CN101219385A - Catalyst, method for producing the same, flue gas denitrating technique by using the catalyst - Google Patents
Catalyst, method for producing the same, flue gas denitrating technique by using the catalyst Download PDFInfo
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- CN101219385A CN101219385A CNA2008100566292A CN200810056629A CN101219385A CN 101219385 A CN101219385 A CN 101219385A CN A2008100566292 A CNA2008100566292 A CN A2008100566292A CN 200810056629 A CN200810056629 A CN 200810056629A CN 101219385 A CN101219385 A CN 101219385A
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Abstract
The invention discloses a catalyst used for denitration of smokes and a preparation method thereof; the catalyst comprises ferrous sulfate and a carrier carrying ferrous sulfate. The invention also discloses a technique for denitration of smokes, comprising the following steps: a denitration reducing agent is added into a smoke flow; the denitration reducing agent and the smoke flow through the fludized bed reactor to eliminate the nitrate ion of the smoke, and the fluidized bed reactor is provided with the catalyst. The catalyst of the invention dramatically enhances the specific surface and mechanical strength of ferrous sulfate as an activated component, and has the advantages of inexpensive cost, availability, long service life and can be discarded; with the denitration technique of the invention, ferrous sulfate in the form of a carrier is used as the catalyst, and the denitration can be performed in the fluidized bed and has high denitration efficiency, low catalyst cost, long service life, thus greatly cutting down the construction and operation cost of denitration under comparatively low pressure decrease while the denitration efficiency is satisfied.
Description
Technical Field
The invention relates to a catalyst for flue gas denitration, a preparation method of the catalyst and a process for flue gas denitration by using the catalyst, in particular to a ferrous sulfate-containing catalyst, a preparation method of the ferrous sulfate-containing catalyst and a dry fluidized bed denitration process for removing nitrogen oxides from flue gas by using the catalyst.
Background
It is known that the NO contained in various industrial fumes emitted into the atmosphereXMainly NO and NO2Causing great harm to human health and human living environment. Aiming at NO in industrial emission flue gasXRemoval has been carried out by various methods.
Selective Catalytic Reduction (SCR) denitration technology is one of the denitration technologies that is widely used. In the SCR denitration technology, a catalyst is placed in a flue in the form of a fixed bed, and NH is arranged in front of a catalyst bed layer3Is sprayed into the flue gas, NH when the flue gas flows through the fixed catalyst bed layer3With NO on a catalyst to form N2And denitration is realized. SCR denitration technology generally adopts a fixed bed reactor, SO that the catalyst is required to have extremely high catalytic efficiency under the condition of large space velocity and excellent anti-pollution capacity to resist SO2，H2Adverse effects of O.And meanwhile, the SCR catalyst also needs to have good thermal shock resistance and mechanical strength performance, so that the SCR catalyst has short service life, unstable operation and higher overall cost of the system.
The SCR denitration technology generally adopts V meeting the requirements2O5Class catalyst for denitration, and V2O5The quasi-catalysts are very expensive, thereby further increasing the cost.
Disclosure of Invention
The object of the present invention is to solve at least one of the above-mentioned problems of the prior art.
To this end, according to one aspect of the present invention, a catalyst is provided that is inexpensive, readily available, disposable, and does not cause secondary damage to the environment.
The catalyst according to the first aspect of the present invention comprises ferrous sulfate as an active ingredient, and a carrier supporting the ferrous sulfate.
The catalyst according to the embodiment of the invention also has the following additional technical features:
the carrier is selected from the group consisting of fluid catalytic cracking spent catalyst, attapulgite, kaolin, natural zeolite, industrial zeolite. The weight ratio of the carrier to the ferrous sulfate is 2: 1. The particle size of the carrier is 50-1000 μm, preferably 450-600 μm.
According to another aspect of the present invention, there is provided a process for preparing a catalyst according to the first aspect of the present invention.
The catalyst preparation method according to another aspect of the present invention comprises: adding ferrous sulfate and a carrier into a solvent; soaking the ferrous sulfate and the carrier in a solvent for a predetermined time so that the ferrous sulfate is carried on the carrier; filtering the carrier carrying ferrous sulfate from the solvent; drying the filtered carrier carrying the ferrous sulfate.
The preparation method of the catalyst provided by the embodiment of the invention also has the following additional technical characteristics:
the carrier is selected from the group consisting of fluid catalytic cracking spent catalyst, attapulgite, kaolin, natural zeolite, industrial zeolite.
The solvent is selected from the group consisting of water, methanol, ethanol, weak acid water, aqueous methanol solution, and aqueous ethanol solution.
The weight ratio of the carrier to the ferrous sulfate is 2: 1.
The drying is carried out at a temperature of 190 ℃.
According to a further aspect of the present invention, there is provided a flue gas denitration process using the catalyst according to the first aspect of the present invention.
The flue gas denitration process according to the other aspect of the invention comprises the following steps: adding a denitration reducing agent into the flue gas flow; and passing the denitration reductant and flue gas stream through a fluidized bed reactor to remove the nitrates in the flue gas, wherein the fluidized bed reactor has a catalyst according to the first aspect of the invention therein.
The flue gas denitration method provided by the embodiment of the invention also has the following additional technical characteristics:
the denitration reductant is selected from the group consisting of ammonia, an ammonia-containing substance, and an ammonia-forming substance.
The nitrate in the flue gas is removed in a fluidized bed reactor at the temperature of 300-500 ℃.
The removal of the nitrates from the flue gases in the fluidized-bed reactor was carried out at a temperature of 420 ℃.
The flue gas velocity in the fluidized bed reactor is 1-20 m/s.
The denitrated flue gas exiting the fluidized bed reactor is subjected to a gas-solid separation to separate entrained solids from the flue gas, wherein the solids include catalyst and dust.
The denitration process according to the invention further comprises: returning part of the solid matters separated by gas and solid to the fluidized bed reactor so as to recycle the catalyst in the solid matters.
The gas-solid separation comprises the following steps: carrying out inertial separation on the flue gas which is discharged from the fluidized bed reactor and is subjected to nitre removal; and carrying out electric precipitation on the flue gas subjected to inertia separation.
The above denitration process according to the present invention further comprises detecting the content of the catalyst in the separated solid matter, wherein a part of the solid matter is returned to the fluidized bed reactor when the content of the catalyst in the separated solid matter is more than 10% by weight.
Compared with the prior art, the invention has at least one of the following advantages:
the ferrous sulfate catalyst supported by the carrier greatly improves the specific surface area and the mechanical strength of ferrous sulfate as an active component, and has the advantages of low price, easy obtainment, long service life and disposability.
When the supported ferrous sulfate catalyst is used for flue gas denitration, the supported ferrous sulfate catalyst can be used for fluidized bed denitration, the denitration efficiency is high, and the generated product after denitration does not cause secondary damage to the environment; does not generate additional pollutants, and is particularly suitable for denitration of flue gas of coal-fired power plants.
The preparation method of the supported ferrous sulfate catalyst has simple process, can improve the specific area and the mechanical strength of the catalyst, and the prepared catalyst is suitable for the denitration of a fluidized bed and has high denitration efficiency.
According to the flue gas denitration process, the ferrous sulfate catalyst in a supported form is used, so that denitration can be performed by using a fluidized bed, the denitration efficiency is high, the catalyst is low in cost and long in service life, and the construction and operation cost of denitration is greatly reduced under the conditions of meeting the denitration efficiency and lowering the pressure drop.
According to the denitration process disclosed by the invention, the denitration efficiency can be further improved and the energy consumption and the cost can be reduced by controlling the temperature regulation in the fluidized bed reactor, such as 300-500 ℃, particularly 420 ℃.
According to the denitration process disclosed by the invention, the catalyst in the solid matters separated from the denitrated flue gas is returned to the fluidized bed reactor, so that the catalyst can be recycled, and the cost is further reduced.
According to the denitration process disclosed by the invention, the inertia separator is adopted to carry out inertia separation on the denitrated flue gas, so thatsolid matters with larger particle sizes, such as dust and a supported ferrous sulfate catalyst, carried by the denitrated flue gas can be primarily separated, then the inertia separated flue gas is subjected to electric precipitation, and solid matters with smaller particle sizes in the flue gas can be separated, so that the flue gas discharged into the atmosphere can be further purified, and the environmental pollution is reduced.
Additional aspects and advantages of the invention will be set forth in part in the description which follows and, in part, will be obvious from the description, or may be learned by practice of the invention.
Drawings
The above and/or other aspects and advantages of the present invention will become apparent and readily appreciated from the following description of the embodiments, taken in conjunction with the accompanying drawings of which:
FIG. 1 is a schematic view of an apparatus used in a denitration process according to an embodiment of the present invention;
FIG. 2 is a flow chart of a method of preparing a catalyst according to a first embodiment of the present invention;
FIG. 3 is a flow chart of a method of preparing a catalyst according to a second embodiment of the present invention;
FIG. 4 is a flow diagram of a flue gas denitration process according to a first embodiment of the invention;
FIG. 5 is a flow chart of a flue gas denitration process according to a second embodiment of the invention;
fig. 6 is a flow chart of a flue gas denitration process according to a first embodiment of the invention.
Detailed Description
Reference will now be made in detail to embodiments of the present invention, examples of which are illustrated in the accompanying drawings, wherein like or similar reference numerals refer to the same or similar elements or elements having the same or similar function throughout. The embodiments described below by referring to the drawings are intended to explain the present invention, and are illustrative rather than to be construed as limiting the present invention.
The catalyst particularly for flue gas denitration according to the embodiment of the present invention includes ferrous sulfate (FeSO) as an active ingredient4.7H2O) and a carrier supporting the iron sulfate (supported), that is, the catalyst according to the present invention is iron sulfate in a form supported by the carrier. The carrier is used for carrying the ferrous sulfate, so that the specific area and the mechanical strength of the ferrous sulfate catalyst can be improved, and the flue gas is subjected to removalIn the denitration, the fluidized bed reactor can be used for denitration, so that the denitration efficiency is improved, and the catalyst disclosed by the invention is cheap, easy to obtain, long in service life and disposable.
The ferrous sulfate-supporting carrier may be Fluid Catalytic Cracking (FCC) spent catalyst, attapulgite, kaolin, natural zeolite, or industrial zeolite. Among them, natural zeolite is preferable because natural zeolite is inexpensive and readily available. The weight ratio of the carrier and the ferrous sulfate is 2: 1, and experiments prove that the ratio is better for denitration efficiency. The particle size of the carrier is 50-1000 μm, preferably in the range of 450-600 μm, which is better for flue gas denitration efficiency.
A method for preparing a catalyst of ferrous sulfate supported by a carrier according to an embodiment of the present invention will be described with reference to fig. 2. As shown in fig. 2, first, ferrous sulfate and a carrier are added to a solvent and stirred, and soaked for a predetermined time so that the ferrous sulfate is carried on the carrier. Subsequently, filtration is performed to filter the carrier carrying the ferrous sulfate from the solvent. And finally, drying the carrier loaded with the ferrous sulfate to obtain the ferrous sulfate loaded by the carrier. The drying of the carrier carrying the ferrous sulfate is carried out at a temperature of 190 ℃.
As described above, the ferrous sulfate-supporting carrier may be Fluid Catalytic Cracking (FCC) spent catalyst, attapulgite, kaolin, natural zeolite, or industrial zeolite. The solvent can be water, methanol, ethanol, weak acid water, methanol water solution or ethanol water solution, wherein ethanol is preferred, and the loading effect is better when ethanol is used for soaking.
The preparation of the catalyst is described below with reference to fig. 3, taking natural zeolite as a carrier and ethanol as a solvent as an example, which is preferred because it is cheap and readily available, and in addition, tests have shown that the effect on ferrous sulfate loading is better with ethanol as a solvent.
First, natural zeolite having a particle size of 50 to 1000 μm, preferably 450-600 μm, and ferrous sulfate are mixed at a ratio of 2: 1 by weight and added to ethanol. Then, the natural zeolite and the ferrous sulfate are soaked in the ethanol for a period of time, such as 72 hours, but other periods of time are also possible, tests show that the loading effect is good for 72 hours and no time is wasted, and then the natural zeolite loaded with the ferrous sulfate is filtered out. Finally, the filtered natural zeolite is dried at 190 ℃ for a period of time, for example 2 hours, to obtain ferrous sulfate in supported form.
Experiments prove that when the carrier with the particle size of 450-600 mu m and ethanol are used as a solvent and are soaked for 72 hours, the effect of loading the ferrous sulfate is better, and the time is not wasted.
The above is merely an example of the present invention and is not to be construed as limiting the present invention, and for example, the carrier may be selected from the other carriers, the solvent may be other solvents such as water, and the time for soaking, the time for drying, and the temperature for drying are not particularly limited as long as the carrier can carry the ferrous sulfate.
A process for removing nitrate from flue gas using a supported form of a ferrous sulfate catalyst according to an embodiment of the present invention is described below with reference to fig. 1 and 4-6.
The apparatus used in the denitration process of the present invention will be described first with reference to FIG. 1. Fig. 1 shows a schematic view of the equipment used in the denitration process. As shown in fig. 1, the equipment for the denitration process includes a fluidized bed reactor 1, and more specifically, the fluidized bed reactor 1 is a fluidized bed reactor which is layered. Before the industrial flue gas enters the fluidized bed reactor 1, a denitration reducing agent, such as ammonia or urea, needs to be added into the flue gas. Ferrous sulfate in a supported form as a catalyst is filled in the fluidized bed reactor 1, and the ferrous sulfate is supported by a carrier, so that the specific surface area and the mechanical strength of the ferrous sulfate can be improved, the service life of the catalyst is prolonged, the denitration efficiency is improved, and the fluidized bed reactor is suitable for denitration of a fluidized bed.
The equipment used for the denitration process also comprises an inertia separator 2 and a cone hopper 4 positioned at the lower part of the inertia separator 2, and the flue gas which is discharged from the fluidized bed reactor 1 and is removed with the nitre enters the inertia separator 2. Since the flue gas discharged from the fluidized-bed reactor 1 is more or less entrained with solid matter, which for example comprises ferrous sulfate catalyst in supported form, and possibly dust.
Therefore, the inertia separator 2 can separate the solid matters with larger particle sizes in the denitrated flue gas from the flue gas, and the separated solid matters are collected in the cone hopper 4.
The cone 4 may be integral with the inertial separator 2, i.e. the cone 4 may be part of the inertial separator 2, or the cone 4 may be a separate component from the inertial separator 2.
The inertial separator 2 is low in cost compared to the electric dust collector 3, which will be described below, and therefore the cost can be further reduced by first using the inertial separator 2 to preliminarily separate most of the solid matter with a larger particle size from the denitrated flue gas.
The equipment used in the denitration process further comprises an electric dust collector 3 and a cone hopper 4 positioned at the lower part of the electric dust collector 3.
The flue gas through inertial separation gets into electrostatic precipitator 3 from inertial separator 2, and electrostatic precipitator 3 is arranged in separating out the less solid matter of granularity in the flue gas to further purify the flue gas, the less solid matter of granularity that separates gets into in the awl fill 4 of electrostatic precipitator 3 lower part. The purified flue gas subjected to electric precipitation can be directly discharged into the atmosphere, and the air cannot be polluted.
The cone 4 may be integral with the electric dust collector 3, i.e. the cone 4 may be part of the electric dust collector 3, or the cone 4 may be a separate component from the electric dust collector 3. In the embodiment shown in fig. 1, the electric dust collector 3 comprises three electric fields, however, the electric fields of the electric dust collector 3 may be any suitable number.
The denitration process shown in fig. 1 further includes a collector 5, and the collector 5 is used for collecting the solid matters separated from the flue gas by the inertial separator 2 and the electric dust collector 3. Since the solid matter separated from the flue gas contains the catalyst, a part of the solid matter collected in the collector 5 can be returned to the fluidized bed reactor 1, so that the catalyst can be recycled, and the cost can be further reduced. Of course, it is also possible to detect the catalyst content in the solid matter in the collector 5 and to return a part of the solid matter to the fluidized-bed reactor 1 only when the catalyst content is greater than a certain value.
The flue gas denitration process according to the embodiment of the invention is described below.
Fig. 4 shows a flowchart of a denitration process according to a first embodiment of the present invention. As shown in fig. 4, a denitration reductant, such as ammonia gas, or a substance containing ammonia, or a substance capable of forming ammonia (such as urea), is injected into the industrial flue gas before the industrial flue gas enters the fluidized bed reactor 1, and the nitrate in the flue gas exists in the form of nitric oxide and/or nitrogen dioxide. Then, the mixture of flue gas and ammonia gas is fed into the fluidized-bed reactor 1. As a catalyst, ferrous sulfate in a carrier-supported form is arranged in the fluidized bed reactor 1.
As noted above, the support is selected from Fluid Catalytic Cracking (FCC) spent catalyst, attapulgite, kaolin, natural zeolite, industrial zeolite, or other natural porous material. For example, a relatively inexpensive natural zeolite and ferrous sulfate are used to prepare a ferrous sulfate catalyst in a supported form using the above method.
The flue gas contains nitrate which is removed in the fluidized bed reactor 1 by a series of chemical reactions, as described above, the nitrate being present in the flue gas mainly in the form of nitric oxide and nitrogen dioxide. The main denitrification chemical reactions in the fluidized bed reactor 1 are as follows:
experiments prove that compared with the method of using pure ferrous sulfate as a catalyst, the denitration rate can be improved by 10-50% by using the supported ferrous sulfate.
As described above, the above-described various substances undergo the gas-solid catalytic reaction in the fluidized bed reactor 1. Due to the different particle sizes of the above-mentioned solid substances, a stratified fluidized state is formed in the fluidized-bed reactor 1, in the lower part of which a dense bed in the form of a flooded bed is formed, and in the upper part of which a rapidly turbulent bed is formed. And the solid matters with large particle sizes are enriched in the cone-shaped structure, while the small particles are carried to the upper part in the fluidized bed reactor 1 by the flue gas, thereby effectively realizing the effective separation of the solid matters with two particle sizes.
Through the above reaction in the fluidized bed reactor 1, nitrogen monoxide and nitrogen dioxide in the flue gas become nitrogen gas, so that the discharged flue gas does not cause pollution to the environment.
The temperature of the fluidized bed reactor 1 is controlled to be 300-500 ℃, so that the reaction is easier to carry out, the denitration effect is good, and further, the temperature is controlled to be 420 ℃, and the effect is better.
The gas velocity in the fluidized-bed reactor 1 is kept at 1 to 20m/s, in particular at 5 to 7 m/s. The average suspended matter density in the fluidized bed is 0.1-100 kg/Nm3Especially 1 to 20kg/Nm3. The denitrated flue gas enters the inertial separator 2 from the fluidized bed reactor 1, and the denitrated flue gas flow discharged from the fluidized bed reactor 1 carries solid matters, wherein the solid matters comprise a ferrous sulfate-containing catalyst and possibly some dust.
In the inertial separator 2, the solid matters with larger particle sizes in the flue gas are separated out through the inertial separation effect.
Then, the flue gas from which the solid matters with larger particle sizes are separated enters an electric dust collector 3 so as to separate the solid matters with smaller particle sizes from the flue gas. In this example, the flue gas is subjected to three times of electric precipitation.
The purified flue gas from which the solid matter is removed is discharged, thereby not polluting the environment.
A flue gas denitration process according to a second embodiment of the present invention will be described with reference to fig. 5, where the embodiment shown in fig. 5 is different from the embodiment shown in fig. 4 in that: the solid matter separated by means of the inertial separator 2 and/or the solid matter separated by means of the electrostatic precipitator 3 is collected, and a part of the collected solid matter is returned to the fluidized-bed reactor 1, thereby recycling the catalyst, further reducing the cost, and collecting the other part of the solid matters to be used for other purposes, since the inertial separator 2 separates the solid matter with a relatively large particle size, it is also possible to return only a part of the solid matter separated by the inertial separator 2 into the fluidized-bed reactor 1, while the solid matter separated by the electric dust collector 3 may be mainly dust, so the solid matter separated by the electric dust collector 3 may not return to the fluidized bed reactor 1, furthermore, it is also possible to return only a part of the solid matter separated by the electric precipitator 3 to the fluidized-bed reactor 1, as will be readily understood by those skilled in the art. Other steps of the embodiment shown in fig. 3 are the same as those of the embodiment shown in fig. 2, and are not described again here.
A flue gas denitration process according to a third embodiment of the present invention will be described with reference to fig. 6, which is different from the embodiment shown in fig. 5 in that: the solid matter separated by inertia separation and/or electric precipitation is collected to detect the content of the catalyst therein, and the detection method can be performed by various known methods, which will not be described in detail herein. When the ferrous sulfate content is, for example, more than 10% by weight, a part of the solid matter is returned to the fluidized-bed reactor 1 to recycle the catalyst, otherwise the solid matter is not returned to the fluidized-bed reactor 1. Other steps of the embodiment shown in fig. 6 are the same as those of the embodiment shown in fig. 5, and are not described again here.
Therefore, according to the denitration process provided by the embodiment of the invention, the supported ferrous sulfate catalyst is adopted, the price is low, and the ferrous sulfate can be obtained from a plurality of industrial wastes, for example, the by-product in the titanium dioxide production process is rich in ferrous sulfate. With the currently widely used SCR catalyst (V)2O5) Compared with simple ferrous sulfate, the denitration catalyst is suitable for denitration of a fluidized bed, the specific area and the mechanical strength are improved, and the denitration efficiency is better.
The technological process of the embodiment of the invention is a dry method, does not consume water, and does not have secondary pollution of water. The catalyst for realizing the reaction processes is a substance which is cheap and easy to obtain, can be discarded and does not cause secondary damage to the environment.
According to an embodiment of the present invention, the fluidized-bed reactor 1 employing stratified fluidization is in a state of turbulent conveyance with large particles in its lower part and small particles in its upper part. Thereby avoiding the reduction of the separation efficiency and the increase of the pressure drop caused by the overlarge load of the inertia separator and the electric dust remover.
Thus, according to the denitration process of the invention, experiments prove that the FeSO loaded is used at the temperature of 300-500 DEG C4(active ingredient, load) as catalyst, denitration efficiency ratio using pure FeSO4As a catalyst, by approximately fifty percent. And the supported catalyst has better mechanical strength, and better fluidization control is realized by controlling the particle size of the carrier.
Although embodiments of the present invention have been shown and described, it would be appreciated by those skilled in the art that changes may be made in these embodiments without departing from the principles and spirit of the invention, the scope of which is defined in the claims and their equivalents.
Claims (21)
1. A catalyst, comprising: ferrous sulfate as an active ingredient, and a carrier carrying the ferrous sulfate.
2. The catalyst of claim 1, wherein the support is selected from the group consisting of fluid catalytic cracking spent catalyst, attapulgite, kaolin, natural zeolite, and industrial zeolite.
3. The catalyst of claim 1, wherein the weight ratio of the support to the ferrous sulfate is 2: 1.
4. A catalyst according to any one of claims 1 to 3, characterized in that the particle size of the support is 50-1000 μm.
5. The catalyst as claimed in claim 4, wherein the particle size of the carrier is 450-600 μm.
6. A preparation method of a catalyst is characterized by comprising the following steps:
adding ferrous sulfate and a carrier into a solvent;
soaking the ferrous sulfate and the carrier in a solvent for a predetermined time so that the ferrous sulfate is carried on the carrier;
filtering the carrier carrying ferrous sulfate from the solvent;
drying the filtered carrier carrying the ferrous sulfate.
7. The method for preparing a catalyst according to claim 6, wherein the carrier is selected from the group consisting of fluid catalytic cracking spent catalyst, attapulgite, kaolin, natural zeolite, and industrial zeolite.
8. The method of preparing a catalyst according to claim 6, wherein the solvent is selected from the group consisting of water, methanol, ethanol, weak acid water, an aqueous solution of methanol, and an aqueous solution of ethanol.
9. The method of claim 6, wherein the weight ratio of the carrier to the ferrous sulfate is 2: 1.
10. The method for preparing the catalyst according to claim 6, wherein the drying is performed at a temperature of 190 ℃.
11. The method for preparing a catalyst according to claim 6, the particle size of the carrier is 50 to 1000 μm.
12. The method for preparing a catalyst according to claim 11, wherein the particle size of the carrier is 450-600 μm.
13. A flue gas denitration process is characterized by comprising the following steps:
adding a denitration reducing agent into the flue gas flow; and
passing a stream of denitration reductant and flue gas through a fluidized bed reactor to remove nitrates from the flue gas, wherein the fluidized bed reactor has a catalyst according to any one of claims 1-5 therein.
14. The flue gas denitration process of claim 13, wherein the denitration reductant is selected from the group consisting of ammonia, ammonia-containing substances, and ammonia-forming substances.
15. The flue gas denitration process according to claim 13, wherein the denitration of flue gas in the fluidized bed reactor is performed at a temperature of 300 ℃ to 500 ℃.
16. The flue gas denitration process according to claim 15, wherein the denitration of flue gas in the fluidized bed reactor is performed at a temperature of 420 ℃.
17. The flue gas denitration process according to claim 13, wherein the flow velocity of the flue gas in the fluidized bed reactor is 1-20 m/s.
18. The flue gas denitration process of claim 13, further comprising gas-solid separation of the denitrated flue gas discharged from the fluidized bed reactor to separate entrained solid matter from the flue gas, wherein the solid matter comprises catalyst and dust.
19. The flue gas denitration process of claim 18, further comprising: returning part of the solid matters separated by gas and solid to the fluidized bed reactor so as to recycle the catalyst in the solid matters.
20. The flue gas denitration process of claim 19, wherein the gas-solid separation comprises:
carrying out inertial separation on the flue gas which is discharged from the fluidized bed reactor and is subjected to nitre removal; and
and performing electric precipitation on the flue gas subjected to inertia separation.
21. The flue gas denitration process of claim 18, further comprising: detecting the content of the catalyst in the separated solid matter, wherein when the content of the catalyst in the separated solid matter is more than 10% by weight, a part of the solid matter is returned to the fluidized bed reactor.
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| CN103272618A (en) * | 2013-05-20 | 2013-09-04 | 大连理工大学 | Denitrating catalyst and preparation method thereof |
| CN105195171A (en) * | 2015-11-03 | 2015-12-30 | 海南中航特玻科技有限公司 | Honeycombed catalyst for low-temperature denitration and preparation method |
| CN108654661A (en) * | 2017-04-01 | 2018-10-16 | 中国科学院大连化学物理研究所 | A kind of SO2Electrochemical oxidation non-precious metal catalyst and its preparation and application |
| CN108889316A (en) * | 2018-08-23 | 2018-11-27 | 攀钢集团攀枝花钢铁研究院有限公司 | A kind of denitrating catalyst and preparation method thereof |
| CN111841322A (en) * | 2020-07-29 | 2020-10-30 | 湖南萃智环保科技有限公司 | Denitration and discharge method for cement kiln |
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2008
- 2008-01-23 CN CNA2008100566292A patent/CN101219385A/en active Pending
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN103272618A (en) * | 2013-05-20 | 2013-09-04 | 大连理工大学 | Denitrating catalyst and preparation method thereof |
| CN105195171A (en) * | 2015-11-03 | 2015-12-30 | 海南中航特玻科技有限公司 | Honeycombed catalyst for low-temperature denitration and preparation method |
| CN108654661A (en) * | 2017-04-01 | 2018-10-16 | 中国科学院大连化学物理研究所 | A kind of SO2Electrochemical oxidation non-precious metal catalyst and its preparation and application |
| CN108889316A (en) * | 2018-08-23 | 2018-11-27 | 攀钢集团攀枝花钢铁研究院有限公司 | A kind of denitrating catalyst and preparation method thereof |
| CN111841322A (en) * | 2020-07-29 | 2020-10-30 | 湖南萃智环保科技有限公司 | Denitration and discharge method for cement kiln |
| CN111841322B (en) * | 2020-07-29 | 2022-08-19 | 安徽萃智环保科技有限公司 | Denitration and discharge method for cement kiln |
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