CN109253448B - Circulating fluidized bed combustion method - Google Patents
Circulating fluidized bed combustion method Download PDFInfo
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- CN109253448B CN109253448B CN201710566859.2A CN201710566859A CN109253448B CN 109253448 B CN109253448 B CN 109253448B CN 201710566859 A CN201710566859 A CN 201710566859A CN 109253448 B CN109253448 B CN 109253448B
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- 238000009841 combustion method Methods 0.000 title abstract description 16
- 239000000463 material Substances 0.000 claims abstract description 77
- MWUXSHHQAYIFBG-UHFFFAOYSA-N nitrogen oxide Inorganic materials O=[N] MWUXSHHQAYIFBG-UHFFFAOYSA-N 0.000 claims abstract description 75
- 238000002485 combustion reaction Methods 0.000 claims abstract description 54
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims abstract description 20
- 239000003546 flue gas Substances 0.000 claims abstract description 20
- 239000000446 fuel Substances 0.000 claims abstract description 18
- 229910044991 metal oxide Inorganic materials 0.000 claims abstract description 17
- 150000004706 metal oxides Chemical class 0.000 claims abstract description 17
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims abstract description 16
- 239000008247 solid mixture Substances 0.000 claims abstract description 13
- 229910052757 nitrogen Inorganic materials 0.000 claims abstract description 8
- 230000001590 oxidative effect Effects 0.000 claims abstract description 5
- 239000002245 particle Substances 0.000 claims description 12
- 238000000034 method Methods 0.000 claims description 11
- JEIPFZHSYJVQDO-UHFFFAOYSA-N iron(III) oxide Inorganic materials O=[Fe]O[Fe]=O JEIPFZHSYJVQDO-UHFFFAOYSA-N 0.000 claims description 4
- 238000006479 redox reaction Methods 0.000 claims description 4
- 230000001502 supplementing effect Effects 0.000 claims description 2
- 238000004519 manufacturing process Methods 0.000 abstract description 4
- 239000003245 coal Substances 0.000 description 18
- 239000002006 petroleum coke Substances 0.000 description 8
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 6
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 6
- 238000005516 engineering process Methods 0.000 description 6
- 229910052760 oxygen Inorganic materials 0.000 description 6
- 239000001301 oxygen Substances 0.000 description 6
- 235000019738 Limestone Nutrition 0.000 description 3
- 229910021529 ammonia Inorganic materials 0.000 description 3
- 230000000052 comparative effect Effects 0.000 description 3
- 239000006028 limestone Substances 0.000 description 3
- 238000005272 metallurgy Methods 0.000 description 3
- 239000000126 substance Substances 0.000 description 3
- RAHZWNYVWXNFOC-UHFFFAOYSA-N Sulphur dioxide Chemical compound O=S=O RAHZWNYVWXNFOC-UHFFFAOYSA-N 0.000 description 2
- 239000002956 ash Substances 0.000 description 2
- 238000010531 catalytic reduction reaction Methods 0.000 description 2
- 239000000203 mixture Substances 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical group [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- 239000006004 Quartz sand Substances 0.000 description 1
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 description 1
- 239000000571 coke Substances 0.000 description 1
- 238000006477 desulfuration reaction Methods 0.000 description 1
- 230000023556 desulfurization Effects 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 230000005611 electricity Effects 0.000 description 1
- 230000002708 enhancing effect Effects 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 239000003344 environmental pollutant Substances 0.000 description 1
- 239000010881 fly ash Substances 0.000 description 1
- 238000002309 gasification Methods 0.000 description 1
- 238000002347 injection Methods 0.000 description 1
- 239000007924 injection Substances 0.000 description 1
- UQSXHKLRYXJYBZ-UHFFFAOYSA-N iron oxide Inorganic materials [Fe]=O UQSXHKLRYXJYBZ-UHFFFAOYSA-N 0.000 description 1
- QJGQUHMNIGDVPM-UHFFFAOYSA-N nitrogen group Chemical group [N] QJGQUHMNIGDVPM-UHFFFAOYSA-N 0.000 description 1
- 231100000719 pollutant Toxicity 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 239000000779 smoke Substances 0.000 description 1
- 239000000243 solution Substances 0.000 description 1
Images
Classifications
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23C—METHODS OR APPARATUS FOR COMBUSTION USING FLUID FUEL OR SOLID FUEL SUSPENDED IN A CARRIER GAS OR AIR
- F23C10/00—Fluidised bed combustion apparatus
- F23C10/02—Fluidised bed combustion apparatus with means specially adapted for achieving or promoting a circulating movement of particles within the bed or for a recirculation of particles entrained from the bed
- F23C10/04—Fluidised bed combustion apparatus with means specially adapted for achieving or promoting a circulating movement of particles within the bed or for a recirculation of particles entrained from the bed the particles being circulated to a section, e.g. a heat-exchange section or a return duct, at least partially shielded from the combustion zone, before being reintroduced into the combustion zone
- F23C10/08—Fluidised bed combustion apparatus with means specially adapted for achieving or promoting a circulating movement of particles within the bed or for a recirculation of particles entrained from the bed the particles being circulated to a section, e.g. a heat-exchange section or a return duct, at least partially shielded from the combustion zone, before being reintroduced into the combustion zone characterised by the arrangement of separation apparatus, e.g. cyclones, for separating particles from the flue gases
- F23C10/10—Fluidised bed combustion apparatus with means specially adapted for achieving or promoting a circulating movement of particles within the bed or for a recirculation of particles entrained from the bed the particles being circulated to a section, e.g. a heat-exchange section or a return duct, at least partially shielded from the combustion zone, before being reintroduced into the combustion zone characterised by the arrangement of separation apparatus, e.g. cyclones, for separating particles from the flue gases the separation apparatus being located outside the combustion chamber
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23C—METHODS OR APPARATUS FOR COMBUSTION USING FLUID FUEL OR SOLID FUEL SUSPENDED IN A CARRIER GAS OR AIR
- F23C10/00—Fluidised bed combustion apparatus
- F23C10/18—Details; Accessories
- F23C10/24—Devices for removal of material from the bed
- F23C10/26—Devices for removal of material from the bed combined with devices for partial reintroduction of material into the bed, e.g. after separation of agglomerated parts
Landscapes
- Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- Combustion & Propulsion (AREA)
- Mechanical Engineering (AREA)
- General Engineering & Computer Science (AREA)
- Fluidized-Bed Combustion And Resonant Combustion (AREA)
Abstract
The invention provides a circulating fluidized bed combustion method, bed materials containing metal oxides in a hearth of a combustion device are fluidized by air, a dense phase region is formed at the bottom of the hearth, and a dilute phase region is formed at the middle upper part of the hearth; placing the fuel in a hearth for combustion, forming a reducing environment in a dense-phase zone, and forming an oxidizing environment in a dilute-phase zone; reducing the bed material in the dense phase area, then reducing nitrogen oxides in the flue gas into nitrogen in the dilute phase area, and simultaneously reoxidizing the bed material; and the gas-solid mixture generated by the hearth enters the cyclone separator, the bed material in the gas-solid mixture is separated and enters the dipleg of the cyclone separator, the bed material is sent back to the hearth through the material returning device of the combustion device to participate in the next round of circulation, and the flue gas in the gas-solid mixture enters the tail flue from the top of the cyclone separator and then is discharged. The combustion scheme of the circulating fluidized bed provided by the invention can reduce the emission of nitrogen oxides in flue gas, has high denitration efficiency, and the bed material provided by the invention has low manufacturing cost and can be recycled.
Description
Technical Field
The invention relates to the technical field of combustion in a furnace, in particular to a circulating fluidized bed combustion method.
Background
Coal combustion is considered to be one of the main sources of atmospheric pollution in China. Due to the natural intrinsic energy of our country, the coal will be dominant for a long time in the future, and the clean coal combustion technology will become more and more important to solve the environmental problem. The circulating fluidized bed boiler combustion technology is internationally recognized as one of clean coal combustion technologies with the best commercialization degree due to the advantages of high combustion efficiency, strong fuel adaptability, low pollutant discharge and the like.
The circulating fluidized bed boiler adopts the in-furnace desulfurization technology and is characterized in that limestone particles and S are added into the furnaceO2Reacted to remove it. The circulating fluidized bed boiler has lower combustion temperature, has lower original emission of nitrogen oxides compared with a pulverized coal furnace, and can generally and directly meet the old emission standard of China. In recent years, the emission standard of coal-fired boilers in China is increasingly strict, the original emission of circulating fluidized bed boilers mostly cannot meet the new emission standard, and the development of the combustion technology of the circulating fluidized bed boiler with ultralow emission becomes urgent. The tail flue adopts SCR (Selective Catalytic Reduction) denitration technology, which can effectively reduce the emission of nitrogen oxides, but has higher operation cost and the problem of ammonia escape. The denitration cost is low by adopting SNCR (Selective non-Catalytic Reduction), but the denitration efficiency is low.
Disclosure of Invention
The present invention provides a circulating fluidized bed combustion method to overcome the above problems or at least partially solve the above problems.
According to one aspect of the present invention, there is provided a circulating fluidized bed combustion method comprising the process steps of:
placing a bed material containing metal oxide in a hearth of a combustion device, fluidizing by air, forming a dense-phase zone at the bottom of the hearth, and forming a dilute-phase zone at the middle upper part of the hearth;
placing fuel in the hearth for combustion, forming a reducing environment in the dense-phase zone and an oxidizing environment in the dilute-phase zone;
reducing the bed material in the dense-phase zone, fluidizing the reduced bed material into the dilute-phase zone, and carrying out oxidation-reduction reaction with nitrogen oxides in flue gas generated by combustion, wherein the reduced bed material is re-oxidized into metal oxides, and the nitrogen oxides are reduced into nitrogen;
and the gas-solid mixture generated in the hearth enters a cyclone separator of the combustion device, bed materials in the gas-solid mixture are separated and enter a dipleg of the cyclone separator, the bed materials are returned to the hearth through a material returning device of the combustion device to participate in the next round of circulation, and flue gas in the gas-solid mixture enters a tail flue of the combustion device from the top of the cyclone separator and then is discharged.
Optionally, the bed material is a material comprising a metal oxide of Fe2O3And CaO.
Optionally, the particle size of the bed material is 100-250 microns.
Optionally, the particle size of the fuel is 50-80 microns.
Optionally, the cyclone separator has a cutoff particle size of 80-100 microns.
Optionally SO in flue gas from combustion2Is removed by CaO in the bed material.
Optionally, the method further includes:
supplementing the bed material during operation of the combustion device to maintain system material balance.
The invention provides a circulating fluidized bed combustion method, based on the technical scheme provided by the invention, bed materials containing metal oxides in a hearth of a combustion device can be fluidized by air, when fuel is combusted in the hearth, the bed materials are reduced in reducing atmosphere of a dense-phase zone at the bottom of the hearth, then nitrogen oxides in smoke are reduced into nitrogen in a dilute-phase zone, and simultaneously the bed materials are reoxidized. The bed material provided by the invention can be used as a desulfurizer and a denitrifier at the same time, and can remarkably reduce SO in original flue gas of a boiler2And the bed material is low in manufacturing cost and can be recycled, and the circulating fluidized bed combustion method based on the bed material is simple and feasible, has wide application in the fields of energy, electricity, chemical industry, metallurgy and the like, and is particularly suitable for being adopted by circulating fluidized bed boilers with ultralow emission.
The foregoing description is only an overview of the technical solutions of the present invention, and the embodiments of the present invention are described below in order to make the technical means of the present invention more clearly understood and to make the above and other objects, features, and advantages of the present invention more clearly understandable.
The above and other objects, advantages and features of the present invention will become more apparent to those skilled in the art from the following detailed description of specific embodiments thereof, taken in conjunction with the accompanying drawings.
Drawings
Various other advantages and benefits will become apparent to those of ordinary skill in the art upon reading the following detailed description of the preferred embodiments. The drawings are only for purposes of illustrating the preferred embodiments and are not to be construed as limiting the invention. Also, like reference numerals are used to refer to like parts throughout the drawings. In the drawings:
fig. 1 is a schematic structural view of a combustion apparatus according to an embodiment of the present invention.
Detailed Description
Exemplary embodiments of the present disclosure will be described in more detail below with reference to the accompanying drawings. While exemplary embodiments of the present disclosure are shown in the drawings, it should be understood that the present disclosure may be embodied in various forms and should not be limited to the embodiments set forth herein. Rather, these embodiments are provided so that this disclosure will be thorough and complete, and will fully convey the scope of the disclosure to those skilled in the art.
The embodiment of the invention provides a circulating fluidized bed combustion method, which comprises the following process steps:
step S1, placing the bed material containing metal oxide in the hearth of the combustion device, fluidizing by air, forming a dense phase zone at the bottom of the hearth and a dilute phase zone at the middle upper part of the hearth;
step S2, placing the fuel in a hearth for combustion, forming a reducing environment in a dense-phase zone and an oxidizing environment in a dilute-phase zone;
step S3, the bed material in the dense phase zone is reduced, the reduced bed material is fluidized and enters the dilute phase zone, and the bed material and the nitrogen oxide in the flue gas generated by combustion are subjected to oxidation-reduction reaction, the reduced bed material is oxidized into metal oxide again, and the nitrogen oxide is reduced into nitrogen;
and step S4, the gas-solid mixture generated in the hearth enters a cyclone separator of the combustion device, the bed material in the gas-solid mixture is separated and enters a dipleg of the cyclone separator, the bed material is sent back to the hearth through a return feeder of the combustion device to participate in the next round of circulation, and the flue gas in the gas-solid mixture enters a tail flue of the combustion device from the top of the cyclone separator and then is discharged.
Based on the technical scheme provided by the invention, the bed material containing the metal oxide in the hearth of the combustion device can be fluidized by air, when fuel is combusted in the hearth, the bed material is reduced in the reducing atmosphere of the dense-phase zone at the bottom of the hearth, then the nitrogen oxide in the flue gas is reduced into nitrogen in the dilute-phase zone, and meanwhile, the bed material is reoxidized. Particularly for combustion of coal, coke, gasification carbon residue and other nitrogen-containing fuels, the circulating fluidized bed combustion method provided by the embodiment of the invention can obviously reduce the original emission of nitrogen oxides in combustion flue gas while ensuring the combustion efficiency, thereby ensuring that the denitration cost is reduced and the denitration efficiency is improved. The whole circulating fluidized bed combustion method is simple and feasible, has wide application in the fields of energy power, chemical industry, metallurgy and the like, and is particularly suitable for being adopted by circulating fluidized bed boilers with ultralow emission.
FIG. 1 is a schematic view of a combustion apparatus used in a circulating fluidized bed combustion process provided by an embodiment of the present invention. As shown in figure 1, the combustion device comprises a hearth 1, a cyclone separator 2, a material returning device 3 and a tail flue 4.
In the embodiment of the invention, when combustion is carried out, artificial metal oxide particles are used as bed materials and are fluidized by air in a hearth 1, a dense-phase zone 5 is formed at the bottom of the hearth, and a dilute-phase zone 6 is formed at the middle upper part of the hearth; the fuel is burnt in the hearth, an integral reducing environment is formed in the dense-phase zone 5 due to insufficient oxygen, an integral oxidizing environment is formed in the dilute-phase zone 6 due to excessive oxygen, the bed material is reduced in the dense-phase zone 5 at the bottom of the hearth, the bed material is fluidized, enters the dilute-phase zone 6 at the middle upper part of the hearth and then undergoes redox reaction with nitrogen oxide in the flue gas, the bed material is oxidized into metal oxide again, and the nitrogen oxide is reduced into nitrogen. Gas-solid mixture generated in the hearth 1 enters the cyclone separator 2, bed material is separated and enters the dipleg, the bed material is returned to the hearth through the material returning device 3 to participate in the next round of circulation, and flue gas enters the tail flue 5 from the top of the cyclone separator 2.
Optionally, the embodiment of the invention providesThe bed material may be a material comprising the metal oxide Fe2O3And CaO. The metal oxide plays a positive role in removing nitrogen oxides and sulfur dioxide, and also plays a positive role in maintaining the balance of circulating materials, enhancing heat exchange and the like as a bed material.
In the embodiment of the invention, the bed material containing the metal oxide can be used as a desulfurizer and a denitrifier at the same time, SO that SO in original flue gas generated during fuel combustion can be remarkably reduced2And nitrogen oxide emissions. Moreover, the bed material is low in manufacturing cost and can be recycled. In practical applications, the present invention is not limited as long as the materials capable of achieving the above effects can be used.
Preferably, the particle size of the bed material is preferably 100-250 microns, and the particle size of the fuel is preferably 50-80 microns; the cutoff particle size of the cyclone separator can be set at 80-100 microns, so that the bed materials can be effectively separated and sent back to the hearth, and fly ash with small particle size is taken out by flue gas.
Further, a certain amount of bed material can be supplemented during the operation of the combustion device to maintain the material balance of the system.
The embodiment of the invention provides a circulating fluidized bed combustion method, based on the technical scheme provided by the invention, bed materials containing metal oxides in a hearth of a combustion device can be fluidized by air, when fuel is combusted in the hearth, the bed materials are reduced in a reducing atmosphere in a dense-phase zone at the bottom of the hearth, then nitrogen oxides in flue gas are reduced into nitrogen in a dilute-phase zone, and simultaneously the bed materials are re-oxidized. By using the circulating fluidized bed combustion method provided by the embodiment of the invention, SO in original flue gas of a boiler can be obviously reduced2And nitrogen oxide emissions, and because ammonia injection is avoided, there is no ammonia slip problem. And the bed material has low manufacturing cost, can realize recycling, and further has low operation cost. The circulating fluidized bed combustion method based on the bed material is simple and feasible, has wide application in the fields of energy power, chemical industry, metallurgy and the like, and is particularly suitable for being adopted by circulating fluidized bed boilers with ultralow emission.
The above embodiments are described in detail below with reference to several preferred embodiments.
Example one
The tests were carried out in a 3 kW circulating fluidized bed combustion plant. The combustion plant is shown in fig. 1, in which the diameter of the furnace is 160 mm. The test fuel is Indonesian coal blended petroleum coke, and the mass ratio of the Indonesian coal blended petroleum coke to the Indonesian coal is 3: 1. The bed material adopts circulating ash, limestone and granular Fe2O3And FeO mixtures. After the system reaches the steady state, the test result is as follows: the temperature of the dilute phase zone at the upper part of the hearth is 889 ℃, and the volume fraction of oxygen at the outlet of the hearth is 3.7 percent. The nitrogen oxide emission is 41 mg/m3。
Comparative example 1
The combustion apparatus used was the same as in the first embodiment. The test fuel is Indonesian coal blended petroleum coke, and the mass ratio of the Indonesian coal blended petroleum coke to the Indonesian coal is 3: 1. The bed material is a conventional bed material, i.e. a mixture of circulating ash, limestone and quartz sand. After the system reaches the steady state, the test result is as follows: the temperature of the dilute phase zone at the upper part of the hearth is 880 ℃, and the volume fraction of oxygen at the outlet of the hearth is 3.6 percent. The nitrogen oxide emission is 252 mg/m3。
Example two
The combustion apparatus used was the same as in the first embodiment. The test fuel is Indonesian coal blended petroleum coke, and the mass ratio of the Indonesian coal blended petroleum coke to the Indonesian coal is 4: 1. The bed material in this example was the same as in example one. After the system reaches the steady state, the test result is as follows: the temperature of a dilute phase zone at the upper part of the hearth is 856 ℃, and the volume fraction of oxygen at the outlet of the hearth is 2.3 percent. The nitrogen oxide emission is 29mg/m3。
Comparative example 2
The combustion apparatus used was the same as in the first embodiment. The test fuel is Indonesian coal blended petroleum coke, and the mass ratio of the Indonesian coal blended petroleum coke to the Indonesian coal is 4: 1. The bed material used was the same as in comparative example 1. After the system reaches the steady state, the test result is as follows: the temperature of the dilute phase zone at the upper part of the hearth is 854 ℃, and the volume fraction of oxygen at the outlet of the hearth is 2.3 percent. The nitrogen oxide emission is 127 mg/m3。
By comparison, the amount of nitrogen oxide discharged by the circulating fluidized bed combustion method provided by the invention is obviously reduced compared with the amount of nitrogen oxide discharged by the conventional combustion method during combustion.
In the description provided herein, numerous specific details are set forth. It is understood, however, that embodiments of the invention may be practiced without these specific details. In some instances, well-known methods, structures and techniques have not been shown in detail in order not to obscure an understanding of this description.
Similarly, it should be appreciated that in the foregoing description of exemplary embodiments of the invention, various features of the invention are sometimes grouped together in a single embodiment, figure, or description thereof for the purpose of streamlining the disclosure and aiding in the understanding of one or more of the various inventive aspects. However, the disclosed method should not be interpreted as reflecting an intention that: that the invention as claimed requires more features than are expressly recited in each claim. Rather, as the following claims reflect, inventive aspects lie in less than all features of a single foregoing disclosed embodiment. Thus, the claims following the detailed description are hereby expressly incorporated into this detailed description, with each claim standing on its own as a separate embodiment of this invention.
Furthermore, those skilled in the art will appreciate that while some embodiments described herein include some features included in other embodiments, rather than other features, combinations of features of different embodiments are meant to be within the scope of the invention and form different embodiments. For example, in the claims, any of the claimed embodiments may be used in any combination.
Thus, it should be appreciated by those skilled in the art that while a number of exemplary embodiments of the invention have been illustrated and described in detail herein, many other variations or modifications consistent with the principles of the invention may be directly determined or derived from the disclosure of the present invention without departing from the spirit and scope of the invention. Accordingly, the scope of the invention should be understood and interpreted to cover all such other variations or modifications.
Claims (5)
1. A circulating fluidized bed combustion process comprising the process steps of:
placing a bed material containing metal oxide in a hearth of a combustion device, fluidizing by air, forming a dense-phase zone at the bottom of the hearth, and forming a dilute-phase zone at the middle upper part of the hearth;
placing fuel in the hearth for combustion, forming a reducing environment in the dense-phase zone and an oxidizing environment in the dilute-phase zone;
reducing the bed material in the dense-phase zone, fluidizing the reduced bed material into the dilute-phase zone, and carrying out oxidation-reduction reaction with nitrogen oxides in flue gas generated by combustion, wherein the reduced bed material is re-oxidized into metal oxides, and the nitrogen oxides are reduced into nitrogen;
the gas-solid mixture generated in the hearth enters a cyclone separator of the combustion device, bed materials in the gas-solid mixture are separated and enter a dipleg of the cyclone separator, the bed materials are returned to the hearth through a material returning device of the combustion device to participate in the next round of circulation, and flue gas in the gas-solid mixture enters a tail flue of the combustion device from the top of the cyclone separator and then is discharged;
the bed material comprises metal oxide Fe2O3And CaO; SO in flue gas generated by combustion2Is removed by CaO in the bed material.
2. The method of claim 1, wherein the bed material has a particle size of 100 to 250 microns.
3. The method of claim 1, wherein the fuel has a particle size of 50 to 80 microns.
4. The method of claim 1, wherein the cyclone has a cutoff particle size of 80 to 100 microns.
5. The method according to any one of claims 1-4, further comprising:
supplementing the bed material during operation of the combustion device to maintain system material balance.
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| CN111947171A (en) * | 2019-05-16 | 2020-11-17 | 新淳(上海)环保科技有限公司 | Denitration method for circulating fluidized bed boiler |
| CN110779010B (en) * | 2019-10-14 | 2021-07-02 | 华中科技大学 | Fluidized bed composite bed material with characteristics of slag bonding resistance and low NOx content |
| CN110594740B (en) * | 2019-11-08 | 2021-01-12 | 中国科学院广州能源研究所 | Micro-scale intensified combustion method for increasing oxygen ion concentration in flame |
| CN114797872B (en) * | 2022-04-29 | 2023-03-14 | 清华大学 | Medium-low temperature additive and process for jointly removing nitrous oxide and NOx in furnace |
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| KR101298667B1 (en) * | 2011-03-24 | 2013-08-21 | 주식회사 씨비비 | Apparatus for purifying exhaust gas |
| CN204891598U (en) * | 2015-07-20 | 2015-12-23 | 清华大学 | System for nitrogen oxide and oxysulfide in while desorption flue gas |
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