CN101666495A - Method for controlling material return quantity of hearth of circulating fluidized bed boiler - Google Patents
Method for controlling material return quantity of hearth of circulating fluidized bed boiler Download PDFInfo
- Publication number
- CN101666495A CN101666495A CN200910094925A CN200910094925A CN101666495A CN 101666495 A CN101666495 A CN 101666495A CN 200910094925 A CN200910094925 A CN 200910094925A CN 200910094925 A CN200910094925 A CN 200910094925A CN 101666495 A CN101666495 A CN 101666495A
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- boiler
- fluidized bed
- feed back
- circulating fluidized
- air
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- 238000000034 method Methods 0.000 title claims abstract description 13
- 239000000463 material Substances 0.000 title abstract description 13
- 230000008878 coupling Effects 0.000 claims description 2
- 238000010168 coupling process Methods 0.000 claims description 2
- 238000005859 coupling reaction Methods 0.000 claims description 2
- 230000001965 increasing effect Effects 0.000 abstract description 7
- 230000001276 controlling effect Effects 0.000 abstract description 5
- 230000001105 regulatory effect Effects 0.000 abstract description 4
- 238000003912 environmental pollution Methods 0.000 abstract description 3
- 230000002708 enhancing effect Effects 0.000 abstract 1
- 239000003818 cinder Substances 0.000 description 3
- 238000005243 fluidization Methods 0.000 description 3
- 238000000926 separation method Methods 0.000 description 3
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 2
- 239000003245 coal Substances 0.000 description 2
- 238000004939 coking Methods 0.000 description 2
- 238000002485 combustion reaction Methods 0.000 description 2
- 238000001816 cooling Methods 0.000 description 2
- 239000000428 dust Substances 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 239000003546 flue gas Substances 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 239000012530 fluid Substances 0.000 description 1
- 239000007789 gas Substances 0.000 description 1
- 238000012423 maintenance Methods 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 230000003134 recirculating effect Effects 0.000 description 1
- 239000002893 slag Substances 0.000 description 1
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Abstract
The invention relates to a method for controlling the material return quantity of a hearth of a circulating fluidized bed boiler by an adjusting valve, which mainly aims at the circulating combustionof the material of the circulating fluidized bed (CFB) boiler and belongs to the technical field of heat energy and power engineering. On the basis of the prior moderate-temperature separate type circulating fluidized bed boiler, the method makes the following improvements: (1) the number of through holes on an air cap of a return valve matched with a cyclone separator is increased; (2) two pipelines connected with a primary air duct are respectively delivered into two material return devices, and primary air is used as the material return air of a return device; and (3) an adjusting valve isadded on a material return air pipe and is used for controlling the material return air quantity and controlling the ash return quantity of the hearth directly. The invention can achieve the aims of regulating the bed temperature automatically and stably, increasing or reducing the load of the CFB boiler quickly, saving energy resources, enhancing the system reliability of the CFB boiler and reducing the environmental pollution.
Description
Technical field
The present invention relates to a kind of method of utilizing control valve to control boiler hearth of circulating fluidized bed feed back amount, mainly is at the circulating combustion of recirculating fluidized bed (CFB) boiler material, belongs to the Thermal Energy and Power Engineering technical field.
Background technology
In warm divergence type CFBB form by front portion and two vertical well gas flue of afterbody, be connected by two cyclone separators arranged side by side between two vertical shafts, the ash that returns that separates from separator mainly enters loop back device, and the circulating ash that the high-head low discharge feedback air that feeding is then provided by 2 roots blowers separates separator is sent into circulating combustion in the burner hearth; The feedback air of material return system provides transmitting power, and material returning valve then provides cinder and the coal supply loopback of equipment in order to separating to advance burner hearth, carries out fluidisation and burning.Go round and begin again, keep ciculation fluidized running status.Spiral ash machine in the material return system is then measured in order to the ash that returns of control separator.The high pressure feedback air that roots blower provided should be able to fully guarantee all to send feed back to burner hearth, revolves cinder conveyer rotating speed control bed temperature so that be in operation by adjustment.A seldom part in addition enters and buries the scraper plate slag conveyer after being transported to the device for cooling ash cooling by spiral ash machine.When CFBB normally moves, by adjusting the spiral ash machine rotating speed burner hearth bed temperature is controlled at about 900 ℃, the grey temperature of returning that cyclone separator separates has only about 400 ℃.In service when one timing of coal amount, the high and low of fire box temperature just relies on back how much regulating of ash amount.
Owing to be the ash amount of the returning control bed temperature that adopts the mode indirect regulation burner hearth of adjustable screw cinder conveyer rotating speed control ash discharge amount, therefore in actual motion, the ash discharge amount of material return system is compared very little with the ash amount of returning of burner hearth, thereby the ash amount occurring returning at short notice after the adjustment of ash discharge amount can obviously not change, control lag causes bed temperature as long as fluctuation takes place and just is difficult to stable phenomenon.Owing to can not in time regulate the ash amount returned, boiler can occur that the bed temperature adjustment is not come and sharply rise and cause high-temperature coking, so frequent the employing cut off interlocking and made feeder stop transport to cause boiler to stop.Simultaneously, owing to adopt the spiral ash machine ash discharge to regulate bed temperature, adjust boiler load,, can not satisfy the needs of Chemical Manufacture with vapour so that boiler adds the velocity anomaly of load shedding is slow.Material return system is adjusted ineffective this situation causes boiler start-stop car frequent, and the operating maintenance cost is huge to be increased, and boiler then all has the possibility of flame-out or overtemperature coking at any time.
In order to solve this unfavorable situation, should adopt suitable new technology control boiler hearth of circulating fluidized bed feed back amount, reach bed temperature and regulate automatically steadily, add load shedding fast, not only but energy savings improves CFB steam generator system reliability, but also can reduce environmental pollution.This method has very major and immediate significance to the strategic objective of warm separation of C FB boiler energy-saving emission-reduction in realizing.
Summary of the invention
Technical problem to be solved by this invention provides a kind of method of controlling boiler hearth of circulating fluidized bed feed back amount, can reach automatic steady and regulate bed temperature, adds and subtracts the CFB boiler load fast, and energy savings improves CFB steam generator system reliability, reduces environmental pollution.
Solving the scheme that technical problem of the present invention adopts is:
(1) with the blast cap of the feeding-back valve of cyclone separator coupling on increase number of openings;
(2) connect two pipelines from air channel and deliver to respectively two feeding back devices, with wind feedback air as loop back device;
(3) on the feed back airduct, set up control valve and control the feed back air quantity, directly control the returned ash in furnace amount.
The through hole of every blast cap of feeding-back valve of the present invention increases by 50%～300%; Blast from two pipelines of an air channel connection is controlled at 10000Pa～30000Pa; With the control valve of setting up on the feed back airduct feed back air quantity is adjusted to 200m
3/ h～500m
3/ h.
The newly-increased through-hole diameter of every blast cap of feeding-back valve of the present invention is 1mm～3mm, and quantity is 5～20; The specification of two pipelines of an air channel connection is DN50～DN300, and preferably, newly-increased through-hole diameter is 3mm, and quantity is 12; The specification of two pipelines of an air channel connection is DN100.
Blast cap at feeding-back valve is newly opened the hole, can guarantee enough feed back air quantity, allows return the function that ash plays the adjusting bed temperature; Cancel two spiral ash machines and two high pressure fluidisation roots blowers that original boiler is equipped with, changed into and connect two DN100 pipelines from an air channel and deliver to respectively two feeding back devices, can reduce operating cost, increased security; Increase control valve on the feed back airduct and control the feed back air quantity, can directly control the returned ash in furnace amount, thereby realize that bed temperature can control automatically in 870 ℃～950 ℃ scopes, boiler load reaches specified 75t/h.
The invention has the beneficial effects as follows:
(1) the feed back air quantity on average can reach 350m
3/ h reaches as high as 400m
3/ h, air quantity have increased by 2～3 times.Because return the increase of ash amount, bed temperature has obtained effective control, boiler also reaches designed capacity.Bed temperature is stable at 920 ℃, and boiler load is stabilized in about 75t/h, is up to 85t/h, and promptly 113% of design load, solved the bottleneck problem of restriction boiler load;
(2) utilize a wind as feedback air, stopped the operation of roots blower, not only reduced the cost of operation, and increased safety in operation.
Description of drawings
Fig. 1 is the prior art processes schematic flow sheet,
Fig. 2 is a process flow diagram of the present invention.
The specific embodiment
Embodiment: every blast cap is newly opened the aperture of 12 3mm on 16 blast caps of feeding-back valve, to guarantee enough feed back air quantity, to allow that returning ash plays the function of regulating bed temperature.Two spiral ash machines and two high pressure fluidisation roots blowers that the cancellation boiler is equipped with, change into and connect two DN100 pipelines from an air channel and deliver to respectively two feeding back devices, substitute hp fluid air that roots blower produces feedback air as loop back device with a wind (blast is 20000Pa); On the feed back airduct, increase control valve control feed back air quantity, make the feed back air quantity can reach 350m
3/ h, directly control the returned ash in furnace amount after, realize that bed temperature can control automatically in 870 ℃～950 ℃ scopes, boiler load reaches specified 75t/h.The middle temperature divergence type CFBB of certain 2 75t/h in chemical plant; furnace outlet flue gas is 430 ℃ when arriving separator; separator gets off the bulky grain dust separation to fall in the feed back standpipe, and a wind that utilizes 20000Pa send the feedback air of device as meeting, and the feed back air quantity on average can reach 340m
3/ h reaches as high as 420m
3/ h.Bed temperature is stabilized in 920 ℃, and boiler load is stabilized in about 78t/h.Simultaneously, owing to stopped the operation of roots blower, not only reduced the cost of operation, and increased safety in operation.
And for example the method for present embodiment is used for the warm divergence type CFBB of certain 1 35t/h of steam power plant; furnace outlet flue gas is 480 ℃; enter behind the cyclone separator in people's feed back standpipe that the bulky grain dust separation got off to fall; utilize the wind of 16000Pa to send the feedback air of device as meeting; and utilize the volume damper that installs additional on this pipeline to carry out air quantity and regulate, control feed back air quantity size is returned the ash amount with control and is regulated the boiler bed temperature.The feed back air quantity on average can reach 260m
3/ h reaches as high as 300m
3/ h.Bed temperature is stabilized in 890 ℃, and boiler load is stabilized in about 36t/h.
Claims (3)
1, a kind of method of controlling boiler hearth of circulating fluidized bed feed back amount is characterized in that:
(1) with the blast cap of the feeding-back valve of cyclone separator coupling on increase number of openings;
(2) connect two pipelines from air channel and deliver to respectively two feeding back devices, with wind feedback air as loop back device;
(3) on the feed back airduct, set up control valve and control the feed back air quantity, directly control the returned ash in furnace amount.
2, by the method for the described control boiler hearth of circulating fluidized bed of claim 1 feed back amount, it is characterized in that: the through hole of every blast cap of described feeding-back valve increases by 50%～300%; Blast from two pipelines of an air channel connection is controlled at 10000Pa～30000Pa; With the control valve of setting up on the feed back airduct feed back air quantity is adjusted to 200m
3/ h～500m
3/ h.
3, by the method for the described control boiler hearth of circulating fluidized bed of claim 2 feed back amount, it is characterized in that: the newly-increased through-hole diameter of every blast cap of feeding-back valve is 3mm, and quantity is 12; The specification of two pipelines of an air channel connection is DN100.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN200910094925A CN101666495A (en) | 2009-09-03 | 2009-09-03 | Method for controlling material return quantity of hearth of circulating fluidized bed boiler |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN200910094925A CN101666495A (en) | 2009-09-03 | 2009-09-03 | Method for controlling material return quantity of hearth of circulating fluidized bed boiler |
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|---|---|
| CN101666495A true CN101666495A (en) | 2010-03-10 |
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|---|---|---|---|
| CN200910094925A Pending CN101666495A (en) | 2009-09-03 | 2009-09-03 | Method for controlling material return quantity of hearth of circulating fluidized bed boiler |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102353042A (en) * | 2011-09-09 | 2012-02-15 | 北京交通大学 | Adjusting method for circulating ash quantity, separator and combustion system |
| CN104266164A (en) * | 2014-07-15 | 2015-01-07 | 神华集团有限责任公司 | Supercritical CFB (Circulating Fluidized Bed) boiler reheating steam temperature adjusting system and adjusting method |
| CN110107891A (en) * | 2019-05-30 | 2019-08-09 | 联盛纸业（龙海）有限公司 | A method of improving paper mill boiler furnace Matter Transfer |
-
2009
- 2009-09-03 CN CN200910094925A patent/CN101666495A/en active Pending
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102353042A (en) * | 2011-09-09 | 2012-02-15 | 北京交通大学 | Adjusting method for circulating ash quantity, separator and combustion system |
| CN104266164A (en) * | 2014-07-15 | 2015-01-07 | 神华集团有限责任公司 | Supercritical CFB (Circulating Fluidized Bed) boiler reheating steam temperature adjusting system and adjusting method |
| CN110107891A (en) * | 2019-05-30 | 2019-08-09 | 联盛纸业（龙海）有限公司 | A method of improving paper mill boiler furnace Matter Transfer |
| CN110107891B (en) * | 2019-05-30 | 2021-09-03 | 联盛纸业（龙海）有限公司 | Method for improving material circulation of boiler furnace of paper mill |
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Open date: 20100310 |