CN210645862U - Dry deacidification treatment system for flue gas of garbage incinerator - Google Patents
Dry deacidification treatment system for flue gas of garbage incinerator Download PDFInfo
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- CN210645862U CN210645862U CN201921222617.2U CN201921222617U CN210645862U CN 210645862 U CN210645862 U CN 210645862U CN 201921222617 U CN201921222617 U CN 201921222617U CN 210645862 U CN210645862 U CN 210645862U
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- Prior art keywords
- flue gas
- sodium bicarbonate
- dry
- deacidification
- reactor
- Prior art date
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- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 title claims abstract description 63
- 239000003546 flue gas Substances 0.000 title claims abstract description 63
- UIIMBOGNXHQVGW-UHFFFAOYSA-M Sodium bicarbonate Chemical compound [Na+].OC([O-])=O UIIMBOGNXHQVGW-UHFFFAOYSA-M 0.000 claims abstract description 54
- 229910000030 sodium bicarbonate Inorganic materials 0.000 claims abstract description 27
- 235000017557 sodium bicarbonate Nutrition 0.000 claims abstract description 27
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims abstract description 22
- 238000001035 drying Methods 0.000 claims abstract description 11
- 229910052799 carbon Inorganic materials 0.000 claims abstract description 10
- 239000007789 gas Substances 0.000 claims abstract description 7
- 239000002699 waste material Substances 0.000 claims abstract description 7
- 238000002347 injection Methods 0.000 claims description 11
- 239000007924 injection Substances 0.000 claims description 11
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 claims description 5
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 3
- 229910021529 ammonia Inorganic materials 0.000 claims description 2
- 238000000034 method Methods 0.000 abstract description 19
- 239000002250 absorbent Substances 0.000 abstract description 10
- 230000002745 absorbent Effects 0.000 abstract description 10
- 239000003344 environmental pollutant Substances 0.000 abstract description 9
- 231100000719 pollutant Toxicity 0.000 abstract description 9
- 238000001179 sorption measurement Methods 0.000 abstract description 9
- 239000002253 acid Substances 0.000 abstract description 6
- 239000002918 waste heat Substances 0.000 abstract description 5
- 238000001816 cooling Methods 0.000 abstract description 4
- 238000005265 energy consumption Methods 0.000 abstract description 4
- 239000002351 wastewater Substances 0.000 abstract description 4
- 230000000694 effects Effects 0.000 abstract description 3
- 238000005201 scrubbing Methods 0.000 abstract description 3
- 239000000428 dust Substances 0.000 description 7
- MWUXSHHQAYIFBG-UHFFFAOYSA-N nitrogen oxide Inorganic materials O=[N] MWUXSHHQAYIFBG-UHFFFAOYSA-N 0.000 description 6
- 230000002378 acidificating effect Effects 0.000 description 4
- 238000010586 diagram Methods 0.000 description 4
- 238000005406 washing Methods 0.000 description 3
- HGUFODBRKLSHSI-UHFFFAOYSA-N 2,3,7,8-tetrachloro-dibenzo-p-dioxin Chemical compound O1C2=CC(Cl)=C(Cl)C=C2OC2=C1C=C(Cl)C(Cl)=C2 HGUFODBRKLSHSI-UHFFFAOYSA-N 0.000 description 2
- AXCZMVOFGPJBDE-UHFFFAOYSA-L calcium dihydroxide Chemical group [OH-].[OH-].[Ca+2] AXCZMVOFGPJBDE-UHFFFAOYSA-L 0.000 description 2
- 229910001861 calcium hydroxide Inorganic materials 0.000 description 2
- 239000000920 calcium hydroxide Substances 0.000 description 2
- 238000010276 construction Methods 0.000 description 2
- 229910001385 heavy metal Inorganic materials 0.000 description 2
- 238000000746 purification Methods 0.000 description 2
- 230000035484 reaction time Effects 0.000 description 2
- 238000004056 waste incineration Methods 0.000 description 2
- 239000010791 domestic waste Substances 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
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- Treating Waste Gases (AREA)
Abstract
In order to solve the existing problem, the utility model provides a waste incinerator flue gas dry process deacidification processing system gets rid of the wet process scrubbing tower, sets up sodium bicarbonate dry process reactor in bag collector's front. Flue gas at the outlet of the waste heat boiler enters a semi-dry type reaction tower to remove most of acid gas and then enters a sodium bicarbonate dry-method reactor, the reactor provides enough time and space for the reaction of the flue gas and a sodium bicarbonate absorbent and the adsorption of active carbon, and the temperature of the flue gas is the proper reaction temperature of the sodium bicarbonate and acid pollutants, so that the good deacidification effect is achieved by using less sodium bicarbonate absorbent, and the adsorption efficiency of the active carbon is improved; compared with wet deacidification, the process flow is greatly simplified, and deacidification wastewater is not generated; because no other cooling links are arranged behind the semi-dry type reaction tower, the reaction temperature is higher, the energy consumption is less when the flue gas is heated to the temperature required by SCR reaction, and the investment and the operation cost are greatly reduced.
Description
Technical Field
The utility model relates to a waste incinerator flue gas processing system especially relates to a waste incinerator flue gas dry process deacidification processing system.
Background
In order to meet the increasingly strict environmental protection requirements, the technical scheme of the existing flue gas purification system for a plurality of domestic waste incineration projects in China is as follows: the method comprises the steps of a semi-dry reaction tower (an absorbent is calcium hydroxide), activated carbon flue gas injection adsorption, a bag type dust collector, a #1 flue gas/flue gas heat exchanger, a wet washing tower, a #2 flue gas/flue gas heat exchanger, a steam/flue gas heat exchanger and an SCR reactor. This scheme is also known as wet deacidification. The process can greatly reduce the emission concentration of pollutants in the flue gas and meet the requirements stricter than the latest standards of European Union.
The method has the problems that the investment and operation cost of the wet deacidification method is very high, and heat exchangers are required to be added in front of and behind the wet deacidification method, so that the land area, the construction investment and the operation cost of a project are greatly increased.
SUMMERY OF THE UTILITY MODEL
In order to solve the existing problem, the utility model provides a waste incinerator flue gas dry process deacidification processing system gets rid of the wet process scrubbing tower, sets up sodium bicarbonate dry process reactor in bag collector's front. Compared with a wet deacidification method, the process flow is greatly simplified, and deacidification wastewater is not generated; because no other cooling links are arranged behind the semi-dry type reaction tower, the reaction temperature is higher, and the energy consumption for heating the flue gas to the temperature required by the SCR reaction is less, thereby greatly reducing the investment and operation cost and effectively solving the problems in the prior art.
The utility model provides a technical scheme that technical problem adopted is, a waste incinerator flue gas dry process deacidification processing system, according to the flow direction of flue gas, comprises semi-dry reaction tower, bag collector, flue gas heat exchanger, steam gas heat exchanger, SCR reactor, draught fan and chimney in proper order set up active carbon flue injection apparatus before the bag collector let in steam and heat the flue gas and remove the comdenstion water that produces before the steam gas heat exchanger let in ammonia, characterized by before the SCR reactor let in sodium bicarbonate dry process reactor in the front of bag collector still set up sodium bicarbonate flue injection apparatus before the active carbon flue injection apparatus.
The method comprises the following steps that flue gas flows out of a waste heat boiler and enters a semi-dry reaction tower for deacidification, the flue gas flowing out of the semi-dry reaction tower enters a sodium bicarbonate dry reactor and is fully mixed with a sodium bicarbonate absorbent and activated carbon sprayed in the semi-dry reaction tower, acidic pollutants in the flue gas are further reduced by utilizing the characteristics of the sodium bicarbonate and the full reaction time in the reaction tower, then the flue gas passes through a bag type dust collector, the acidic pollutants, heavy metals, dioxin and particulate matters in the flue gas are further removed from the surface of a filter bag, and finally the flue gas is discharged into the atmosphere through a chimney after reaching the SCR reaction temperature through a heat exchanger to remove nitrogen oxides.
The utility model has the advantages that: the utility model provides a waste incinerator flue gas dry process deacidification processing system gets rid of the wet process scrubbing tower, sets up sodium bicarbonate dry process reactor in bag collector's front. Flue gas at the outlet of the waste heat boiler enters a semi-dry type reaction tower to remove most of acid gas and then enters a sodium bicarbonate dry-method reactor, the reactor provides enough time and space for the reaction of the flue gas and a sodium bicarbonate absorbent and the adsorption of active carbon, and the temperature of the flue gas is the proper reaction temperature of the sodium bicarbonate and acid pollutants, so that the good deacidification effect is achieved by using less sodium bicarbonate absorbent, and the adsorption efficiency of the active carbon is improved; compared with wet deacidification, the process flow is greatly simplified, and deacidification wastewater is not generated; because no other cooling links are arranged behind the semi-dry type reaction tower, the reaction temperature is higher, the energy consumption is less when the flue gas is heated to the temperature required by SCR reaction, and the investment and the operation cost are greatly reduced.
Drawings
Fig. 1 is a schematic diagram of an apparatus arrangement according to an embodiment of the prior art.
Fig. 2 is a schematic diagram of an apparatus layout according to an embodiment of the present invention.
Detailed Description
Fig. 1 is a schematic diagram of an apparatus arrangement according to an embodiment of the prior art. In the prior art, the flue gas purification system for the waste incineration project adopts a combined process system of a semi-dry reaction tower (an absorbent is calcium hydroxide), activated carbon flue gas injection adsorption, a bag type dust collector, a 1 st flue gas/flue gas heat exchanger, a wet washing tower, a 2 nd flue gas/flue gas heat exchanger, a steam/flue gas heat exchanger and SCR, so that the process can greatly reduce the emission concentration of pollutants in the flue gas and meet the requirements of the latest standards of the European Union. However, the investment and operation cost of wet deacidification is very high, and heat exchangers are required to be added in front of and behind the investment and operation cost, so that the land area, the construction investment and the operation cost of a project are greatly increased.
Fig. 2 is a schematic diagram of an apparatus layout according to an embodiment of the present invention. In the figure, the system for dry deacidification of the flue gas of the garbage incinerator in the embodiment comprises a semi-dry reaction tower, a bag type dust collector, a flue gas/flue gas heat exchanger, a steam/flue gas heat exchanger, an SCR reactor, an induced draft fan and a chimney in sequence according to the flow direction of the flue gas, wherein an activated carbon flue injection device is arranged in front of the bag type dust collector, steam is introduced in front of the steam/flue gas heat exchanger to heat the flue gas and discharge the generated condensed water, and ammonia gas is introduced in front of the SCR reactor. Different from the prior art, in the embodiment, a wet washing tower is not arranged, a sodium bicarbonate dry reactor is arranged in front of the bag type dust collector, and a sodium bicarbonate flue injection device is arranged before the activated carbon flue injection adsorption.
The method comprises the following steps that flue gas flows out of a waste heat boiler and enters a semi-dry reaction tower for deacidification, the flue gas flowing out of the semi-dry reaction tower enters a sodium bicarbonate dry reactor and is fully mixed with a sodium bicarbonate absorbent and activated carbon sprayed in the semi-dry reaction tower, acidic pollutants in the flue gas are further reduced by utilizing the characteristics of the sodium bicarbonate and the full reaction time in the reaction tower, then the flue gas passes through a bag type dust collector, the acidic pollutants, heavy metals, dioxin and particulate matters in the flue gas are further removed from the surface of a filter bag, and finally the flue gas is discharged into the atmosphere through a chimney after reaching the SCR reaction temperature through a heat exchanger to remove nitrogen oxides.
Compared with the prior art, in the embodiment, the flue gas at the outlet of the waste heat boiler enters the semi-dry type reaction tower to remove most of acid gas and then enters the sodium bicarbonate dry reactor, the reactor provides enough time and space for the reaction of the flue gas and a sodium bicarbonate absorbent and the adsorption of active carbon, and the temperature of the flue gas is the proper reaction temperature of the sodium bicarbonate and acid pollutants, so that the good deacidification effect is ensured by using less sodium bicarbonate absorbent, and the adsorption efficiency of the active carbon is improved; compared with wet deacidification, the process flow is greatly simplified, and deacidification wastewater is not generated; because no other cooling links are arranged behind the semi-dry type reaction tower, the reaction temperature is higher, the energy consumption is less when the flue gas is heated to the temperature required by SCR reaction, and the investment and the operation cost are greatly reduced.
Claims (1)
1. The utility model provides a waste incinerator flue gas dry process deacidification processing system, according to the flow direction of flue gas, comprises half dry reaction tower, bag collector, flue gas heat exchanger, steam gas heat exchanger, SCR reactor, draught fan and chimney in proper order set up active carbon flue injection apparatus before the bag collector steam is let in before the steam gas heat exchanger and is heated the flue gas and discharge the comdenstion water that produces let in before the SCR reactor and let in the ammonia, characterized by bag collector set up sodium bicarbonate dry process reactor in the front, still set up sodium bicarbonate flue injection apparatus before active carbon flue injection apparatus.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201921222617.2U CN210645862U (en) | 2019-07-29 | 2019-07-29 | Dry deacidification treatment system for flue gas of garbage incinerator |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201921222617.2U CN210645862U (en) | 2019-07-29 | 2019-07-29 | Dry deacidification treatment system for flue gas of garbage incinerator |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN210645862U true CN210645862U (en) | 2020-06-02 |
Family
ID=70832940
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201921222617.2U Active CN210645862U (en) | 2019-07-29 | 2019-07-29 | Dry deacidification treatment system for flue gas of garbage incinerator |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN210645862U (en) |
-
2019
- 2019-07-29 CN CN201921222617.2U patent/CN210645862U/en active Active
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Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| GR01 | Patent grant | ||
| GR01 | Patent grant | ||
| CP01 | Change in the name or title of a patent holder | ||
| CP01 | Change in the name or title of a patent holder |
Address after: 518046 13th Floor, Times Financial Center, 4001 Shennan Avenue, Futian District, Shenzhen City, Guangdong Province Patentee after: Shenzhen Energy and environmental protection Co.,Ltd. Address before: 518046 13th Floor, Times Financial Center, 4001 Shennan Avenue, Futian District, Shenzhen City, Guangdong Province Patentee before: SHENZHEN ENERGY ENVIRONMENTAL ENGINEERING Co.,Ltd. |
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| PE01 | Entry into force of the registration of the contract for pledge of patent right | ||
| PE01 | Entry into force of the registration of the contract for pledge of patent right |
Denomination of utility model: A Dry Acid Removal Treatment System for Waste Incinerator Smoke Effective date of registration: 20231130 Granted publication date: 20200602 Pledgee: Shenzhen Energy Finance Co.,Ltd. Pledgor: Shenzhen Energy and environmental protection Co.,Ltd. Registration number: Y2023980068515 |
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| PC01 | Cancellation of the registration of the contract for pledge of patent right | ||
| PC01 | Cancellation of the registration of the contract for pledge of patent right |
Granted publication date: 20200602 Pledgee: Shenzhen Energy Finance Co.,Ltd. Pledgor: Shenzhen Energy and environmental protection Co.,Ltd. Registration number: Y2023980068515 |