A (en) * | 2019-02-02 | 2020-08-11 | 广东万引科技发展有限公司 | Novel composite biomass denitration water agent for dry-process cement kiln, use method of composite biomass denitration water agent and denitration system |
| 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 |
| 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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| CN100434142C (en) | 2008-11-19 |
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Granted publication date: 20081119 Termination date: 20110518 |