CN1272088C - Method of proceeding desulfurzation of smoke using waste alkali slag - Google Patents

Method of proceeding desulfurzation of smoke using waste alkali slag Download PDF

Info

Publication number
CN1272088C
CN1272088C CN 200410009477 CN200410009477A CN1272088C CN 1272088 C CN1272088 C CN 1272088C CN 200410009477 CN200410009477 CN 200410009477 CN 200410009477 A CN200410009477 A CN 200410009477A CN 1272088 C CN1272088 C CN 1272088C
Authority
CN
China
Prior art keywords
flue gas
desulfurization
tower
semi
smoke
Prior art date
Application number
CN 200410009477
Other languages
Chinese (zh)
Other versions
CN1597062A (en
Inventor
蒋宏利
姜鸿安
孙涛
张益�
陈建国
曹俊斌
金坚
Original Assignee
北京中科通用能源环保有限责任公司
Priority date (The priority date 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 date listed.)
Filing date
Publication date
Application filed by 北京中科通用能源环保有限责任公司 filed Critical 北京中科通用能源环保有限责任公司
Priority to CN 200410009477 priority Critical patent/CN1272088C/en
Publication of CN1597062A publication Critical patent/CN1597062A/en
Application granted granted Critical
Publication of CN1272088C publication Critical patent/CN1272088C/en

Links

Abstract

The present invention relates to a method of proceeding the desulphurization of smoke using waste alkali slag, which comprises the following steps: 1. the dust of smoke generated by a boiler furnace is firstly removed by a dust remover, and the smoke enters a temperature reducing absorption tower to be cooled down and primarily make SO2 eliminated after the dust of the smoke is removed; 2. the sprayed absorbent slurry which is arranged in the temperature reducing absorption tower is collected to a slurry washing circulation tank, and part of the slurry in the slurry washing circulation tank returns to the temperature reducing absorption tower to be circularly sprayed; 3. the smoke subsequently enters a semi-dry type smoke desulphurization tower to be further desulfurized after primary desulphurization is carried out for the smoke, and the slurry which is sprayed in the semi-dry type smoke desulphurization tower is from the slurry washing circulating tank; 4. the smoke which is desulfurized twice passes through the dust remover and is discharged from a chimney. The method has the advantages of high desulphurization efficiency, high utilization rate of absorbents, no waste water discharge, and difficult scale formation in the desulphurization tower; thereby, the characteristic of treating waste objects by the waste objects is realized.

Description

Utilize waste soda residue to carry out the method for flue gas desulfurization

Technical field:

The invention belongs to the gaseous contamination control technology, is a kind of fume desulphurization method.

Background technology:

China is coal-fired big country, and coal always in occupation of critical role, owing to the discharging of coal combustion pollution thing, has caused huge pressure for the environmental protection of China in China's production of energy supply for a long time.The major pollutants of fire coal boiler fume are flue dust and sulfur dioxide.

At present, the technology of flue gas desulfurization mainly comprises three kinds: dry method, semidry method and wet method.Its core technology principle is with the SO in alkaline matter and the coal-fired flue-gas 2Deng acid gas component generation neutralization reaction, reach the purpose that removes sour gas in the flue gas.Used alkaline matter is that (be lime stone, main component is CaCO to natural calcium base mineral matter mostly 3) and manufactured goods (as CaO powder, Ca (OH) 2Slurry etc.).The Wet technique technical maturity, desulfurized effect good (desulfurization degree is more than 90%), absorbent utilization rate height (the absorbent utilization rate is about 85%), but complex process, investment are high, and produce waste water in the processing procedure, need further to handle waste water.Dry process is simple, emits no waste water, and investment and operating cost are low, but absorbent utilization rate low (the absorbent utilization rate is about 40%), desulfurized effect poor (desulfurization degree is about 50%).It is simple that semi-dry method flue gas desulfurization technique has system, desulfurized effect relatively good (desulfurization degree is about 80%), the absorbent utilization rate is than higher (the absorbent utilization rate is about 70%), to advantages such as coal adaptability are strong, to have a desulfuration efficiency low but compare with wet method, the utilization rate of absorbent is on the low side, and the shortcoming of the interior fouling easily of desulfuration absorbing tower etc. requires further improvement.

Be noted that exploitation utilizes the natural limestone desulfurization that environment is caused negative effect, destroyed geomorphologic landscape, produce lime stone and will consume a large amount of coals, discharge a large amount of CO 2Deng pernicious gas, contaminated environment.

Summary of the invention:

At present, the annual waste soda residue that produces millions of tons of the basic industry of China is analyzed according to the waste soda residue that basic industry is produced dirt, finds the little Ca (OH) of alkaline residue 2, Mg (OH) 2, KOH content is higher, accounts for respectively about 45%, 10%, 5%, water content is about about 35%, after waste soda residue is dissolved in water, pH value higher (being about 12.5).According to analysis result, soda-manufacturing waste residue promptly be can be made into desulfurizing agent through further processing.

Fume desulphurization method of the present invention, be the waste soda residue that produces with basic industry as desulfurizing agent, provide a kind of desulfuration efficiency height, absorbent utilization rate height, desulfurization product are dry state, non-wastewater discharge, less scaling in the desulfurizing tower, the fume desulphurization method of " treatment of wastes with processes of wastes against one another ".

The method of utilizing waste soda residue to carry out flue gas desulfurization, its basic step is as follows:

1. the flue gas that is come by boiler at first passes through elementary deduster dedusting, and the collected ash of elementary deduster enters bulk cement storage tank and stores;

2. entering the desuperheat absorption tower subsequently through the flue gas after the elementary dedusting carries out flue gas cool-down and tentatively removes SO 2Gas, the exhanst gas outlet temperature on desuperheat absorption tower are controlled in 110 ℃~120 ℃ scopes; The waste soda residue absorbent slurry of the adding 10%~15% that sprays in the desuperheat absorption tower and be pooled to washing slurries circulatory pool together from the slurries of the circulated sprinkling in the washing slurries circulatory pool, the part slurries in the washing slurries circulatory pool return and carry out circulated sprinkling in the desuperheat absorption tower;

3. the flue gas after the preliminary desulfurization enters the further desulfurization of semi-dry fume desulfuration tower subsequently, flue gas flow rate in the semi-dry fume desulfuration Tata is controlled in 2m/s~4m/s scope, the slurries that spray in the semi-dry fume desulfuration tower are from washing slurries circulatory pool, and its concentration is in 20%~30% scope;

4. separate the desulfurization ash through the flue gas after the further desulfurization of semi-dry fume desulfuration tower through the final stage deduster, clean flue gas is discharged from chimney by air-introduced machine.

Above-mentioned desuperheat absorption tower is spray column or packed tower, its effect be to flue gas lower the temperature, humidification and tentatively remove SO 2Gas.Be provided with washing slurry preparation pond in outside, desuperheat absorption tower, be used for preparing and storage waste soda residue desulfurization slurry.The slurries that prepare are sent in the desuperheat absorption tower from the top by pump, spray then.Different along with smoke components and flue-gas temperature, the waste soda residue content of waste soda residue slurries is also different, and the mass concentration of waste soda residue is in 10%~15% scope generally speaking.Waste soda residue slurries drop in the desuperheat absorption tower in the dropping process, on one side flue gas is carried out humidification and cooling, on one side by with flue gas in SO 2Gas reacts, thereby removes the SO in the flue gas 2

Do not wash the slurries circulatory pool outside the desuperheat absorption tower, in order to deposit the slurries that the absorption tower inner bottom part compiles, the slurries after compiling are sent in the washing slurries circulatory pool by gravity effect or slush pump.In order to improve the utilization rate of waste soda residue desulfurization, part slurries in the washing slurries circulatory pool are sent in the absorption tower by circulating pump, carry out circulated sprinkling from the top, another part slurries then are sent to the further desulfurization of semi-dry fume desulfuration tower of back by slush pump.In order further to improve the utilization rate of desulfurizing agent, add the partial desulfurization ash that a part separates from the final stage deduster in the washing slurries circulatory pool.

Enter into the further desulfurization of semi-dry fume desulfuration tower subsequently through the flue gas after desuperheat absorption tower desuperheat, humidification and the preliminary desulfurization.This semi-dry fume desulfuration tower both can adopt the spray-drying mode also can adopt the fluid bed mode.The desulfurization slurry that is sprayed in this semi-dry fume desulfuration tower comes from washing slurries circulatory pool, and concentration of slurry is in 20%~30% (in mass) scope.After slurries spray in the half dry type desulfurizing tower, and separate the particle that circulates from separator and deduster and mix strongly, along with flowing of flue gas, the desulfurization slurry drop is dry gradually, when arriving the desulfurizing tower outlet at last, the water content of particle drops to below 5%, is dry state.For reaching reasonable desulfurized effect, the exhanst gas outlet temperature of semi-dry fume desulfuration tower is controlled in 80 ℃~90 ℃ scopes.Be furnished with separator in semi-dry fume desulfuration tower outlet, be used for the solid particle that contained in the branch separable flue gas, the particle that separates is sent in the semi-dry fume desulfuration tower and is circulated.Through the dedusting of final stage deduster, clean flue gas is discharged from chimney by air-introduced machine through the flue gas after the further desulfurization of semi-dry fume desulfuration tower.The desulfurization ash 20%~40% that the final stage deduster separates is sent into and is carried out circulation desulfurization in the semi-dry fume desulfuration tower, and 20%~40% sends into washing slurries circulatory pool circulates once more, and remainder then enters desulfurization ash storehouse.Waste soda residue desulfurization ash can be used as the additive in roadbed material additive, soil conditioner, cement plant etc.

In traditional half dry type absorption technique, the main cause that desulfuration efficiency is not high is that the absorption tower entrance flue gas temperature is higher, humidity of flue gas is low, and the evaporation rate of absorbent slurry particle is fast, and absorbent slurry particle and acidic gas in flue gas effective reaction time are short.In traditional half dry type absorption technique, be easy to fouling in the absorption tower in addition, its main cause is, entrance flue gas temperature is higher, and the injection flow rate that is used for flue gas cool-down in the tower is big.And in this technology, because after previous stage, flue gas was through desuperheat absorption tower desuperheat humidification, temperature is controlled in 110 ℃~120 ℃ scopes, therefore, the inlet temperature of semi-dry fume desulfuration tower is than low 50 ℃~80 ℃ of traditional half dry type absorption technique, humidity of flue gas will increase by 40%~60%, thereby reduces the evaporation rate of absorbent slurry particle, has prolonged the SO in absorbent slurry particle and the flue gas 2The gas effective reaction time has improved smoke desulfurization efficiency significantly, owing to significantly reduced injection flow rate in the absorption tower, has avoided a dirt of scale formation in the desulfurizing tower effectively.

Advantage: adopted the two-step desulfurization technology among the present invention, thereby significantly improved the total desulfuration efficiency of whole system.In first order desuperheat absorption tower, desulfuration efficiency is about 60%~70%; Second level semi-dry fume desulfuration tower, desulfuration efficiency is about 80%~90%, and total desulfuration efficiency is about 92%~97%.

Adopted the Multiple Cycle mode of desulfurizing agent among the present invention, thereby the utilization that has improved desulfurizing agent greatly comprises: (1) desulfurizing agent is on the desuperheat absorption tower and wash slurries and follow between the pond and circulate; (2) desulfurizing agent circulates between separator and semi-dry fume desulfuration tower; (3) desulfurizing agent also circulates between dedusting agent and semi-dry fume desulfuration tower.Its circulation route is: deduster---washs slurries circulatory pool---desuperheat absorption tower---semi-dry fume desulfuration tower---deduster.

Adopted waste soda residue to make desulfurizing agent among the present invention, reached " treatment of wastes with processes of wastes against one another ".

Description of drawings:

Accompanying drawing is to utilize waste soda residue to carry out the process chart of the method for flue gas desulfurization.

Among the figure, the 1st, elementary deduster, the 2nd, bulk cement storage tank, the 3rd, spray column, the 4th, washing slurries circulatory pool, the 5th, washing slurry preparation pond, the 6th, the fluid bed flue gas desulfurization tower, 7 is cyclone separator, and 8 is the final stage deduster, and 9 are desulfurization ash storehouse.

The specific embodiment:

Embodiment:

See accompanying drawing, the hot flue gas of discharging from boiler at first passes through electric cleaner 1 dedusting, and electric cleaner 1 collected ash enters bulk cement storage tank 2 and stores, and can be transported to the cement plant then, brickmaking factory makes additive and uses; Flue gas after the dedusting enters spray column 3 to carry out flue gas cool-down and tentatively removes SO 2Gas, the exhanst gas outlet temperature of spray column are controlled in 100 ℃~120 ℃ scopes; Be provided with washing slurry preparation pond 5 in spray column 3 outsides, be used for preparing the waste soda residue desulfurization slurry, the waste soda residue concentration of slurry is 10%~15%, and the slurries that prepare are sent in the spray column from the top by pump, spray then; The absorbent slurry that sprays in the desuperheat absorption tower is pooled to washing slurries circulatory pool 4, and the part slurries in the washing slurries circulatory pool return and carry out circulated sprinkling in the spray column; Enter the 6 further desulfurization of fluid bed flue gas desulfurization tower subsequently through the flue gas after the preliminary desulfurization, the exhanst gas outlet temperature of desulfurizing tower is controlled in 80 ℃~90 ℃ scopes, the slurries that spray in the fluid bed flue gas desulfurization tower 6 come from washing slurries circulatory pool 4, and concentration of slurry is 20%~30%; , separate ash and return in the fluid bed flue gas desulfurization tower 6 and circulate through cyclone separator 7 through the flue gas after the further desulfurization; The flue gas that comes out from cyclone separator 7 enters sack cleaner 8 dedustings subsequently, discharge from chimney through air blast from the flue gas that sack cleaner 8 comes out, the desulfurization ash that deduster 8 separates is sent in the fluid bed flue gas desulfurization tower 6 from 20%~40% and is carried out circulation desulfurization, 20%~44% sends into washing slurries circulatory pool 4 circulates, and remainder then enters desulfurization ash storehouse 9.

Semi-dry fume desulfuration tower in above-mentioned is spray-drying formula column for smoke purification or damp dry type flue gas purifying tower.Wherein, the damp dry type flue gas purifying tower can be used the fluidized bed type column for smoke purification.

The desulfurizing agent of putting in the washing slurry preparation pond 5 is the waste soda residue that basic industry produces, its preparation method, be with waste soda residue air dry or oven dry, make its water content be lower than for 10% (in mass) after, broken, be screened to and make 98% (in mass) above grain diameter less than 44 microns.The washing concentration of slurry that uses is 20%~30%.

If setting the boiler export exhaust gas volumn is 60000Nm 3/ h, flue-gas temperature is 210 ℃, SO 2Content is 2250mg/Nm 3When desuperheat is absorbed as spray column, then velocity of flue gas is 1.5m/s in the tower, the tower outlet temperature is 115 ℃, initiate waste soda residue slurries ratio is 10%~15%, velocity of flue gas 2.5m/s in the damp dry type flue gas purifying Tata, 83 ℃ of tower outlet temperatures, the concentration of slurry that sprays in the tower is 28%, and the desulfurization ash that deduster separates has 20% to be sent to washing slurries circulatory pool and to circulate.Desulfuration efficiency is 95.3%, and the alkaline residue utilization rate is 88.6%.

Claims (8)

1, the method for utilizing waste soda residue to carry out flue gas desulfurization, its basic step is as follows:
1. the flue gas that is come by boiler at first passes through elementary deduster dedusting, and the collected ash of elementary deduster enters bulk cement storage tank and stores;
2. entering the desuperheat absorption tower subsequently through the flue gas after the elementary dedusting carries out flue gas cool-down and tentatively removes SO 2Gas, the exhanst gas outlet temperature on desuperheat absorption tower are controlled in 110 ℃~120 ℃ scopes; The waste soda residue absorbent slurry of the adding 10%~15% that sprays in the desuperheat absorption tower and be pooled to washing slurries circulatory pool together from the slurries of the circulated sprinkling in the washing slurries circulatory pool, the part slurries in the washing slurries circulatory pool return and carry out circulated sprinkling in the desuperheat absorption tower;
3. the flue gas after the preliminary desulfurization enters the further desulfurization of semi-dry fume desulfuration tower subsequently, flue gas flow rate in the semi-dry fume desulfuration Tata is controlled in 2m/s~4m/s scope, the slurries that spray in the semi-dry fume desulfuration tower are from washing slurries circulatory pool, and its concentration is in 20%~30% scope;
4. separate the desulfurization ash through the flue gas after the further desulfurization of semi-dry fume desulfuration tower through the final stage deduster, clean flue gas is discharged from chimney by air-introduced machine.
2, according to the described method of utilizing waste soda residue to carry out flue gas desulfurization of claim 1, it is characterized in that: the desuperheat absorption tower is a spray column.
3, according to the described method of utilizing waste soda residue to carry out flue gas desulfurization of claim 1, it is characterized in that: the desuperheat absorption tower is a packed tower.
4, according to the described method of utilizing waste soda residue to carry out flue gas desulfurization of claim 1, it is characterized in that step 3. semi-dry fume desulfuration tower outlet be furnished with separator, the particle that separates is sent in the semi-dry fume desulfuration tower and is circulated.
5, according to the described method of utilizing waste soda residue to carry out flue gas desulfurization of claim 1, it is characterized in that step 3. the exhanst gas outlet temperature of semi-dry fume desulfuration tower be controlled in 80 ℃~90 ℃ scopes.
6, according to the described method of utilizing waste soda residue to carry out flue gas desulfurization of claim 1, it is characterized in that step 3. the semi-dry fume desulfuration tower be spray-drying formula column for smoke purification.
7, according to the described method of utilizing waste soda residue to carry out flue gas desulfurization of claim 1, it is characterized in that step 3. the semi-dry fume desulfuration tower be the fluidized bed type column for smoke purification.
8, according to the described method of utilizing waste soda residue to carry out flue gas desulfurization of claim 1, it is characterized in that: the desulfurization ash 20%~40% that the final stage deduster separates is sent into and is carried out circulation desulfurization in the semi-dry fume desulfuration tower, 20%~40% sends into washing slurries circulatory pool circulates once more, and remainder then enters desulfurization ash storehouse.
CN 200410009477 2004-08-24 2004-08-24 Method of proceeding desulfurzation of smoke using waste alkali slag CN1272088C (en)

Priority Applications (1)

Application Number Priority Date Filing Date Title
CN 200410009477 CN1272088C (en) 2004-08-24 2004-08-24 Method of proceeding desulfurzation of smoke using waste alkali slag

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
CN 200410009477 CN1272088C (en) 2004-08-24 2004-08-24 Method of proceeding desulfurzation of smoke using waste alkali slag

Publications (2)

Publication Number Publication Date
CN1597062A CN1597062A (en) 2005-03-23
CN1272088C true CN1272088C (en) 2006-08-30

Family

ID=34662508

Family Applications (1)

Application Number Title Priority Date Filing Date
CN 200410009477 CN1272088C (en) 2004-08-24 2004-08-24 Method of proceeding desulfurzation of smoke using waste alkali slag

Country Status (1)

Country Link
CN (1) CN1272088C (en)

Families Citing this family (10)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN101143293B (en) * 2006-09-15 2010-07-21 中国石油化工股份有限公司 Method for deodorant waste lye for absorbing treating smoke
US10208951B2 (en) * 2007-09-13 2019-02-19 The Babcock & Wilcox Company Spray dryer absorber and related processes
CN102000481B (en) * 2009-08-31 2012-10-10 宝山钢铁股份有限公司 Method for treating desulfurization ash
CN101712039B (en) * 2009-10-28 2012-06-27 上海河图石化工程有限公司 Processing technology of neutralizing, extracting and oxidizing alkaline residue
CN102949924B (en) * 2011-08-31 2014-11-26 中国石油化工股份有限公司 Method for applying petrochemical exhausted lye to semidry-method flue gas desulfurization
CN102357326A (en) * 2011-10-18 2012-02-22 中国华能集团清洁能源技术研究院有限公司 Decarbonization smoke preprocessing system integrated with gas desulfurization system
CN103143228A (en) * 2013-03-29 2013-06-12 广东大众农业科技股份有限公司 Method for purifying air at low cost
CN104445287B (en) * 2014-12-02 2016-04-06 成都华西堂投资有限公司 A kind of converting waste caustic soda that utilizes is for the method for sodium bicarbonate in gas cleaning
CN104857831B (en) * 2015-05-29 2017-07-11 唐山三友化工股份有限公司 Alkaline residue liquid apparatus for preparing desulphurizing agent and method
CN107899408A (en) * 2017-11-30 2018-04-13 南京师范大学 A kind of wet method combines flue gas desulphurization system and sulfur method with dry method

Also Published As

Publication number Publication date
CN1597062A (en) 2005-03-23

Similar Documents

Publication Publication Date Title
RU2645987C2 (en) Method and device for removing impurities from exhaust gases
US8506916B2 (en) Methods and devices for reducing hazardous air pollutants
US20170197180A1 (en) Process and device for desulphurization and denitration of flue gas
KR0143304B1 (en) Method and system for so2 and so3 control by dry sorbent/reagent injection and wet scrubbing
CN1089622C (en) Flue gas desulfurization method and apparatus
CN101422691B (en) Multi-pollutant removing technique and device of fuel coal smoke
AU2010325773B2 (en) A method and device for cleaning a carbon dioxide rich flue gas
CN102974185B (en) Modularized integrated smoke purification system and method for removing plurality of pollutants
CN102512927B (en) Integrated flue gas desulfurizing and denitrating purification system and purification technology for same
CN1239235C (en) Dry smoke cleaning process for desulfurizing and denitrating simultaneously and its system
CN100551496C (en) Unite the Wet-type ammonia process flue gas purifying technique and the system thereof that remove multiple pollutant
CN101797470B (en) Method for circularly trapping SO2 and CO2 by using calcium-based absorbent
RU2459655C2 (en) Device and method of smoke fumes
CN103239985B (en) Efficient fuel coal flue gas desulfurizing and hydrargyrum-removing method and device thereof
CN1087644C (en) Process for dry desulphurisation of combustion gas
CN105080332B (en) Agglomerates of sintered pellets reclamation system and process
CN100551494C (en) Ammonia process removes the method and the system thereof of carbon dioxide in the generating plant flue gas
CN101053747A (en) Simultaneously desulfurization and denitration wet ammonia flue gas cleaning technology and system thereof
CN1231286C (en) A circulating fluidized bed process for cleaning fume by adding iron ash and its equipment
WO2016011681A1 (en) Equipment and method for circulating fluidized bed semidry simultaneous desulfurization and denitration of sintering flue gas
CN102350208B (en) Flue gas absorbent which simultaneously has functions of desulphurization and denitration and preparation method and application thereof
CN100393395C (en) Desulfurization denitration dust collecting integral purifier for coal burning boiler fume gas
CN101648099B (en) Purifying treatment device and purifying treatment method for flue gas multicomponent pollutant generated by incinerating refuse
CN203447967U (en) Combined smoke desulfuration, denitration and demercuration device of industrial boiler
CN101053748A (en) Simultaneously removing various pollutant wet ammonia flue gas cleaning technology and system thereof

Legal Events

Date Code Title Description
PB01 Publication
C06 Publication
SE01 Entry into force of request for substantive examination
C10 Entry into substantive examination
GR01 Patent grant
C14 Grant of patent or utility model
EE01 Entry into force of recordation of patent licensing contract

Assignee: Anhui Shengyun Group

Assignor: Beijing Zhongke Universal Energy Environmental Protection Co., Ltd.

Contract record no.: 2011340000160

Denomination of invention: Method of proceeding desulfurzation of smoke using waste alkali slag

Granted publication date: 20060830

License type: Exclusive License

Open date: 20050323

Record date: 20110721

CF01 Termination of patent right due to non-payment of annual fee

Granted publication date: 20060830

Termination date: 20130824

C17 Cessation of patent right