CN1401411A - Compound desulfurizing process of circulating fluidized bed boiler - Google Patents

Compound desulfurizing process of circulating fluidized bed boiler Download PDF

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Publication number
CN1401411A
CN1401411A CN 02135540 CN02135540A CN1401411A CN 1401411 A CN1401411 A CN 1401411A CN 02135540 CN02135540 CN 02135540 CN 02135540 A CN02135540 A CN 02135540A CN 1401411 A CN1401411 A CN 1401411A
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CN
China
Prior art keywords
desulfurization
humidification
bed boiler
conditioning tower
fluidized bed
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CN 02135540
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Chinese (zh)
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CN1172738C (en
Inventor
马春元
董勇
陈莲芳
徐夕仁
李京
李玉忠
田风国
周广锋
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山东大学
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Priority to CNB021355401A priority Critical patent/CN1172738C/en
Publication of CN1401411A publication Critical patent/CN1401411A/en
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Publication of CN1172738C publication Critical patent/CN1172738C/en

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Abstract

A combined desulfurizing process for removing the SO2 gas from the flue gas generated by circualting fluidized-bed boiler is characterized by that the raw lime stone reacts with the SO2 in the bed layer of boiler to remove part of SO2 by combustion and the unreacted and escaped calcium oxide further reacts with SO2 in the moistening tower for external removal of SO2. Its advantages are low cost and optimal desulfurizing effect.

Description

Compound desulfurizing process of circulating fluidized bed boiler
1, technical field
The invention belongs to environmental protection technical field, particularly relate to the compound desulfurizing process of circulating fluidized bed boiler that is used for removing the sulfur in smoke gas that produces behind the burning in circulating fluid bed boiler.
2, background technology
At present, the sulfur method of CFBB mainly is a desulphurization during combustion.The burning in circulating fluid bed boiler sweetening process is that granularity is sent in the stove less than 2.0 millimeters lime particle, and decomposition of limestone becomes calcium oxide and carbon dioxide, and calcium oxide and the sulfur dioxide gas precursor reactant that burning generates reach the desulfurization purpose.
In the burning in circulating fluid bed boiler sweetening process, except the influence of limestone granularity to desulfurization, its bed temperature has material impact to desulfuration efficiency.The CFBB bed temperature distributes and the hole blocking characteristic, thereby influences desulfuration efficiency and sorbent utilization reaction speed, the solid product that the influence of desulfurization mainly is to have changed desulfurizing agent.Propose among " CFBB theoretical with operation " works such as () Cen Kefa P367, bubbling bed the best desulfurization temperature of generally acknowledging is 850 ℃, and many researchers think that the optimum temperature of circulating fluid bed boiler desulfurization is 850~900 ℃.
But, in the actual motion of CFBB, its ignition temperature is generally 900-1100 ℃, and this temperature has exceeded the optimum temperature of burning in circulating fluid bed boiler desulfurization, caused the decline significantly of stove internal combustion desulfuration efficiency, desulfuration efficiency is 30-40% generally speaking; Simultaneously, cause desulfurizing agent, cause the desulfurizing agent waste with the flue gas stove that flies out.
3, summary of the invention
The objective of the invention is to overcome above-mentioned the deficiencies in the prior art, a kind of compound desulfurizing process of circulating fluidized bed boiler is provided, make CFBB under existing ignition temperature and load, in the scope that the induced draught system resistance allows, make full use of existing site condition,, improve total desulfuration efficiency of CFBB and sorbent utilization by desulfurization of stove internal combustion and flue gas afterbody humidification desulfurization, avoid the huge waste of desulfurizing agent, reduce operating cost.
The present invention realizes in the following way:
Compound desulfurizing process of circulating fluidized bed boiler, at first granular lime stone is sent in the CFBB by the lime stone charging gear, lime stone resolves into calcium oxide and carbon dioxide in stove, calcium oxide and sulfur dioxide gas precursor reactant generate calcium sulfite, feature of the present invention is: increased the humidification desulfurization system between CFBB back-end ductwork and electric cleaner, the conditioning Tower that unreacted calcium oxide particle and sulfur dioxide gas enter humidification system in the CFBB through back-end ductwork with flue gas, in conditioning Tower, calcium oxide particle and the water droplet reaction that sprays through the water atomization system, generate calcium hydroxide, calcium hydroxide further reacts with sulfur dioxide, generate calcium sulfite, finish the outer humidification desulfurization process of stove.
Above-mentioned compound desulfurizing process of circulating fluidized bed boiler, two loop structures that the ash circulation of humidification system is made up of one-level inertial separator and secondary downward air discharge cyclone separation device.
Above-mentioned compound desulfurizing process of circulating fluidized bed boiler, the outer loop mode is adopted in the ash circulation that it is characterized by humidification system, delivers to the conditioning Tower upper entrance from a part of flying dust of conditioning Tower and electric cleaner through desulfurization ash induction system.
Above-mentioned compound desulfurizing process of circulating fluidized bed boiler, its feature also are to deliver to atomization system from the desulfurized mortar liquid that the desulfurization ash of conditioning Tower bottom and electric cleaner is made by pulping system through the slurries delivery pump, carry out humidification and realize the ash circulation.
Because adopt above-mentioned sulfur removal technology, the granularity of limestone desulfurizer can adopt relative broad range, be convenient to the desulfurizing agent preparation.Because behind the decomposition reaction of the limestone particle of larger particles process, the vulcanization reaction, through reentering in the bed after the separation of boiler high temperature separator, because the endocorpuscular collision effect of bed, secondary response again after sorbent particle exposes new surface again enters back-end ductwork with flue gas behind the cutting particle diameter of calcium oxide particle granularity less than high-temperature separator.These enter and further carry out gas-liquid with sulfur dioxide in the conditioning Tower of residue calcium oxide particle between back-end surfaces and electric cleaner of back-end ductwork and react admittedly, carry out desulphurization reaction, because conditioning Tower adopts two loop structures of being made up of the twin-stage inertial separation, make and the interior unreacted sorbent particle recycled for multiple times of conditioning Tower further improved sorbent utilization and desulfuration efficiency.Like this,, farthest utilized varigrained desulfurizing agent, improved total sorbent utilization and the desulfuration efficiency of system through stove internal combustion desulfurization and afterbody humidification desulfurization.
The ignition temperature (900-1100 ℃) when the present invention has overcome CFBB high load capacity, high burning efficiency stable operation and the contradiction of desulfuration in furnace optimal reaction temperature (850-900 ℃), both realized the economy of burning, ensured the environmental protection characteristic of CFBB again, had broad application prospects.
4, description of drawings
Fig. 1 is for adopting the compound desulfurizing process of circulating fluidized bed boiler schematic diagram of two circulation conditioning Tower.
Fig. 2 is for adopting the compound desulfurizing process of circulating fluidized bed boiler schematic diagram of outside grey circulation conditioning Tower.
Fig. 3 is for adopting the compound desulfurizing process of circulating fluidized bed boiler schematic diagram of circulating ash slurry spraying.
1 is coal feeder among the figure, and 2 is the lime stone charging gear, and 3 is CFBB, 4 is high temperature cyclone separator, and 5 is back-end ductwork, and 6 is conditioning Tower, 7 are the water atomization system, and 8 is the one-level inertial separator, and 9 is the secondary downward air discharge cyclone separation device, 10 is helix transporting device, and 11 is electric cleaner, and 12 is ash discharging gear, 13 is venturi, and 14 is uptake flue, and 15 is the conditioning Tower upper entrance, 16 are desulfurization ash induction system, and 17 is pulping system, and 18 is the slurries delivery pump.
5, the specific embodiment
Provide a most preferred embodiment of the present invention below in conjunction with accompanying drawing 1.
Granularity is sent into CFBB 3 less than the limestone particle of 2mm by lime stone charging gear 2, the CaO particle of calcining and decomposing carries out gas-solid reaction with sulfur dioxide under the bed temperature in stove in stove, the calcium oxide particle of larger particles and coal-fired particle are after the CFBB high-temperature separator separates, enter bed again and further react, remove a part of sulfur dioxide and finish an internal combustion sweetening process.Granularity enters conditioning Tower 6 with flue gas through back-end ductwork 5, venturi 13 less than the calcium oxide particle of the cutting particle diameter of high-temperature separator, arranged that on venturi top 7 pairs of flue gases of water atomization system carry out humidifying cooling and handle, make the electric cleaner entrance flue gas temperature reach 50-90 ℃, the calcium hydroxide of the generation in sulfur in smoke and the conditioning Tower further reacts, and carries out the outer humidification desulfurization process of stove.The part that calcium oxide in the conditioning Tower 6, calcium hydroxide and fly ash granule get off through one-level inertial separator 8, reenter and participate in reaction in the conditioning Tower, flue gas after the one-level inertial separation enters secondary downward air discharge cyclone separation device 9, calcium hydroxide, fly ash granule under separating sent in the conditioning Tower recycling once more by helix transporting device 10, the partial reaction product is discharged by bottom ash discharging gear 12.Like this, by the conditioning Tower binary cycle system that venturi, one-level inertial separator, secondary inertial separator and spiral loop back device are formed, guaranteed that the tiny calcium oxide particle that flies out in the CFBB reaches maximum utilization.Flue gas after the secondary inertia separator separates enters electric cleaner 11, discharges after dedusting.
An alternative embodiment of the invention is the structure that adopts as shown in Figure 2, and the outer loop mode is adopted in its desulfurization ash circulation.Flow through behind the back-end ductwork 5 through the flue gas after the burning in circulating fluid bed boiler desulfurization, turning back upwards enters the upper entrance 15 of conditioning Tower through uptake flue 14, carries out humidification desulfurization by 7 pairs of flue gases of the water atomization system that is arranged in conditioning Tower 6 tops.The desulfurization ash of part conditioning Tower bottom and from the desulfurization ash of electric cleaner 11 is transported to the upper entrance 15 of conditioning Tower 6 through desulfurization ash induction system 16, enters conditioning Tower and further carries out desulphurization reaction.
The third embodiment of the present invention adopts structure as shown in Figure 3, and desulfurized mortar liquid endless form is adopted in the circulation of its desulfurization ash.Flow through behind the back-end ductwork 5 through the flue gas after the burning in circulating fluid bed boiler desulfurization, turning back upwards enters conditioning Tower through uptake flue 14 by the upper entrance 15 of conditioning Tower.The desulfurization ash from conditioning Tower bottom and electric cleaner that a part contains the unreacted desulfurizing agent enters pulping system 17, and the slurries of making are delivered to atomization system 7 through slurries delivery pump 18, and the flue gas in the conditioning Tower 6 is carried out humidification desulfurization.

Claims (4)

1, compound desulfurizing process of circulating fluidized bed boiler, at first granular lime stone is sent in the CFBB [3] by lime stone charging gear [2], lime stone resolves into calcium oxide and carbon dioxide in stove, calcium oxide and sulfur dioxide gas precursor reactant generate calcium sulfite, finish stove internal combustion sweetening process; Feature of the present invention is: increased the humidification desulfurization system between CFBB back-end ductwork [5] and electric cleaner [11], interior unreacted calcium oxide particle of CFBB [3] and sulfur dioxide gas enter the conditioning Tower [6] of humidification desulfurization system through back-end ductwork [5] with flue gas, in conditioning Tower [6], calcium oxide particle and the water droplet reaction that sprays through water atomization system [7], generate calcium hydroxide, calcium hydroxide further reacts with sulfur dioxide, generate calcium sulfite, finish afterbody humidification desulfurization process.
2, compound desulfurizing process of circulating fluidized bed boiler according to claim 1 is characterized by: two loop structures that the ash circulation of humidification system is made up of one-level inertial separator [8] and secondary downward air discharge cyclone separation device [9].
3, compound desulfurizing process of circulating fluidized bed boiler according to claim 1, it is characterized by: the outer loop mode is adopted in the ash circulation of humidification system, delivers to conditioning Tower upper entrance [15] from a part of flying dust of conditioning Tower [6] and electric cleaner [11] through desulfurization ash induction system [16].
4, compound desulfurizing process of circulating fluidized bed boiler according to claim 1, it is characterized by: deliver to atomization system [7] from the desulfurized mortar liquid that the desulfurization ash of conditioning Tower [6] bottom and electric cleaner [11] is made by pulping system [17] through slurries delivery pump [18], carry out humidification and realize the ash circulation.
CNB021355401A 2002-09-17 2002-09-17 Compound desulfurizing process of circulating fluidized bed boiler CN1172738C (en)

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Cited By (13)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN100372596C (en) * 2005-01-13 2008-03-05 清华大学 Method and device for removing coal fire discharged absorptive particles and precursor thereof
CN100436941C (en) * 2005-07-05 2008-11-26 中国石油大学(北京) Coal-tar powder combustion method and apparatus
CN101288825B (en) * 2008-06-16 2012-02-22 万若(北京)环境工程技术有限公司 Semi-dry type fume cleaning method and device
CN101732958B (en) * 2009-12-11 2012-10-03 云南大唐国际红河发电有限责任公司 Method for improving desulfuration efficiency of fluidized bed boiler
CN102961961A (en) * 2012-12-06 2013-03-13 碧水蓝天环境工程有限公司 Desulfuration device and desulfuration method
CN103239984A (en) * 2013-05-15 2013-08-14 山西平朔煤矸石发电有限责任公司 Dry-process fine continuous desulfurization device and method for CFB (Circulating Fluidized Bed) boiler
CN103272475A (en) * 2013-05-31 2013-09-04 神华集团有限责任公司 Desulfurization system of circulating fluidized bed boiler
CN103285726A (en) * 2013-06-21 2013-09-11 山西平朔煤矸石发电有限责任公司 Circulating fluidized bed boiler desulfurization method
CN103672874A (en) * 2013-12-17 2014-03-26 太原锅炉集团有限公司 System for desulfurizing limestone in circulating fluidized bed boiler on basis of flow state reconstruction
CN105498473A (en) * 2015-11-25 2016-04-20 广东电网有限责任公司电力科学研究院 Wet method flue gas desulfurizing system and circulating fluidized bed boiler system
CN105903332A (en) * 2016-06-23 2016-08-31 山东大学 Semi-dry method desulfurization and denitrification integrated process and device in synergism with charged oxidation
CN106178877A (en) * 2016-08-31 2016-12-07 大连华锐重工集团股份有限公司 A kind of coke oven flue waste gas purification waste heat recovery apparatus and technique
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

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US7938071B2 (en) * 2007-03-13 2011-05-10 Alstom Technology Ltd. Secondary air flow biasing apparatus and method for circulating fluidized bed boiler systems
CN101596398B (en) * 2009-05-08 2012-05-23 朱学智 Re-devulcanization method based on circulating fluidized bed boiler flue

Cited By (16)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN100372596C (en) * 2005-01-13 2008-03-05 清华大学 Method and device for removing coal fire discharged absorptive particles and precursor thereof
CN100436941C (en) * 2005-07-05 2008-11-26 中国石油大学(北京) Coal-tar powder combustion method and apparatus
CN101288825B (en) * 2008-06-16 2012-02-22 万若(北京)环境工程技术有限公司 Semi-dry type fume cleaning method and device
CN101732958B (en) * 2009-12-11 2012-10-03 云南大唐国际红河发电有限责任公司 Method for improving desulfuration efficiency of fluidized bed boiler
CN102961961A (en) * 2012-12-06 2013-03-13 碧水蓝天环境工程有限公司 Desulfuration device and desulfuration method
CN102961961B (en) * 2012-12-06 2016-01-20 碧水蓝天环境工程有限公司 Desulfurizer and sulfur method
CN103239984A (en) * 2013-05-15 2013-08-14 山西平朔煤矸石发电有限责任公司 Dry-process fine continuous desulfurization device and method for CFB (Circulating Fluidized Bed) boiler
CN103239984B (en) * 2013-05-15 2015-05-06 山西平朔煤矸石发电有限责任公司 Dry-process fine continuous desulfurization device and method for CFB (Circulating Fluidized Bed) boiler
CN103272475B (en) * 2013-05-31 2016-02-03 神华集团有限责任公司 The desulphurization system of CFBB
CN103272475A (en) * 2013-05-31 2013-09-04 神华集团有限责任公司 Desulfurization system of circulating fluidized bed boiler
CN103285726A (en) * 2013-06-21 2013-09-11 山西平朔煤矸石发电有限责任公司 Circulating fluidized bed boiler desulfurization method
CN103672874A (en) * 2013-12-17 2014-03-26 太原锅炉集团有限公司 System for desulfurizing limestone in circulating fluidized bed boiler on basis of flow state reconstruction
CN105498473A (en) * 2015-11-25 2016-04-20 广东电网有限责任公司电力科学研究院 Wet method flue gas desulfurizing system and circulating fluidized bed boiler system
CN105903332A (en) * 2016-06-23 2016-08-31 山东大学 Semi-dry method desulfurization and denitrification integrated process and device in synergism with charged oxidation
CN106178877A (en) * 2016-08-31 2016-12-07 大连华锐重工集团股份有限公司 A kind of coke oven flue waste gas purification waste heat recovery apparatus and technique
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

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