CN101053764A - Twin tower circulating fluidized bed fume desulfurizing method and device - Google Patents
Twin tower circulating fluidized bed fume desulfurizing method and device Download PDFInfo
- Publication number
- CN101053764A CN101053764A CN 200710037863 CN200710037863A CN101053764A CN 101053764 A CN101053764 A CN 101053764A CN 200710037863 CN200710037863 CN 200710037863 CN 200710037863 A CN200710037863 A CN 200710037863A CN 101053764 A CN101053764 A CN 101053764A
- Authority
- CN
- China
- Prior art keywords
- tower
- gas
- ash bucket
- flue gas
- solid separator
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Granted
Links
Images
Abstract
The invention relates to a double-tower cycle fluidized bed flue gas desulfurization method and a device, which comprises a desulfurization reaction tower, a sprayer, a digestor, a revert unit, a gas-solid separator and a ash hopper thereof, and is characterized in that the dirty flue gas discharged by combustion equipment is divided into two parts: wherein one part enters into the king tower, and the other part enter into the tail tower formed by the ash hopper of the gas-solid separator. The advantage is that the flue gas can move is a lower temperature in the desulfurization reaction king tower, the efficiency of desulfurization is high, and volume of the king tower is small; the cycle ash can be heated effectively in the ash hopper, has a good fluidity without the defect of glue, fouling and corrosion, and the reliability of the device is well; and the invention can greatly reduce the electric heating power and energy consumption of desulfurization.
Description
Technical field
The present invention relates to a kind of flue gas desulfurization technique and device, relate in particular to a kind of circulating fluid bed flue gas desulfurization method and device, be used for removing sulfur oxide and other harmful sour gas of the flue gas of discharging by boiler or other combustion apparatus, as HCL, HF etc.
Background technology
In common circulating fluid bed flue-gas desulfurizing technology, as technology such as CFB-FGD, RCFB-FGD and NID, be that calcium hydroxide and water are sent in the desulfurizing tower with flue gas mixing and reaction, desulfurization product separates through gas-solid separator, fall into ash bucket, great majority are sent desulfurizing tower by strength skewed slot and material-returning device back to as recycle stock and are continued to participate in reaction.In above-mentioned technology, along with the reduction of flue-gas temperature moves closer to dew-point temperature, smoke desulfurization efficiency also significantly improves thereupon, but the risk that the bonding of recycle stock and conglomeration are stopped up also increases, especially at the ash bucket place.In order to take into account the reliability of desulfuration efficiency and device, in the flue gas desulfurization of coal-burning boiler, the temperature of circulating fluidized bed desulfurization tower is controlled at about 70 ℃ usually, and needs ash bucket is taked the measure of electricity or steam heated insulation.The further raising that this limits smoke desulfurization efficiency on the one hand also will expend a large amount of electricity or steam on the other hand, makes operating cost increase.These prior aries all are that all flue gases that combustion apparatus is discharged all are sent in the desulfurizing tower in addition, cause common desulfurizing tower all to need a relatively large volume.
Summary of the invention
The objective of the invention is in order to overcome above-mentioned the deficiencies in the prior art, provide a kind of flue gas that utilizes that ash bucket is heated, and a kind of twin tower circulating fluidized bed fume desulfurizing method and device that part of smoke is reacted in ash bucket.
The objective of the invention is to be achieved through the following technical solutions: a kind of twin tower circulating fluidized bed fume desulfurizing method, it is that the dirty flue gas that combustion apparatus is got rid of is sent in the desulfurization reaction tower, through spray cooling, with reactive desulfurizing agent, desulfurization product is separated by gas-solid separator, falls into ash bucket, sends desulfurizing tower back to by strength skewed slot and material-returning device, be characterized in: the dirty flue gas that combustion apparatus is discharged is divided into two: the one tunnel enters normally used desulfurization reaction tower, i.e. king-tower; The desulphurization reaction secondary tower that the dirty flue gas in another road constitutes by ash bucket below gas-solid separator, the dirty flue gas that enters king-tower through with water, desulfurizing agent and recycle stock hybrid reaction after, carry mixed material and enter gas-solid separator, another road enters into the dirty flue gas of secondary tower after fallen mixed material carries out fluidized reaction with gas-solid separator, also enter same gas-solid separator, two-way is discharged from gas-solid separator through the cleaning flue gases of desulfurization and dedusting.
In said method, the dirty flue gas that enters the desulphurization reaction secondary tower passageway of ash bucket of flowing through earlier, dirty flue gas heats ash bucket, and the periphery from the ash bucket bottom evenly enters ash bucket again, be the desulphurization reaction secondary tower, this can thoroughly be avoided the fallen material of gas-solid separator to deposit conglomeration on ash bucket.
A kind of twin tower circulating fluidized bed fume desulfurizing device of realizing above-mentioned flue gas desulfurization technique method, it comprises desulfurization reaction tower, digester, material-returning device, gas-solid separator and ash bucket thereof and strength skewed slot, be characterized in: described desulfurization reaction tower is made up of the major-minor double tower, king-tower is normally used form, secondary tower ash bucket and strength skewed slot below gas-solid separator are formed, inclined-plane at ash bucket is provided with the passageway, and bellows are arranged on the top of ash bucket, and exhanst gas outlet is distributed on the ash bucket bottom.
Because characteristics of the present invention are that the dirty flue gas that will be got rid of by combustion apparatus is divided into two: the one tunnel enters king-tower; Another road enters the secondary tower that is formed by the gas-solid separator ash bucket, therefore, the invention has the beneficial effects as follows, is that flue gas can be with lower temperature operation in the desulphurization reaction king-tower, the desulfuration efficiency height, and reaction king-tower volume is little; Circulating ash can effectively be heated in ash bucket, good fluidity, the sorrow of no bonding, fouling and corrosion, the good reliability of device; Can significantly reduce the electricity or the steam consumption of heating ash bucket, the desulfurization energy consumption is little.
Description of drawings
Accompanying drawing 1 is a kind of structural representation of twin tower circulating fluidized bed fume desulfurizing device.
Accompanying drawing 2 is the A-A cutaway view of accompanying drawing 1, expresses grey bucket structure and shape.
Specify technical process of the present invention, operation principle, design feature and preferred forms below in conjunction with accompanying drawing:
By shown in Figure 1, device of the present invention mainly comprises desulphurization reaction king-tower 3, gas-solid separator 5 and ash bucket 6, desulphurization reaction king-tower 3 joins with gas-solid separator 5 by connecting flue 4, lower disposed at gas-solid separator 5 has ash bucket 6, strength skewed slot 7 is arranged in the bottom of ash bucket 6, arrange outlet 8 of desulfurization ash and material-returning device 9 on strength skewed slot 7, dirty flue gas is divided into two respectively and enters desulphurization reaction king-tower and gas approach 2 from gas approach 1 to enter ash bucket 6 be the desulphurization reaction secondary tower.Dirty flue gas is same water in the desulphurization reaction king-tower, after desulfurizing agent and the recycle stock hybrid reaction, sour gas is wherein effectively removed, dirty flue gas enters gas-solid separator 5 along air flow direction 11, the mixed material that gas-solid separator 5 separates, the desulfurizing agent that contains a large amount of not complete reactions, fall under gravity into ash bucket 6, another road enters into the dirty flue gas of secondary tower with the abundant fluidisation hybrid reaction of these mixed materials, sour gas is also efficiently removed, dirty flue gas upwards directly enters gas-solid separator 5, gas-solid separator 5 is removed solid particles most in two strands of dirty flue gases, finally, cleaning flue gases is discharged by the exhanst gas outlet 10 that is located on the separator, wherein Jue Dabufen mixed material returns desulphurization reaction king-tower 3 as recycle stock by strength skewed slot 7 and material-returning device 9, and is remaining from desulfurization ash outlet 8 discharges.
The desulfuration efficiency of circulating fluid bed flue-gas desulfurizing is to improve along with the reduction of flue-gas temperature, but the corresponding increase of the moisture content of recycle stock, the risk that the bonding of recycle stock and conglomeration are stopped up also increases.In common circulating fluid bed flue-gas desulfurizing technology, because the effect of heat radiation, the temperature levels at ash bucket place is minimum, mixed material is in sliding mode again herein, for fear of the bonding of mixed material, to coal burning flue gas desulfurization the time, generally need its temperature is controlled at more than 65 ℃, though mixed material fluidisation turbulence in desulfurizing tower is strong, be difficult for bonding, the temperature of desulfurizing tower also can only be controlled at about 70 ℃.The present invention adopts the bypass part of smoke that the recycle stock in the ash bucket is heated method with fluidisation, because the space of ash bucket is very big, this part flue gas generally is lower than 0.5 meter per second at ash bucket along the average speed of short transverse, the flue gas time of staying herein is than much longer in king-tower, and flue gas can mix fluidisation fully with recycle stock, so acidic gas in flue gas can obtain efficient chemical combination.Flue gas is in king-tower and the reaction of secondary tower two places like this, to coal-fired flue gas desulfurization the time, one can improve the temperature levels of ash bucket place recycle stock significantly, generally be that it is brought up to about 80 ℃ from 60 ℃, the temperature of ash bucket shell can be brought up to more than 90 ℃, prevents the bonding and the conglomeration obstruction of recycle stock effectively; Two can be reduced to the operation flue-gas temperature of desulphurization reaction king-tower about 60 ℃ from 70 ℃, significantly improve smoke desulfurization efficiency; Three can reduce by desulphurization reaction king-tower exhaust gas volumn, dwindle reaction king-tower volume.To the refuse furnace deacidifying flue gas time because the hygroscopicity of calcium chloride, deacidifying device temperature everywhere should corresponding raising.
In said method, the exhaust gas temperature of combustion apparatus such as boiler is generally 140 ℃, the exhaust gas volumn that enters the desulphurization reaction secondary tower is big more, the temperature rise of ash bucket shell and mixed material is high more, and the effect of anti-stick is good more, but it is short more in the time of staying of desulphurization reaction secondary tower, desulfuration efficiency also decreases, when the exhaust gas volumn that enters secondary tower greater than 30% the time, the smoke desulfurization efficiency of secondary tower obviously descends, perhaps need with the volume of secondary tower do very big.The ratio that the dirty exhaust gas volumn that enters the desulphurization reaction secondary tower accounts for total exhaust gas volumn is 5%～30%, can effectively heat recycle stock like this, prevents that the bonding of recycle stock and conglomeration from stopping up, and can guarantee the desulfuration efficiency of desulphurization reaction secondary tower again.
In said method, combustion apparatus such as boiler 16, flue-gas temperature behind the heating surface 17 is different everywhere, exhaust gas temperature is minimum, for ash bucket is carried out more effective heating, can extract warm flue gas the some out from the middle part of combustion apparatus, adopt flue to link to each other with the inlet of king-tower and secondary tower, warm adjustment doors 18 and low temperature adjustment doors 19 in flue, being provided with, by adjustment to these two adjustment doors apertures, make high-temperature flue gas in the dirty flue gas blending some that enters the desulphurization reaction secondary tower, mixing temperature reaches 160 ℃～300 ℃, warm flue gas during the dirty flue gas that perhaps will enter the desulphurization reaction secondary tower all uses makes its temperature reach 300 ℃～450 ℃.The raising of flue-gas temperature can reduce the exhaust gas volumn that enters the desulphurization reaction secondary tower, reduces the flue-gas temperature level of desulphurization reaction king-tower, improves the smoke desulfurization efficiency of desulphurization reaction main and auxiliary tower.
Shown in accompanying drawing 2, the inclined-plane of ash bucket 6 of the present invention is provided with passageway 13, and bellows 12 are arranged on the top of ash bucket, and exhanst gas outlet 14 is distributed on the ash bucket bottom.After flue gas enters bellows, shown in flue gas flow direction 11, in passageway 13, from top to bottom flow, after the ash bucket heating, enter ash bucket from exhanst gas outlet 14, the recycle stock of falling the ash bucket inclined-plane can be slipped in the skewed slot 7 smoothly.
Better scheme is, being provided with shape of cross section above exhanst gas outlet is the homogenizing plate 15 of taper, on described homogenizing plate 15, be evenly equipped with a plurality of passages, after flue gas enters ash bucket, under the effect of taper homogenizing plate 15, evenly pass through ash bucket, taper homogenizing plate cocycle material can natural landing, dust stratification can not take place.
Gas-solid separator 5 can be electrostatic precipitator or sack cleaner, it also can be inertia or cyclone dust collectors assembly with electrostatic precipitator or sack cleaner, when adopting electrostatic precipitator,, should reduce the ratio that enters the secondary tower exhaust gas volumn in order to improve efficiency of dust collection.
Claims (7)
1. twin tower circulating fluidized bed fume desulfurizing method, it is that the dirty flue gas that combustion apparatus is got rid of is sent in the desulfurization reaction tower, through spray cooling, with reactive desulfurizing agent, desulfurization product is separated by gas-solid separator, falls into ash bucket, sends desulfurizing tower by strength skewed slot and material-returning device back to as recycle stock, it is characterized in that: the dirty flue gas that combustion apparatus is discharged is divided into two: the one tunnel enters normally used desulfurization reaction tower, i.e. king-tower; The desulphurization reaction secondary tower that another road constitutes by ash bucket below gas-solid separator, the dirty flue gas that enters king-tower through with water, desulfurizing agent and recycle stock hybrid reaction after, carry mixed material and enter gas-solid separator, another road enters into the dirty flue gas of secondary tower after fallen mixed material carries out fluidized reaction with gas-solid separator, also enter same gas-solid separator, two-way is discharged from gas-solid separator through the cleaning flue gases of desulfurization and dedusting.
2. method according to claim 1 is characterized in that: the dirty flue gas that enters the desulphurization reaction secondary tower passageway of ash bucket of flowing through earlier, and dirty flue gas heats ash bucket, and the periphery from the ash bucket bottom evenly enters ash bucket again.
3. method according to claim 1 is characterized in that: the ratio that the dirty exhaust gas volumn that enters the desulphurization reaction secondary tower accounts for total exhaust gas volumn is 5%～30%.
4. method according to claim 1 is characterized in that: to high-temperature flue gas in the dirty flue gas blending some that enters the desulphurization reaction secondary tower, make its mixing temperature reach 160 ℃～300 ℃.
5. method according to claim 1 is characterized in that: the dirty flue gas that enters the desulphurization reaction secondary tower is all extracted out from the middle-temperature section of combustion apparatus, and its temperature is 300 ℃～450 ℃.
6. twin tower circulating fluidized bed fume desulfurizing device of realizing the described fume desulphurization method of claim 1, it comprises desulfurization reaction tower, digester, material-returning device, gas-solid separator and ash bucket thereof and strength skewed slot, it is characterized in that: described desulfurization reaction tower is made up of the major-minor double tower, king-tower is normally used form, secondary tower ash bucket and strength skewed slot below gas-solid separator are formed, inclined-plane at ash bucket is provided with the passageway, bellows are arranged on the top of ash bucket, and exhanst gas outlet is distributed on the ash bucket bottom.
7. twin tower circulating fluidized bed fume desulfurizing device according to claim 6 is characterized in that: be provided with the homogenizing plate that shape of cross section is taper above described exhanst gas outlet, be evenly equipped with a plurality of passages on described homogenizing plate.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB2007100378636A CN100490948C (en) | 2007-03-07 | 2007-03-07 | Twin tower circulating fluidized bed fume desulfurizing method and device |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB2007100378636A CN100490948C (en) | 2007-03-07 | 2007-03-07 | Twin tower circulating fluidized bed fume desulfurizing method and device |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN101053764A true CN101053764A (en) | 2007-10-17 |
| CN100490948C CN100490948C (en) | 2009-05-27 |
Family
ID=38793921
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CNB2007100378636A Expired - Fee Related CN100490948C (en) | 2007-03-07 | 2007-03-07 | Twin tower circulating fluidized bed fume desulfurizing method and device |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN100490948C (en) |
Cited By (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101879410A (en) * | 2010-07-20 | 2010-11-10 | 辽宁科林环保工程有限责任公司 | Controllable flue gas desulfurization method and system for coal-fired power station boiler |
| CN101829494B (en) * | 2009-03-11 | 2012-10-31 | 上海立谊环保工程技术有限公司 | Dry ash wetting and recycling technology for desulfurizing sintered fume by rotary spraying and drying method |
| CN104338422A (en) * | 2013-07-29 | 2015-02-11 | 碧水蓝天环境工程有限公司 | Desulfurization device and desulphurization method thereof |
| CN107670491A (en) * | 2017-10-24 | 2018-02-09 | 上海电力学院 | Improve the device of fume circulating fluidized bed desulfurization system material return mechanism characteristic using heat smoke |
| CN109647148A (en) * | 2019-02-28 | 2019-04-19 | 兖矿集团有限公司 | A kind of circulating fluidized bed boiler flue gas desulphurization system and its processing method |
| CN110182838A (en) * | 2019-06-25 | 2019-08-30 | 湘潭大学 | A kind of modified technique system and method for flue gas desulfurization ash |
| CN112791554A (en) * | 2020-12-31 | 2021-05-14 | 清华大学 | Flue gas treatment method and system |
| CN112947623A (en) * | 2021-01-27 | 2021-06-11 | 华能国际电力股份有限公司营口电厂 | Intelligent control method for electric dust removal and ash conveying steam heat tracing system |
| CN113318871A (en) * | 2021-05-20 | 2021-08-31 | 内蒙古万邦清源环保科技有限公司 | Method for preparing carbon superfine powder material from coal chemical industry byproduct gasified slag |
-
2007
- 2007-03-07 CN CNB2007100378636A patent/CN100490948C/en not_active Expired - Fee Related
Cited By (11)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101829494B (en) * | 2009-03-11 | 2012-10-31 | 上海立谊环保工程技术有限公司 | Dry ash wetting and recycling technology for desulfurizing sintered fume by rotary spraying and drying method |
| CN101879410A (en) * | 2010-07-20 | 2010-11-10 | 辽宁科林环保工程有限责任公司 | Controllable flue gas desulfurization method and system for coal-fired power station boiler |
| CN101879410B (en) * | 2010-07-20 | 2012-12-26 | 辽宁科林环保工程有限责任公司 | Controllable flue gas desulfurization method and system for coal-fired power station boiler |
| CN104338422A (en) * | 2013-07-29 | 2015-02-11 | 碧水蓝天环境工程有限公司 | Desulfurization device and desulphurization method thereof |
| CN107670491A (en) * | 2017-10-24 | 2018-02-09 | 上海电力学院 | Improve the device of fume circulating fluidized bed desulfurization system material return mechanism characteristic using heat smoke |
| CN109647148A (en) * | 2019-02-28 | 2019-04-19 | 兖矿集团有限公司 | A kind of circulating fluidized bed boiler flue gas desulphurization system and its processing method |
| CN110182838A (en) * | 2019-06-25 | 2019-08-30 | 湘潭大学 | A kind of modified technique system and method for flue gas desulfurization ash |
| CN110182838B (en) * | 2019-06-25 | 2023-10-17 | 湘潭大学 | Modification process system and method for flue gas desulfurization ash |
| CN112791554A (en) * | 2020-12-31 | 2021-05-14 | 清华大学 | Flue gas treatment method and system |
| CN112947623A (en) * | 2021-01-27 | 2021-06-11 | 华能国际电力股份有限公司营口电厂 | Intelligent control method for electric dust removal and ash conveying steam heat tracing system |
| CN113318871A (en) * | 2021-05-20 | 2021-08-31 | 内蒙古万邦清源环保科技有限公司 | Method for preparing carbon superfine powder material from coal chemical industry byproduct gasified slag |
Also Published As
| Publication number | Publication date |
|---|---|
| CN100490948C (en) | 2009-05-27 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN100490948C (en) | Twin tower circulating fluidized bed fume desulfurizing method and device | |
| CN102872712B (en) | Semi-dry-process desulfurization apparatus | |
| CN100467100C (en) | Circulating suspension state dried method desulfurizing technology and special purpose desulfurizing tower thereof | |
| CN105597475A (en) | United roller method desulfurization and dust removal purifying device system | |
| CN201302374Y (en) | Selective desulfurization device for flue gas of sintering machine head | |
| CN101077470A (en) | Composite humidifying process suitable for circulating fluid bed semi-drying method flue gas desulfurization | |
| CN110975582A (en) | Flue gas desulfurization, denitrification and dust removal system of biomass circulating fluidized bed boiler | |
| CN105327602A (en) | Floating glass melting furnace flue gas waste heat utilization and denitration purification treatment device | |
| CN201389423Y (en) | Flue gas desulphurization dust removing tower for coal burning boiler | |
| CN206295800U (en) | A kind of semi-dry flue gas desulfurization device | |
| CN2647417Y (en) | Double-side variable speed multi-circulating fluidized flue gas desulfurization apparatus | |
| CN102350211B (en) | Three-stage desulfurization device for circulating fluidized bed boiler | |
| CN205007834U (en) | Float glass melting furnace flue gas waste heat utilization and denitration purification unit | |
| CN107352614A (en) | A kind of wet desulphurization wastewater zero emission treatment method and system | |
| CN204447734U (en) | A kind of Pneumatic emulsifying desulfurization and dedusting integrated tower and system thereof | |
| CN201439047U (en) | Recycling material fluidization conveying device of semi-dry desulphurization system | |
| CN203671593U (en) | Internal and external cooperated pollutant removing device for boiler of flow state reconstructed circulating fluidized bed | |
| CN201108808Y (en) | Prepositioned cyclone pre-dedusting SCR smoke-gas denitration device | |
| CN107321166B (en) | Semi-dry desulfurization device | |
| CN1745875A (en) | Assembling device of double-stage wetting dust-proof desulfurizer | |
| CN201421186Y (en) | High-efficiency energy-saving emission-reducing organic heat carrier boiler of circulating fluidize bed | |
| CN103398371B (en) | A kind of two low type boiler using high basic metal coal | |
| CN203507814U (en) | Efficient circulating fluidized bed desulfurizer | |
| CN2753974Y (en) | Wet desulfurizing dust-remover | |
| CN207175528U (en) | A kind of wet desulphurization Wastewater zero-discharge treatment system |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| C17 | Cessation of patent right | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20090527 Termination date: 20130307 |