CN1087645C - Method and equipment for desulfurizing flue gas by circulation and fluidization - Google Patents
Method and equipment for desulfurizing flue gas by circulation and fluidization Download PDFInfo
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- CN1087645C CN1087645C CN96100084A CN96100084A CN1087645C CN 1087645 C CN1087645 C CN 1087645C CN 96100084 A CN96100084 A CN 96100084A CN 96100084 A CN96100084 A CN 96100084A CN 1087645 C CN1087645 C CN 1087645C
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Abstract
The present invention relates to a desulphurization method with a flue gas circulating and desulphurizing method and a desulphurization device of the desulphurization method, which belongs to the technical field of environmental protection. The present invention has the method that heat flue gas flows through a desulphurization tower at the speed of 3 to 12 m/s with the time of 1 to 10 seconds, is in contact with, is mixed with, and reacts with an absorbent or circular reactants entering the desulphurization tower, mixtures and compounds then enter a duster connected with the desulphurization tower along with the flue gas, and the duster newly sends most of collected solid reactants to the desulphurization tower to circulate and use the reactants; the flue gas purified by the duster can be discharged into the atmosphere or directly discharged into the atmosphere by removing dust for another time.
Description
The invention relates to a flue gas circulating fluidized method desulfurization method and a device, which belong to the technical field of environmental protection of industrial flue gas purification, are suitable for desulfurizing industrial flue gas such as flue gas discharged by coal-fired and oil-fired boilers, and are particularly suitable for desulfurizing occasions of flue gas discharged by combustion equipment of a thermal power plant. The process belongs to the field of desulfurizing technology.
The existing semi-dry flue gas desulfurization method is mainly a rotary spraying method, which enables flue gas to enter from the lower part of a desulfurization tower, and lime slurry to enter from the upper part and is sprayed on a high-speed rotating wheel to atomize the flue gas. SO in atomized lime slurry and flue gas2And directly discharging waste residues generated after the reaction from the bottom of the tower. The disadvantages of this method are: 1. the utilization rate of the absorbent is low, and the calcium-sulfur ratio is high, namely the lime consumption is large; 2. the desulfurization efficiency is relatively low; 3. the lime slurry is sprayed into a mist shape by the high-speed rotating wheel, and the lime slurry and reaction products are very easy to adhere to the inner wall of the tower to form scale, so that the volume in the tower is influenced, the tower body is corroded, and the maintenance cost is increased; 4. the spraying wheel is a vulnerable part and is expensive, and the rotating speed of the wheel is high, so that the spraying wheel is difficult to be made into a large size, and the scale of the desulfurizing tower is influenced. The other semi-dry desulfurizing method is biphase flow spraying method, which uses compressed air and lime slurry to enter the tower simultaneously to realize atomization without rotating wheel, the flue gas and the lime slurry flow relatively, and the waste slag is discharged from the bottom of the tower directly. The above methods all have the problem that the absorbent channel is easy to block because the requirement on the granularity of the absorbent is high.
The invention aims to: the method and the device overcome the defects of the method and provide the flue gas circulating fluidized desulfurization method and the desulfurization device so as to improve the desulfurization efficiency, greatly reduce the system manufacturing cost and the operation and maintenance cost and improve the system reliability to ensure the atmospheric environment quality.
The technical scheme of the flue gas circulating fluidization desulfurization method for realizing the aim of the invention is as follows: enabling hot flue gas to enter a Venturi desulfurization tower from the lower part at the speed of 3-12 m/s for 1-10 seconds, contacting, mixing and reacting with a fluidized sulfur dioxide absorbent and a reactant entering the desulfurization tower, and enabling the generated mixture or reactant to enter a dust remover connected with the desulfurization tower along with the flue gas; the dust remover repeatedly sends the collected solid mixture and the reactant to the desulfurizing tower for recycling; the flue gas purified by the dust remover is discharged into the atmosphere, or is discharged into the atmosphere after dust removal is carried out again.
A circulating fluidized method desulfurization device for realizing the method of the invention is as follows: it comprises a desulfurizing tower 2; the desulfurizing tower is provided with a flue gas inlet 10, an absorbent inlet 3 and a desulfurized flue gas discharge channel 11; the desulfurizing tower is also provided with an input port 15 for recycled reactants to enter the tower; the inlet 15 and the absorbent inlet 3 are positioned near the flue gas inlet 10; the desulfurized flue gas discharge channel 11 is connected with the dust remover 5; the slag discharge channel 13 of the dust remover is communicated with a conveying device 4 which can send slag as a circulating reactant into the tower for recycling.
The method comprises the following process flows and principles: the hot flue gas enters the vertical Venturi desulfurization tower from the lower part of the tower and contacts and mixes with fluidized solid particles consisting of calcium hydroxide and recycled reactants. Fresh lime slurry can be directly sprayed into the desulfurizing tower by a double-phase flow nozzle, and the water in the lime slurry humidifies flue gas to improve SO2The removal rate of (3). Because the system has a relatively high flue gas flow velocity (which can be 7.5m/s generally), the system is convenient for flowing and conveying the particles in the desulfurizing tower and simultaneously promoting SO2And the reaction of the particulate matter. The spent solids and fly ash are carried out of the top of the desulfurization tower and collected in a dust collector coupled to the desulfurization tower. Most of the solids collected by the dust collector are recycled to the desulfurization tower, so that the residual absorbent in the solids can be fully utilized, and the solids can be humidified again, thereby providing more reaction surface area. The residual solids in the flue gas, such as fly ash, etc., can be removed by a downstream dust collector, typically an electric dust collector or a bag-type dust collector.
In the method of the invention, the chemical reaction process and the corresponding reaction formula of the reactants are as follows:
1. lime slurry: calcium hydroxide slurry was formed from quicklime digested with water:
2. after entering the desulfurizing tower (sprayed into the desulfurizing tower by a double-phase flow nozzle), the lime slurry reacts with the flue gas with the temperature of about 130 ℃ in the tower, and the reaction formula is as follows:
compared with other semi-dry process technologies, the invention has the advantages that:
1. the solid reactant returned by the dust remover is recycled, so that the concentration of solid particles in the desulfurizing tower is very high and can be generally as high as 500-1500 g/Nm3The concentration is 50-100 times of that in the common spray drying process. Meanwhile, as the solid particles in the desulfurizing tower are rapidly dried in the fluidizing process, the scaling problem which usually occurs in the common spray drying process can be avoided in the tower.
2. Because of the quite long contact time of the flue gas and the reactant of the absorbent, the contact time is obtained by depending on that the lime particles pass through the desulfurizing tower for hundreds of times of circulation, thereby greatly improving the utilization rate of the absorbent.
3. The recycled reactant is continuously coated with a new absorbent on the surface, and the activity of the product of the fly ash and the lime slurry in a hot state is enhanced, so that the capability of absorbing sulfur dioxide is greatly improved compared with thatof a pure lime slurry absorbent.
4. The system has simple structure, low cost, low operation and maintenance cost and high desulfurization efficiency.
Compared with a wet limestone/gypsum method, the method has the main advantages that:
1) the scale formation and corrosion are reduced, and the equipment investment and maintenance cost are reduced; this is because the reducing liquid contacts the flue gas and rarely contacts the walls of the system. Therefore, equipment such as a slurry tank can be made of low carbon steel without using a rust-proof lining.
2) The invention has the advantages of small dosage of washing liquid, small number of pumps and low energy consumption. The product of the present invention can be treated with a conventional fly ash system due to drying, and a dewatering system is not required.
3) The flue gas discharged by the system of the invention does not need to be reheated, thereby reducing the manufacturing cost and energy consumption.
The method and the desulfurization device thereof are further described by combining the accompanying drawings and examples as follows:
FIG. 1 is a schematic diagram of the apparatus and process flow of the process of the present invention.
FIG. 2 is a schematic view of a desulfurization unit of the present invention.
The device names included in the figure are: 1. combustion equipment (e.g., boilers); 2. a desulfurizing tower; 3. an absorbent inlet; 4. the reactant recycling conveying device; 5. a dust remover; 6. a secondary dust collector; 7. a fan; 8. smoking bittern; 9. a flue gas channel; 10. a flue gas inlet; 11. a desulfurized flue gas discharge channel; 12. a flue gas outlet; 13. a slag discharge channel; 14. a circulating reactant channel; 15. a reactant inlet; 16. a slag discharge port; 17. a nozzle; 18. a compressed air inlet.
The figure shows that hot flue gas discharged from a combustion device 1 can be pressurized and accelerated to be sent to a desulfurizing tower 2, and reactants in the desulfurizing tower are SO to be removed from the flue gas2Solid fly ash and lime slurry, namely calcium hydroxide, which is sprayed into the desulfurization tower from an absorbent inlet 3, and residual reactants which are collected by a dust collector 5 and then returned to the desulfurization tower 2 through a reactant recycling conveying device 4. The speed of the flue gas flowing through the desulfurizing tower is 3-12 m/s, and the time of the flue gas flowing through the desulfurizing tower is 1-10 seconds. The flue gas enters the tower from the lower part of a vertically arranged Venturi desulfurization tower, and the lime slurry and the circulating reactant simultaneously enter the tower to react. The calcium-sulfur ratio (Ca/S) of the desulfurization system is 1.2-1.4, and when the calcium-sulfur ratio is 1.3, the desulfurization efficiency can reach 90%; when the calcium-sulfur ratio is 1.0, the desulfurization efficiency can reach more than 75 percent. A two-phase flow nozzle is arranged at the center of the tower to form absorbent liquid dropsGood water mist is spread, so that the reactants are fully reacted in the tower. The flue gas discharged from the desulfurizing tower 2 enters a dust remover; a re-precipitator can be connected thereafter when further dust removal is required. The absorbent inlet 3 shares a nozzle 17 with the compressed air inlet 18, which is located at the flue gas inlet 10 of the desulfurization tower 2.
To further illustrate the present invention, the following is further exemplified:
flue gas flow 100 ten thousand Nm3/h
The flue gas temperature (outlet of air preheater) is 136 DEG C
Time of flue gas flowing through the tower: 3S
Velocity of flue gas flowing through the tower: 7.5m/s
A dust remover: the first stage is a cyclone dust collector, and the second stage is an electric dust collector;
calcium to sulfur ratio (Ca/s): 1.3
The effect is as follows: the desulfurization rate is as high as more than 90%.
The method and the device have the advantages of high desulfurization efficiency and absorbent utilization rate, no scale formation in the tower, reliable operation, no need of special personnel for operation and management, and low requirement on the absorbent, so the manufacturing cost and the operation cost are low.
Claims (8)
1. A flue gas circulating fluidization method for desulfurization is characterized in that hot flue gas enters a Venturi desulfurization tower from the lower part at a speed of 3-12 m/s for 1-10 seconds, contacts and is mixed with a fluidized sulfur dioxide absorbent and a reactant entering the desulfurization tower and reacts with the absorbent, and the generated mixture and the reactant enter a dust remover connected with the desulfurization tower together with the flue gas; the dust remover repeatedly sends the collected solid mixture and the reactant to the desulfurizing tower for recycling; the flue gas purified by the dust remover is discharged into the atmosphere, or is discharged into the atmosphere after dust removal is carried out again.
2. The desulfurization method according to claim 1, wherein the reactants in the desulfurization tower are sulfur dioxide and solid fly ash in the flue gas, a sulfur dioxide absorbent entering the desulfurization tower, and the recycled reactants collected by the dust collector and returned to the desulfurization tower.
3. The desulfurization method according to claim 1, wherein the velocity of the flue gas flowing through the desulfurization tower is 3m/s for 10 seconds.
4. The desulfurization method according to claim 1, wherein the velocity of the flue gas flowing through the desulfurization tower is 12m/s and the time is 1 second.
5. The desulfurization method according to claim 1, wherein the velocity of the flue gas flowing through the desulfurization tower is 7.5m/s and the time is 3 seconds.
6. The desulfurization method of claim 1, wherein the venturi desulfurization tower is vertically arranged, and the flue gas enters the tower simultaneously with the absorbent and the recycled reactant to react.
7. A desulfurization device of a desulfurization method by a circulating fluidized method comprises a desulfurization tower (2); the desulfurizing tower is provided with a flue gas inlet (10), an absorbent inlet (3) and a desulfurized flue gas discharge channel (11); it is characterized in that the desulfurizing tower is also provided with an input port (15) for the recycled reactant to enter the tower; the inlet (15) and the absorbent inlet (3) are positioned near the flue gas inlet (10); the desulfurized flue gas discharge channel (11) is connected with the dust remover (5); the slag discharge channel (13) of the dust remover is communicated with a conveying device (4) which can send slag materials into the tower as a circulating reactant for recycling.
8. The apparatus according to claim 7, wherein the absorbent inlet (3) shares a nozzle (17) with the compressed air inlet (18), which is located at the flue gas inlet (10) of the desulfurization tower (2).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN96100084A CN1087645C (en) | 1996-01-11 | 1996-01-11 | Method and equipment for desulfurizing flue gas by circulation and fluidization |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN96100084A CN1087645C (en) | 1996-01-11 | 1996-01-11 | Method and equipment for desulfurizing flue gas by circulation and fluidization |
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| Publication Number | Publication Date |
|---|---|
| CN1154263A CN1154263A (en) | 1997-07-16 |
| CN1087645C true CN1087645C (en) | 2002-07-17 |
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| Application Number | Title | Priority Date | Filing Date |
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| CN96100084A Expired - Fee Related CN1087645C (en) | 1996-01-11 | 1996-01-11 | Method and equipment for desulfurizing flue gas by circulation and fluidization |
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Families Citing this family (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1089023C (en) * | 1998-10-16 | 2002-08-14 | 清华大学 | Middle temp. dry type circulating fluidized bed fume desulfurizing method and device |
| CN1113682C (en) * | 2000-01-05 | 2003-07-09 | 浙江大学 | Two-segment desulfurizing method for high-temp combustion |
| CN1114467C (en) * | 2000-12-15 | 2003-07-16 | 清华大学 | Dry cyclic suspension bed fume desulfurizing process and system |
| CN1100590C (en) * | 2000-12-20 | 2003-02-05 | 岳建华 | High temperature plasma fume desulfurizer |
| CN1100591C (en) * | 2000-12-21 | 2003-02-05 | 岳建华 | High temperature plasma fume desulfurizing method |
| CN1281297C (en) * | 2003-08-19 | 2006-10-25 | 武汉凯迪电力股份有限公司 | Dry process stack gas desulfur reaction tower with variation structure |
| US10208951B2 (en) * | 2007-09-13 | 2019-02-19 | The Babcock & Wilcox Company | Spray dryer absorber and related processes |
| DE102007050904B4 (en) * | 2007-10-23 | 2013-07-25 | Babcock Noell Gmbh | Plant and process for the purification of flue gases |
| CN101462022B (en) * | 2009-01-12 | 2011-06-29 | 宁波怡诺能源科技有限公司 | Circulating fluid bed flue-gas desulfurizing device |
| CN102093023B (en) * | 2010-12-27 | 2012-12-05 | 马鞍山钢铁股份有限公司 | Non-fired brick and preparation method thereof |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4324770A (en) * | 1980-09-22 | 1982-04-13 | Peabody Process Systems, Inc. | Process for dry scrubbing of flue gas |
| CN1089881A (en) * | 1993-01-20 | 1994-07-27 | 斯坦工业公司 | The flue gas treatment apparatus of polluting objects containing |
| US5607577A (en) * | 1993-10-25 | 1997-03-04 | Alberta Oil Sands Technology And Research Authority | Prevention of sulfur gas emissions from a rotary processor using lime addition |
-
1996
- 1996-01-11 CN CN96100084A patent/CN1087645C/en not_active Expired - Fee Related
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4324770A (en) * | 1980-09-22 | 1982-04-13 | Peabody Process Systems, Inc. | Process for dry scrubbing of flue gas |
| CN1089881A (en) * | 1993-01-20 | 1994-07-27 | 斯坦工业公司 | The flue gas treatment apparatus of polluting objects containing |
| US5607577A (en) * | 1993-10-25 | 1997-03-04 | Alberta Oil Sands Technology And Research Authority | Prevention of sulfur gas emissions from a rotary processor using lime addition |
Non-Patent Citations (1)
| Title |
|---|
| 化学工业过和及设备 1956.7.1 张洪沅等高等教育出版社出版 * |
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Address after: 430077, 2 Ting Road, Wuchang, Wuhan, East Lake Hubei Province Press and Publication Administration veteran cadre department contact Peng Siqiao Applicant after: Peng Sigan Address before: 430071 contact Liang Hanqiao, No. 492, democracy Road, Wuhan, Hubei, Wuchang Applicant before: Peng Sigan Co-applicant before: Zhongnan Power Design Institute of the Ministry of electronics industry, Shenzhen Jingyuan Environmental Protection Technology Co., Ltd. |
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