CN115055054A - Low-resistance active coke flue gas purification device and process method - Google Patents
Low-resistance active coke flue gas purification device and process method Download PDFInfo
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- CN115055054A CN115055054A CN202210851990.4A CN202210851990A CN115055054A CN 115055054 A CN115055054 A CN 115055054A CN 202210851990 A CN202210851990 A CN 202210851990A CN 115055054 A CN115055054 A CN 115055054A
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- flue gas
- desulfurization
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- denitration
- active coke
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- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 title claims abstract description 156
- 239000003546 flue gas Substances 0.000 title claims abstract description 156
- 239000000571 coke Substances 0.000 title claims abstract description 107
- 238000000746 purification Methods 0.000 title claims abstract description 57
- 238000000034 method Methods 0.000 title claims abstract description 33
- 238000006477 desulfuration reaction Methods 0.000 claims abstract description 162
- 230000023556 desulfurization Effects 0.000 claims abstract description 160
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 claims abstract description 144
- 229910021529 ammonia Inorganic materials 0.000 claims abstract description 72
- 238000002347 injection Methods 0.000 claims abstract description 26
- 239000007924 injection Substances 0.000 claims abstract description 26
- 238000006243 chemical reaction Methods 0.000 claims abstract description 18
- 238000005192 partition Methods 0.000 claims description 55
- 238000005507 spraying Methods 0.000 claims description 43
- 239000000463 material Substances 0.000 claims description 13
- 238000001179 sorption measurement Methods 0.000 claims description 11
- 239000000203 mixture Substances 0.000 claims description 8
- 239000003344 environmental pollutant Substances 0.000 claims description 7
- 231100000719 pollutant Toxicity 0.000 claims description 7
- 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 claims description 6
- UCKMPCXJQFINFW-UHFFFAOYSA-N Sulphide Chemical compound [S-2] UCKMPCXJQFINFW-UHFFFAOYSA-N 0.000 claims description 6
- 229910001385 heavy metal Inorganic materials 0.000 claims description 6
- 241000251468 Actinopterygii Species 0.000 claims description 5
- 239000000428 dust Substances 0.000 claims description 5
- 238000010531 catalytic reduction reaction Methods 0.000 claims description 3
- 239000007921 spray Substances 0.000 claims description 3
- 150000003568 thioethers Chemical class 0.000 claims description 3
- RAHZWNYVWXNFOC-UHFFFAOYSA-N Sulphur dioxide Chemical compound O=S=O RAHZWNYVWXNFOC-UHFFFAOYSA-N 0.000 description 14
- MWUXSHHQAYIFBG-UHFFFAOYSA-N nitrogen oxide Inorganic materials O=[N] MWUXSHHQAYIFBG-UHFFFAOYSA-N 0.000 description 9
- 239000007789 gas Substances 0.000 description 8
- 239000000779 smoke Substances 0.000 description 7
- IJGRMHOSHXDMSA-UHFFFAOYSA-N nitrogen Substances N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 6
- 229910052757 nitrogen Inorganic materials 0.000 description 6
- 229910052717 sulfur Inorganic materials 0.000 description 6
- 239000011593 sulfur Substances 0.000 description 6
- 239000002245 particle Substances 0.000 description 3
- 238000004140 cleaning Methods 0.000 description 2
- 239000006227 byproduct Substances 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 239000000243 solution Substances 0.000 description 1
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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
- B01D53/86—Catalytic processes
- B01D53/90—Injecting reactants
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D49/00—Separating dispersed particles from gases, air or vapours by other methods
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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
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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
- B01D53/64—Heavy metals or compounds thereof, e.g. mercury
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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
- B01D53/72—Organic compounds not provided for in groups B01D53/48 - B01D53/70, e.g. hydrocarbons
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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
- 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
- B01D53/86—Catalytic processes
- B01D53/8621—Removing nitrogen compounds
- B01D53/8625—Nitrogen oxides
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2251/00—Reactants
- B01D2251/20—Reductants
- B01D2251/206—Ammonium compounds
- B01D2251/2062—Ammonia
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- 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
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- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2259/00—Type of treatment
- B01D2259/40—Further details for adsorption processes and devices
- B01D2259/40011—Methods relating to the process cycle in pressure or temperature swing adsorption
- B01D2259/40077—Direction of flow
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
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- B01D2259/40—Further details for adsorption processes and devices
- B01D2259/404—Further details for adsorption processes and devices using four beds
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Abstract
The invention belongs to the technical field of flue gas purification, and particularly relates to a low-resistance active coke flue gas purification device and a process method. The flue gas of the invention completes the reactions of desulfurization, ammonia injection and denitration in the active coke flue gas purification device, the flue gas does not need to be subjected to desulfurization, then is converged, redistributed and then is subjected to denitration, the flow field of the flue gas in the active coke flue gas purification device is uniform, the flue gas does not need to be turned back, and the running resistance of the system can be effectively reduced.
Description
Technical Field
The invention belongs to the technical field of flue gas purification, and particularly relates to a low-resistance active coke flue gas purification device and a process method.
Background
The active coke method flue gas purification technology can realize the integrated removal of various pollutants such as sulfide, oxynitride, particulate matters, dioxin, heavy metals and the like, has no secondary pollutant, can recycle byproducts, and can realize the economic and environmental collaborative development.
The active coke device and the process are divided into a counter-current bed device and a process and a cross-current bed device and a process according to different contact modes of flue gas and a coke layer in an active coke bed layer. The countercurrent bed device and the process are characterized in that two phases between the flue gas and the active coke are in countercurrent contact, and the cross flow bed device and the process are in vertical contact.
The countercurrent bed device and the process cause that the running resistance of the system is very large after the flue gas passes through the active coke adsorption bed layer due to the process principle and the structure form. The existing cross-flow bed device and process divide an active coke device into a desulfurization section and a denitration section, increase the processes of flue gas convergence in the desulfurization section and flue gas redistribution in the denitration section, have complex process flow of flue gas in an active coke system, and increase the running resistance of the system. According to the statistics of the air volume of each 100 ten thousand working conditions, the power consumption of the fan is increased by 35 kilowatts when the resistance of the system is increased by 100Pa, and the annual operation cost is greatly increased.
Disclosure of Invention
The invention aims to provide a low-resistance active coke flue gas purification device and a process method, which can optimize the flow process of flue gas in an active coke device, simultaneously complete the functions of desulfurization and denitrification in one active coke unit, and have small running resistance of the flue gas in the active coke flue gas purification device.
The purpose of the invention is realized by the following technical scheme:
the invention relates to a low-resistance active coke flue gas purification device, which is characterized in that one active coke flue gas purification device unit comprises an air inlet chamber, two desulfurization beds, two ammonia spraying chambers, two denitration beds and two air outlet chambers, wherein the two desulfurization beds and the two denitration beds are positioned on the same horizontal height, one ammonia spraying chamber is positioned between one pair of desulfurization beds and the denitration beds, the other ammonia spraying chamber is positioned between the other pair of desulfurization beds and the denitration beds, the air inlet chamber is positioned between the two desulfurization beds, the two air outlet chambers are positioned at two sides of one active coke flue gas purification device unit,
the desulfurization bed layer adopts a first desulfurization partition plate and a second desulfurization partition plate to divide the material layer into a first desulfurization bed, a second desulfurization bed and a third desulfurization bed along the flowing direction of the flue gas, and a desulfurization section discharger is respectively arranged below the corresponding desulfurization beds,
the denitration bed adopts first denitration division board and second denitration division board to separate into first denitration bed, second denitration bed, the third denitration bed of material along flue gas flow direction, sets up the denitration section tripper below the denitration bed of correspondence respectively.
The utility model discloses a denitration device, including the air inlet chamber, the denitration bed, the air inlet chamber, set up first division board of admitting air between desulfurization bed layer, the desulfurization bed layer respectively with spout and set up the first division board of giving vent to anger between the ammonia chamber, spout and set up the second division board of admitting air between ammonia chamber and the denitration bed layer, the denitration bed layer with go out to set up the second division board of giving vent to anger between the air outlet chamber, first division board, the first division board of giving vent to anger, the second division board of admitting air and the second division board of giving vent to anger be "shutter" type grid plate, "fish scale board" or perforated plate.
The desulfurization bed layer set up first desulfurization division board and second desulfurization division board, the denitration bed layer set up first denitration division board and second denitration division board, first desulfurization division board, second desulfurization division board, first denitration division board and second denitration division board be "shutter" type's grid plate, "fish scale board" or perforated plate.
The circulation speed of the active coke in the first desulfurization bed is higher than that of the active coke in the second desulfurization bed, the circulation speed of the active coke in the second desulfurization bed is higher than that of the active coke in the third desulfurization bed, the circulation speed of the active coke in the first denitrification bed is higher than that of the active coke in the second denitrification bed, and the circulation speed of the active coke in the second denitrification bed is higher than that of the active coke in the third denitrification bed.
The ammonia spraying chamber is a rectangular, trapezoidal or wedge-shaped cavity, and a plurality of layers of ammonia spraying grids, a plurality of ammonia spraying ports or spray guns are arranged in the ammonia spraying chamber.
The smoke in the two air outlet chambers is respectively converged by a pipeline and is respectively controlled by a valve or the smoke in the two air outlet chambers is converged into a pipeline and is uniformly controlled by the valve.
A low-resistance active coke flue gas purification process method is characterized in that: after entering an air inlet chamber of the active coke flue gas purification device, the flue gas uniformly flows to the desulfurization bed layers at two sides, and the flue gas and the active coke are subjected to adsorption reaction in the desulfurization bed layers to remove sulfides in the flue gas;
the flue gas after the sulfide removal enters an ammonia spraying chamber, an ammonia spraying device is arranged in the ammonia spraying chamber, and the flue gas is fully mixed with ammonia gas sprayed by the ammonia spraying device to form flue gas-ammonia gas mixture;
the flue gas-ammonia gas mixture sequentially enters a denitration bed layer, selective catalytic reduction denitration reaction is carried out in the denitration bed layer, after nitrogen oxides in the flue gas are removed, the flue gas enters an air outlet chamber and then is discharged out of the system;
the flue gas synchronously completes the adsorption reaction of pollutants such as dust, dioxin, heavy metals and the like in a desulfurization bed layer and a denitration bed layer.
The invention has the advantages that:
according to the low-resistance active coke flue gas purification device and the process method, flue gas is subjected to desulfurization, ammonia spraying and denitration reactions in one active coke flue gas purification device, the flue gas is not required to be subjected to desulfurization, then is converged, redistributed and then is subjected to denitration, the flow field of the flue gas in the active coke flue gas purification device is uniform, the flue gas is not required to be turned back, and the running resistance of the system can be effectively reduced.
Drawings
Fig. 1 is a front view of embodiment 1 of the present invention.
Fig. 2 is a plan view of embodiment 1 of the present invention.
Fig. 3 is a front view of embodiment 2 of the present invention.
Fig. 4 is a top view of embodiment 2 of the present invention.
Reference numerals: a-an inlet chamber; b1 and b 2-desulfurization beds; b11, b 21-first desulfurization bed; b12, b 22-second desulfurization bed; b13, b 23-third desulfurization bed; c1, c 2-ammonia spraying chamber; e1, e 2-denitration beds; e11, e 21-first denitrating bed; e12, e 22-second denitrating bed; e13, e 23-third denitrif iotacation bed; f1, f 2-outlet chamber; s1, S1' -first desulfurization splitter plate; s2, S2' -second desulfurization partition plate; n1, N1' -first denitration separating plate; n2, N2' -second denitration separator; t1, T1' first intake splitter plate; t2, T2' -the first air outlet partition plate; t3, T3' -second intake splitter plate; t4, T4' -the second air outlet partition board; d1, d 2-ammonia injection device; XS11, XS12, XS13, XS21, XS22, XS 23-desulfurization section discharger; XN11, XN12, XN13, XN21, XN22, XN 23-denitration section discharger.
Detailed Description
The following further describes the embodiments of the present invention with reference to the drawings.
As shown in fig. 1-4, the low resistance active coke flue gas purification device of the invention is characterized in that one active coke flue gas purification device unit comprises an air inlet chamber a, two desulfurization beds b1 and b2, two ammonia injection chambers c1 and c2, two denitration beds e1 and e2, and two air outlet chambers f1 and f2, wherein the two desulfurization beds b1 and b2 and the two denitration beds e1 and e2 are all at the same horizontal height, the ammonia injection chamber c1 is located between the desulfurization bed b1 and the denitration bed e1, the ammonia injection chamber c2 is located between the desulfurization bed b2 and the denitration bed e2, the air inlet chamber a is located between the desulfurization beds b1 and b2, the air outlet chambers f1 and f2 are located at two sides of one active coke flue gas purification device unit,
the desulfurization beds b1 and b2 adopt a first desulfurization partition plate S1 (S1 ') and a second desulfurization partition plate S2 (S2') to divide a material layer into a first desulfurization bed b11 and b21, a second desulfurization bed b12 and b22 and a third desulfurization bed b13 and b23 along the flow direction of flue gas, and desulfurization section dischargers XS11, XS12, XS13, XS21, XS22 and XS23 are respectively arranged below the corresponding desulfurization beds, wherein the first desulfurization beds b11 and b21, the second desulfurization beds b12 and b22 and the third desulfurization beds b13 and b23 are optional, and the number of the separation of the desulfurization beds is 1-3.
The denitration beds e1 and e2 adopt a first denitration division plate N1 (N1 ') and a second denitration division plate N2 (N2') to divide the material layer into a first denitration bed e11 and e21, a second denitration bed e12 and e22 and a third denitration bed e13 and e23 along the flowing direction of the flue gas, and denitration section dischargers XN11, XN12, XN13, XN21, XN22 and XN23 are respectively arranged below the corresponding denitration beds. The first denitration beds e11 and e21, the second denitration beds e12 and e22 and the third denitration beds e13 and e23 are optional, and the number of the denitration beds is 1-3.
Determining the thicknesses of the material layers of the first desulfurization beds b11 and b21, the second desulfurization beds b12 and b22 and the third desulfurization beds b13 and b23 according to the concentration of sulfur dioxide in the flue gas, determining the thicknesses of the material layers of the first denitrification beds e11 and e21, the second denitrification beds e12 and e22 and the third denitrification beds e13 and e23 according to the concentration of nitrogen oxides in the flue gas, and respectively controlling the feeding speed through variable-frequency dischargers XS11, XS21, XS12, XS22, XS13, XS23, XN11, XN21, XN12, XN22, XN13 and XN23 below the respective material layers.
A first air inlet partition plate T1 (T1 ') is arranged between the air inlet chamber a and the desulfurization beds b1 and b2, first air outlet partition plates T2 (T2') are arranged between the desulfurization beds b1 and b2 and the ammonia injection chambers c1 and c2 respectively, second air inlet partition plates T3 (T3 ') are arranged between the ammonia injection chambers c1 and c2 and the denitration beds e1 and e2, second air outlet partition plates T4 (T4') are arranged between the denitration beds e1 and e2 and the air outlet chambers f1 and f2, and the first air inlet partition plate T1 (T1 '), the first air outlet partition plate T2 (T2'), the second air inlet partition plate T3 (T3 ') and the second air outlet partition plate T4 (T4') are louver type grating plates or porous plates. The partition plate has a structure which allows smoke to pass through but does not allow active coke particles to pass through,
the desulfurization bed layer a is provided with a first desulfurization partition plate S1 (S1 ') and a second desulfurization partition plate S2 (S2'), and the denitration bed layer b is provided with a first denitration partition plate N1 (N1 ') and a second denitration partition plate N2 (N2'), wherein the first desulfurization partition plate S1 (S1 '), the second desulfurization partition plate S2 (S2'), the first denitration partition plate N1 (N1 ') and the second denitration partition plate N2 (N2') are louver type grating plates, fish scale plates or porous plates.
The circulation speed of the active coke in the first desulfurization beds b11 and b21 is higher than that of the active coke in the second desulfurization beds b12 and b22, the circulation speed of the active coke in the second desulfurization beds b12 and b22 is higher than that of the active coke in the third desulfurization beds b13 and b23, the circulation speed of the active coke in the first denitrification beds e11 and e21 is higher than that of the active coke in the second denitrification beds e12 and e22, and the circulation speed of the active coke in the second denitrification beds e12 and e22 is higher than that of the active coke in the third denitrification beds e13 and e 23.
The ammonia spraying chambers c1 and c2 are rectangular, trapezoidal or wedge-shaped cavities, and a plurality of layers of ammonia spraying grids and a plurality of ammonia spraying openings or spray guns are arranged in the ammonia spraying chambers c1 and c 2.
The flue gas in the two outlet chambers f1 and f2 is respectively controlled by valves when being converged by pipelines or the flue gas in the two outlet chambers f1 and f2 is converged into one pipeline and is controlled by valves uniformly.
The active coke device can be formed by connecting a plurality of active coke device units in parallel or in series according to the amount of flue gas to be treated.
A low-resistance active coke flue gas purification process method is characterized in that: after entering an air inlet chamber a of the active coke flue gas purification device, flue gas uniformly flows to the desulfurization bed layers b1 and b2 on two sides, and the flue gas and active coke in the desulfurization bed layers b1 and b2 are subjected to adsorption reaction to remove sulfides in the flue gas;
the flue gas after sulfide removal enters ammonia spraying chambers c1 and c2, ammonia spraying devices d1 and d2 are arranged in the ammonia spraying chambers c1 and c2, and the flue gas is fully mixed with ammonia sprayed by the ammonia spraying devices d1 or d2 to form flue gas-ammonia gas mixture;
the flue gas-ammonia gas mixture sequentially enters a denitration bed layer e1 and a denitration bed layer e2, selective catalytic reduction denitration reaction is carried out in the denitration bed layer, after nitrogen oxides in the flue gas are removed, the flue gas enters gas outlet chambers f1 and f2, and then is discharged out of the system;
the flue gas synchronously completes the adsorption reaction of pollutants such as dust, dioxin, heavy metals and the like in a desulfurization bed layer b1, a desulfurization bed layer b2, a denitration bed layer e1 and a denitration bed layer e 2.
In order to make the objects, technical solutions and advantages of the present invention more apparent, the present invention will be described in detail with reference to the accompanying drawings and specific embodiments.
Fig. 1 and fig. 2 show a front view and a top view of a low resistance active coke flue gas cleaning device according to embodiment 1 of the present invention, respectively. The low-resistance active coke flue gas purification device unit comprises 1 air inlet chamber a; 2 desulfurization beds b1 and b 2; 2 ammonia injection chambers c1 and c 2; 2 denitration beds e1 and e 2; 2 outlet chambers f1 and f 2. 2 desulfurization beds b1 and b2 and 2 denitration beds e1 and e2 are all located at the same horizontal height, and ammonia injection chamber c1 is located between desulfurization bed b1 and denitration bed e1, and ammonia injection chamber c2 is located between desulfurization bed b2 and denitration bed e2, and inlet chamber a is located between desulfurization beds b1 and b2, and outlet chambers f1 and f2 are located on both sides of an active coke flue gas purification device unit.
Desulfurization beds b1 and b2, first desulfurization beds b11 and b21, second desulfurization beds b12 and b22, and third desulfurization beds b13 and b23 which divide the material layer into two parts along the flowing direction of the flue gas by using a first desulfurization partition plate S1 (S1 ') and a second desulfurization partition plate S2 (S2');
denitration beds e1 and e2, first denitration beds e11 and e21 and second denitration beds e12 and e22 which divide the material layer into a first denitration bed e11 and e21 and a second denitration bed e12 and e22 along the flowing direction of the flue gas by adopting first denitration partition plates N1 and N1';
the low-resistance active coke flue gas purification device of embodiment 1 treats high-sulfur low-nitrogen flue gas, and the process flow of the flue gas in the device is as follows: when the high-sulfur low-nitrogen flue gas enters the air inlet chamber a of the flue device, the high-sulfur low-nitrogen flue gas uniformly flows to the two side desulfurization beds b1 and b 2. In the desulfurization bed layers b1 and b2, the flue gas firstly passes through the first desulfurization beds b11 and b21, most of sulfur dioxide in the flue gas is adsorbed in the beds, and the active coke in the first desulfurization beds is quickly discharged out of the system through the bottom dischargers XS11 and XS 21. The flue gas then flows horizontally to the second desulfurization beds b12 and b22, in the second desulfurization beds b12 and b22, the residual sulfur dioxide in the flue gas is continuously contacted with the sulfur dioxide in the beds to generate an adsorption reaction, and the active coke in the second desulfurization beds is discharged out of the system through the bottom dischargers XS12 and XS 22. The flue gas then advects to a third desulfurization bed b13, b23, after deep desulfurization in the bed, advects to an ammonia spraying chamber c1 and c 2. The active coke in the third desulfurization bed is discharged out of the system through the bottom dischargers XS13 and XS 23.
The total thickness of the desulfurization beds is 2200mm, wherein the thicknesses of the first desulfurization beds b11 and b21 are 400mm, the thicknesses of the second desulfurization beds b12 and b22 are 700mm, and the thicknesses of the third desulfurization beds b13 and b23 are 1100 mm.
The flue gas after sulfide removal enters the ammonia spraying chambers c1 and c2, and is fully mixed with ammonia gas sprayed by the ammonia spraying devices d1 and d2 arranged in the ammonia spraying chambers c1 and c2 to form flue gas-ammonia gas mixed gas. . The concentration of oxynitride in the flue gas is lower, and 2 rows of 3 layers of ammonia spraying grids are arranged in the ammonia spraying chamber. Flue gas-ammonia gas mixture advection enters a denitration bed layer e1 and a denitration bed layer e2, most oxynitride is removed in a first denitration bed e11 and a first denitration bed e21, active coke in the first denitration bed is discharged out of a system through a discharger XN11 and a discharger XN21 which are arranged at the bottom, the flue gas advection flows to a second denitration bed e12 and a second denitration bed e22, after deep denitration reaction occurs in the bed layers, the flue gas advection flows to a gas outlet chamber f1 and a gas outlet chamber f2, and the active coke in the second denitration bed is discharged out of the system through a discharger XN12 and a discharger XN22 which are arranged at the bottom. The flue gas synchronously completes the adsorption reaction of pollutants such as dust, dioxin, heavy metals and the like in a desulfurization bed layer b1, a desulfurization bed layer b2, a denitration bed layer e1 and a denitration bed layer e 2. The whole flue gas flowing process is advection, and the flue gas running resistance is small.
The total thickness of the denitration beds is 1600mm, wherein the thicknesses of the first denitration beds e11 and e21 are 500mm, and the thicknesses of the second denitration beds e12 and e22 are 1100 mm.
Further, in the low resistance active coke flue gas purification device with the structure, a first air inlet division plate T1 (T1 ') is arranged between the air inlet chamber a and the desulfurization beds b1 and b2, first air outlet division plates T2 (T2 ') are arranged between the desulfurization beds b1 and b2 and the ammonia injection chambers c1 and c2 respectively, second air inlet division plates T3 (T3 ') are arranged between the ammonia injection chambers c1 and c2 and the denitration beds e1 and e2, and second air outlet division plates T4 (T4 ') are arranged between the denitration beds e1 and e2 and the air outlet chambers f1 and f2, and the grid plates in a ' louver ' type ' are adopted, so that the low resistance active coke flue gas purification device has a structure which allows flue gas to pass through and does not allow active coke particles to pass through.
Further, in the low resistance active coke flue gas purification device with the structure, the desulfurization bed layer a is provided with the first desulfurization partition plate S1 (S1 ') and the second desulfurization partition plate S2 (S2 '), the denitration bed layer b is provided with the first denitration partition plate N1 (N1 '), and the partition plate adopts a porous plate.
Further, the low-resistance active coke flue gas purification device with the structure has the advantages that the ammonia spraying chambers c1 and c2 are of rectangular structures, the width is 500-600 mm, and the requirement for overhauling of the ammonia spraying device is met.
Further, the smoke in the two gas outlet chambers f1 and f2 of the low-resistance active coke smoke purification device with the structure is converged and then is independently controlled by a valve on a converging pipeline, so that the device has higher operation adaptability and operation elasticity.
Furthermore, according to the low-resistance active coke flue gas purification device with the structure, 4 low-resistance active coke flue gas purification device units are selected and connected in parallel to jointly treat the flue gas to be treated according to the flue gas treatment amount.
Fig. 3 and fig. 4 show a front view and a top view of a low resistance active coke flue gas cleaning device of embodiment 2 of the present invention, respectively. The low-resistance active coke flue gas purification device unit comprises 1 air inlet chamber a; 2 desulfurization beds b1 and b 2; 2 ammonia injection chambers c1 and c 2; 2 denitration beds e1 and e 2; 2 outlet chambers f1 and f 2. 2 desulfurization beds b1 and b2 and 2 denitration beds e1 and e2 are all located at the same horizontal height, and ammonia injection chamber c1 is located between desulfurization bed b1 and denitration bed e1, and ammonia injection chamber c2 is located between desulfurization bed b2 and denitration bed e2, and inlet chamber a is located between desulfurization beds b1 and b2, and outlet chambers f1 and f2 are located on both sides of an active coke flue gas purification device unit.
The desulfurization bed layers b1 and b2 adopt first desulfurization partition plates S1 and S1' along the flowing direction of the flue gas to divide the material layer into first desulfurization beds b11 and b21 and second desulfurization beds b12 and b 22;
denitration beds e1 and e2, wherein a first denitration partition plate N1 (N1 ') and N2 (N2') are adopted to divide the material layer into a first denitration bed e11 and e21, a second denitration bed e12 and e22 and a third denitration bed e13 and e23 along the flowing direction of the flue gas;
the low-resistance active coke flue gas purification device of embodiment 2 treats low-sulfur high-nitrogen flue gas, and the process flow of the flue gas in the device is as follows: when the low-sulfur high-nitrogen flue gas enters the air inlet chamber a of the flue device, the low-sulfur high-nitrogen flue gas uniformly flows to the desulfurization bed layers b1 and b2 on two sides. In the desulfurization bed layers b1 and b2, the flue gas firstly passes through the first desulfurization beds b11 and b21, most of sulfur dioxide in the flue gas is adsorbed in the beds, and the active coke in the first desulfurization beds is quickly discharged out of the system through the bottom dischargers XS11 and XS 21. The flue gas then flows to the second desulfurization beds b12 and b22 in an advection mode, in the second desulfurization beds b12 and b22, the residual sulfur dioxide in the flue gas is continuously contacted with the sulfur dioxide in the beds, after deep adsorption reaction, the flue gas flows to the ammonia spraying chambers c1 and c2 in an advection mode, and the active coke in the second desulfurization beds is discharged out of the system through the bottom dischargers XS12 and XS 22.
The total thickness of the desulfurization bed layers is 2000mm, wherein the thicknesses of the first desulfurization beds b11 and b21 are 500mm, and the thicknesses of the second desulfurization beds b12 and b22 are 1500 mm.
The flue gas after sulfide removal enters the ammonia spraying chambers c1 and c2, and is fully mixed with ammonia gas sprayed by the ammonia spraying devices d1 and d2 arranged in the ammonia spraying chambers c1 and c2 to form flue gas-ammonia gas mixed gas. The concentration of oxynitride in the flue gas is higher, and 4 rows of 4 layers of ammonia spraying grids are arranged in the ammonia spraying chamber. Flue gas-ammonia gas mixture advection enters a denitration bed layer e1 and a denitration bed layer e2, most oxynitride is removed in a first denitration bed e11 and a first denitration bed e21, active coke in the first denitration bed is discharged out of a system through a discharger XN11 and an discharger XN21 arranged at the bottom, the flue gas advection enters a second denitration bed e12 and a second denitration bed e22, denitration reaction continues to occur in the beds, the active coke in the second denitration bed is discharged out of the system through the discharger XN12 and the discharger XN22 arranged at the bottom, the flue gas advection flows to the second denitration bed e13 and the second denitration bed e23, the flue gas enters an air outlet chamber f1 and an air outlet chamber f2 after deep denitration in the beds, and the active coke in the third denitration bed is discharged out of the system through the discharger XN13 and the discharger XN23 arranged at the bottom. The flue gas synchronously completes the adsorption reaction of pollutants such as dust, dioxin, heavy metals and the like in a desulfurization bed layer b1, a desulfurization bed layer b2, a denitration bed layer e1 and a denitration bed layer e 2. The whole flue gas flowing process is advection, and the flue gas running resistance is small.
The total thickness of the denitration beds is 2000mm, wherein the thicknesses of the first denitration beds e11 and e21 are 300mm, the thicknesses of the second denitration beds e12 and e22 are 600mm, and the thicknesses of the third denitration beds e13 and e23 are 1100 mm.
Further, in the low resistance active coke flue gas purification device with the structure, a first air inlet division plate T1 (T1 ') is arranged between the air inlet chamber a and the desulfurization beds b1 and b2, first air outlet division plates T2 (T2 ') are arranged between the desulfurization beds b1 and b2 and the ammonia injection chambers c1 and c2 respectively, second air inlet division plates T3 (T3 ') are arranged between the ammonia injection chambers c1 and c2 and the denitration beds e1 and e2, and second air outlet division plates T4 (T4 ') are arranged between the denitration beds e1 and e2 and the air outlet chambers f1 and f2, and the grid plates in a ' louver ' type ' are adopted, so that the low resistance active coke flue gas purification device has a structure which allows flue gas to pass through and does not allow active coke particles to pass through.
Further, in the low-resistance active coke flue gas purification device with the structure, the desulfurization bed layer a is provided with the first desulfurization partition plate S1 (S1 '), the denitration bed layer b is provided with the first denitration partition plate N1 (N1 ') and the second denitration partition plate N2 (N2 '), and porous plates are adopted as the partition plates.
Further, the active burnt gas purification device of low resistance of this kind of structure, ammonia injection chamber c1 and c2 are the rectangle structure, and the width is ~800mm to and satisfied the requirement that the arrangement of ammonia injection grid requires and satisfied the demand that the ammonia injection device overhauld again.
Further, the smoke in the two gas outlet chambers f1 and f2 of the low-resistance active coke smoke purification device with the structure is converged and then is independently controlled by a valve on a converging pipeline, so that the device has higher operation adaptability and operation elasticity.
Furthermore, according to the low-resistance active coke flue gas purification device with the structure, 3 low-resistance active coke flue gas purification device units are selected and connected in parallel to jointly treat the flue gas to be treated according to the flue gas treatment amount.
According to the low-resistance active coke flue gas purification device and the process method, flue gas is subjected to desulfurization, ammonia spraying and denitration reactions in one active coke flue gas purification device, the flue gas is not required to be subjected to desulfurization, then is converged, redistributed and then is subjected to denitration, the flow field of the flue gas in the active coke flue gas purification device is uniform, the flue gas is not required to be turned back, and the running resistance of the system can be effectively reduced.
Claims (7)
1. A low-resistance active coke flue gas purification device is characterized in that one active coke flue gas purification device unit comprises an air inlet chamber, two desulfurization beds, two ammonia spraying chambers, two denitration beds and two air outlet chambers, wherein the two desulfurization beds and the two denitration beds are at the same horizontal height, one ammonia spraying chamber is positioned between one pair of desulfurization beds and one denitration bed, the other ammonia spraying chamber is positioned between the other pair of desulfurization beds and the other denitration beds, the air inlet chamber is positioned between the two desulfurization beds, the two air outlet chambers are positioned at two sides of one active coke flue gas purification device unit,
the desulfurization bed layer adopts a first desulfurization partition plate and a second desulfurization partition plate to divide the material layer into a first desulfurization bed, a second desulfurization bed and a third desulfurization bed along the flowing direction of the flue gas, and a desulfurization section discharger is respectively arranged below the corresponding desulfurization beds,
the denitration bed adopts first denitration division board and second denitration division board to become first denitration bed, second denitration bed, the third denitration bed that the bed of material separated into along flue gas flow direction, sets up the denitration section tripper below the corresponding denitration bed respectively.
2. The low-resistance active coke flue gas purification device according to claim 1, wherein a first air inlet partition plate is arranged between the air inlet chamber and the desulfurization bed layer, a first air outlet partition plate is arranged between the desulfurization bed layer and the ammonia injection chamber, a second air inlet partition plate is arranged between the ammonia injection chamber and the denitration bed layer, a second air outlet partition plate is arranged between the denitration bed layer and the air outlet chamber, and the first air inlet partition plate, the first air outlet partition plate, the second air inlet partition plate and the second air outlet partition plate are louver-type grid plates, "fish scales" or perforated plates.
3. The low-resistance active coke flue gas purification device of claim 1, wherein the desulfurization bed layer is provided with a first desulfurization partition plate and a second desulfurization partition plate, the denitrification bed layer is provided with a first denitrification partition plate and a second denitrification partition plate, and the first desulfurization partition plate, the second desulfurization partition plate, the first denitrification partition plate and the second denitrification partition plate are louver-type grid plates, "fish scales" or perforated plates.
4. The low-resistance active coke flue gas purification device of claim 1, wherein the circulation speed of the active coke in the first desulfurization bed is higher than the circulation speed of the active coke in the second desulfurization bed, the circulation speed of the active coke in the second desulfurization bed is higher than the circulation speed of the active coke in the third desulfurization bed, the circulation speed of the active coke in the first denitrification bed is higher than the circulation speed of the active coke in the second denitrification bed, and the circulation speed of the active coke in the second denitrification bed is higher than the circulation speed of the active coke in the third denitrification bed.
5. The low-resistance active coke flue gas purification device according to claim 1, wherein the ammonia injection chamber is a rectangular, trapezoidal or wedge-shaped cavity, and a multilayer ammonia injection grid, a plurality of ammonia injection ports or a spray gun is arranged in the ammonia injection chamber.
6. The low resistance active coke flue gas purification device of claim 1, wherein the flue gas in the two outlet chambers is respectively controlled by valves for converging pipes or is uniformly controlled by valves for converging the flue gas in the two outlet chambers into a pipe.
7. A low-resistance active coke flue gas purification process method is characterized in that: after entering an air inlet chamber of the active coke flue gas purification device, flue gas uniformly flows to the desulfurization bed layers on two sides, and the flue gas and active coke are subjected to adsorption reaction in the desulfurization bed layers to remove sulfides in the flue gas;
the flue gas after the sulfide removal enters an ammonia spraying chamber, an ammonia spraying device is arranged in the ammonia spraying chamber, and the flue gas is fully mixed with ammonia gas sprayed by the ammonia spraying device to form flue gas-ammonia gas mixture;
the flue gas-ammonia gas mixture sequentially enters a denitration bed layer, a selective catalytic reduction denitration reaction is carried out in the denitration bed layer, after oxynitride in the flue gas is removed, the flue gas enters an air outlet chamber and then is discharged out of a system;
the flue gas synchronously completes the adsorption reaction of pollutants such as dust, dioxin, heavy metals and the like in a desulfurization bed layer and a denitration bed layer.
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN116726682A (en) * | 2023-08-14 | 2023-09-12 | 北京中航泰达环保科技股份有限公司 | Dry desulfurization, denitrification and dust removal device and modular dry desulfurization, denitrification and dust removal system |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103203160A (en) * | 2013-02-28 | 2013-07-17 | 煤炭科学研究总院 | Flue gas combined desulfurization denitration demercuration device and method thereof |
| CN107469600A (en) * | 2017-09-27 | 2017-12-15 | 重集团大连工程建设有限公司 | A kind of composite bed purifying column |
| CN207614615U (en) * | 2017-12-07 | 2018-07-17 | 国电科学技术研究院 | A kind of activated coke smoke eliminator of sulphur nitre integration removing |
| CN215086187U (en) * | 2021-04-30 | 2021-12-10 | 一重集团大连工程建设有限公司 | A multistage ammonia purification tower that spouts for flue gas active coke method degree of depth SOx/NOx control |
| CN217662574U (en) * | 2022-07-20 | 2022-10-28 | 中冶北方（大连）工程技术有限公司 | Low-resistance active coke flue gas purification device |
-
2022
- 2022-07-20 CN CN202210851990.4A patent/CN115055054A/en active Pending
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103203160A (en) * | 2013-02-28 | 2013-07-17 | 煤炭科学研究总院 | Flue gas combined desulfurization denitration demercuration device and method thereof |
| CN107469600A (en) * | 2017-09-27 | 2017-12-15 | 重集团大连工程建设有限公司 | A kind of composite bed purifying column |
| CN207614615U (en) * | 2017-12-07 | 2018-07-17 | 国电科学技术研究院 | A kind of activated coke smoke eliminator of sulphur nitre integration removing |
| CN215086187U (en) * | 2021-04-30 | 2021-12-10 | 一重集团大连工程建设有限公司 | A multistage ammonia purification tower that spouts for flue gas active coke method degree of depth SOx/NOx control |
| CN217662574U (en) * | 2022-07-20 | 2022-10-28 | 中冶北方（大连）工程技术有限公司 | Low-resistance active coke flue gas purification device |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN116726682A (en) * | 2023-08-14 | 2023-09-12 | 北京中航泰达环保科技股份有限公司 | Dry desulfurization, denitrification and dust removal device and modular dry desulfurization, denitrification and dust removal system |
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