CN110841452A - Process method and device for ultra-clean emission of flue gas desulfurization - Google Patents
Process method and device for ultra-clean emission of flue gas desulfurization Download PDFInfo
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
- B01D53/75—Multi-step processes
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D46/00—Filters or filtering processes specially modified for separating dispersed particles from gases or vapours
- B01D46/02—Particle separators, e.g. dust precipitators, having hollow filters made of flexible material
- B01D46/023—Pockets filters, i.e. multiple bag filters mounted on a common frame
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/46—Removing components of defined structure
- B01D53/48—Sulfur compounds
- B01D53/50—Sulfur oxides
- B01D53/501—Sulfur oxides by treating the gases with a solution or a suspension of an alkali or earth-alkali or ammonium compound
- B01D53/502—Sulfur oxides by treating the gases with a solution or a suspension of an alkali or earth-alkali or ammonium compound characterised by a specific solution or suspension
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
- B01D53/77—Liquid phase processes
- B01D53/78—Liquid phase processes with gas-liquid contact
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
- B01D53/80—Semi-solid phase processes, i.e. by using slurries
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2251/00—Reactants
- B01D2251/30—Alkali metal compounds
- B01D2251/304—Alkali metal compounds of sodium
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2251/00—Reactants
- B01D2251/40—Alkaline earth metal or magnesium compounds
- B01D2251/404—Alkaline earth metal or magnesium compounds of calcium
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2251/00—Reactants
- B01D2251/60—Inorganic bases or salts
- B01D2251/604—Hydroxides
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2258/00—Sources of waste gases
- B01D2258/02—Other waste gases
- B01D2258/0283—Flue gases
Abstract
The invention discloses a process method of a flue gas desulfurization ultra-clean discharge device, and relates to the technical field of flue gas purification. It comprises the following steps: step 1: flue gas enters a semi-dry process reaction tower through a first flue gas inlet pipeline, lime slurry is sprayed into the semi-dry process reaction tower through a rotary atomization device, and SO in the flue gas2With Ca (OH) in lime slurry droplets2Acting to generate CaSO3And CaSO4And is solidified; step 2: the flue gas enters a Venturi jet mixer; the alkali liquor enters a Venturi jet mixer, and the flue gas and alkali liquor fog drops are produced in the Venturi jet mixerMixing the mixture by using a mixer, and then feeding the mixture into an atomization deacidification reaction tower; SO in flue gas2Reacting with NaOH in alkali liquor fog drops to generate Na2SO3And Na2SO4And is removed; and step 3: the flue gas enters a bag type dust collector to realize the ultra-clean emission of flue gas desulfurization. The alkali liquor used as the absorbent in the invention has larger contact area with the flue gas after being atomized, faster reaction and higher efficiency. The invention also relates to a device for the process.
Description
Technical Field
The invention relates to the technical field of flue gas purification, in particular to a flue gas desulfurization ultra-clean process method. The invention also relates to a device for the process.
Background
At present, the treatment mode of domestic garbage in China is gradually changed from landfill to incineration process, and although the process can better realize the reduction and the harmlessness of the garbage, the smoke generated by incineration often has certain pollution and still needs to be treated. Oxysulfide is used as a main pollutant in waste incineration flue gas and is usually treated by a semi-dry method (SDA). With the stricter requirements on domestic environmental protection, the allowable emission concentration of sulfur oxides in flue gas is also lower. The combined semi-dry and wet desulfurizing process is one well-known fume purifying technology with high desulfurizing effect, and may be used in garbage incinerating plant to treat SO in fume2Processing is performed to achieve lower emission standards.
The basic principle of the wet desulphurization system is as follows: acid gases (mainly SO) in flue gas2) Contact with caustic soda solution, followed by reaction to produce Na2SO3、Na2SO4And the like. The wet process needs to ensure that the flue gas in the tower is at a low flow velocity, so the size of the wet tower is generally large, which not only causes large occupied area of the wet tower, but also increases equipment cost to a certain extent. In the operation process of the wet desulphurization system, sufficient circulation of alkali liquor and dehumidification water needs to be ensured, and a large-flow circulating pump is usually adopted, so that the operation cost of the wet process is high. The wet desulphurization process also increases the humidity of the flue gas, and influences the operation of a subsequent system. In addition, wet desulfurization processes also existThe high-concentration salt solution generated in the operation process is difficult to treat, and the like. Due to the defects of the wet desulphurization system, the semi-dry and wet desulphurization process is difficult to be implemented in most new construction or reconstruction projects.
Therefore, it is necessary to provide a process for ultra-clean emission of flue gas desulfurization.
Disclosure of Invention
The first purpose of the invention is to overcome the defects of the background technology, and provide a process method for flue gas desulfurization and ultra-clean emission.
It is a second object of the invention to provide an apparatus for such a process.
In order to achieve the first object, the technical scheme of the invention is as follows: the technological process of the ultra-clean exhaust device for flue gas desulfurization is characterized by comprising the following steps:
step 1: flue gas enters a semi-dry reaction tower through a first flue gas inlet pipeline, lime slurry is sprayed into the semi-dry reaction tower through a rotary atomization device, and the flue gas and lime slurry fog drops are mixed and contacted in the semi-dry reaction tower, so that the cooling of the flue gas is realized, and the flue gas reacts; SO in flue gas2With Ca (OH) in lime slurry droplets2Acting to generate CaSO3And CaSO4And is solidified;
step 2: the flue gas treated in the step 1 enters a Venturi jet mixer through a second flue gas inlet pipe; after being atomized by an alkali liquor atomization device, alkali liquor enters a Venturi jet mixer through an atomized alkali liquor inlet pipe, and flue gas and alkali liquor droplets are mixed under the action of the Venturi jet mixer and then enter an atomization deacidification reaction tower;
the mixed gas of the flue gas and the alkali liquor fog drops is further mixed by a plurality of turbulence pattern plates; at the same time, SO in the flue gas2Reacting with NaOH in alkali liquor fog drops to generate Na2SO3And Na2SO4And is removed;
and step 3: and (3) enabling the flue gas treated in the step (2) to enter a bag type dust collector, and removing dust particles in the flue gas by using the bag type dust collector to realize ultra-clean emission of flue gas desulfurization.
In the technical scheme, in the step 3, the flue gas treated in the step 2 enters the bag type dust collector together with Ca (OH) which is not completely reacted in the step 1 and the step 22And NaOH powder, and the alkaline powder is adsorbed on the surface of the filter bag and further reacts with the flue gas passing through the bag type dust collector, so that the ultra-clean emission of flue gas desulfurization is further realized.
In the technical scheme, in the step 1, the concentration of the lime slurry is 6-10%.
In the technical scheme, in the step 1, the retention time of the flue gas in the semidry method reaction tower is more than 20 s.
In the technical scheme, in the step 2, the alkali liquor is NaOH solution with the concentration of 25-30%, and the grain diameter of the alkali liquor fog drops is not more than 10 mu m.
In the above technical scheme, in the step 2, the residence time of the flue gas in the atomization deacidification reaction tower is more than 6 s.
In the technical scheme, in the step 1, the step 2 and the step 3, the generated fly ash is collected by the first ash bucket, the second ash bucket and the third ash bucket, the gate valve of the ash buckets is opened, the fly ash is discharged through the ash discharge pipe, and the ash removal work is finished.
In order to achieve the second object, the invention has the technical scheme that: flue gas desulfurization ultra-clean discharging equipment, its characterized in that: comprises a semidry process reaction tower, an atomization deacidification reaction tower and a bag type dust collector;
the top of the semidry reaction tower is connected with a first flue gas inlet pipeline through a rotary atomizing device, and the bottom of the semidry reaction tower is connected with a first ash bucket;
the atomization deacidification reaction tower comprises a plurality of turbulence pattern plates positioned in the middle and a second ash hopper positioned in the lower part; one end of a second flue gas inlet pipe is connected with the first ash hopper, and the other end of the second flue gas inlet pipe is connected with the second ash hopper; a venturi jet mixer is positioned in the second flue gas inlet pipe; one end of an atomized alkali liquor inlet pipe is connected with a Venturi jet mixer, and the other end of the atomized alkali liquor inlet pipe is connected with an alkali liquor atomization device;
the upper part of the atomization deacidification reaction tower is connected with the left side of the bag type dust collector through a third flue gas inlet pipe;
the bag type dust collector comprises a plurality of filter bags, a third ash bucket is arranged at the bottom of each filter bag, and the right side of the bag type dust collector is connected with the flue gas conveying pipeline.
In the technical scheme, the bottoms of the first ash bucket, the second ash bucket and the third ash bucket are connected with the ash discharge pipe through ash bucket gate valves.
Compared with the prior art, the invention has the following advantages:
1) the alkali liquor used as the absorbent in the invention has larger contact area with the flue gas after being atomized, faster reaction and higher efficiency.
2) The reaction speed of the atomization deacidification method adopted by the invention is faster, so the size of the atomization deacidification reaction tower can be very small, and the equipment investment is reduced.
3) The atomization deacidification reaction tower has smaller size and lower construction cost. Therefore, the method is not only suitable for newly-built projects, but also suitable for upgrading and transforming projects of the smoke purification system of the waste incineration plant with short reserved land.
4) The atomization deacidification reaction tower has the advantages of simple structure, fewer devices, easier installation and more convenient maintenance.
5) After the flue gas is treated by the semidry method tower, the residual SO in the flue gas2The concentration is low, so the dosage of the absorbent NaOH required for realizing ultra-low ultra-clean discharge is less, and the water consumption for preparing the solution is low; the consumption of the absorbent is low, so that the flow of the required transfer equipment such as a solution pump is low, the energy consumption is low, and the operation cost is saved.
6) The invention adopts the Venturi jet mixer, does not need to consume other energy sources, and further saves the operation cost.
7) The invention utilizes the bag-type dust collector as the final treatment system of the process, and unreacted alkaline powder adsorbed on the filter bag can further remove SO in the flue gas2Further ensuring SO in the outlet flue gas2And (4) ultra-clean discharge.
8) The invention adopts the bag type dust collector, and unreacted alkaline powder adsorbed on the filter bag can further remove SO in the flue gas2Further ensuring SO in the outlet flue gas2Ultra-clean rowAnd (4) placing.
Drawings
FIG. 1 is a schematic structural diagram of the present invention.
FIG. 2 is a flow chart of the present invention.
Detailed Description
The embodiments of the present invention will be described in detail with reference to the accompanying drawings, which are not intended to limit the present invention, but are merely exemplary. While the advantages of the invention will be apparent and readily appreciated by the description.
With reference to the accompanying drawings: the technological process of the ultra-clean fume desulfurizing and exhausting equipment includes the following steps:
step 1: flue gas enters a semi-dry reaction tower 1 through a first flue gas inlet pipeline 12, lime slurry is sprayed into the semi-dry reaction tower 1 through a rotary atomizing device 11, and the flue gas and lime slurry fog drops are mixed and contacted in the semi-dry reaction tower 1, so that the cooling of the flue gas is realized, and the flue gas reacts; SO in flue gas2With Ca (OH) in lime slurry droplets2Acting to generate CaSO3And CaSO4And is solidified;
step 2: the flue gas treated in the step 1 enters a venturi jet mixer 24 through a second flue gas inlet pipe 23; after being atomized by an alkali liquor atomizing device 26, the alkali liquor enters a Venturi jet mixer 24 through an atomized alkali liquor inlet pipe 25, and the flue gas and alkali liquor droplets are mixed under the action of the Venturi jet mixer 24 and then enter an atomized deacidification reaction tower 2;
the mixed gas of the flue gas and the alkali liquor fog drops is further mixed through a plurality of turbulence flower plates 11; at the same time, SO in the flue gas2Reacting with NaOH in alkali liquor fog drops to generate Na2SO3And Na2SO4And is removed; this step causes SO in the flue gas at the outlet2The concentration is lower than 20mg/Nm3。
And step 3: the flue gas treated in the step 2 enters a bag type dust collector 3, and the bag type dust collector 3 removes dust particles in the flue gas, so that ultra-clean emission of flue gas desulfurization is realized.
In step 3, the flue gas treated in the step 2 enters the bag type dust collector 3 together with the step 1 and the stepIncompletely reacted Ca (OH) in step 22And NaOH powder, and the alkaline powder is adsorbed on the surface of the filter bag 32 and further reacts with the flue gas passing through the bag-type dust collector 3, so that the ultra-clean emission of the flue gas desulfurization is further realized.
In the step 1, the concentration of the lime slurry is 6-10%.
In the step 1, the retention time of the flue gas in the semi-dry reaction tower 1 is more than 20 s.
In the step 2, the alkali liquor is NaOH solution with the concentration of 25-30%, and the grain diameter of the alkali liquor fog drops is not more than 10 mu m.
In the step 2, the retention time of the flue gas in the atomization deacidification reaction tower 2 is more than 6 s.
In the steps 1, 2 and 3, the generated fly ash is collected by the first ash hopper 13, the second ash hopper 22 and the third ash hopper 33, the ash hopper gate valve 41 is opened, and the fly ash is discharged through the ash discharge pipe 42, so that the ash removal work is completed.
The ultra-clean emission device for flue gas desulfurization comprises a semi-dry reaction tower 1, an atomization deacidification reaction tower 2 and a bag type dust collector 3;
the top of the semidry method reaction tower 1 is connected with a first flue gas inlet pipeline 12 through a rotary atomizing device 11, and the bottom of the semidry method reaction tower is connected with a first ash bucket 13;
the atomization deacidification reaction tower 2 comprises a plurality of flow disturbing flower plates 21 positioned in the middle and a second ash hopper 22 positioned in the lower part; one end of a second flue gas inlet pipe 23 is connected with the first ash hopper 13, and the other end is connected with the second ash hopper 22; a venturi jet mixer 24 is located in the second flue gas inlet pipe 23; one end of an atomized alkali liquor inlet pipe 25 is connected with a Venturi jet mixer 24, and the other end is connected with an alkali liquor atomization device 26;
the upper part of the atomization deacidification reaction tower 2 is connected with the left side of the bag type dust collector 3 through a third flue gas inlet pipe 31;
the bag type dust collector 3 comprises a plurality of filter bags 32, a third ash bucket 33 is arranged at the bottom of each filter bag 32, and the right side of the bag type dust collector 3 is connected with a flue gas conveying pipeline 34.
The bottoms of the first ash hopper 13, the second ash hopper 22 and the third ash hopper 33 are connected with an ash discharge pipe 42 through an ash hopper gate valve 41.
The first ash bucket 13, the second ash bucket 22 and the third ash bucket 33 are provided with manholes 43 for later maintenance and overhaul.
In actual use, the particle diameters of the lime slurry fog drops generated in the step 1 and the alkali liquor fog drops generated in the step 2 are very small, and after the lime slurry fog drops and the alkali liquor fog drops are contacted with flue gas with high temperature, water in the fog drops can be evaporated to form alkaline solid powder.
Step 1, SO in flue gas is treated by lime slurry fog drops2The primary absorption is carried out, the desulfurization efficiency can reach more than 90 percent, and the SO is discharged2The concentration is about 50mg/Nm3。
The lime slurry used in step 1 has a concentration of 6-10%, preferably 8%.
The specific parameters of each device in the invention are determined after being designed according to the smoke condition.
The sequence of steps 1-3 must not be adjusted at will;
step 1, primary treatment: removing most of SO in flue gas2Reducing the medicament consumption of the step 2;
The fly ash discharged in the steps 1-3 is treated according to hazardous waste.
The invention is only a process flow of the flue gas desulfurization system of the waste incineration plant, and other systems are added before and after the process to achieve the denitration effect.
The invention realizes SO in flue gas in the waste incineration industry2And the construction cost and the operation cost of the desulfurization system are reduced as much as possible while the ultra-low emission target is achieved.
Compared with the existing flue gas desulfurization ultra-clean emission process, the flue gas desulfurization ultra-clean emission process has the advantages of simpler structure, smaller occupied area, higher practicability and higher commercial value, and is suitable for upgrading and transforming the flue gas purification system of old plants (particularly waste incineration plants with insufficient reserved land).
Other parts not described belong to the prior art.
Claims (9)
1. The technological process of the ultra-clean exhaust device for flue gas desulfurization is characterized by comprising the following steps:
step 1: flue gas enters the semi-dry reaction tower (1) through a first flue gas inlet pipeline (12), lime slurry is sprayed into the semi-dry reaction tower (1) through a rotary atomizing device (11), and the flue gas and lime slurry fog drops are mixed and contacted in the semi-dry reaction tower (1), so that the cooling of the flue gas is realized, and the flue gas is reacted; SO in flue gas2With Ca (OH) in lime slurry droplets2Acting to generate CaSO3And CaSO4And is solidified;
step 2: the flue gas treated in the step 1 enters a Venturi jet mixer (24) through a second flue gas inlet pipe (23); after being atomized by an alkali liquor atomization device (26), alkali liquor enters a Venturi jet mixer (24) through an atomized alkali liquor inlet pipe (25), and flue gas and alkali liquor fog drops are mixed under the action of the Venturi jet mixer (24) and then enter an atomized deacidification reaction tower (2);
the mixed gas of the flue gas and the alkali liquor fog drops is further mixed through a plurality of turbulence pattern plates (11); at the same time, SO in the flue gas2Reacting with NaOH in alkali liquor fog drops to generate Na2SO3And Na2SO4And is removed;
and step 3: and (3) enabling the flue gas treated in the step (2) to enter a bag type dust collector (3), and removing dust particles in the flue gas by using the bag type dust collector (3) to realize ultra-clean emission of flue gas desulfurization.
2. The process method of the flue gas desulfurization ultra-clean discharge device according to claim 1, wherein in the step 3, Ca (OH) which is not completely reacted in the step 1 and the step 2 is introduced into the bag-type dust collector (3) together with the flue gas treated in the step 22And NaOH powder, and the alkaline powder is adsorbed on the surface of the filter bag (32) and further reacts with the flue gas passing through the bag type dust collector (3), so that the ultra-clean emission of flue gas desulfurization is further realized.
3. The process method of the flue gas desulfurization ultra-clean discharging device according to claim 1, characterized in that in step 1, the concentration of the lime slurry is 6-10%.
4. The process method of the flue gas desulfurization ultra-clean discharging device according to the claim 3, characterized in that in the step 1, the residence time of the flue gas in the semi-dry reaction tower (1) is more than 20 s.
5. The process method of the flue gas desulfurization ultra-clean discharging device according to claim 4, characterized in that in step 2, the alkali solution is NaOH solution with concentration of 25% -30%, and the particle size of the alkali solution fog drops is not more than 10 μm.
6. The process method of the flue gas desulfurization ultra-clean discharging device according to the claim 5, characterized in that in the step 2, the residence time of the flue gas in the atomization deacidification reaction tower (2) is more than 6 s.
7. The process method of the flue gas desulfurization ultra-clean discharge device according to the claim 1, characterized in that in the steps 1, 2 and 3, the generated fly ash is collected by the first ash bucket (13), the second ash bucket (22) and the third ash bucket (33), the ash bucket gate valve (41) is opened, and the fly ash is discharged through the ash discharge pipe (42) to finish the ash removal work.
8. The flue gas desulfurization ultra-clean discharging device of the process method of the flue gas desulfurization ultra-clean discharging device according to any one of claims 1 to 7, characterized in that: comprises a semidry process reaction tower (1), an atomization deacidification reaction tower (2) and a bag type dust collector (3);
the top of the semidry method reaction tower (1) is connected with a first flue gas inlet pipeline (12) through a rotary atomizing device (11), and the bottom of the semidry method reaction tower is connected with a first ash bucket (13);
the atomization deacidification reaction tower (2) comprises a plurality of flow disturbing flower plates (21) positioned in the middle and a second ash bucket (22) positioned at the lower part; one end of a second flue gas inlet pipe (23) is connected with the first ash hopper (13), and the other end is connected with the second ash hopper (22); a venturi jet mixer (24) is located in the second flue gas inlet pipe (23); one end of an atomized alkali liquor inlet pipe (25) is connected with a Venturi jet mixer (24), and the other end is connected with an alkali liquor atomization device (26);
the upper part of the atomization deacidification reaction tower (2) is connected with a flue gas inlet of the bag type dust collector (3) through a third flue gas inlet pipe (31);
the bag type dust collector (3) comprises a plurality of filter bags (32), a third ash bucket (33) is arranged at the bottom of each filter bag (32), and the right side of the bag type dust collector (3) is connected with a flue gas conveying pipeline (34).
9. The flue gas desulfurization ultra-clean discharging device of claim 8, characterized in that: the bottoms of the first ash bucket (13), the second ash bucket (22) and the third ash bucket (33) are connected with an ash discharge pipe (42) through ash bucket gate valves (41).
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Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103406011A (en) * | 2013-08-26 | 2013-11-27 | 环境保护部南京环境科学研究所 | Equipment for treating burning tail gas of pesticide package waste |
| WO2014201487A1 (en) * | 2013-06-20 | 2014-12-24 | Technische Universität Wien | Process and apparatus for desulfurizing gas mixtures |
| CN109847554A (en) * | 2019-01-28 | 2019-06-07 | 淮阴工学院 | Middle high-sulfur flue gas compound desulfurizing process |
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Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2014201487A1 (en) * | 2013-06-20 | 2014-12-24 | Technische Universität Wien | Process and apparatus for desulfurizing gas mixtures |
| CN103406011A (en) * | 2013-08-26 | 2013-11-27 | 环境保护部南京环境科学研究所 | Equipment for treating burning tail gas of pesticide package waste |
| CN109847554A (en) * | 2019-01-28 | 2019-06-07 | 淮阴工学院 | Middle high-sulfur flue gas compound desulfurizing process |
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