CN1231286C - A circulating fluidized bed process for cleaning fume by adding iron ash and its equipment - Google Patents
A circulating fluidized bed process for cleaning fume by adding iron ash and its equipment Download PDFInfo
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- CN1231286C CN1231286C CN 01115484 CN01115484A CN1231286C CN 1231286 C CN1231286 C CN 1231286C CN 01115484 CN01115484 CN 01115484 CN 01115484 A CN01115484 A CN 01115484A CN 1231286 C CN1231286 C CN 1231286C
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Abstract
The present invention relates to a method for purifying flue by using a circulating fluidized bed and adding iron flyash and an apparatus thereof. The present invention is characterized in that the flue after acceleration and exhausted from combustion equipment is sprayed into a fluidized bed reactor with a bed material composed of a calcium-based removing agent and an adsorbing agent, and the bed material is driven by the flue to be fluidized together; quicklime slurry and the iron flyash are added in the fluidized bed reactor to form the granules of an active absorbing agent and a desulfurizing agent, the granules can be used for improving desulfurization efficiency, and can be used for effectively removing fine granules PM2.5 and the heavy metals of As, Se and Hg. Compared with the prior art, the present invention has the characteristics of removal of multiple kinds of pollutants, high removal efficiency, simple technique, simple apparatus and strong load adaptability.
Description
The invention belongs to dry fume tail gas clean-up technical field, relate in particular to the method and apparatus of pollutant removing in the flue gas that pulverized-coal fired boiler, incinerator, grate firing boiler or other combustion apparatus hold in both hands out.
The semidry method or the dry type flue gas desulfurizing technology of coal-burning boiler or other the employed calcium-based desulfurizing agent of combustion apparatus mainly contain the spraying flue gas desulfurization method at present, in-furnace calcium spraying adds humidification activation method (LIFAC) and tail flue gas dry-type circulating fluidized bed desulfurization method.Preceding two technology calcium-based desulfurizing agent utilization rates are lower, generally at 0.3-0.4.Desulfuration efficiency is not high yet, is 2 o'clock at Ca/S, is 0.5-0.8.Simultaneously in reactor or the perishable and fouling of humidification activation device inwall.Tail flue gas circulating fluidized bed desulfur method has effectively overcome above-mentioned defective, and its calcium base utilization rate is higher, can reach 0.7, and its smoke desulfurization efficiency is also higher.This kind desulphurization system mainly comprises circulating fluid bed reactor, separator and outer loop back device.Its technical process is with the flue gas of boiler or the discharge of other combustion apparatus, sends into circulating fluid bed reactor, and its material is the mixture of calcium-based desulfurizing agent or desulfurizing agent and flying dust.Oxysulfide in the flue gas and the reaction of bed material form solid chemical compound, quantitatively discharge desulphurization system then.Discharge the sorbent particle suspension of the not complete reaction that flue gas leaves with recirculating fluidized bed, enter the particle separator of the multi-form routine that is arranged on the fluidized-bed reactor outside, and the solid particle that separator separates turned back in the circulating fluid bed reactor, finish cyclic process.In the practical project project, the common flying dust of above-mentioned use is subjected to certain limitation as the method desulfuration efficiency of recycle stock, and for the fine grained PM that produces in the coal-fired process
2.5With heavy metal As, Se, harmful substances such as Hg can't effectively remove, and directly influence the clean-up effect of flue gas.
At above-mentioned problems of the prior art, the purpose of this invention is to provide a kind of circulating fluidized bed process for cleaning fume and device thereof that adds iron ash.Use it can not only prevent inner-walls of duct corrosion and fouling, further improve the efficient of desulfurization, and can effectively remove the fine grained PM in the flue gas
2.5With heavy metal element As, Se, harmful substances such as Hg.
Technical scheme of the present invention realizes in the following way:
A kind of circulating fluidized bed process for cleaning fume that adds iron ash the steps include:
1. spray into after the flue gas combustion apparatus held in both hands out quickens through de Laval noz(zle) to remove in the flowing bed reactor that agent and adsorbent are the bed material and drive bed and expect fluidisation together with the calcium base;
2. spray into the quick lime slurries and in fluid mapper process, fully contact mixing with the flue gas that sprays into by being arranged on nozzle around the circulating fluid bed reactor with iron ash, alkaline matter taking place to the oxysulfide neutralization reaction, oxysulfide is converted into the solid chemical compound that can remove;
With quick lime slurry and iron ash formation remove the agent particle with fully the contacting in the mixed process of flue gas to the fine grained PM in the flue gas
2.5With heavy metal element As, Se, Hg etc. carry out strong adsorption;
4. will react the material that forms with absorption back stay remove in the agent with fixed form and not the bed of complete reaction expect to send into gas-solid separator with flue gas;
5. after gas-solid separator separated, solid particle entered fluidized-bed reactor and recycles, the clean flue gas after the purification by air-introduced machine by the chimney qualified discharge.
Realize the circulating fluidized bed process for cleaning fume and the device thereof of above-mentioned interpolation iron ash, it comprises with the calcium base and removes flowing bed reactor, the gas-solid separator that agent and adsorbent are the bed material.Its design feature is, the bottom inlet end of described fluidized-bed reactor is provided with the de Laval noz(zle) that flue gas is quickened, and the de Laval noz(zle) other end and smoke inlet pipe join.Be provided with iron ash inlet and lime white inlet around the bottom of fluidized-bed reactor.The top of fluidized-bed reactor is that exhanst gas outlet joins by connecting with gas-solid separator.The top of gas-solid separator is equipped with the clean gas outlet that is connected with air-introduced machine, and the below of gas-solid separator is equipped with in the tube connector and incoming stream fluidized bed reactor of material capable of circulation.
The present invention compared with prior art has the following advantages and good effect:
(1) on conventional dry recirculating fluidized bed flue gases purification basis, utilize the calcium base that contains iron ash to remove agent and react the sour gas of removing in the tail gas, remove fine grained PM simultaneously
2.5With heavy metal element As, Se, harmful substances such as Hg.Technology of the present invention is simple, compact conformation, and saving fund and floor space, gas cleaning is effective, satisfies environmental requirement fully, and flue gas is held in both hands to amplify and is lower than present environmental protection standard greatly.
(2) in removing the process of pollutant, the bed material keeps the relatively dry state, has effectively avoided corrosive pipeline and blockage problem in wet method and the semidry method cleaning system.
(3) owing to adopt the dry-type circulating fluidized bed desulfurization technology, the required moisture of equipment is few, and product is dry state, has reduced water consumption, has avoided the water pollution problems in the wet method, and has reduced the processing cost of product.
Below in conjunction with accompanying drawing and concrete embodiment the present invention is described further.
Accompanying drawing is an apparatus structure connection layout of implementing the inventive method.
The concrete steps of the inventive method are: spray into after the flue gas that (1) holds in both hands out combustion apparatus quickens through de Laval noz(zle) to remove in the flowing bed reactor that agent and adsorbent are the bed material and drive bed with the calcium base and expect fluidisation together, fluidizing velocity is designed to 5-10m/s:(2) spray into the quick lime slurries and in fluid mapper process, fully contact mixing with the flue gas that sprays into by being arranged on nozzle around the circulating fluid bed reactor with iron ash, alkaline matter takes place to the oxysulfide neutralization reaction, oxysulfide is converted into the solid chemical compound that can remove, the granularity of described iron ash particle is less than 100 μ m, wherein Fe
2O
3Content is not less than 10%; (3) with quick lime slurry and iron ash formation remove the agent particle with fully the contacting in the mixed process of flue gas to the fine grained PM in the flue gas
2.5With heavy metal element As, Se, Hg etc. carry out strong adsorption; (4) will react the material that forms with absorption back stay remove in the agent with fixed form and not the bed of complete reaction expect to send into gas-solid separator with flue gas; (5) after gas-solid separator separated, solid particle entered fluidized-bed reactor and recycles, and the clean flue gas after the purification is put by chimney handful up to standard by air-introduced machine.
Referring to accompanying drawing, implement the device of the inventive method, it comprises with the calcium base and removes agent and adsorbent is flowing bed reactor 3, the gas-solid separator 6 of bed material.The bottom inlet end of described fluidized-bed reactor 3 is provided with the de Laval noz(zle) 1 that flue gas is quickened, the thick hyperbola pipe in thin two ends in the middle of the shape of de Laval noz(zle) 1 is.De Laval noz(zle) 1 other end and smoke inlet pipe 9 join.The bottom of fluidized-bed reactor 3 is provided with iron ash inlet 8 and lime white inlet 2.Fluidized-bed reactor 3 tops are that exhanst gas outlet joins by tube connector 4 and gas-solid separator 6.The top of gas-solid separator 6 is equipped with the clean gas outlet 5 that is connected with air-introduced machine, and the below of gas-solid separator 6 is equipped with in the tube connector 7 and incoming stream fluidized bed reactor 3 of material capable of circulation.
When this device uses, the flue gas that comes out from combustion apparatus, by smoke inlet pipe 9, after de Laval noz(zle) 1 acceleration, enter circulating fluid bed reactor 3, flue gas fully contacts with original material with the lime slurry that enters from lime white entrance 2 in fluidized-bed reactor 3, drives bed and expects fluidisation together, fluidizing velocity fully conducts heat and mass transfer simultaneously up to 3-10m/s.In addition, the iron ash inlet 8 by fluidized-bed reactor 3 bottoms replenishes the iron ash that adds in the recycle stock.In this process, sour gas such as carbon dioxide, sulfur trioxide etc. and the calcium base alkali compounds generation neutralization reaction that contains iron ash in the tail gas generate solid calcium salt, simultaneously fine grained PM in the tail gas
2.5With heavy metal element As, Se, harmful substances such as Hg with bed expect in the abundant mixed process by in the bed material contain iron ash to remove agent adsorbed and remove.Solid particle after reaction and the absorption enters gas-solid separator 6 with the exhanst gas outlet of air-flow process reactor by tube connector 4, and purified gas discharges by clean gas outlet 5 through air-introduced machine.Gas-solid separator 6 removes the solid particle that gets off and turns back in the fluidized-bed reactor 3 by recycle stock tube connector 7 and recycle.This device desulfuration efficiency can reach more than 95%, fine grained PM
2.5With heavy metal element As, Se, harmful substance removal rates such as Hg are more than 90%.
Claims (5)
1. circulating fluidized bed process for cleaning fume that adds iron ash, its step is; 1. spray into after the flue gas that combustion apparatus is discharged quickens through de Laval noz(zle) to remove in the flowing bed reactor that agent and adsorbent are the bed material and drive bed and expect fluidisation together with the calcium base; 2. spray into the quick lime slurries and in fluid mapper process, fully contact mixing with the flue gas that sprays into by being arranged on nozzle around the circulating fluid bed reactor with iron ash, alkaline matter taking place to the oxysulfide neutralization reaction, oxysulfide is converted into the solid chemical compound that can remove; 3. with quick lime slurry and iron ash formation remove the agent particle with fully the contacting in the mixed process of flue gas to fine grained in the flue gas (PM2.5) and heavy metal element As, Se, Hg etc. carry out strong adsorption: 4. will react the material that forms with absorption back stay remove in the agent with fixed form and not the bed of complete reaction expect to send into gas-solid separator with flue gas; 5. after gas-solid separator separated, solid particle entered fluidized-bed reactor and recycles, the clean flue gas after the purification by air-introduced machine by the chimney qualified discharge.
2. according to the circulating fluidized bed process for cleaning fume of the described interpolation iron ash of claim 1, it is characterized in that: the fluidizing velocity in the described circulating fluid bed reactor is designed to 3-10m/s.
3. according to the circulating fluidized bed process for cleaning fume of claim 1 or 2 described interpolation iron ash, it is characterized in that: the granularity of described iron ash particle is less than 100m, wherein Fe
2O
3Content is not less than 10%.
4. realize the device of the circulating fluidized bed process for cleaning fume of claim 1 or 3 described interpolation iron ash, it comprises with the calcium base and removes the flowing bed reactor (3) that agent and adsorbent are the bed material, gas-solid separator (6), it is characterized in that: the bottom inlet end of described fluidized-bed reactor (3) is provided with the de Laval noz(zle) (1) that flue gas is quickened, compiling blooie pipe (1) other end and smoke inlet pipe (9) joins, the bottom of fluidized-bed reactor (3) is provided with iron ash inlet (8) and lime white inlet (2), the top of fluidized-bed reactor (3) is that exhanst gas outlet passes through tube connector (4) and gas-solid separator (6) joins, the top of gas-solid separator (6) is equipped with the clean gas outlet (5) that is connected with air-introduced machine, and the below of gas-solid separator (6) is equipped with in the tube connector (7) and incoming stream fluidized bed reactor (3) of material capable of circulation.
5. according to the device of the circulating fluidized bed process for cleaning fume of the described interpolation iron ash of claim 4, it is characterized in that: the thick hyperbola pipe in thin two ends in the middle of the shape of described de Laval noz(zle) (1) is.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 01115484 CN1231286C (en) | 2001-04-28 | 2001-04-28 | A circulating fluidized bed process for cleaning fume by adding iron ash and its equipment |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 01115484 CN1231286C (en) | 2001-04-28 | 2001-04-28 | A circulating fluidized bed process for cleaning fume by adding iron ash and its equipment |
Publications (2)
| Publication Number | Publication Date |
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| CN1382516A CN1382516A (en) | 2002-12-04 |
| CN1231286C true CN1231286C (en) | 2005-12-14 |
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| Application Number | Title | Priority Date | Filing Date |
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| CN 01115484 Expired - Lifetime CN1231286C (en) | 2001-04-28 | 2001-04-28 | A circulating fluidized bed process for cleaning fume by adding iron ash and its equipment |
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Families Citing this family (13)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| BE1015949A3 (en) * | 2004-03-15 | 2005-12-06 | Lhoist Rech & Dev Sa | Method for reduction of mercury and heavy metal smoke gas. |
| CN100441270C (en) * | 2005-01-13 | 2008-12-10 | 清华大学 | Adhesive flume absorbable grain purification method and its device |
| CN101480555B (en) * | 2008-12-23 | 2011-06-22 | 东华大学 | Integrated control method capable of simultaneously removing inhalable particles and heavy metal from fire coal |
| US9074767B2 (en) * | 2010-02-11 | 2015-07-07 | Alstom Technology Ltd | Rotary bottom ash regeneration system |
| CN102059052A (en) * | 2010-10-22 | 2011-05-18 | 天津聚贤技术研发中心 | Method for integrally desulphurizing, denitrating and dedusting flue gas by double-nozzle rectangular spouted bed |
| CN102671509A (en) * | 2012-06-04 | 2012-09-19 | 中国华能集团清洁能源技术研究院有限公司 | Device and method for removing volatile trace elements from coal-fired flue |
| CN103657330B (en) * | 2012-09-03 | 2015-12-02 | 杨凯翔 | Industrial waste gas treatment system and processing method |
| CN103239985B (en) * | 2013-05-14 | 2016-04-20 | 中国环境科学研究院 | Efficient fuel coal flue gas desulfurizing and hydrargyrum-removing method and device thereof |
| CN104941435B (en) * | 2015-06-19 | 2017-06-13 | 清华大学 | A kind of semidry-method recirculating fluidized bed flue gas desulphurization system of normal temperature and method |
| CN107020195A (en) * | 2017-04-13 | 2017-08-08 | 东南大学 | A kind of device and method of coal tar oxygen carrier granule separation |
| CN107158942A (en) * | 2017-06-30 | 2017-09-15 | 合肥天翔环境工程有限公司 | A kind of sintering furnace flue-gas dust-removing and desulfurization system |
| CN108325307B (en) * | 2017-12-28 | 2019-05-10 | 中南大学 | Based on the sintering flue gas PM for strengthening bed of material absorption2.5Discharge-reducing method |
| CN110330062B (en) * | 2019-06-28 | 2020-08-14 | 华中科技大学 | Heterogeneous coagulation adsorbent for heavy metal adsorption and preparation method and application thereof |
-
2001
- 2001-04-28 CN CN 01115484 patent/CN1231286C/en not_active Expired - Lifetime
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| CN1382516A (en) | 2002-12-04 |
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Owner name: QINGHUA UNIVERSITY; TONGFANG CO., LTD. Free format text: FORMER NAME OR ADDRESS: QINGHUA UNIVERSITY; TSINGHUA TONGFANG CO., LTD. |
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Address after: 100083 Beijing Tsinghua Tongfang science and Technology Square A block 2907 Co-patentee after: Tongfang Co., Ltd. Patentee after: Tsinghua University Address before: 100083 Beijing Tsinghua Tongfang science and Technology Square A block 2907 Co-patentee before: Qinghua Tongfang Co., Ltd. Patentee before: Tsinghua University |
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Effective date of registration: 20081212 Address after: A, Tsinghua Tongfang science and Technology Square, Beijing 2907, postcode: 100083 Co-patentee after: Tongfang Environment Co., Ltd. Patentee after: Tsinghua University Address before: Beijing Tsinghua Tongfang science and Technology Square, block A, 2907, post code: 100083 Co-patentee before: Tongfang Co., Ltd. Patentee before: Tsinghua University |
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