CN113144772A - Two-section type electrolytic flue gas purification and discharge device, control system and method - Google Patents
Two-section type electrolytic flue gas purification and discharge device, control system and method Download PDFInfo
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- CN113144772A CN113144772A CN202110483469.5A CN202110483469A CN113144772A CN 113144772 A CN113144772 A CN 113144772A CN 202110483469 A CN202110483469 A CN 202110483469A CN 113144772 A CN113144772 A CN 113144772A
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- 238000000746 purification Methods 0.000 title claims abstract description 173
- 239000003546 flue gas Substances 0.000 title claims abstract description 90
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 title claims abstract description 86
- 238000000034 method Methods 0.000 title claims abstract description 45
- 238000001179 sorption measurement Methods 0.000 claims abstract description 147
- 238000006477 desulfuration reaction Methods 0.000 claims abstract description 119
- 230000023556 desulfurization Effects 0.000 claims abstract description 115
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 claims abstract description 76
- 229910001861 calcium hydroxide Inorganic materials 0.000 claims abstract description 60
- 239000000920 calcium hydroxide Substances 0.000 claims abstract description 60
- AXCZMVOFGPJBDE-UHFFFAOYSA-L calcium dihydroxide Chemical compound [OH-].[OH-].[Ca+2] AXCZMVOFGPJBDE-UHFFFAOYSA-L 0.000 claims abstract description 59
- 238000006243 chemical reaction Methods 0.000 claims abstract description 36
- 230000003009 desulfurizing effect Effects 0.000 claims abstract description 26
- 238000005868 electrolysis reaction Methods 0.000 claims abstract description 23
- 238000002156 mixing Methods 0.000 claims abstract description 22
- 239000007921 spray Substances 0.000 claims abstract description 20
- 238000005507 spraying Methods 0.000 claims abstract description 17
- 238000000926 separation method Methods 0.000 claims abstract description 14
- 239000007789 gas Substances 0.000 claims abstract description 12
- XAGFODPZIPBFFR-UHFFFAOYSA-N aluminium Chemical compound [Al] XAGFODPZIPBFFR-UHFFFAOYSA-N 0.000 claims abstract description 10
- 229910052782 aluminium Inorganic materials 0.000 claims abstract description 10
- 238000006115 defluorination reaction Methods 0.000 claims abstract description 8
- 239000000428 dust Substances 0.000 claims description 291
- 239000004744 fabric Substances 0.000 claims description 61
- 238000002347 injection Methods 0.000 claims description 48
- 239000007924 injection Substances 0.000 claims description 48
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 27
- 238000004140 cleaning Methods 0.000 claims description 11
- 238000001914 filtration Methods 0.000 claims description 11
- 238000007599 discharging Methods 0.000 claims description 9
- 238000004519 manufacturing process Methods 0.000 claims description 9
- KRHYYFGTRYWZRS-UHFFFAOYSA-N Fluorane Chemical compound F KRHYYFGTRYWZRS-UHFFFAOYSA-N 0.000 claims description 8
- 229910000040 hydrogen fluoride Inorganic materials 0.000 claims description 8
- QNRATNLHPGXHMA-XZHTYLCXSA-N (r)-(6-ethoxyquinolin-4-yl)-[(2s,4s,5r)-5-ethyl-1-azabicyclo[2.2.2]octan-2-yl]methanol;hydrochloride Chemical compound Cl.C([C@H]([C@H](C1)CC)C2)CN1[C@@H]2[C@H](O)C1=CC=NC2=CC=C(OCC)C=C21 QNRATNLHPGXHMA-XZHTYLCXSA-N 0.000 claims description 7
- 239000000203 mixture Substances 0.000 claims description 7
- 238000004891 communication Methods 0.000 claims description 3
- 238000012423 maintenance Methods 0.000 claims description 3
- 238000012795 verification Methods 0.000 claims description 3
- 210000001503 joint Anatomy 0.000 claims description 2
- 230000011218 segmentation Effects 0.000 claims 1
- 230000008569 process Effects 0.000 abstract description 7
- 239000003344 environmental pollutant Substances 0.000 abstract description 2
- 231100000719 pollutant Toxicity 0.000 abstract description 2
- 239000003517 fume Substances 0.000 abstract 1
- 239000002956 ash Substances 0.000 description 26
- 239000000779 smoke Substances 0.000 description 13
- RAHZWNYVWXNFOC-UHFFFAOYSA-N Sulphur dioxide Chemical compound O=S=O RAHZWNYVWXNFOC-UHFFFAOYSA-N 0.000 description 6
- 239000000463 material Substances 0.000 description 5
- 238000007664 blowing Methods 0.000 description 4
- TWNQGVIAIRXVLR-UHFFFAOYSA-N oxo(oxoalumanyloxy)alumane Chemical compound O=[Al]O[Al]=O TWNQGVIAIRXVLR-UHFFFAOYSA-N 0.000 description 4
- 239000002994 raw material Substances 0.000 description 3
- 230000009467 reduction Effects 0.000 description 3
- 239000002253 acid Substances 0.000 description 2
- 230000001174 ascending effect Effects 0.000 description 2
- 239000010426 asphalt Substances 0.000 description 2
- OSGAYBCDTDRGGQ-UHFFFAOYSA-L calcium sulfate Chemical compound [Ca+2].[O-]S([O-])(=O)=O OSGAYBCDTDRGGQ-UHFFFAOYSA-L 0.000 description 2
- 239000003795 chemical substances by application Substances 0.000 description 2
- 150000001875 compounds Chemical class 0.000 description 2
- 238000001514 detection method Methods 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 238000009826 distribution Methods 0.000 description 2
- 238000001035 drying Methods 0.000 description 2
- 238000004134 energy conservation Methods 0.000 description 2
- 239000010419 fine particle Substances 0.000 description 2
- 239000010881 fly ash Substances 0.000 description 2
- 238000003860 storage Methods 0.000 description 2
- 239000000725 suspension Substances 0.000 description 2
- 239000002351 wastewater Substances 0.000 description 2
- 238000004065 wastewater treatment Methods 0.000 description 2
- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 description 1
- WNROFYMDJYEPJX-UHFFFAOYSA-K aluminium hydroxide Chemical compound [OH-].[OH-].[OH-].[Al+3] WNROFYMDJYEPJX-UHFFFAOYSA-K 0.000 description 1
- 239000011575 calcium Substances 0.000 description 1
- 229910052791 calcium Inorganic materials 0.000 description 1
- GBAOBIBJACZTNA-UHFFFAOYSA-L calcium sulfite Chemical compound [Ca+2].[O-]S([O-])=O GBAOBIBJACZTNA-UHFFFAOYSA-L 0.000 description 1
- 235000010261 calcium sulphite Nutrition 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000011161 development Methods 0.000 description 1
- 238000003487 electrochemical reaction Methods 0.000 description 1
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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
- 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
- B01D46/04—Cleaning filters
-
- 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
- B01D46/66—Regeneration of the filtering material or filter elements inside the filter
- B01D46/70—Regeneration of the filtering material or filter elements inside the filter by acting counter-currently on the filtering surface, e.g. by flushing on the non-cake side of the filter
- B01D46/71—Regeneration of the filtering material or filter elements inside the filter by acting counter-currently on the filtering surface, e.g. by flushing on the non-cake side of the filter with pressurised gas, e.g. pulsed air
-
- 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
- B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
- B01D53/81—Solid phase 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
- B01D53/86—Catalytic processes
- B01D53/8659—Removing halogens or halogen compounds
-
- 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
- B01D2257/00—Components to be removed
- B01D2257/20—Halogens or halogen compounds
- B01D2257/204—Inorganic halogen compounds
- B01D2257/2047—Hydrofluoric acid
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Abstract
The invention relates to the field of aluminum electrolysis flue gas purification and emission, in particular to an electrolysis flue gas purification and emission device, a control system and a control method. The method comprises the steps of adopting an alumina dry method for adsorption and purification and adopting a reaction tower to spray calcium hydroxide at multiple points for mixed separation for desulfurization. The dry alumina adsorption process for purifying electrolytic fume includes adsorbing and purifying most of HF, granular matter and SO in 10%2The purified flue gas enters a desulfurizing tower of a multi-point spraying calcium hydroxide mixing and separating method desulfurizing device through an S-shaped turning flue, and a plurality of calcium hydroxide cloths arranged at the bottom of the desulfurizing towerCa (OH) sprayed by the feeder2And H2And reacting after mixing the O, and performing desulfurization and defluorination. The emission indexes of the treated gas are far lower than the national standard limit value, no secondary pollutant is generated, and ultralow emission is realized.
Description
Technical Field
The invention relates to the field of aluminum electrolysis flue gas purification, in particular to an electrolysis flue gas purification and discharge device, a control system and a method.
Background
At present, domestic electrolytic aluminum production enterprises adopt an aluminum electrolysis flue gas dry purification technology to recover HF and particulate matters in the electrolytic flue gas. The technological process is the flue gas (CO, CO) produced in the electrochemical reaction process of aluminum electrolysis2Small amount of HF, CF4、SO2、H2S) is collected to a bag type dust collector through an electrolytic bath gas collecting hood, a smoke discharging branch pipe and a smoke discharging main pipe, aluminum oxide which is used as raw material for electrolytic production is put into a flue through a star-shaped efficient reactor before smoke enters the bag type dust collector, the aluminum oxide is fully mixed with the smoke by utilizing the characteristics that the aluminum oxide is large in porosity and specific surface area, is an amphoteric compound, has good adsorbability on acid gas and asphalt volatile components and can be adsorbed by electrolytic smoke, hydrogen fluoride in the smoke is adsorbed by the aluminum oxide and is blocked on the outer surface of a cloth bag of the bag type dust collector, and the purified smoke is discharged to the atmosphere through a chimney. Along with the prolonging of the service life of the dust removing equipment, the adsorption capacity of the dust removing cloth bag is reduced, the purification efficiency of the electrolytic flue gas is reduced, and even the excessive emission occasionally occurs, the electrolysis production industry faces severe environmental protection pressure, and a new electrolytic flue gas purification system is urgently needed to purify the electrolytic flue gas, ensure that all indexes of the electrolytic flue gas reach the standard emission or the ultra-low emission, and achieve the purposes of energy conservation and emission reduction.
Disclosure of Invention
Aiming at the defects of the prior art and aiming at solving the problem of purification and emission of flue gas pollutants in the electrolytic aluminum industry, the invention provides a two-section type electrolytic flue gas purification and emission device, a control system and a method. By implementing the method, the electrolytic flue gas purification capacity is further improved, the electrolytic flue gas is discharged at an ultralow level, the purposes of energy conservation and emission reduction are achieved, and the sustainable development of human society is realized.
The technical scheme adopted by the invention for solving the technical problems is as follows:
on the one hand, a two-stage type electrolysis gas cleaning and discharging device comprises:
the alumina dry method adsorption purification device utilizes the adsorption reaction between alumina and hydrogen fluoride gas in the electrolytic flue gas;
a desulfurization device adopting a reaction tower multi-point spraying calcium hydroxide mixed separation method, which utilizes calcium hydroxide, water and SO in the electrolysis flue gas2Carrying out reaction;
and the turning flue is positioned between the alumina dry-method adsorption and purification device and the reaction tower multi-point injection calcium hydroxide mixing and separating method desulfurization device, and is in butt joint communication with the alumina dry-method adsorption, purification and discharge device and the reaction tower multi-point injection calcium hydroxide mixing and separating method desulfurization device respectively, so that the temperature of the electrolytic flue gas is reduced.
Wherein: the alumina dry-process adsorption purification device comprises:
at least one adsorption purification dust remover;
the inlet flue is formed by connecting an inlet horizontal flue of the adsorption purification dust remover and an inlet vertical flue of the adsorption purification dust remover, is positioned at the inlet of the adsorption purification dust remover and is used for introducing electrolysis flue gas;
the inlet valve of the adsorption and purification dust remover is arranged between the outlet of the vertical flue at the inlet of the adsorption and purification dust remover and the adsorption and purification dust remover;
the outlet flue of the adsorption purification dust remover is positioned at the outlet of the adsorption purification dust remover and is used for outputting the flue gas subjected to adsorption purification treatment from the adsorption purification dust remover;
the outlet valve of the adsorption purification dust remover is arranged between the outlet of the adsorption purification dust remover and the outlet flue of the adsorption purification dust remover;
an alumina high efficiency reactor for providing alumina to the inlet flue;
the fresh alumina bin is used for providing fresh alumina for adsorption and purification for the alumina high-efficiency reactor;
preferably, the inlet valve and the outlet valve of the adsorption and purification dust remover adopt online adjustable electric flap valves.
Preferably, the box body of the adsorption purification dust remover is divided into an upper box body, a middle box body and a lower box body; the lower box body of the adsorption purification dust remover is provided with a guide plate and an ash bucket; the middle box body of the adsorption purification dust collector is provided with a plurality of frameworks and dust collection cloth bags; the upper box body of the adsorption purification dust remover is provided with a pattern plate, an injection pipe, an air bag and a pulse valve;
preferably, the dust removal cloth bag is a rhombic folded cloth bag, and the filtering area is increased by increasing the surface area of the dust removal cloth bag, so that the dust removal capacity of the dust removal cloth bag is improved.
Preferably, the device comprises an alumina high-efficiency reactor, wherein the alumina high-efficiency reactor is arranged at the joint of the horizontal flue at the inlet of the adsorption purification dust remover and the vertical flue at the inlet of the adsorption purification dust remover; the high-efficiency alumina reactor adopts three-point distributed blanking, achieves 360-degree full coverage and improves the adsorption and purification efficiency.
Preferably, the blanking of the alumina high-efficiency reactor is multipoint distributed blanking or multipoint multilayer distributed blanking, so that the adsorption purification efficiency is further improved.
Wherein: the reaction tower multi-point spraying calcium hydroxide mixing separation method desulphurization unit comprises:
the desulfurizing tower is used for reacting the flue gas with the calcium hydroxide;
at least one desulfurization dust separator;
the inlet flue of the desulfurization dust remover is connected with the desulfurization tower and the desulfurization dust remover;
the inlet valve of the desulfurization dust remover is arranged between the inlet flue of the desulfurization dust remover and the desulfurization dust remover;
the dust remover outlet flue is positioned at the outlet of the desulfurization dust remover and used for discharging the air desulfurized by the desulfurization dust remover;
the outlet valve of the desulfurization dust remover is arranged between the desulfurization dust remover and the outlet flue of the desulfurization dust remover;
the calcium hydroxide distributing device is used for spraying calcium hydroxide into the desulfurizing tower;
the water spray gun is used for spraying water into the desulfurizing tower;
and the desulfurizer bin is used for providing the calcium hydroxide desulfurizer for desulfurization to the calcium hydroxide distributor.
Preferably, the inlet valve and the outlet valve of the desulfurization dust remover adopt online adjustable electric flap valves.
Preferably, the desulfurization dust collector comprises: the lower box body, the middle box body and the upper box body of the desulfurization dust remover are matched and provided with an inlet valve and an outlet valve of the desulfurization dust remover. The lower box body of the desulfurization dust remover is provided with a guide plate and an ash bucket, the middle box body of the desulfurization dust remover is provided with a plurality of frameworks and a dust removal cloth bag, and the upper box body of the desulfurization dust remover is internally provided with a pattern plate, an injection pipe, an air bag and a pulse valve.
Preferably, the dust removal cloth bag is a rhombic folded cloth bag, and the filtering area is increased by increasing the surface area of the dust removal cloth bag, so that the dust removal capacity of the dust removal cloth bag is improved.
Preferably, the device comprises a calcium hydroxide distributor and a water spray gun, wherein the calcium hydroxide distributor and the water spray gun are arranged at the bottom of the desulfurization tower; the desulfurizer bin is provided with a storage bin, a super-concentrated phase conveying chute and a digester.
Preferably, the bottom of the desulfurization tower is provided with a plurality of calcium hydroxide distributors and water spray guns, the calcium hydroxide distributors are positioned below the water spray guns, and calcium hydroxide and water are sprayed at multiple points.
Preferably, the turning flue is of an S-shaped structure, the S-shaped turning flue can realize seamless connection between the alumina dry-method adsorption, purification and discharge device and two sections of devices of the reaction tower multi-point injection calcium hydroxide mixing and separation method desulfurization device, SO that the flue gas flow loss is reduced, the flue gas temperature is reduced, and SO is reduced along with the reduction of the flue gas temperature2Is easier to be dissolved by water, and the efficiency of the desulfurization device adopting the reaction tower and the multi-point spraying calcium hydroxide mixing and separating method is maximized.
In a second aspect, a two-stage electrolytic flue gas purification and discharge method. The working process of the method comprises the following steps:
collecting flue gas generated in the aluminum electrolysis production process to an inlet horizontal flue of an adsorption purification dust remover of an alumina dry-method adsorption purification device;
the flue enters the adsorption purification dust remover through an inlet of the adsorption purification dust remover and is vertical to the flue; wherein: putting alumina into an alumina high-efficiency reactor at the joint of a horizontal flue at the inlet of the adsorption and purification dust remover and a vertical flue at the inlet of the adsorption and purification dust remover, and performing adsorption reaction with hydrogen fluoride gas in the flue gas to achieve the aim of defluorination;
the mixture of the flue gas and the alumina after the reaction is blocked and filtered by a dust removal cloth bag of an adsorption purification dust remover, and the alumina mixture blocked on the dust removal cloth bag is blown and falls into an ash bucket of a lower box body of the dust remover;
the temperature of the flue gas filtered by the dust removal cloth bag is reduced through a diversion flue;
the flue gas with reduced temperature enters a desulfurizing tower, and a calcium hydroxide distributor and a water spray gun which are arranged at the bottom of the desulfurizing tower respectively spray calcium hydroxide and water and SO in the flue gas2The residual hydrogen fluoride reacts to perform desulfurization and defluorination;
the reacted mixture and the flue gas are uniformly introduced into a desulfurization dust remover for filtering, and the cleaned air is discharged into the atmosphere through an outlet flue of the desulfurization dust remover and a chimney.
In a third aspect, an electrolysis flue gas purification and dust removal control system comprises: three injection control modes, namely a differential pressure injection control mode, a timing injection control mode and a manual injection control mode, are adopted. Wherein:
the differential pressure injection control mode is that a plurality of dust collectors (or called unit chambers) form a group, a differential pressure injection control program carries out injection cleaning on a dust collector dust collection cloth bag with the dust collector differential pressure reaching a set upper limit value according to a set dust collector differential pressure upper limit value, the pressure difference value between an upper box body and a lower box body of the dust collector is called differential pressure, the differential pressure of each dust collector of the group is compared, the dust collector dust collection cloth bag with the dust collector differential pressure reaching the set upper limit value is cleaned until the dust collector differential pressure reaches a set lower limit value, then the dust collector differential pressure comparison is carried out again, the dust collector dust collection cloth bag with the dust collector differential pressure reaching the set upper limit value is still preferably subjected to injection cleaning, and the above steps are repeated in a circulating mode.
The negative pressure of the flue gas main pipe can be kept continuously and stably in a differential pressure control mode.
The timing blowing control mode is that a plurality of dust collectors (or called unit chambers) form a group, and the timing blowing control program performs blowing cleaning on dust collecting cloth bags of each dust collector of the group in sequence according to the preset time of the program until the differential pressure of the dust collectors reaches the set lower limit.
The manual blowing control mode is mainly used for equipment offline maintenance and pulse valve fault verification.
The control system adopts three different control modes and is used for meeting the working requirements at different periods. The differential pressure injection control mode and the timing injection control mode are used for automatic dust removal control of a dust removal cloth bag; the manual injection control mode is used for offline maintenance of equipment, fault verification of a pulse valve and manual ash removal of a dust removal cloth bag, and local strain of the dust removal cloth bag is avoided through switching of three control modes.
Drawings
Fig. 1 is a schematic structural diagram of a two-stage electrolytic flue gas purification and discharge device of the present invention.
Description of the drawings: 1-fresh alumina bin, 2-fluorine-carrying alumina bin, 3-adsorption purification dust remover outlet valve, 4-adsorption purification dust remover outlet flue, 5-turning flue, 6-desulfurization dust remover outlet valve, 7-desulfurization dust remover outlet flue, 8-desulfurization dust remover, 9-desulfurization dust remover inlet valve, 10-water spray gun, 11-desulfurizing tower, 12-calcium hydroxide distributor, 13-proportion blending bin, 14-adsorption purification dust remover, 15-alumina high-efficiency reactor, 16-adsorption purification dust remover inlet horizontal flue, 17-adsorption purification dust remover inlet vertical flue, 18-adsorption purification dust remover inlet valve, 19-adsorption purification dust remover guide plate, 141-adsorption purification dust remover lower box body, 142-adsorption purification dust remover middle box body, 143-an upper box body of an adsorption purification dust remover, 801-a lower box body of a desulfurization dust remover, 802-a middle box body of the desulfurization dust remover and 803-an upper box body of the desulfurization dust remover.
Detailed Description
The invention provides a two-section type electrolytic flue gas purification and discharge device and a method. By implementing the invention, the purification capacity of the electrolytic flue gas is further improved, and the electrolytic flue gas reaches the standard and is even discharged at an ultra-low level, so that the human society can be continuously developed. Especially, the added reaction tower multi-point spraying calcium hydroxide mixing separation method desulfurization device and method have the advantages of low investment cost, simple system structure, easy operation and management, no wastewater generation, no secondary pollution and no subsequent wastewater treatment system.
The two-stage electrolytic flue gas purification and discharge device and method according to the present invention will be described in further detail with reference to the accompanying drawings and examples, and it is apparent that the described examples are only a part of the examples, not all of the examples.
In the description of the present invention, it is to be understood that the terms "longitudinal", "lateral", "vertical", "up", "down", "front", "back", "left", "right", "vertical", "horizontal", "top", "bottom", "inner", "outer", etc., indicate orientations or positional relationships based on those shown in the drawings, and are used only for convenience in describing the present invention and for simplicity in description, and do not indicate or imply that the device or element being referred to must have a particular orientation, be constructed and operated in a particular orientation, and thus, should not be construed as limiting the present invention.
In the description of the present invention, unless otherwise specified and limited, it is to be noted that the terms "mounted," "connected," and "connected" are to be interpreted broadly, and may be, for example, a mechanical connection or an electrical connection, a communication between two elements, a direct connection, or an indirect connection via an intermediate medium, and specific meanings of the terms may be understood by those skilled in the art according to specific situations.
FIG. 1 is a schematic diagram of a two-stage type electrolytic flue gas purification and discharge device of the present invention.
As shown in fig. 1, a two-stage electrolytic flue gas purification and discharge device may include an alumina dry adsorption purification device, a turning flue and a reaction tower multi-point injection calcium hydroxide mixing separation desulfurization device. Wherein: the alumina dry method adsorption purification device carries out defluorination by utilizing the adsorption reaction of alumina and hydrogen fluoride gas in the electrolytic flue gas;
the flue gas after defluorination enters a reaction tower multi-point spraying calcium hydroxide mixing separation method desulphurization device after being cooled by a turning flue, and the SO in the flue gas is electrolyzed by using calcium hydroxide, water2Reaction takes place for desulfurization.
In this embodiment, the flue that turns to adopts S-shaped structure, and S-shaped turns to the flue and can realize the seamless connection of alumina dry process adsorption purification device and the two sections devices of reaction tower multiple spot injection calcium hydroxide mixed separation method desulphurization unit reduces flue gas flow loss, reduces flue gas temperature, makes the efficiency of desulfurization system dust remover reach the maximize.
In this embodiment, the alumina dry adsorption purification device may include an inlet flue, an alumina high-efficiency reactor 15, an adsorption purification dust collector 14, and an adsorption purification dust collector outlet flue 4.
The inlet flue is formed by connecting an adsorption purification dust remover inlet horizontal flue 16 and an adsorption purification dust remover inlet vertical flue 17, is positioned at the inlet of the adsorption purification dust remover 14 and is used for introducing electrolysis flue gas.
An inlet valve 18 of the adsorption purification dust remover can be arranged between the outlet of the vertical flue 17 of the inlet of the adsorption purification dust remover and the adsorption purification dust remover 14.
The alumina high-efficiency reactor 15 is arranged at the joint of the horizontal flue 16 at the inlet of the adsorption and purification dust remover and the vertical flue 17 at the inlet of the adsorption and purification dust remover; fresh alumina for adsorption and purification is provided to the alumina high-efficiency reactor 15 from the fresh alumina bin 1; the alumina high-efficiency reactor 15 can be fed in a three-point distributed manner, so that 360-degree full coverage is achieved, and the adsorption and purification efficiency is improved; the charging and controlling valve is arranged at the discharging opening of the super-dense phase conveying chute (distribution chute for short) of the alumina high-efficiency reactor 15.
The inlet flue is connected to at least one (e.g. 12) adsorption cleaning dust separator 14. The box body of the adsorption purification dust remover 14 is divided into an upper box body 143, a middle box body 142 and a lower box body 141; the lower box body 141 of the adsorption purification dust remover is provided with a guide plate and an ash bucket; the middle box body 1402 of the adsorption purification dust collector is provided with 600 skeletons, for example 600 dust removing cloth bags, the dust removing cloth bags can adopt rhombic folded cloth bags, and the filtering area is increased by increasing the surface area of the dust removing cloth bags, so that the dust removing capacity of the dust removing cloth bags is improved; the upper tank 1403 of the adsorption purification dust collector is provided with a card, an injection pipe, an air bag, and a pulse valve.
The outlet of the adsorption purification dust remover 14 is connected with the outlet flue 4 of the adsorption purification dust remover and is used for outputting the electrolysis flue gas from the adsorption purification dust remover 14.
An outlet valve 3 of the adsorption purification dust remover is arranged between the adsorption purification dust remover 14 and the outlet of the outlet flue 4 of the adsorption purification dust remover.
The outlet flue 4 of the adsorption purification dust remover is connected with an S-shaped turning flue 5.
The inlet valve 18 of the adsorption purification dust remover and the outlet valve 3 of the adsorption purification dust remover adopt online adjustable electric flap valves.
The fluorine-carrying alumina generated by the adsorption reaction passes through a super-concentrated phase conveying chute and returns to alumina lifting equipment to enter a fluorine-carrying alumina bin 2, and the fluorine-carrying alumina is used as a raw material for production.
A material loading and controlling valve is arranged at a material outlet of a super-concentrated phase conveying chute (a material distribution chute for short) of the high-efficiency alumina reactor; the vertical flue at the inlet of the adsorption purification dust remover is provided with an independent feeding port of the alumina high-efficiency reactor and an independent outlet flue.
In this embodiment, the reaction tower multi-point spraying calcium hydroxide mixing and separating method desulfurization device may include a desulfurization tower 11, an aluminum hydroxide distributor 12, a water spray gun 10, a desulfurization dust collector inlet flue, a desulfurization dust collector 8, and a desulfurization dust collector outlet flue 7.
The bottom of the desulfurizing tower 11 is connected with an S-shaped turning flue 5, the bottom of the desulfurizing tower 11 is also provided with 12 calcium hydroxide distributing devices 12, such as 12 water spraying guns 10, the calcium hydroxide distributing devices 12 are positioned below the water spraying guns 10 and spray calcium hydroxide and water at multiple points, and a calcium hydroxide desulfurizing agent for desulfurization is provided to the calcium hydroxide distributing devices 12 from a desulfurizing agent bin.
The upper part of the desulfurizing tower 11 is connected with an inlet flue of a desulfurizing dust remover, and the inlet flue of the desulfurizing dust remover is provided with an inlet valve 9 of the desulfurizing dust remover and is connected with 12 desulfurizing dust removers 8 for example.
The desulfurization dust remover includes: the lower box 801 of the desulfurization dust remover, the middle box 802 of the desulfurization dust remover and the upper box 803 of the desulfurization dust remover are provided with an inlet valve 9 of the desulfurization dust remover and an outlet valve 6 of the desulfurization dust remover in a matching way. The lower box body 801 of the desulfurization dust remover is provided with a guide plate and an ash bucket, the middle box body 802 of the desulfurization dust remover is provided with 600 frameworks, for example 600 dust removing cloth bags, the dust removing cloth bags can adopt rhombic folded cloth bags, and the filtering area is increased by increasing the surface area of the dust removing cloth bags, so that the dust removing capacity of the dust removing cloth bags is improved; the upper box 803 of the desulfurization dust remover is internally provided with a pattern plate, an injection pipe, an air bag and a pulse valve.
The inlet valve 9 of the desulfurization dust remover and the outlet valve 6 of the desulfurization dust remover adopt online adjustable electric flap valves.
A desulfurization ash bin is arranged below the desulfurization dust remover 8, and desulfurization ash generated after desulfurization is detected to meet the emission requirement and then is introduced into the desulfurization ash bin through a desulfurization ash conveying chute; the desulfurized ash which is generated after desulfurization and does not meet the discharge requirement after detection enters a proportion blending bin 13, and is blended with fresh calcium hydroxide and then is put into a desulfurizer bin to be used as the fresh calcium hydroxide.
The outlet of the desulfurization dust remover 8 is connected with the outlet flue 7 of the desulfurization dust remover through the outlet valve 6 of the desulfurization dust remover, and the clean air after desulfurization is discharged through the outlet flue 7 of the desulfurization dust remover.
The desulfurized fly ash conveying chute is provided with an air heater and a fan dust filtering device; the desulfurization ash bin is provided with an ash discharge winch wheel for discharging ash; the proportional mixing bin 13 is provided with an ash discharge air stripping and super-concentrated phase conveying chute; the desulfurizer bin is provided with a storage bin, a super-concentrated phase conveying chute and a digester.
In this embodiment, the dust-collecting cloth bag of the adsorption purification dust collector 14 and the dust-collecting cloth bag of the desulfurization dust collector 8 both use rhombic pleated cloth bags, and compared with the cylindrical dust-collecting cloth bags used in the past, the filtering area of the dust-collecting cloth bags is increased by 278.5%, so that the dust-collecting capacity of the dust collector is greatly improved.
The embodiment discloses a two-stage electrolytic flue gas purification and discharge method. The working process is as follows:
HF, SO produced in the process of aluminum electrolysis production2When smoke and dust are absorbed into a gas collecting hood of an electrolytic cell, a smoke exhaust branch pipe and a smoke exhaust main pipe through negative pressure wind speed and wind quantity generated when a high-power main smoke exhaust fan of the aluminum electrolysis production equipment works, the smoke and dust are collected into a horizontal flue 16 of an adsorption purification dust remover in an alumina dry method adsorption purification device through the horizontal flue 17 of the adsorption purification dust remover, the smoke and dust enters an adsorption purification dust remover 14 through a vertical flue 17 of the adsorption purification dust remover, an alumina high-efficiency reactor 15 arranged at the joint of the horizontal flue 16 of an inlet of the adsorption purification dust remover and the vertical flue 17 of the inlet of the adsorption purification dust remover sprays enough (the amount of fresh alumina put into each hour of 12 reactors is 20-22 t/h, namely the amount of fresh alumina put into each hour of each alumina high-efficiency reactor 15 is 1.7-1.8 t/h), and the raw material alumina is produced by utilizing the porosity and the large specific surface area of the alumina and is an amphoteric compound, Has good adsorption property on acid gas and asphalt volatile components, HF and a small amount of SO in the flue gas2The adsorption reaction is carried out to achieve the aim of defluorination, and HF and SO are generated in the reaction process2Is adsorbed by the alumina to generate fluorine-carrying alumina, the fluorine-carrying alumina and the flue gas enter the lower box body 141 of the adsorption and purification dust remover through the inlet valve 18 of the adsorption and purification dust remover, and is uniformly introduced into each filtering dust-collecting cloth bag of the middle box body 142 of the adsorption and purification dust collector by the guide plate 19, 600 filtering dust-collecting cloth bags are arranged in each middle box body 142 of the adsorption and purification dust collector, large granular substances (fluorine-carrying alumina) are blocked on the outer surface of the dust removing cloth bag through the filtration of the dust removing cloth bag, when the material adhered on the outer surface of the dust removing cloth bag reaches a certain amount, which causes the differential pressure of the dust remover to reach the upper limit set value 1000Pa (the pressure difference between the upper box body and the lower box body is called differential pressure, and the differential pressure is detected by a differential pressure transmitter in real time and data is uploaded), the differential pressure injection control program of the adsorption purification dust remover is started, the differential pressure injection control mode is that every three adsorption purification dust removers 14 are in a group, and the upper limit value of the differential pressure injection control program is set to be 100 according to the adsorption purification dust removers 14.And (3) comparing the pressure difference of the three adsorption and purification dust collectors 14, preferentially performing spray cleaning on one adsorption and purification dust collector 14 with the pressure difference reaching an upper limit set value of 1000Pa until the pressure difference of the adsorption and purification dust collector 14 drops to a lower limit set value of 600Pa, then performing the pressure difference comparison of the adsorption and purification dust collectors 14 again, still preferentially performing spray cleaning on one adsorption and purification dust collector 14 with the pressure difference reaching the upper limit set value of 1000Pa, and repeating the steps. The material adhered on the dust removal cloth bag is blown to fall into an ash bucket of an adsorption purification dust remover 14, and is conveyed to a fluorine-carrying alumina bin 2 by a super-concentrated phase conveying chute and a pneumatic elevator for production and use of an electrolytic tank, so that the aim of recycling is fulfilled.
The flue gas and the residual fine particle dust filtered by the dust removal cloth bag enter a reaction tower multi-point spraying calcium hydroxide mixing separation method desulfurization device for desulfurization and dust removal through an outlet flue 4 and a turning flue 5 of the adsorption purification dust remover.
The defluorinated flue gas and the residual fine particle dust enter an outlet flue 4 of an adsorption purification dust remover through a dust removing cloth bag, an S-shaped turning flue 5 enters the bottom of a desulfurizing tower 11 and is suspended to move upwards, the desulfurizing tower 11 is a reaction tower for reacting the flue gas with calcium hydroxide, 12 calcium hydroxide distributors 12 and 12 water spray guns 10 are arranged at the upper position of the bottom of the desulfurizing tower 11, sufficient calcium hydroxide and water are continuously sprayed into the desulfurizing tower 11, the calcium hydroxide and the water are both in a suspension ascending state and react with sulfur dioxide in the flue gas in the suspension ascending process to remove the sulfur dioxide in the flue gas and generate calcium sulfite and calcium sulfate (also called as desulfurized ash), the mixture of the desulfurized ash and the flue gas generated after the reaction is uniformly introduced into lower box bodies 801 of 12 desulfurization dust removers 8 and then enters a middle box body 802 of the desulfurization dust remover 8, and the desulfurized ash is adhered to the outer surfaces of 600 dust removing cloth bags of the desulfurization dust remover 8, the timed injection control program is used for controlling the injection to fall into the ash bucket of the dust remover in a timed injection mode, the timed injection control program of the embodiment is set to inject once every 12 hours, and the time control program stops when the differential pressure of the desulfurization dust remover in the group after injection is reduced to the lower limit value 600Pa set by the control program. The desulfurization ash falling into the ash bucket of the dust remover after being injected is lifted to a proportion blending bin 13 through a super dense phase conveying chute, a separator and a pneumatic hoist, and then is put into a desulfurization dust remover 8 through the super dense phase conveying chute and a multi-point calcium hydroxide distributor 12 to participate in secondary and multiple desulfurization reactions until the content of calcium in the calcium hydroxide in the desulfurization ash is lower than 10 percent, and then is discharged into a desulfurization ash bin through the pneumatic hoist, and is discharged into an ash discharging winch to be pulled into a fixed-point ash field for burying treatment. In the embodiment, the sampling detection period of the desulfurized fly ash is once every 48 hours. The cleaned flue gas enters an upper box 803 of the desulfurization dust remover 8 and is discharged into the atmosphere through an outlet flue 7 of the desulfurization dust remover and a chimney.
The invention relates to a two-section type electrolytic flue gas purification and discharge device and a method thereof, which adopt an alumina dry method adsorption purification device and a method thereof and a reaction tower multi-point injection calcium hydroxide mixing separation method desulfurization device and a method thereof. The reaction tower multi-point spraying calcium hydroxide mixing separation method desulfurization device has the advantages of low investment cost, simple system structure, easy operation and management, no wastewater generation, no secondary pollution and no subsequent wastewater treatment system.
The above-mentioned embodiments are intended to illustrate the objects, technical solutions and advantages of the present invention in further detail, and it should be understood that the above-mentioned embodiments are merely exemplary embodiments of the present invention, and are not intended to limit the scope of the present invention, and any modifications, equivalent substitutions, improvements and the like made within the spirit and principle of the present invention should be included in the scope of the present invention.
Claims (15)
1. The utility model provides a two segmentation electrolysis gas cleaning discharging equipment which characterized in that includes:
the alumina dry method adsorption purification device utilizes the adsorption reaction between alumina and hydrogen fluoride gas in the electrolytic flue gas;
a desulfurization device adopting a reaction tower multi-point spraying calcium hydroxide mixed separation method, which utilizes calcium hydroxide, water and SO in the electrolysis flue gas2Carrying out reaction;
and the turning flue is positioned between the alumina dry-method adsorption and purification device and the reaction tower multi-point injection calcium hydroxide mixing and separating method desulfurization device, and is in butt joint communication with the alumina dry-method adsorption, purification and discharge device and the reaction tower multi-point injection calcium hydroxide mixing and separating method desulfurization device respectively, so that the temperature of the electrolytic flue gas is reduced.
2. The two-stage electrolytic flue gas purification and discharge device according to claim 1, wherein the alumina dry adsorption purification device comprises:
at least one adsorption purification dust remover;
the inlet flue is formed by connecting an inlet horizontal flue of the adsorption purification dust remover and an inlet vertical flue of the adsorption purification dust remover, is positioned at the inlet of the adsorption purification dust remover and is used for introducing electrolysis flue gas;
the inlet valve of the adsorption and purification dust remover is arranged between the outlet of the vertical flue at the inlet of the adsorption and purification dust remover and the adsorption and purification dust remover;
the outlet flue of the adsorption purification dust remover is positioned at the outlet of the adsorption purification dust remover and is used for outputting the flue gas subjected to adsorption purification treatment from the adsorption purification dust remover;
the outlet valve of the adsorption purification dust remover is arranged between the outlet of the adsorption purification dust remover and the outlet flue of the adsorption purification dust remover;
an alumina high efficiency reactor for providing alumina to the inlet flue;
and the fresh alumina bin is used for providing fresh alumina for adsorption and purification for the alumina high-efficiency reactor.
3. The two-stage electrolytic flue gas purification and discharge device according to claim 2, wherein: the inlet valve of the adsorption purification dust remover and the outlet valve of the adsorption purification dust remover adopt online adjustable electric flap valves.
4. The two-stage electrolytic flue gas purification and discharge device according to claim 2, wherein: the box body of the adsorption purification dust remover is divided into an upper box body, a middle box body and a lower box body; the lower box body of the adsorption purification dust remover is provided with a guide plate and an ash bucket; the middle box body of the adsorption purification dust collector is provided with a plurality of frameworks and dust collection cloth bags; the upper box body of the adsorption purification dust remover is provided with a pattern plate, an injection pipe, an air bag and a pulse valve.
5. The two-stage electrolytic flue gas purification and discharge device according to claim 4, wherein: the dust removal cloth bag is a rhombic folded cloth bag.
6. The two-stage electrolytic flue gas purification and discharge device according to claim 2, wherein: the device comprises an alumina high-efficiency reactor, wherein the alumina high-efficiency reactor is arranged at the joint of a horizontal flue at the inlet of the adsorption and purification dust remover and a vertical flue at the inlet of the adsorption and purification dust remover; the high-efficiency alumina reactor adopts three-point distributed blanking, and achieves 360-degree full coverage.
7. The two-stage electrolytic flue gas purification and discharge device according to claim 6, wherein: the blanking of the alumina high-efficiency reactor is multipoint distributed blanking or multipoint multilayer distributed blanking.
8. The two-stage electrolytic flue gas purification and discharge device according to claim 1, wherein: the reaction tower multi-point spraying calcium hydroxide mixing separation method desulphurization unit comprises:
the desulfurizing tower is used for reacting the flue gas with the calcium hydroxide;
at least one desulfurization dust separator;
the inlet flue of the desulfurization dust remover is connected with the desulfurization tower and the desulfurization dust remover;
the inlet valve of the desulfurization dust remover is arranged between the inlet flue of the desulfurization dust remover and the desulfurization dust remover;
the dust remover outlet flue is positioned at the outlet of the desulfurization dust remover and used for discharging the air desulfurized by the desulfurization dust remover;
the outlet valve of the desulfurization dust remover is arranged between the desulfurization dust remover and the outlet flue of the desulfurization dust remover;
the calcium hydroxide distributing device is used for spraying calcium hydroxide into the desulfurizing tower;
the water spray gun is used for spraying water into the desulfurizing tower;
and the desulfurizer bin is used for providing the calcium hydroxide desulfurizer for desulfurization to the calcium hydroxide distributor.
9. The two-stage electrolytic flue gas purification and discharge device according to claim 8, wherein: and the inlet valve of the desulfurization dust remover and the outlet valve of the desulfurization dust remover both adopt online adjustable electric flap valves.
10. The two-stage electrolytic flue gas purification and discharge device according to claim 8, wherein: the desulfurization dust remover comprises a lower desulfurization dust remover box body, a middle desulfurization dust remover box body and an upper desulfurization dust remover box body; the lower box body of the desulfurization dust remover is provided with a guide plate and an ash bucket; the middle box body of the desulfurization dust remover is provided with a plurality of frameworks and dust removing cloth bags; and a pattern plate, an injection pipe, an air bag and a pulse valve are arranged in the upper box body of the desulfurization dust remover.
11. The two-stage electrolytic flue gas purification and discharge device according to claim 10, wherein: the dust removal cloth bag is a rhombic folded cloth bag.
12. The two-stage electrolytic flue gas purification and discharge device according to claim 12, wherein: the bottom of the desulfurization tower is provided with a plurality of calcium hydroxide distributors and water spray guns, and the calcium hydroxide distributors are arranged below the water spray guns.
13. The two-stage electrolytic flue gas purification and discharge device according to claim 1, wherein: the turning flue is of an S-shaped structure and is used for realizing seamless connection between the alumina dry-method adsorption, purification and discharge device and the two-stage device of the reaction tower multi-point injection calcium hydroxide mixing and separation method desulfurization device.
14. A two-stage electrolysis flue gas purification and emission method is characterized by comprising the following steps:
collecting flue gas generated in the aluminum electrolysis production process to an inlet horizontal flue of an adsorption purification dust remover of an alumina dry-method adsorption purification device;
the flue enters the adsorption purification dust remover through an inlet of the adsorption purification dust remover and is vertical to the flue; wherein: putting alumina into an alumina high-efficiency reactor at the joint of a horizontal flue at the inlet of the adsorption and purification dust remover and a vertical flue at the inlet of the adsorption and purification dust remover, and performing adsorption reaction with hydrogen fluoride gas in the flue gas to achieve the aim of defluorination;
the mixture of the flue gas and the alumina after the reaction is blocked and filtered by a dust removal cloth bag of an adsorption purification dust remover, and the alumina mixture blocked on the dust removal cloth bag is blown and falls into an ash bucket of a lower box body of the dust remover;
the temperature of the flue gas filtered by the dust removal cloth bag is reduced through a diversion flue;
the flue gas with reduced temperature enters a desulfurizing tower, and a calcium hydroxide distributor and a water spray gun which are arranged at the bottom of the desulfurizing tower respectively spray calcium hydroxide and water and SO in the flue gas2The residual hydrogen fluoride reacts to perform desulfurization and defluorination;
the reacted mixture and the flue gas are uniformly introduced into a desulfurization dust remover for filtering, and the cleaned air is discharged into the atmosphere through an outlet flue of the desulfurization dust remover and a chimney.
15. An electrolysis flue gas purification and dust removal control system is characterized in that the electrolysis flue gas purification and dust removal control system adopts three injection control modes, namely a differential pressure injection control mode, a timing injection control mode and a manual injection control mode; wherein:
the differential pressure injection control mode is that a plurality of dust collectors (or called unit chambers) form a group, a differential pressure injection control program carries out injection cleaning on a dust collector with the differential pressure reaching a set upper limit value according to a set upper limit value of a dust collection cloth bag differential pressure, the differential pressure difference between an upper box body and a lower box body of the dust collector is called differential pressure, the differential pressure of each dust collection cloth bag of the group is compared, the dust collector with the differential pressure reaching the set upper limit value is cleaned until the differential pressure of the dust collector reaches a set lower limit value, then the differential pressure comparison of the dust collector is carried out again, the dust collector with the differential pressure reaching the set upper limit value is still preferably subjected to injection cleaning, and the above-mentioned steps are repeated; the negative pressure of the flue gas main pipe can be kept continuously and stably in a differential pressure control mode;
the timing injection control mode is that a plurality of dust collectors (or called unit chambers) form a group, and a timing injection control program performs injection cleaning on dust collecting cloth bags of each dust collector of the group in sequence according to the preset time of a program until the differential pressure of the dust collecting cloth bags reaches a lower limit value set by the control program;
the control system comprises three control modes, wherein the three control modes are used for meeting different periods, a differential pressure injection control mode and a timing injection control mode are used for automatic dust removal control of the dust removal cloth bag, and the manual injection control mode is mainly used for offline maintenance of equipment, fault verification of a pulse valve and manual dust removal of the dust removal cloth bag.
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