CN111701394A - Flue gas alternating-current type activated carbon desulfurization and denitrification integrated process system and application - Google Patents
Flue gas alternating-current type activated carbon desulfurization and denitrification integrated process system and application Download PDFInfo
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- CN111701394A CN111701394A CN202010703808.1A CN202010703808A CN111701394A CN 111701394 A CN111701394 A CN 111701394A CN 202010703808 A CN202010703808 A CN 202010703808A CN 111701394 A CN111701394 A CN 111701394A
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- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 title claims abstract description 342
- 238000006477 desulfuration reaction Methods 0.000 title claims abstract description 113
- 230000023556 desulfurization Effects 0.000 title claims abstract description 110
- 239000003546 flue gas Substances 0.000 title claims abstract description 93
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 title claims abstract description 91
- 238000000034 method Methods 0.000 title claims abstract description 88
- 230000008569 process Effects 0.000 title claims abstract description 73
- 238000001179 sorption measurement Methods 0.000 claims abstract description 173
- 238000003795 desorption Methods 0.000 claims abstract description 16
- 239000000779 smoke Substances 0.000 claims abstract description 6
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims description 122
- 229910052757 nitrogen Inorganic materials 0.000 claims description 59
- 239000002245 particle Substances 0.000 claims description 55
- 239000007789 gas Substances 0.000 claims description 54
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 claims description 47
- 239000000463 material Substances 0.000 claims description 43
- 238000003860 storage Methods 0.000 claims description 37
- 238000010438 heat treatment Methods 0.000 claims description 34
- 229910052799 carbon Inorganic materials 0.000 claims description 32
- HRZFUMHJMZEROT-UHFFFAOYSA-L sodium disulfite Chemical compound [Na+].[Na+].[O-]S(=O)S([O-])(=O)=O HRZFUMHJMZEROT-UHFFFAOYSA-L 0.000 claims description 31
- 229940001584 sodium metabisulfite Drugs 0.000 claims description 31
- 238000004458 analytical method Methods 0.000 claims description 30
- 235000010262 sodium metabisulphite Nutrition 0.000 claims description 30
- 239000002699 waste material Substances 0.000 claims description 28
- 238000004519 manufacturing process Methods 0.000 claims description 23
- 229910021529 ammonia Inorganic materials 0.000 claims description 21
- 238000001816 cooling Methods 0.000 claims description 19
- 238000005245 sintering Methods 0.000 claims description 17
- 239000003344 environmental pollutant Substances 0.000 claims description 13
- 231100000719 pollutant Toxicity 0.000 claims description 13
- 239000000126 substance Substances 0.000 claims description 10
- 238000007599 discharging Methods 0.000 claims description 8
- 238000002309 gasification Methods 0.000 claims description 8
- VHUUQVKOLVNVRT-UHFFFAOYSA-N Ammonium hydroxide Chemical compound [NH4+].[OH-] VHUUQVKOLVNVRT-UHFFFAOYSA-N 0.000 claims description 7
- 235000011114 ammonium hydroxide Nutrition 0.000 claims description 7
- 229910001873 dinitrogen Inorganic materials 0.000 claims description 7
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- 238000003756 stirring Methods 0.000 claims description 7
- 230000009471 action Effects 0.000 claims description 5
- 238000001514 detection method Methods 0.000 claims description 4
- UCKMPCXJQFINFW-UHFFFAOYSA-N Sulphide Chemical compound [S-2] UCKMPCXJQFINFW-UHFFFAOYSA-N 0.000 claims description 3
- 230000008929 regeneration Effects 0.000 abstract description 7
- 238000011069 regeneration method Methods 0.000 abstract description 7
- 238000012546 transfer Methods 0.000 abstract description 6
- 229920006395 saturated elastomer Polymers 0.000 abstract description 2
- 230000009977 dual effect Effects 0.000 abstract 1
- 238000006243 chemical reaction Methods 0.000 description 12
- CDBYLPFSWZWCQE-UHFFFAOYSA-L Sodium Carbonate Chemical compound [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 description 8
- 239000000428 dust Substances 0.000 description 8
- 230000000694 effects Effects 0.000 description 7
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 6
- 230000008901 benefit Effects 0.000 description 6
- 238000005265 energy consumption Methods 0.000 description 6
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Chemical compound O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 6
- DWAQJAXMDSEUJJ-UHFFFAOYSA-M Sodium bisulfite Chemical compound [Na+].OS([O-])=O DWAQJAXMDSEUJJ-UHFFFAOYSA-M 0.000 description 5
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 description 5
- 229910002092 carbon dioxide Inorganic materials 0.000 description 5
- 238000011068 loading method Methods 0.000 description 5
- 238000002360 preparation method Methods 0.000 description 5
- 239000010865 sewage Substances 0.000 description 5
- 235000010267 sodium hydrogen sulphite Nutrition 0.000 description 5
- GEHJYWRUCIMESM-UHFFFAOYSA-L sodium sulfite Chemical compound [Na+].[Na+].[O-]S([O-])=O GEHJYWRUCIMESM-UHFFFAOYSA-L 0.000 description 5
- 238000013461 design Methods 0.000 description 4
- 239000011261 inert gas Substances 0.000 description 4
- 229910000029 sodium carbonate Inorganic materials 0.000 description 4
- 208000003569 Central serous chorioretinopathy Diseases 0.000 description 3
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 3
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- 229910001220 stainless steel Inorganic materials 0.000 description 3
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- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 2
- 229910000831 Steel Inorganic materials 0.000 description 2
- BFNBIHQBYMNNAN-UHFFFAOYSA-N ammonium sulfate Chemical compound N.N.OS(O)(=O)=O BFNBIHQBYMNNAN-UHFFFAOYSA-N 0.000 description 2
- 229910052921 ammonium sulfate Inorganic materials 0.000 description 2
- 235000011130 ammonium sulphate Nutrition 0.000 description 2
- 230000005540 biological transmission Effects 0.000 description 2
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- XLYOFNOQVPJJNP-ZSJDYOACSA-N heavy water Substances [2H]O[2H] XLYOFNOQVPJJNP-ZSJDYOACSA-N 0.000 description 2
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- 206010000369 Accident Diseases 0.000 description 1
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- QAOWNCQODCNURD-UHFFFAOYSA-L Sulfate Chemical compound [O-]S([O-])(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-L 0.000 description 1
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 1
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- 238000010531 catalytic reduction reaction Methods 0.000 description 1
- 239000003638 chemical reducing agent Substances 0.000 description 1
- 239000000571 coke Substances 0.000 description 1
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- 239000013078 crystal Substances 0.000 description 1
- 125000004122 cyclic group Chemical group 0.000 description 1
- 230000003009 desulfurizing effect Effects 0.000 description 1
- 125000000524 functional group Chemical group 0.000 description 1
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- 238000012423 maintenance Methods 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 150000004767 nitrides Chemical class 0.000 description 1
- 229910000069 nitrogen hydride Inorganic materials 0.000 description 1
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- 230000003647 oxidation Effects 0.000 description 1
- 238000007254 oxidation reaction Methods 0.000 description 1
- 239000013618 particulate matter Substances 0.000 description 1
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- 235000011149 sulphuric acid Nutrition 0.000 description 1
- 230000001502 supplementing effect Effects 0.000 description 1
- 239000002351 wastewater 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
- B01D53/02—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 by adsorption, e.g. preparative gas chromatography
- B01D53/04—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 by adsorption, e.g. preparative gas chromatography with stationary adsorbents
-
- 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
- B01D46/10—Particle separators, e.g. dust precipitators, using filter plates, sheets or pads having plane surfaces
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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
- B01D53/8631—Processes characterised by a specific device
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
- B01F25/00—Flow mixers; Mixers for falling materials, e.g. solid particles
- B01F25/20—Jet mixers, i.e. mixers using high-speed fluid streams
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B65—CONVEYING; PACKING; STORING; HANDLING THIN OR FILAMENTARY MATERIAL
- B65G—TRANSPORT OR STORAGE DEVICES, e.g. CONVEYORS FOR LOADING OR TIPPING, SHOP CONVEYOR SYSTEMS OR PNEUMATIC TUBE CONVEYORS
- B65G37/00—Combinations of mechanical conveyors of the same kind, or of different kinds, of interest apart from their application in particular machines or use in particular manufacturing processes
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B65—CONVEYING; PACKING; STORING; HANDLING THIN OR FILAMENTARY MATERIAL
- B65G—TRANSPORT OR STORAGE DEVICES, e.g. CONVEYORS FOR LOADING OR TIPPING, SHOP CONVEYOR SYSTEMS OR PNEUMATIC TUBE CONVEYORS
- B65G47/00—Article or material-handling devices associated with conveyors; Methods employing such devices
- B65G47/74—Feeding, transfer, or discharging devices of particular kinds or types
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F16—ENGINEERING ELEMENTS AND UNITS; GENERAL MEASURES FOR PRODUCING AND MAINTAINING EFFECTIVE FUNCTIONING OF MACHINES OR INSTALLATIONS; THERMAL INSULATION IN GENERAL
- F16J—PISTONS; CYLINDERS; SEALINGS
- F16J15/00—Sealings
- F16J15/02—Sealings between relatively-stationary surfaces
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- B—PERFORMING OPERATIONS; TRANSPORTING
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- B01D—SEPARATION
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- B01D2251/206—Ammonium compounds
- B01D2251/2062—Ammonia
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
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- B01D2257/30—Sulfur compounds
- B01D2257/302—Sulfur oxides
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2258/00—Sources of waste gases
- B01D2258/02—Other waste gases
- B01D2258/0283—Flue gases
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- B—PERFORMING OPERATIONS; TRANSPORTING
- 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
- B01D2259/40083—Regeneration of adsorbents in processes other than pressure or temperature swing adsorption
- B01D2259/40088—Regeneration of adsorbents in processes other than pressure or temperature swing adsorption by heating
- B01D2259/4009—Regeneration of adsorbents in processes other than pressure or temperature swing adsorption by heating using hot gas
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- B—PERFORMING OPERATIONS; TRANSPORTING
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Abstract
The invention relates to a flue gas alternating-current type activated carbon desulfurization and denitrification integrated process system and application, wherein a desulfurization and denitrification process unit of the system comprises two adsorption towers with dual functions of flue gas adsorption and activated carbon desorption; the adsorption tower comprises a denitration box body, a desulfurization box body and an ash bucket bin, wherein the denitration box body and the desulfurization box body are arranged in a vertically separated mode, and the ash bucket bin is connected to the bottom of the desulfurization box body; the upper space of the grid air guide plate in the desulfurization box body is connected with the lower space of the honeycomb air guide plate in the denitrification box body through an external pipeline A; the ash hopper bins of the two adsorption towers are respectively connected with an external pipeline B; the smoke outlets of the desulfurization box bodies of the two adsorption towers are respectively connected with an external pipeline C. The adsorption tower is provided with two adsorption towers which have the same function and integrate the adsorption and desorption functions, when the flue gas adsorption function of one adsorption tower is in a saturated state, the adsorption tower transfers the flue gas adsorption function to another alternative operation, and the adsorption tower self-starts the desorption and regeneration functions of the activated carbon.
Description
Technical Field
The invention relates to a flue gas alternating-current type activated carbon desulfurization and denitrification integrated process system and application, and belongs to the technical field of industrial flue gas pollution treatment.
Background
Aiming at the comprehensive treatment of sintering flue gas, at present, there are three technical schemes for treating the sintering flue gas of iron and steel enterprises, namely an SCR method, an oxidation method and an activated carbon method. According to a large amount of research at home and abroad, the only method which can simultaneously remove various pollutants in the smoke is the activated carbon method. The activated carbon has a highly developed pore structure and a large specific surface area in the interior, is good in chemical stability and thermal stability, contains various oxygen-containing functional groups on the surface, can be used as an adsorbent and a catalyst carrier, and has strong adsorption capacity. The active carbon process mainly comprises the following steps: single-stage activated carbon process, two-stage activated carbon process, counter-current activated carbon process.
The currently industrially used desulfurization and denitrification activated carbon is mostly columnar granular activated carbon with the diameter of 8-9 mm, and different from the conventional activated carbon, the desulfurization and denitrification activated carbon is an adsorbing material with high comprehensive strength (pressure resistance and wear resistance), large specific surface area and large sulfur capacity, and in the using process, the heating regeneration is equivalent to the reactivation of the activated carbon, so that the desulfurization and denitrification performances are increased.
A counter-flow (CSCR) activated carbon desulfurization and denitrification integrated process is a production process which is currently concerned at home and abroad, and comprises the following steps: the method comprises three main components of a flue gas desulfurization and denitrification process, a sodium metabisulfite preparation process, a wastewater treatment process and the like. The integrated process has the outstanding advantage of removing SO in one system2NOx, particulate matter, heavyMetal and other multicomponent pollutant while eliminating SO2NH generated in the denitration process3The comprehensive utilization of resources is carried out, the method is used for producing sodium metabisulfite and ammonium sulfate, no solid waste is generated, and zero emission of waste water is realized. SO (SO)2The emission reaches less than 10 mg per cubic meter, and the desulfurization rate reaches more than 99.5 percent; NOx emission reaches below 50 mg per cubic meter, the denitration rate reaches above 85%, the produced sodium metabisulfite and ammonium sulfate reach the high-class standard, and all indexes of the process are at domestic advanced levels.
The flue gas desulfurization and denitration process system in the counter-flow (CSCR) activated carbon desulfurization and denitration integrated process mainly comprises: the system comprises a flue gas system, an adsorption system, an analytic system, an activated carbon conveying system and an automatic control system. For example, chinese patent document CN210495771U provides a comprehensive utilization system for desulfurization and denitrification of activated carbon, which includes an activated carbon powder storage and conveying system, a circulating fluidized bed device, a bag-type dust collector, an activated carbon adsorption tower, an activated carbon desorption tower, an activated carbon vibrating screen, and an activated carbon powder bin. The discharge port of the activated carbon desorption tower is provided with an activated carbon vibrating screen connected with an activated carbon powder bin, and the activated carbon powder bin is connected to an activated carbon powder storage and conveying system; the bottom of the circulating fluidized bed device is provided with an activated carbon powder spraying device connected with an activated carbon powder storage and conveying system; the exhaust port of the circulating fluidized bed device is connected to the air inlet of the bag-type dust collector; the air outlet of the bag-type dust collector is connected to the air inlet of the activated carbon adsorption tower. The system has the outstanding characteristics that the adsorption system and the desorption system are respectively and independently arranged and operated, the adsorption system and the desorption system carry out closed-loop reciprocating transfer and conveying on activated carbon particles with the weight of thousands of tons by virtue of the activated carbon conveying system, and in the process, the activated carbon conveying system bears huge conveying capacity, so that the defects of huge and complicated structure, complex process production process, high equipment investment cost, high conveying energy consumption, high production fault occurrence rate and the like of the whole production process system are caused.
In view of the above problems, how to optimize, upgrade and transform a flue gas desulfurization and denitrification process in the existing counter-flow type (CSCR) activated carbon desulfurization and denitrification integrated process, and transform the working state of activated carbon from a "flow type" to a "static type", so as to achieve the purpose of large-scale reduction of an activated carbon conveying system, becomes a fundamental problem to be solved in the present invention.
Disclosure of Invention
Aiming at the defects of the prior art, the invention provides a flue gas alternating-current activated carbon desulfurization and denitrification integrated process system, which integrates the desulfurization and denitrification of flue gas, the analysis and regeneration functions of activated carbon into an adsorption tower to complete through upgrading and improving a sintering flue gas desulfurization and denitrification process in a counter-current manner, and the activated carbon does not need to be circularly transferred to the analysis tower for treatment. The system of the invention is characterized in that two adsorption towers with completely identical functions and integrated adsorption and desorption functions are respectively arranged in each unit, the two adsorption towers synchronously alternate in function operation or synchronously adsorb and desorb at different times, when the flue gas adsorption function of one adsorption tower is close to a saturated state, the adsorption towers automatically start the desorption and regeneration functions of the activated carbon, and simultaneously, the adsorption function of the flue gas is completely completed by the other adsorption tower.
The invention also provides an operation method of the flue gas alternating-current type activated carbon desulfurization and denitrification integrated process system.
The technical scheme of the invention is as follows:
a flue gas exchange type integrated process system for desulfurization and denitrification of activated carbon comprises two adsorption towers which are operated in a matching way;
the adsorption tower comprises a denitration box body, a desulfurization box body and an ash bucket bin which are sequentially arranged from top to bottom, wherein the denitration box body and the desulfurization box body are separately arranged up and down, and the desulfurization box body is communicated with the ash bucket bin up and down; a honeycomb gas guide plate is arranged in the denitration box body, and divides the space in the denitration box body into an upper part and a lower part; a grid air guide plate is arranged in the desulfurization box body;
the top of the adsorption tower is provided with a feeding flow dividing pipe, the feeding flow dividing pipe is respectively inserted into the denitration box body and the desulfurization box body, and activated carbon particles are respectively injected into the denitration box body and the desulfurization box body through the feeding flow dividing pipe;
the upper space of the grid air guide plate in the desulfurization box body is connected with the lower space of the honeycomb air guide plate in the denitrification box body through an external pipeline A;
the ash hopper bins of the two adsorption towers are respectively connected with an external pipeline B; the smoke outlets of the desulfurization box bodies of the two adsorption towers are respectively connected with an external pipeline C.
The invention adopts an alternate operation mode that two adsorption towers are mutually matched and staggered, and the adsorption function of the adsorption towers and the analysis function of the analysis tower in the traditional process system are completely integrated in the adsorption towers to be completed, when one adsorption tower carries out adsorption work, the other adsorption tower can carry out adsorption or analysis work, or when one adsorption tower carries out analysis work, the other adsorption tower carries out adsorption work, thereby not only ensuring the uninterrupted continuous operation of the flue gas adsorption work, but also realizing that the analysis work can be alternately completed between the two adsorption towers after the analysis tower is abolished. Through the innovation of the technology, the independent establishment process of the desorption tower in the traditional process can be eliminated, the operation process of long-distance and reciprocating cyclic transportation of the activated carbon particles between the adsorption tower and the desorption tower is eliminated, and the purposes of simplifying the production process flow, reducing the equipment scale, reducing the system construction investment cost, reducing the production operation energy consumption and the like are further achieved. When the adsorption tower carries out adsorption or analysis operation, the adsorption tower can realize the switching between the adsorption operation function and the analysis operation function of the flue gas only by switching the pipeline communication among the sintering flue gas pipeline, the high-temperature nitrogen pipeline and the low-temperature nitrogen pipeline through the external pipeline B and switching the pipeline communication between the denitration box body and the sodium metabisulfite preparation system through the first butterfly valve and the second butterfly valve.
Preferably, the bottom of the honeycomb air guide plate and the bottom of the grid air guide plate are respectively communicated with a waste discharge pipe, and the two waste discharge pipes extend to the outside of the adsorption tower.
Preferably, the honeycomb air guide plate is mainly formed by connecting four identical sub-plates, the sub-plates incline downwards by 10-15 degrees from the outer side edge to the inner side edge of the sub-plates, a plurality of funnel grooves are formed in the sub-plates, and filter screens are arranged at the bottoms of the funnel grooves.
Preferably, the grid air guide plate is mainly formed by connecting four same daughter boards, the daughter boards incline downwards 10-15 degrees from the outer side edge to the inner side edge of the daughter boards, a plurality of holes are formed in the daughter boards, and filter screens are arranged at the holes.
Preferably, the mesh aperture of the filter screen on the honeycomb air guide plate and the grid air guide plate is 4-5 mm.
Preferably, a stirrer is arranged in the desulfurization box body and positioned above the grid air guide plate.
Preferably, the agitator includes stirring rake, rotation axis, drive chain and motor, and the stirring rake sets up on the rotation axis, and the one end of rotation axis is connected on the inner wall of desulfurization box, and the other end of rotation axis is worn out the desulfurization box and is passed through the drive chain transmission with the motor output shaft and be connected.
Preferably, be provided with the airtight storehouse of motor on the outer wall of desulfurization box, motor, drive chain and rotating shaft tip all are encapsulated in the airtight storehouse of motor, and the airtight storehouse of motor is provided with the access hole.
Preferably, the external pipeline A is provided with a first butterfly valve and an annular ammonia sprayer, the annular ammonia sprayer is connected with the ammonia water gasification furnace through the external pipeline D, and the ammonia water gasification furnace is connected with the ammonia heating furnace.
Preferably, the annular ammonia sprayer is an annular vent pipe, and a plurality of nozzles are uniformly distributed on the inner wall of the annular vent pipe.
Preferably, the process system further comprises a wet scrubber, a sodium metabisulfite system, a nitrogen storage tank and a nitrogen heating furnace; the wet scrubber is connected with the external pipeline C, the wet scrubber is connected with the sodium metabisulfite system through a pipeline, the sodium metabisulfite system is connected with the nitrogen storage tank through a pipeline, the nitrogen storage tank is connected with the nitrogen heating furnace and the external pipeline B through a pipeline, and the nitrogen heating furnace is also connected with the external pipeline B.
Preferably, the wet scrubber is further connected to a sewage treatment system.
Preferably, the nitrogen storage tank is also connected with a nitrogen making device.
Preferably, the feeding shunt pipe is communicated with the bottom of the active carbon bin of the adsorption tower. The advantage of this design is that the interior active carbon granule of piling up of feed bin is carried in passing through the material loading shunt tubes respectively to denitration box, the desulfurization box.
Preferably, the process system further comprises a feeding system, wherein the feeding system comprises an activated carbon particle storage bin, an activated carbon lifting machine, a belt material conveying machine and a fixed-point discharger; the active carbon granule storage bin is located active carbon lifting machine bottom one side, and the belt material transporting machine is located active carbon lifting machine top one side, and the fixed point tripper is installed on the belt material transporting machine and is located the adsorption tower active carbon feed bin directly over.
Preferably, the fixed-point discharging device comprises a cylinder, a bracket, a lifting bracket and a discharging plate; the support sets up in the both sides of belt material transporting machine, and the cylinder setting is at the support top, and the lifting support is connected to the piston rod of cylinder, and the stripper is connected to one side of lifting support, and the stripper is located the top of belt material transporting machine, and the width of stripper is greater than the width of material transporting belt.
Preferably, the lifting support comprises a guide sliding plate, a guide sliding shaft and cross beam plates, the guide sliding plate is fixedly connected with a piston rod of the air cylinder, the guide sliding shaft is arranged on two sides of the guide sliding plate and installed in a guide sliding groove formed in the support, the same side of the guide sliding plate is connected with the two cross beam plates, and the two cross beam plates are connected with the stripper plate.
Preferably, the process system further comprises a scraper which is positioned below the ash hopper and the waste discharge pipe. The design has the advantage that the produced waste is uniformly discharged into the conveying pipe of the scraper conveyor and then conveyed out by the scraper conveyor.
Preferably, install first dome valve on the waste material of honeycomb air deflector bottom intercommunication is excreteed and is managed, install second dome valve on the waste material of grid air deflector bottom intercommunication is excreted and manage, and the third dome valve is installed to the bottom in ash hopper storehouse, and fourth dome valve is installed on material loading shunt tubes top, installs the second butterfly valve on the outside pipeline C, installs the sixth butterfly valve on the outside pipeline D.
Preferably, the external pipeline B is provided with three communicated branch pipes, and a third butterfly valve is arranged on the first branch pipe and used for introducing sintering flue gas; a fourth butterfly valve is arranged on the second branch pipe, is communicated with the nitrogen storage tank and is used for introducing cooling air; the third branch pipe is provided with a fifth butterfly valve and communicated with the nitrogen heating furnace for introducing hot air.
Preferably, the chemical inert gas for heating air separation is selected from nitrogen. The design has the advantages that the chemical inert gas can implement physical isolation protection on the analysis process of the activated carbon, and is prevented from being interfered by outside chemicals, so that the analysis efficiency is improved, the spontaneous combustion phenomenon of the activated carbon is prevented, and in addition, the preparation cost of the nitrogen is lower.
Preferably, the cooling air separation uses chemical inert gas, preferably nitrogen. The design has the advantages that the chemical inert gas can prevent the activated carbon from generating chemical reaction with oxygen at a high temperature state, so that the unnecessary consumption of the activated carbon is reduced, the emission of greenhouse gas (carbon dioxide) is reduced, and in addition, the preparation cost of the nitrogen is lower.
Preferably, a chimney is arranged at the top of the denitration box body.
Preferably, a heat insulation layer is arranged between the denitration box body and the desulfuration box body.
An operation method of a flue gas alternating-current type activated carbon desulfurization and denitrification integrated process system, wherein the adsorption and analysis processes of two adsorption towers are alternately operated, or the adsorption and analysis processes are synchronously performed but the analysis operations are staggered, comprises the following steps:
1) the activated carbon hoister conveys the activated carbon particles to a belt material conveyer, the belt material conveyer conveys the activated carbon particles, and the activated carbon particles on the belt material conveyer are pushed and turned to an activated carbon bin of an adsorption tower below the belt material conveyer through a fixed-point discharger to be accumulated;
2) respectively conveying the activated carbon particles in the activated carbon bin of the adsorption tower onto a honeycomb air guide plate or a grid air guide plate through a feeding flow dividing pipe;
3) introducing sintering flue gas into an ash hopper bin of one adsorption tower through an external pipeline B, wherein the sintering flue gas upwards passes through a grid gas guide plate from the ash hopper bin, passes through an activated carbon particle layer, and enters a lower space of a honeycomb gas guide plate in a denitration box body through an external pipeline A;
4) the desulfurized flue gas passes through the honeycomb gas guide plate from the lower space of the honeycomb gas guide plate upwards, passes through the activated carbon particle layer, and the purified flue gas after denitration is discharged into the atmosphere from a chimney;
5) when the content of pollutants in the flue gas discharged by the adsorption tower is detected to be close to the standard exceeding by the online detection device, the flue gas adsorption function of the adsorption tower is immediately stopped, the production mode of the analysis function is switched to, and meanwhile, the flue gas adsorption function of the adsorption tower is combined by the other adsorption tower;
6) when the adsorption tower is switched to an analytic function production mode, gas introduced into the ash hopper bin through the external pipeline B is switched into hot air from sintering flue gas, the hot air upwards passes through the grid gas guide plate from the ash hopper bin to enter the activated carbon particle layer, and fully contacts with the activated carbon particle layer under the stirring action of the stirrer to be heated, and the sulfide pollutants adsorbed by the activated carbon particle layer are analyzed to be changed into gaseous state and then are carried away by the hot air, and then enter the wet scrubber through the external pipeline C;
7) the wet scrubber primarily treats the desorbed gaseous substances to remove SO2Conveying the sodium metabisulfite to a sodium metabisulfite system for preparing a sodium metabisulfite product, supplementing N2 discharged by the sodium metabisulfite system and N2 generated by nitrogen making equipment into a nitrogen storage tank, conveying N2 to a nitrogen heating furnace again by the nitrogen storage tank for high-temperature heating, and then circularly conveying the nitrogen heating furnace into a desulfurization box body;
8) repeating the steps 5) to 7) until SO in the exhaust gas of the desulfurization box body2The content is detected to be qualified after reaching the standard;
9) after the production mode of the analytic function of the adsorption tower is completed, gas introduced into the ash hopper bin through an external pipeline B is switched into cooling air by heating air, the cooling air cools a high-temperature activated carbon particle layer in the desulfurization box, partial heat of the high-temperature activated carbon is taken away by the cooling air, the gas enters a wet scrubber through an external pipeline C to be cooled, then the gas is conveyed into a nitrogen storage tank through a sodium metabisulfite system to be used as cooling air again, the gas enters the ash hopper bin through the external pipeline B again to perform circulating cooling treatment on the high-temperature activated carbon particle layer, and the gas is circulated repeatedly until the temperature of the activated carbon particle layer in the desulfurization box is detected to be qualified after reaching the standard;
meanwhile, when the adsorption tower carries out the steps 3) to 4), the other adsorption tower can synchronously carry out the operations of the steps 3) to 4) after finishing the operations of the steps 5) to 9); when the adsorption tower performs the operations of the steps 5) to 9), the other adsorption tower performs the operations of the steps 3) to 4); when the other adsorption tower performs the operation of the steps 3) to 4), the adsorption tower can perform the operation of the steps 3) to 4) synchronously after completing the operation of the steps 5) to 9); when the other adsorption tower performs the operations of the steps 5) to 9), the other adsorption tower performs the operations of the steps 3) to 4); the circulation is repeated, so that the alternate operation of flue gas adsorption and pollutant analysis between the two adsorption towers is realized.
Preferably, the working method further comprises a step 10) of discharging the waste material to a scraper outside the adsorption tower through a waste material discharge pipe and transporting the waste material to other places by the scraper when the adsorption function of the activated carbon is reduced to be incapable of meeting the production requirement.
The invention has the beneficial effects that:
1. the invention changes the working state of the active carbon from the traditional 'flow type' to the 'static type', eliminates the independent establishment process of the analytic tower, further greatly simplifies the scale of the conveying system of the active carbon, reduces the transportation energy consumption of materials, reduces the occurrence rate of production equipment faults and reduces the investment cost of system construction.
2. According to the invention, the stirrer is additionally arranged in the desulfurization box body, and the stirrer slowly and uniformly stirs the activated carbon layer, so that the filtering and adsorption effects of the activated carbon on the flue gas can be more sufficient and remarkable, or the heat contact with high-temperature nitrogen is more sufficient.
3. According to the invention, the plurality of gas guide structures are uniformly distributed on the grid gas guide plate in the desulfurization box body, so that the flue gas can uniformly penetrate through the activated carbon layer, and the flue gas filtering effect is better; a plurality of gas guide structures which are uniformly distributed on the honeycomb gas guide plate in the denitration box body are beneficial to enabling flue gas to uniformly penetrate through the activated carbon layer, so that the catalytic action of the denitration chemical reaction is better.
4. The aperture of the stainless steel grid mesh of the grid air guide plate and the honeycomb air guide plate is set to be about 4-5 mm, so that the screening and removal of dust and crushed activated carbon particles in an activated carbon layer are facilitated; the air guide hole structure of the honeycomb air guide plate is of a funnel-shaped structure, and full contact between the flue gas and the activated carbon layer is facilitated.
5. The nitrogen is adopted as the cooling gas of the activated carbon in the desulfurization box body, and the purpose is to utilize the chemical stability of N2 to implement physical isolation protection on the activated carbon so as to prevent the activated carbon from generating chemical reaction with oxygen, thereby avoiding spontaneous combustion fire accidents caused by overhigh temperature of local hot spots of the activated carbon.
6. According to the invention, the annular ammonia sprayer is adopted to mix the ammonia gas and the desulfurized flue gas, so that the ammonia gas and the desulfurized flue gas are mixed more uniformly, the mixing effect is more obvious, and the flue gas denitration chemical reaction is more favorably carried out.
7. According to the invention, the end of the feeding shunt pipe is additionally provided with the secondary shunt pipe structure, so that the forming thickness of the feeding layer is more uniform, and the flue gas treatment efficiency is improved.
8. The feeding system of the adsorption tower adopts a multi-fixed-point belt material conveying machine system structure to replace the conveying mode of the traditional chain bucket conveyor, and is beneficial to reducing the structural complexity of the system, thereby reducing the investment cost, reducing the energy consumption of conveying power and reducing the occurrence rate of equipment faults.
9. One end of a rotating shaft of the stirrer penetrates through the side wall of the box body to be in meshed connection with an external driving motor through a chain, and the driving motor is not directly and tightly connected with the side wall of the box body, so that the heat supply amplitude of heat in the box body to the driving motor is reduced; a sealing box body is arranged outside the driving motor, and the box body is hermetically welded with the side wall of the desulfurization box body, so that the sealing property of the desulfurization box body is ensured; the sealed box body is reserved with a sealed access hole, so that the maintenance operation of the equipment is facilitated.
Drawings
FIG. 1 is a schematic diagram of a conventional process;
FIG. 2 is a schematic diagram of the composition of the process system of the present invention;
FIG. 3 is a top view of an adsorption column of the present invention;
FIG. 4 is a schematic cross-sectional view of an annular ammonia sprayer according to the present invention;
FIG. 5 is a perspective view of a spot unloader of the present invention;
FIG. 6 is a side view of a spot unloader of the present invention;
FIG. 7 is a top view of a honeycomb air guide plate according to the present invention;
FIG. 8 is a side view of a honeycomb air guide plate according to the present invention;
FIG. 9 is a top view of a grid air guide plate according to the present invention;
in the figure: 1-activated carbon particles, 2-adsorption tower activated carbon silo, 3-fourth dome valve, 4-feeding shunt pipe, 5-denitration box, 6-honeycomb gas guide plate, 7-adsorption tower, 8-waste discharge pipe, 9-desulfurization box, 10-first dome valve, 11-scraper machine, 12-waste bin, 13-chimney, 14-ring ammonia sprayer, 15-external pipeline A, 16-first butterfly valve, 17-second butterfly valve, 18-stirrer, 19-grid gas guide plate, 20-ash hopper bin, 21-third dome valve, 22-second dome valve, 23-belt conveyer, 24-sixth butterfly valve, 25-third butterfly valve, 26-fourth butterfly valve, 27-fifth butterfly valve, 28-wet scrubber, 29-sewage treatment system, 30-sodium metabisulfite system, 31-nitrogen storage tank, 32-nitrogen heating furnace, 33-ammonia heating furnace, 34-ammonia water gasification furnace, 35-nitrogen making equipment, 36-fixed point discharger, 37-activated carbon lifter, 38-activated carbon particle storage bin, 39-motor closed bin, 40-manhole, 41-driving chain, 42-motor, 43-nozzle, 44-cylinder, 45-stripper, 46-bracket, 47-sliding guide shaft, 48-material conveying belt, 49-crossbeam plate, 50-filter screen, 51-discharge hole, 52-funnel groove, 53-filter screen, 54-steel plate, 55-discharge hole, 56-external pipeline B, 57-external pipeline C, 58-external pipeline D, 59-guide chute and 60-guide sliding plate.
Detailed Description
The present invention will be further described by way of examples, but not limited thereto, with reference to the accompanying drawings.
The chemical working principle of the desulfurization and denitrification process is as follows:
the adsorption characteristic and the catalysis characteristic of the active carbon are utilized to ensure that SO in the flue gas2O2 and water vapor are respectively adsorbed on the surface of the activated carbon, and H2SO4 generated by reaction is adsorbed in the micropores of the activated carbon, thereby achieving the effect of desulfurization.
2SO2+O2+2H2O→2H2SO4
And the activated carbon denitration mainly utilizes the catalytic performance of the activated carbon to carry out Selective Catalytic Reduction (SCR) reaction, and NOx is reduced to N2 under the action of a reducing agent NH 3.
4NO+4NH3+O2→4N2+6H2O
2NO2+4NH3+O2→3N2+6H2O
a. And (3) analysis and regeneration of the activated carbon: will adsorb SO2Heating saturated activated carbon to 390-450 ℃, decomposing and desorbing sulfuric acid or sulfate accumulated in the activated carbon, wherein the generated main decomposed product is SO2、N2、CO2、H2O in the form of high-concentration SO2The gas of (2). The main reaction is the reaction of sulfuric acid with activated carbon:
2H2SO4+C→2SO2+CO2+2H2O
the regeneration reaction can recover the activity of the activated carbon, and the adsorption and catalytic capacity of the activated carbon can be improved.
b. Conversion and utilization of by-products:
(1) introducing SO into sodium carbonate solution2To produce a sodium bisulfite solution.
Na2CO3+2SO2+H2O→2NaHSO3+CO2
(2) Sodium carbonate is added into the sodium bisulfite solution, and the sodium bisulfite solution is converted into sodium sulfite.
Na2CO3+2NaHSO3→2Na2SO3+CO2+H2O
(3) Sodium sulfite and SO2The reaction, in turn, produces a sodium bisulfite solution.
Na2SO3+SO2+H2O→2NaHSO3
(4) When the sodium bisulfite content in the solution reaches the supersaturated concentration, sodium metabisulfite crystals are separated out.
2NaHSO3→Na2S2O5+H2O
As shown in fig. 1, a schematic diagram of a conventional flue gas desulfurization and denitration process is shown, and the desulfurization and denitration system mainly comprises an adsorption system, an analytic system, an activated carbon transfer system, a flue gas system, an ammonia station system, a dust removal system, a sodium metabisulfite system, a sewage treatment system, a main control building and the like.
And (3) enabling the sintering flue gas to enter an adsorption tower for flue gas desulfurization and denitration operation, firstly desulfurizing and then denitrating in the tower, and enabling the flue gas to come out from the tower top and be sent back to a chimney through a draught fan for emission. The active carbon in the adsorption tower is transferred to an analysis tower through a transfer system for analysis treatment, and the analyzed SO2The gas is conveyed to a sodium metabisulfite system for processing and manufacturing by-products. In the desorption tower, the desorbed active carbon is reactivated to achieve the regeneration function, and then is transported back to the adsorption tower by the transport system to perform the adsorption function of the smoke pollutants again.
Example 1:
as shown in fig. 2, the embodiment provides a flue gas exchange type integrated process system for desulfurization and denitrification of activated carbon, which includes two adsorption towers working in cooperation, two identical adsorption towers being arranged in a left-right manner, and the following description takes the left adsorption tower as an example;
the adsorption tower comprises a denitration box body 5, a desulfurization box body 9 and an ash hopper bin 20 which are sequentially connected from top to bottom, wherein the denitration box body 5 and the desulfurization box body 9 are arranged in a vertically separated manner, and the ash hopper bin 20 is connected to the bottom of the desulfurization box body 9; the denitration box body 5 and the desulfurization box body 9 are connected in a split manner, a heat insulation layer is arranged between the denitration box body and the desulfurization box body, and the ash hopper bin 20 is communicated with the desulfurization box body 9; a honeycomb gas guide plate 6 is arranged in the denitration box body 5, the inside of the denitration box body 5 is divided into an upper part and a lower part by the honeycomb gas guide plate 6, and the bottom of the honeycomb gas guide plate 6 is communicated with a waste discharge pipe 8; a grid air guide plate 19 is arranged in the desulfurization box body 9, and the bottom of the grid air guide plate 19 is also communicated with a waste discharge pipe; two waste discharge pipes lead out of the adsorption tower 7; the denitration box body 5 and the desulfuration box body 9 are cylindrical, and the ash bucket bin 20 is in an inverted cone shape.
A feeding flow distribution pipe 4 is arranged at the top of the adsorption tower 7, the feeding flow distribution pipe 4 is inserted into the denitration box body 5, and a discharge hole of the feeding flow distribution pipe 4 is positioned above the honeycomb gas guide plate 6; in material loading shunt tubes 4 inserted the desulfurization box after passing the denitration box, its discharge gate was located grid air guide plate 9 tops.
The upper space of the grid air guide plate 19 in the desulfurization box body 9 is connected with the lower space of the honeycomb air guide plate 6 in the denitration box body 5 through an external pipeline A15; the ash hopper bins of the two adsorption towers are respectively connected with a sintering flue gas supply pipeline through an external pipeline B56, and the smoke outlets of the desulfurization box bodies of the two adsorption towers are respectively indirectly connected with a sodium metabisulfite preparation system and a wastewater treatment system through an external pipeline C57.
Wherein, the top of denitration box 5 is equipped with chimney 13, and the clean flue gas after the SOx/NOx control is accomplished discharges into the atmosphere from the chimney.
As shown in fig. 7 and 8, the honeycomb air guide plate 6 is mainly formed by welding four identical sub-plates, the material of the sub-plate is stainless steel, the sub-plates are inclined downwards by 10 to 15 degrees from the outer side edges to the inner side edges, a plurality of funnel grooves 52 are arranged on the sub-plates, and filter screens 50 are arranged at the bottoms of the funnel grooves. The center of the honeycomb air guide plate 6 enclosed by the four sub-plates is a discharge hole 51, and the discharge hole 51 is used for connecting the waste discharge pipe 8, so that the material is convenient to discharge. Inside the denitration box 5 was erect to honeycomb air deflector 6, two spaces about dividing the internal space of denitration box 5 into.
As shown in fig. 9, the grid air guide plate 19 is formed by welding four identical sub-plates, the material of the grid air guide plate is stainless steel, the sub-plates incline downwards by 10 to 15 degrees from the outer side edges to the inner side edges, a plurality of holes are formed in the sub-plates, and a filter screen 53 is arranged at the holes. The center of the grid air guide plate 19 enclosed by the four sub-plates is a discharge hole 55, and the discharge hole 55 is used for connecting a waste discharge pipe, so that the material can be discharged conveniently. The grid air guide plate 19 is located at the joint of the desulfurization box body 9 and the ash bucket bin 20, that is, the desulfurization box body 9 and the ash bucket bin 20 are isolated by the grid air guide plate.
The aperture of the filter screen meshes of the honeycomb air guide plate 6 and the grid air guide plate 19 is 4-5 mm.
The external pipeline A15 is a flue gas transfer box guide pipe, a first butterfly valve 16 and an annular ammonia sprayer 14 are installed on the external pipeline A15, the two annular ammonia sprayers on the left adsorption tower and the right adsorption tower are respectively connected with an ammonia water gasification furnace 34 through external pipelines D58, and the ammonia water gasification furnace 34 is connected with an ammonia heating furnace 32. The combined action of the ammonia heating furnace 32 and the ammonia water gasification furnace 34 is utilized to obtain mixed gas (NH3+ air), the ammonia content of the mixed gas is 3% -5% at 200 ℃, and then the mixed gas and the desulfurized flue gas are fully and uniformly mixed through the annular ammonia sprayer 14 and then enter the denitration box body 5.
As shown in fig. 4, the annular ammonia sprayer 14 is an annular vent pipe, a plurality of nozzles 43 are uniformly distributed on the inner wall of the annular vent pipe, the number of the nozzles is set according to requirements, the plurality of nozzles 43 are uniformly distributed on the inner wall of the annular vent pipe by 360 degrees, when the desulfurized flue gas passes through the middle of the annular vent pipe, the plurality of nozzles 43 spray ammonia gas simultaneously, and the ammonia gas and the desulfurized flue gas are uniformly mixed and then enter the denitration box body 5.
The process system also comprises a wet scrubber 28, a sodium metabisulfite system 30, a nitrogen storage tank 31, a nitrogen heating furnace 32 and a nitrogen making device 35, wherein an external pipeline C57 is connected with the wet scrubber 28 through a pipeline, the wet scrubber 28 is connected with the sodium metabisulfite system 30 through a pipeline, the sodium metabisulfite system 30 is connected with the nitrogen storage tank 31 through a pipeline, the nitrogen storage tank 31 is connected with the nitrogen making device 35, the nitrogen heating furnace 32 and an external pipeline B56 through pipelines, the nitrogen heating furnace 32 is also connected with the external pipeline B56, and the nitrogen making device can be a conventional nitrogen making machine.
The feeding shunt tubes 4 are communicated with the bottom of the active carbon bin 2 of the adsorption tower, the fourth dome valve 3 is installed at the top ends of the feeding shunt tubes 4, and the discharging action of the coke bin is opened or closed through the fourth dome valve 3. The active carbon particles piled up in the storage bin are respectively conveyed into the denitration box body and the desulfurization box body through the feeding flow dividing pipe 4. As shown in fig. 3, the terminal top position in denitration box 5, desulfurization box 9 of material loading shunt tubes 4, and 2 short spinal branch pipes of terminal branch of material loading shunt tubes 4, so can more evenly the unloading, evenly put the active carbon granule on honeycomb air guide 6 and grid air guide 19, the active carbon granule layer about 70cm is placed to honeycomb air guide 6 top, the active carbon granule layer about 70cm has been placed to grid air guide 19 top.
The process system further comprises a feeding system, the feeding system comprises an active carbon particle storage bin 38, an active carbon lifting machine 37, a belt material conveying machine 23 and a fixed-point discharger 36, the bottom end of the active carbon lifting machine 37 is located on one side of the active carbon particle storage bin 38, the top end of the active carbon lifting machine 37 is located above one end of the belt material conveying machine 23, the belt material conveying machine 23 passes through the fixed-point discharger 36, and the fixed-point discharger 36 is installed above the active carbon storage bin 2 of the adsorption tower.
Wherein, active carbon granule storehouse, active carbon lifting machine, belt fortune material machine are conventional equipment.
Install first dome valve 10 on the waste material drainage pipe of honeycomb air deflector 6 bottom intercommunication, install second dome valve 22 on the waste material drainage pipe of grid air deflector 19 bottom intercommunication, third dome valve 21 is installed to the bottom in ash bucket storehouse, installs second butterfly valve 17 on the outside pipeline C, installs sixth butterfly valve 24 on the outside pipeline D58.
The external pipeline B56 is provided with three communicated branch pipes, wherein the first branch pipe is provided with a third butterfly valve 25 for introducing sintering flue gas; a fourth butterfly valve 26 is arranged on the second branch pipe, is communicated with the nitrogen storage tank and is used for introducing cooling air (nitrogen); the third branch pipe is provided with a fifth butterfly valve 27 and is communicated with a nitrogen heating furnace 32 for introducing heating air (nitrogen). The conduction switching among the pipelines is realized through the switching of the switches among the butterfly valves on the pipelines.
Compared with the traditional process, the technical scheme of the embodiment has the following advantages:
(1) the desulfurization and denitrification effects are more obvious;
(2) the process of independently setting up the analytical tower is eliminated, so that the structure of the whole production process line is simpler, and the production organization and management are more convenient;
(3) the transfer process of the large-amount active carbon between the adsorption tower and the desorption tower is eliminated, so that the number of the mobile equipment of the whole process system is greatly reduced, the occurrence rate of equipment faults is effectively reduced, and the operation energy consumption of the equipment is reduced;
(4) the probability of local hot spots caused by uneven heating of the activated carbon on the desulfurization layer is reduced, so that spontaneous combustion fire caused by over-high local temperature of the activated carbon is avoided, the safety of a system is ensured, and the running stability of the system is improved.
Example 2:
example 1 was repeated with the following differences: three stirrers 18 are arranged in the desulfurization box body, and the stirrers 18 are positioned 10cm above the grid air guide plate 19. The three stirrers are arranged in the same horizontal direction in the desulfurization box body at equal intervals.
The agitator 18 includes stirring rake, rotation axis, drive chain 41 and motor 42, and the stirring rake passes through welded mounting on the rotation axis, and the one end of rotation axis is connected on the inner wall of desulfurization box, and the other end of rotation axis is worn out the desulfurization box and is connected through the drive chain 41 transmission with the motor output shaft, and the rotation axis both ends are fixed in the fixing bearing on the desulfurization box inner wall.
The outer wall of the desulfurization box body 9 is provided with a motor closed bin 39, the end parts of the motor, the driving chain and the rotating shaft are all packaged in the motor closed bin 39, and a sealed access hole 40 is reserved in the motor closed bin.
Example 3:
example 1 was repeated with the following differences: the wet scrubber is also connected to a sewage treatment system 29, which is conventional. The scrubbing solution in the wet scrubber reaches a certain concentration and is discharged to a sewage treatment system for purification treatment.
Example 4:
example 1 was repeated with the following differences: the fixed point discharging device comprises a cylinder 44, a bracket 46, a lifting bracket and a discharging plate 45; support 46 is C type frame, erects the both sides at belt material transporting machine 23, and cylinder 44 passes through the bolt and installs at support 46 top, and lifting support is connected to cylinder 44's piston rod, and stripper 45 is connected to one side of lifting support, and stripper 45 is located the top of belt material transporting machine 23, and the width of stripper 45 is greater than the width of transporting material belt 48. As shown in fig. 5 and 6.
The lifting support comprises a guide sliding plate 60, a guide sliding shaft 47 and cross beam plates 49, the guide sliding plate 60 is fixedly connected with a piston rod of the air cylinder 44, two sides of the guide sliding plate 60 are connected with the guide sliding shaft 47, the guide sliding shaft 47 is installed in a guide sliding groove 59 formed in the support 46, the same side of the guide sliding plate 60 is connected with the two cross beam plates 49, and the two cross beam plates 49 are connected with the discharging plate 45.
The stripper plate 45 is mainly composed of two identical special-shaped structural plates, the overall shape of the special-shaped structural plates is concave towards the outside, and the bottom contour lines of the special-shaped structural plates are matched with the concave contour lines of the conveying belts. The appearance structure of the utility model is similar to a colter for plowing.
When the piston rod of cylinder 44 descends, drive lifting support and stripper 45 together and descend, make stripper 45 descend to fortune material belt 48 upper surface, activated carbon particle 1 on (advancing) fortune material belt 48 this moment is blockked by stripper 45, activated carbon particle is piled up the lifting, and in being overturned the adsorption tower activated carbon storage bin 2 of fortune material belt both sides below along stripper 45 of concave curved surface form, the opening width in adsorption tower activated carbon storage bin 2 will be greater than the width of fortune material belt 48, avoid falling the adsorption tower activated carbon storage bin 2 outside.
Example 5:
example 1 was repeated with the following differences: the process system also comprises a scraper 11, and the scraper 11 is positioned below the ash hopper 20 and the waste discharge pipe 8. And (3) opening corresponding valves of the produced waste materials, uniformly draining the waste materials onto the scraper conveyor 11, conveying the waste materials out of the scraper conveyor 11, and finally conveying the waste materials out of the vehicle.
Example 6:
the operation method of the flue gas exchange type activated carbon desulfurization and denitrification integrated process system according to embodiment 1 is that, referring to fig. 2, the analytic functions of the left adsorption tower and the right adsorption tower are alternately matched to operate, and the operation flow of the whole process system is mainly described by the left adsorption tower:
1) the activated carbon hoister 37 transports the activated carbon particles 1 to a belt material transporting machine, the belt material transporting machine transports the activated carbon particles 1 to the activated carbon bins 2 of the left and right adsorption towers through the fixed-point discharger 36, and the activated carbon particles 1 are stored for later use;
2) the active carbon particles in the active carbon bin 2 of the adsorption tower are respectively conveyed to a honeycomb air guide plate 6 and a grid air guide plate 19 through a feeding flow dividing pipe 4; corresponding activated carbon particle layers are arranged in the desulfurization box body 9 and the denitration box body 5 of the adsorption towers at the left side and the right side;
3) the first dome valve 10, the second dome valve 22, the third dome valve 21, the fourth dome valve 3, the second butterfly valve 17, the fourth butterfly valve 26, and the fifth butterfly valve 27 are closed, and the first butterfly valve 16, the third butterfly valve 25, and the sixth butterfly valve 24 are opened.
Sintering flue gas is introduced into the ash hopper bin 20 of the left adsorption tower through a first branch pipe on an external pipeline B56, the sintering flue gas upwards passes through the grid gas guide plate 19 from the ash hopper bin 20 and passes through the activated carbon particle layer, and SO in the flue gas2The multi-component pollutants such as dust, heavy metals and the like are adsorbed by the activated carbon, the desulfurized flue gas enters the space below the honeycomb gas guide plate 6 in the denitration box body 5 through an external pipeline A15, and the flue gas is uniformly mixed with the ammonia-containing mixed gas heated in the annular ammonia sprayer before entering the denitration box body 5;
4) the flue gas passes through the honeycomb gas guide plate 6 from the lower space of the honeycomb gas guide plate 6 upwards and passes through the activated carbon particle layer, in the process that the flue gas passes through the activated carbon particle layer, nitrides in the flue gas and ammonia gas from the outside generate chemical reaction, and the denitrated clean flue gas is discharged into the atmosphere from a chimney 13;
5) when the content of pollutants in the flue gas discharged by the left adsorption tower is detected to be close to the standard exceeding by the online detection device, the flue gas adsorption function of the left adsorption tower is immediately stopped, the production mode of the analysis function is switched to, and meanwhile, the flue gas adsorption function of the right adsorption tower is combined with the flue gas adsorption function of the left adsorption tower;
when switching the production mode, the first dome valve 10, the second dome valve 22, the third dome valve 21, the fourth dome valve 3, the first butterfly valve 16, the third butterfly valve 25, the fourth butterfly valve 26, and the sixth butterfly valve 24 need to be closed, and the second butterfly valve 17 and the fifth butterfly valve 27 need to be opened.
6) Heating air (high-temperature nitrogen) with the temperature of 390-450 ℃ is introduced into an ash bucket bin 20 of the left adsorption tower through an external pipeline B56, the heating air upwards passes through a grid air guide plate 19 from the ash bucket bin 20 to enter an activated carbon particle layer, and fully contacts and is heated with the activated carbon particle layer in a desulfurization box body 9, and sulfide pollutants adsorbed by the activated carbon particle layer are resolved into a gas state and then are taken away by the high-temperature nitrogen, and then enter a wet scrubber 28 through an external pipeline C57;
7) wet scrubber 28 is used for scrubbing the gaseous stateSubjecting the material to a preliminary treatment to remove SO therefrom2The nitrogen gas is conveyed to a sodium metabisulfite system 30 to prepare a sodium metabisulfite product, N2 discharged from the sodium metabisulfite system 30 and N2 generated by a nitrogen making device 35 are supplemented into a nitrogen gas storage tank 31, and the nitrogen gas storage tank 31 conveys N2 to a nitrogen gas heating furnace 32 again to carry out high-temperature heating and then conveys the nitrogen gas to a desulfurization box body 9 again;
8) repeating the steps 5) to 7) until SO in the exhaust gas of the left adsorption tower desulfurization box body 92The content is detected to be qualified after reaching the standard;
9) after the analysis function production mode is completed, gas introduced into the ash hopper bin 20 of the left adsorption tower through the external pipeline B56 is switched from heating air (N2) to cooling air (N2), at the moment, the fifth butterfly valve 27 needs to be closed, the fourth butterfly valve 26 needs to be opened, low-temperature nitrogen carries out cooling treatment on a high-temperature activated carbon particle layer in the desulfurization box body 9, the low-temperature nitrogen carries away part of heat of the high-temperature activated carbon, enters the wet scrubber 28 through the external pipeline C57 to carry out cooling, then is conveyed into the nitrogen storage tank 31 through the sodium metabisulfite system 30, is used as cooling air again, enters the ash hopper bin 20 again through the external pipeline B56, carries out circulating cooling treatment on the high-temperature activated carbon particle layer, and circulates repeatedly until the temperature of the activated carbon particle layer in the desulfurization box body 9 reaches the standard and is qualified;
meanwhile, when the left adsorption tower carries out the steps 3) to 4), the right adsorption tower can synchronously carry out the operations of the steps 3) to 4) after finishing the operations of the steps 5) to 9); when the left adsorption tower performs the operations of the steps 5) to 9), the right adsorption tower performs the operations of the steps 3) to 4); when the right adsorption tower performs the operations of the steps 3) to 4), the left adsorption tower can perform the operations of the steps 3) to 4) synchronously after completing the operations of the steps 5) to 9); when the right adsorption tower performs the operations of steps 5) to 9), the left adsorption tower performs the operations of steps 3) to 4). The circulation is repeated, so that the alternate operation of flue gas adsorption and pollutant analysis of the left adsorption tower and the right adsorption tower is realized.
10) After the desulfurization and denitrification process is carried out for a certain time (several days or several months, determined according to process requirements), once the activity of the activated carbon is attenuated to a degree that the production requirements cannot be met, the first dome valve 10, the second dome valve 22 and the third dome valve 21 are opened, the ash hopper bin 20 and the waste discharge pipe 8 discharge activated carbon particles and dust onto the scraper conveyor 11, the activated carbon particles and the dust are uniformly conveyed away by the scraper conveyor 11, and then new activated carbon is reloaded into the desulfurization box body or the denitrification box body through the feeding system.
In the operation process of the left and right adsorption towers, the control of corresponding valves and conventional detection and control technologies can realize the mutual alternate operation of the left and right adsorption towers to realize the matching process of adsorption and analysis, thereby realizing that a single adsorption tower can have the double functions of simultaneously realizing adsorption and analysis, eliminating the process of independently setting up the analysis tower in the traditional process and omitting the process of carrying out desulfurization and analysis on activated carbon particles to the analysis tower for a long distance in the traditional method. Therefore, the technological process of the whole production system is simplified, the working efficiency is improved, the production energy consumption is reduced, and the failure rate of the mobile equipment is reduced.
Claims (10)
1. A flue gas exchange type activated carbon desulfurization and denitrification integrated process system is characterized by comprising two adsorption towers which are operated in a matching way;
the adsorption tower comprises a denitration box body, a desulfurization box body and an ash bucket bin which are sequentially arranged from top to bottom, wherein the denitration box body and the desulfurization box body are separately arranged up and down, and the desulfurization box body is communicated with the ash bucket bin up and down; a honeycomb gas guide plate is arranged in the denitration box body, and divides the space in the denitration box body into an upper part and a lower part; a grid air guide plate is arranged in the desulfurization box body;
the top of the adsorption tower is provided with a feeding flow dividing pipe, the feeding flow dividing pipe is respectively inserted into the denitration box body and the desulfurization box body, and activated carbon particles are respectively injected into the denitration box body and the desulfurization box body through the feeding flow dividing pipe;
the upper space of the grid air guide plate in the desulfurization box body is connected with the lower space of the honeycomb air guide plate in the denitrification box body through an external pipeline A;
the ash hopper bins of the two adsorption towers are respectively connected with an external pipeline B; the smoke outlets of the desulfurization box bodies of the two adsorption towers are respectively connected with an external pipeline C.
2. The integrated flue gas ac-type activated carbon desulfurization and denitrification process system according to claim 1, wherein the bottom of the honeycomb gas guide plate and the bottom of the grid gas guide plate are respectively communicated with a waste discharge pipe, and the two waste discharge pipes extend to the outside of the adsorption tower.
3. The integrated flue gas ac type activated carbon desulfurization and denitrification process system according to claim 1, wherein a stirrer is arranged in the desulfurization box body, and the stirrer is positioned above the grid gas guide plate.
4. The integrated process system for desulfurization and denitrification of flue gas by AC type activated carbon as claimed in claim 2, wherein the external pipe A is provided with a first butterfly valve and an annular ammonia sprayer, the annular ammonia sprayer is connected with an ammonia water gasification furnace through an external pipe D, and the ammonia water gasification furnace is connected with an ammonia heating furnace.
5. The integrated flue gas ac-type activated carbon desulfurization and denitrification process system according to claim 1, further comprising a wet scrubber, a sodium metabisulfite system, a nitrogen storage tank and a nitrogen heating furnace; the wet scrubber is connected with the external pipeline C, the wet scrubber is connected with the sodium metabisulfite system through a pipeline, the sodium metabisulfite system is connected with the nitrogen storage tank through a pipeline, the nitrogen storage tank is connected with the nitrogen heating furnace and the external pipeline B through a pipeline, and the nitrogen heating furnace is also connected with the external pipeline B.
6. The flue gas ac type activated carbon desulfurization and denitrification integrated process system according to claim 1, wherein the feeding shunt pipe is communicated with the bottom of the activated carbon bin of the adsorption tower.
7. The integrated flue gas ac-type activated carbon desulfurization and denitrification process system according to claim 6, further comprising a feeding system, wherein the feeding system comprises an activated carbon particle storage bin, an activated carbon elevator, a belt conveyor and a fixed-point discharger; the active carbon granule storage bin is located active carbon lifting machine bottom one side, and the belt material transporting machine is located active carbon lifting machine top one side, and the fixed point tripper is installed on the belt material transporting machine and is located the adsorption tower active carbon feed bin directly over.
8. The integrated flue gas alternating-current activated carbon desulfurization and denitrification process system as claimed in claim 4, wherein a first dome valve is installed on a waste discharge pipe communicated with the bottom of the honeycomb gas guide plate, a second dome valve is installed on a waste discharge pipe communicated with the bottom of the grid gas guide plate, a third dome valve is installed at the bottom end of the ash hopper, a fourth dome valve is installed at the top end of the feeding shunt pipe, a second butterfly valve is installed on the external pipeline C, and a sixth butterfly valve is installed on the external pipeline D.
9. The integrated flue gas ac type activated carbon desulfurization and denitrification process system as claimed in claim 5, wherein the external pipe B is provided with three communicating branch pipes, and a third butterfly valve is installed on the first branch pipe for introducing sintering flue gas; a fourth butterfly valve is arranged on the second branch pipe, is communicated with the nitrogen storage tank and is used for introducing cooling air; the third branch pipe is provided with a fifth butterfly valve and communicated with the nitrogen heating furnace for introducing hot air.
10. The operation method of the integrated flue gas ac type activated carbon desulfurization and denitrification process system according to any one of claims 1 to 9, wherein the adsorption and desorption processes of the two adsorption towers are alternately operated, or the adsorption and desorption processes are synchronously performed but the desorption processes are staggered, wherein the operation method comprises the following steps:
1) the activated carbon hoister conveys the activated carbon particles to a belt material conveyer, the belt material conveyer conveys the activated carbon particles, and the activated carbon particles on the belt material conveyer are pushed and turned to an activated carbon bin of an adsorption tower below the belt material conveyer through a fixed-point discharger to be accumulated;
2) respectively conveying the activated carbon particles in the activated carbon bin of the adsorption tower onto a honeycomb air guide plate or a grid air guide plate through a feeding flow dividing pipe;
3) introducing sintering flue gas into an ash hopper bin of one adsorption tower through an external pipeline B, wherein the sintering flue gas upwards passes through a grid gas guide plate from the ash hopper bin, passes through an activated carbon particle layer, and enters a lower space of a honeycomb gas guide plate in a denitration box body through an external pipeline A;
4) the desulfurized flue gas passes through the honeycomb gas guide plate from the lower space of the honeycomb gas guide plate upwards, passes through the activated carbon particle layer, and the purified flue gas after denitration is discharged into the atmosphere from a chimney;
5) when the content of pollutants in the flue gas discharged by the adsorption tower is detected to be close to the standard exceeding by the online detection device, the flue gas adsorption function of the adsorption tower is immediately stopped, the production mode of the analysis function is switched to, and meanwhile, the flue gas adsorption function of the adsorption tower is combined by the other adsorption tower;
6) when the adsorption tower is switched to an analytic function production mode, gas introduced into the ash hopper bin through the external pipeline B is switched into hot air from sintering flue gas, the hot air upwards passes through the grid gas guide plate from the ash hopper bin to enter the activated carbon particle layer, and fully contacts with the activated carbon particle layer under the stirring action of the stirrer to be heated, and the sulfide pollutants adsorbed by the activated carbon particle layer are analyzed to be changed into gaseous state and then are carried away by the hot air, and then enter the wet scrubber through the external pipeline C;
7) the wet scrubber primarily treats the desorbed gaseous substances to remove SO2Conveying to a sodium metabisulfite system to prepare a sodium metabisulfite product, and discharging N through the sodium metabisulfite system2With N produced by nitrogen plant2Supplementing into nitrogen storage tank, and conveying N again2After the nitrogen gas is heated in the nitrogen heating furnace at high temperature, the nitrogen gas is circularly conveyed into the desulfurization box body again;
8) repeating the steps 5) to 7) until SO in the exhaust gas of the desulfurization box body2The content is detected to be qualified after reaching the standard;
9) after the production mode of the analytic function of the adsorption tower is completed, gas introduced into the ash hopper bin through an external pipeline B is switched into cooling air by heating air, the cooling air cools a high-temperature activated carbon particle layer in the desulfurization box, partial heat of the high-temperature activated carbon is taken away by the cooling air, the gas enters a wet scrubber through an external pipeline C to be cooled, then the gas is conveyed into a nitrogen storage tank through a sodium metabisulfite system to be used as cooling air again, the gas enters the ash hopper bin through the external pipeline B again to perform circulating cooling treatment on the high-temperature activated carbon particle layer, and the gas is circulated repeatedly until the temperature of the activated carbon particle layer in the desulfurization box is detected to be qualified after reaching the standard;
meanwhile, when the adsorption tower carries out the steps 3) to 4), the other adsorption tower can synchronously carry out the operations of the steps 3) to 4) after finishing the operations of the steps 5) to 9); when the adsorption tower performs the operations of the steps 5) to 9), the other adsorption tower performs the operations of the steps 3) to 4); when the other adsorption tower performs the operation of the steps 3) to 4), the adsorption tower can perform the operation of the steps 3) to 4) synchronously after completing the operation of the steps 5) to 9); when the other adsorption tower performs the operations of the steps 5) to 9), the other adsorption tower performs the operations of the steps 3) to 4); the circulation is repeated, so that the alternate operation of flue gas adsorption and pollutant analysis between the two adsorption towers is realized.
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