CN115582016B - Ultralow-temperature desulfurization and denitrification process special for lime kiln - Google Patents
Ultralow-temperature desulfurization and denitrification process special for lime kiln Download PDFInfo
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- CN115582016B CN115582016B CN202211390883.2A CN202211390883A CN115582016B CN 115582016 B CN115582016 B CN 115582016B CN 202211390883 A CN202211390883 A CN 202211390883A CN 115582016 B CN115582016 B CN 115582016B
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- 235000008733 Citrus aurantifolia Nutrition 0.000 title claims description 67
- 235000011941 Tilia x europaea Nutrition 0.000 title claims description 67
- 239000004571 lime Substances 0.000 title claims description 67
- 238000006477 desulfuration reaction Methods 0.000 title claims description 40
- 230000023556 desulfurization Effects 0.000 title claims description 40
- 238000000034 method Methods 0.000 title claims description 23
- 230000008569 process Effects 0.000 title claims description 22
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims description 63
- 239000003546 flue gas Substances 0.000 claims description 63
- MWUXSHHQAYIFBG-UHFFFAOYSA-N nitrogen oxide Inorganic materials O=[N] MWUXSHHQAYIFBG-UHFFFAOYSA-N 0.000 claims description 51
- RAHZWNYVWXNFOC-UHFFFAOYSA-N Sulphur dioxide Chemical compound O=S=O RAHZWNYVWXNFOC-UHFFFAOYSA-N 0.000 claims description 36
- 239000003054 catalyst Substances 0.000 claims description 31
- 239000003795 chemical substances by application Substances 0.000 claims description 28
- 230000003009 desulfurizing effect Effects 0.000 claims description 28
- UIIMBOGNXHQVGW-UHFFFAOYSA-M Sodium bicarbonate Chemical compound [Na+].OC([O-])=O UIIMBOGNXHQVGW-UHFFFAOYSA-M 0.000 claims description 24
- 238000000498 ball milling Methods 0.000 claims description 24
- OSGAYBCDTDRGGQ-UHFFFAOYSA-L calcium sulfate Chemical compound [Ca+2].[O-]S([O-])(=O)=O OSGAYBCDTDRGGQ-UHFFFAOYSA-L 0.000 claims description 24
- 239000000428 dust Substances 0.000 claims description 23
- CPLXHLVBOLITMK-UHFFFAOYSA-N magnesium oxide Inorganic materials [Mg]=O CPLXHLVBOLITMK-UHFFFAOYSA-N 0.000 claims description 18
- 239000011159 matrix material Substances 0.000 claims description 18
- 239000000178 monomer Substances 0.000 claims description 18
- 239000002245 particle Substances 0.000 claims description 15
- 230000004048 modification Effects 0.000 claims description 14
- 238000012986 modification Methods 0.000 claims description 14
- 239000000463 material Substances 0.000 claims description 13
- 229910021536 Zeolite Inorganic materials 0.000 claims description 12
- 229910000281 calcium bentonite Inorganic materials 0.000 claims description 12
- FNAQSUUGMSOBHW-UHFFFAOYSA-H calcium citrate Chemical compound [Ca+2].[Ca+2].[Ca+2].[O-]C(=O)CC(O)(CC([O-])=O)C([O-])=O.[O-]C(=O)CC(O)(CC([O-])=O)C([O-])=O FNAQSUUGMSOBHW-UHFFFAOYSA-H 0.000 claims description 12
- 239000001354 calcium citrate Substances 0.000 claims description 12
- 229960004494 calcium gluconate Drugs 0.000 claims description 12
- 239000004227 calcium gluconate Substances 0.000 claims description 12
- 235000013927 calcium gluconate Nutrition 0.000 claims description 12
- NEEHYRZPVYRGPP-UHFFFAOYSA-L calcium;2,3,4,5,6-pentahydroxyhexanoate Chemical compound [Ca+2].OCC(O)C(O)C(O)C(O)C([O-])=O.OCC(O)C(O)C(O)C(O)C([O-])=O NEEHYRZPVYRGPP-UHFFFAOYSA-L 0.000 claims description 12
- HNPSIPDUKPIQMN-UHFFFAOYSA-N dioxosilane;oxo(oxoalumanyloxy)alumane Chemical compound O=[Si]=O.O=[Al]O[Al]=O HNPSIPDUKPIQMN-UHFFFAOYSA-N 0.000 claims description 12
- YDEXUEFDPVHGHE-GGMCWBHBSA-L disodium;(2r)-3-(2-hydroxy-3-methoxyphenyl)-2-[2-methoxy-4-(3-sulfonatopropyl)phenoxy]propane-1-sulfonate Chemical compound [Na+].[Na+].COC1=CC=CC(C[C@H](CS([O-])(=O)=O)OC=2C(=CC(CCCS([O-])(=O)=O)=CC=2)OC)=C1O YDEXUEFDPVHGHE-GGMCWBHBSA-L 0.000 claims description 12
- WPEXVRDUEAJUGY-UHFFFAOYSA-B hexacalcium;(2,3,4,5,6-pentaphosphonatooxycyclohexyl) phosphate Chemical compound [Ca+2].[Ca+2].[Ca+2].[Ca+2].[Ca+2].[Ca+2].[O-]P([O-])(=O)OC1C(OP([O-])([O-])=O)C(OP([O-])([O-])=O)C(OP([O-])([O-])=O)C(OP([O-])([O-])=O)C1OP([O-])([O-])=O WPEXVRDUEAJUGY-UHFFFAOYSA-B 0.000 claims description 12
- 239000007788 liquid Substances 0.000 claims description 12
- 239000000395 magnesium oxide Substances 0.000 claims description 12
- 239000011812 mixed powder Substances 0.000 claims description 12
- 238000002156 mixing Methods 0.000 claims description 12
- 239000000843 powder Substances 0.000 claims description 12
- 238000002791 soaking Methods 0.000 claims description 12
- 235000017557 sodium bicarbonate Nutrition 0.000 claims description 12
- 229910000030 sodium bicarbonate Inorganic materials 0.000 claims description 12
- 235000013337 tricalcium citrate Nutrition 0.000 claims description 12
- 239000010457 zeolite Substances 0.000 claims description 12
- 238000010438 heat treatment Methods 0.000 claims description 8
- 238000005507 spraying Methods 0.000 claims description 7
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Chemical compound O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 7
- 235000021355 Stearic acid Nutrition 0.000 claims description 6
- 229960004256 calcium citrate Drugs 0.000 claims description 6
- 235000011132 calcium sulphate Nutrition 0.000 claims description 6
- 239000008367 deionised water Substances 0.000 claims description 6
- 229910021641 deionized water Inorganic materials 0.000 claims description 6
- GVGUFUZHNYFZLC-UHFFFAOYSA-N dodecyl benzenesulfonate;sodium Chemical compound [Na].CCCCCCCCCCCCOS(=O)(=O)C1=CC=CC=C1 GVGUFUZHNYFZLC-UHFFFAOYSA-N 0.000 claims description 6
- 238000001035 drying Methods 0.000 claims description 6
- 238000001914 filtration Methods 0.000 claims description 6
- 238000007710 freezing Methods 0.000 claims description 6
- 230000008014 freezing Effects 0.000 claims description 6
- AXZKOIWUVFPNLO-UHFFFAOYSA-N magnesium;oxygen(2-) Chemical compound [O-2].[Mg+2] AXZKOIWUVFPNLO-UHFFFAOYSA-N 0.000 claims description 6
- QIQXTHQIDYTFRH-UHFFFAOYSA-N octadecanoic acid Chemical compound CCCCCCCCCCCCCCCCCC(O)=O QIQXTHQIDYTFRH-UHFFFAOYSA-N 0.000 claims description 6
- OQCDKBAXFALNLD-UHFFFAOYSA-N octadecanoic acid Natural products CCCCCCCC(C)CCCCCCCCC(O)=O OQCDKBAXFALNLD-UHFFFAOYSA-N 0.000 claims description 6
- 229920002401 polyacrylamide Polymers 0.000 claims description 6
- 238000002360 preparation method Methods 0.000 claims description 6
- 229940080264 sodium dodecylbenzenesulfonate Drugs 0.000 claims description 6
- 239000008117 stearic acid Substances 0.000 claims description 6
- 239000011800 void material Substances 0.000 claims description 6
- 238000001354 calcination Methods 0.000 description 10
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 8
- 230000002378 acidificating effect Effects 0.000 description 6
- 239000011148 porous material Substances 0.000 description 6
- 239000003245 coal Substances 0.000 description 5
- 150000001875 compounds Chemical class 0.000 description 5
- 238000005516 engineering process Methods 0.000 description 5
- 230000007613 environmental effect Effects 0.000 description 5
- 230000000737 periodic effect Effects 0.000 description 5
- 239000004575 stone Substances 0.000 description 5
- 239000000126 substance Substances 0.000 description 4
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 3
- 229910021529 ammonia Inorganic materials 0.000 description 3
- 239000003638 chemical reducing agent Substances 0.000 description 3
- 238000005265 energy consumption Methods 0.000 description 3
- 239000011593 sulfur Substances 0.000 description 3
- 229910052717 sulfur Inorganic materials 0.000 description 3
- 239000002253 acid Substances 0.000 description 2
- BIGPRXCJEDHCLP-UHFFFAOYSA-N ammonium bisulfate Chemical compound [NH4+].OS([O-])(=O)=O BIGPRXCJEDHCLP-UHFFFAOYSA-N 0.000 description 2
- 238000006243 chemical reaction Methods 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 239000007789 gas Substances 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- 239000007921 spray Substances 0.000 description 2
- VHUUQVKOLVNVRT-UHFFFAOYSA-N Ammonium hydroxide Chemical compound [NH4+].[OH-] VHUUQVKOLVNVRT-UHFFFAOYSA-N 0.000 description 1
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 1
- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 description 1
- 229910004742 Na2 O Inorganic materials 0.000 description 1
- 230000009471 action Effects 0.000 description 1
- 230000004913 activation Effects 0.000 description 1
- 229910052784 alkaline earth metal Inorganic materials 0.000 description 1
- 150000001342 alkaline earth metals Chemical class 0.000 description 1
- 235000011114 ammonium hydroxide Nutrition 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 229960005069 calcium Drugs 0.000 description 1
- 229910052791 calcium Inorganic materials 0.000 description 1
- 239000011575 calcium Substances 0.000 description 1
- 238000004364 calculation method Methods 0.000 description 1
- 238000010276 construction Methods 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 239000003344 environmental pollutant Substances 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 238000007254 oxidation reaction Methods 0.000 description 1
- 239000002574 poison Substances 0.000 description 1
- 231100000614 poison Toxicity 0.000 description 1
- 231100000719 pollutant Toxicity 0.000 description 1
- 230000008929 regeneration Effects 0.000 description 1
- 238000011069 regeneration method Methods 0.000 description 1
- 238000003860 storage Methods 0.000 description 1
Classifications
-
- 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
-
- 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
-
- 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
- B01D53/82—Solid phase processes with stationary reactants
-
- 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
-
- 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
Landscapes
- Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- Environmental & Geological Engineering (AREA)
- Health & Medical Sciences (AREA)
- Biomedical Technology (AREA)
- Analytical Chemistry (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Treating Waste Gases (AREA)
Abstract
The invention discloses a special ultralow-temperature desulfurization and denitrification process for a lime kiln, which belongs to the technical field of desulfurization and denitrification, and comprises low-temperature SCR denitration and SDS dry desulfurization; the low-temperature SCR denitration, namely, lime kiln flue gas enters an SCR reactor for denitration after passing through a blower, a calcining zone of the SCR reactor is moved to 27-27.5 m, the coal ratio is controlled to be 7.5-7.8%, and the calcining temperature is controlled to be 180-185 ℃; the SDS dry desulfurization is carried out, the flue gas of the lime kiln after denitration is heated to 125-135 ℃, and then the flue gas is introduced into a dust remover, the temperature of the dust remover is controlled to be 110-270 ℃, and a desulfurizing agent is sprayed into a flue before the dust remover; the invention has stable process performance, low energy consumption, small occupied area, convenient implementation, and can carry out desulfurization at the temperature lower than 140 ℃ and higher than 250 ℃, and can improve the desulfurization efficiency when the sulfur content exceeds 1000mg/Nm 3.
Description
Technical Field
The invention relates to the technical field of desulfurization and denitrification, in particular to a special ultralow-temperature desulfurization and denitrification process for a lime kiln.
Background
Lime kiln, which is a process form of main equipment for producing lime, occupies a large proportion in the production of lime in China, and with the continuous increase of the atmospheric treatment force in China, the large-area coverage of flue gas treatment in the electric power industry is gradually becoming the important field of flue gas treatment in the non-electric industry.
The flue gas temperature of the lime kiln is generally 180-240 ℃, and the lime kiln industrial tail gas dust contains a large amount of calcium and alkaline earth metals (CaO and K 2O、Na2 O), has small dust particle size, high viscosity, low tail gas denitration temperature and other special conditions, so that the treatment difficulty of nitrogen oxides and sulfur dioxide is high, and the most commonly used treatment method is the combination of an SCR denitration process and SDS dry desulfurization at present.
The principle of the SCR denitration technology is that under the action of a catalyst, a reducing agent NH 3 selectively reduces NO and NO 2 into N 2 at 290-400 ℃, and almost NO oxidation reaction of NH 3 and O 2 occurs, so that the selectivity of N 2 is improved, and the consumption of NH 3 is reduced. That is, in a reactor containing a catalyst, ammonia is used as a reducing agent to remove nitrogen oxides, and NOx in the flue gas generally consists of about 95% NO and 5% NO 2% by volume, and NOx is converted into molecular nitrogen and water vapor through a denitration reaction.
However, the SCR denitration process has some obvious disadvantages: the activation temperature is 220-400 ℃, and secondary heating is generally required; the flue gas tends to have complex components, and certain pollutants can poison the denitration catalyst; the dust particles with high dispersity can cover the surface of the catalyst, so that the activity of the catalyst is reduced; the SCR denitration system has the functions of unreacted NH 3 and SO 2 in the flue gas to generate ammonia sulfate (NH 4)2SO4 and ammonia bisulfate NH 4HSO4 which are easy to corrode and block denitration equipment, and meanwhile the ammonia utilization rate is reduced), the traditional SCR denitration equipment has higher investment and operation cost, liquid ammonia serving as an SCR reducing agent belongs to dangerous chemicals, has certain potential safety hazards in storage and use, the SCR denitration system uses liquid ammonia or ammonia water as a denitration agent, the problem of ammonia escape is difficult to solve to form secondary pollution, the SCR denitration equipment must adopt an expensive catalyst, and the denitration catalyst must be returned to a factory for regeneration or scrapped after a certain time limit is used.
In addition, the traditional SCR denitration technology adopts a medium-low temperature SCR denitration technology added at the tail part of a bag-type dust collector, the original flue gas temperature is required to be raised from 50-80 ℃ to 220 ℃ for denitration treatment, the flue gas is required to be heated, the energy consumption is huge, the operation cost is extremely high, the heating cost of a single kiln is required to be 800-1200 ten thousand according to 7.5 ten thousand air quantity calculation, and most of established lime production enterprises only consider flue gas desulfurization and dust removal in the construction period, and the flue gas denitration problem is not considered, so that enough denitration sites cannot be reserved on site.
The SDS dry desulfurization spraying technology is to uniformly spray a high-efficiency desulfurizing agent (particle size is 20-25 mu m) into a pipeline, the desulfurizing agent is thermally activated in the pipeline, the specific surface area is rapidly increased, the desulfurizing agent is fully contacted with acid flue gas in a large area in a limited space of the pipeline, physical and chemical reactions occur, and acid substances such as sulfur dioxide in the flue gas are absorbed and purified. The desulfurizing agent has high removal rate for acidic substances, and has high removal rate for acidic substances such as HCl, SO3, HF and the like; however, the desulfurizing agent in the existing SDS dry desulfurization spray technology has high requirements on the flue gas temperature range, and has to be more than 140 ℃ and less than 250 ℃, and when the sulfur content exceeds 1000mg/Nm 3, the desulfurizing effect is poor.
Disclosure of Invention
Aiming at the defects of the prior art, the invention provides the ultralow-temperature desulfurization and denitration process special for the lime kiln, which has stable process performance, low energy consumption, small occupied area and convenient implementation, can perform desulfurization at the temperature lower than 140 ℃ and higher than 250 ℃, and can improve the desulfurization efficiency when the sulfur content exceeds 1000mg/Nm 3.
In order to solve the technical problems, the technical scheme adopted by the invention is as follows:
An ultralow-temperature desulfurization and denitrification process special for a lime kiln comprises low-temperature SCR denitration and SDS dry desulfurization;
the low-temperature SCR denitration, namely, lime kiln flue gas enters an SCR reactor for denitration after passing through a blower, a calcining zone of the SCR reactor is moved to 27-27.5 m, the coal ratio is controlled to be 7.5-7.8%, and the calcining temperature is controlled to be 180-185 ℃; adopting periodic continuous feeding, carrying out stone material feeding for 3 times in one hour, and carrying out six times, wherein each time is 1.6-1.8 tons, and the low-temperature SCR denitration is finished to obtain lime kiln flue gas after denitration;
the rotating speed of the blower is 32-35Hz, and the air quantity is 20000-22000m 3/h;
The temperature of the lime kiln flue gas is maintained at 160-170 ℃, the content of particles is 5-5.6g/m 3, the content of sulfur dioxide is 200-1100mg/m 3, the content of nitrogen oxides is 200-350mg/m 3, and the flow is 75000-75500Nm 3/h;
the catalyst in the SCR reactor is of the type of honeycomb WDSCR-22, the manufacturer is Shanghai compound wing environmental protection technology Co., ltd, the initial catalyst volume is 14.9-15.5m 3, the catalyst pore number is 22-25 pores, the catalyst monomer length is 150-155mm, the monomer width is 150-155mm, the monomer height is 1150-1180mm, the specific surface area is 527-530m 2/m3, the volume density is 450-455mg/cm 3, and the void ratio is 74.88-74.95%.
Heating the flue gas of the lime kiln after denitration to 125-135 ℃, then introducing the flue gas into a dust remover, controlling the temperature of the dust remover to be 110-270 ℃, spraying a desulfurizing agent on a flue before the dust remover, and obtaining the flue gas of the lime kiln after desulfurization;
The preparation method of the desulfurizing agent comprises the following steps: mixing calcium bentonite, magnesium oxide and zeolite powder, performing first ball milling, controlling the ball-material ratio at 10-12:1, the rotation speed at 320-350rpm, the time at 28-32min, obtaining mixed powder after ball milling, adding the mixed powder into surface modification liquid, soaking, controlling the temperature at 50-55 ℃ for 40-45min, filtering after soaking, freezing filter residues at-30 ℃ to-25 ℃ for 35-40min, drying at 120-125 ℃ to obtain a matrix, mixing the matrix, calcium gluconate, calcium citrate, calcium phytate, calcium sulfate, sodium bicarbonate and sodium lignin sulfonate, performing second ball milling, controlling the ball-material ratio at 12-15:1, the rotation speed at 300-320rpm, and the time at 38-42min, and obtaining the desulfurizing agent after the second ball milling;
The surface modification liquid comprises the following components in parts by weight: 4-6 parts of sodium dodecyl benzene sulfonate, 3-4 parts of zwitterionic polyacrylamide, 5-8 parts of stearic acid and 50-52 parts of deionized water.
Wherein the weight ratio of the calcium bentonite to the magnesia to the zeolite powder is 50-52:3-5:6-9;
Wherein, the weight ratio of the matrix to the calcium gluconate to the calcium citrate to the calcium phytate to the calcium sulfate to the sodium bicarbonate to the sodium lignin sulfonate is 50-55:7-10:12-16:10-13:5-8:9-12:3-6.
Compared with the prior art, the invention has the beneficial effects that:
(1) The ultralow-temperature desulfurization and denitrification process special for the lime kiln has stable process performance, low energy consumption, small occupied area and convenient implementation;
(2) The special ultralow-temperature desulfurization and denitrification process for the lime kiln can carry out desulfurization at the temperature lower than 140 ℃ and higher than 250 ℃, and can expand the desulfurization temperature range to 110-270 ℃;
(3) The special ultralow-temperature desulfurization and denitrification process for the lime kiln can improve the desulfurization efficiency when the sulfur content exceeds 1000mg/Nm 3 and remove the lime kiln flue gas with the initial sulfur dioxide content of 200-1100mg/m 3;
(4) According to the ultralow-temperature desulfurization and denitrification process special for the lime kiln, the content of particles in the flue gas of the lime kiln after denitrification and desulfurization is 5.2-6.9mg/m 3, the content of sulfur dioxide is 11.5-30.4mg/m 3, and the content of nitrogen oxides is 6.7-7.5mg/m 3.
Detailed Description
Specific embodiments of the present invention will now be described in order to provide a clearer understanding of the technical features, objects and effects of the present invention.
Example 1
An ultralow temperature desulfurization and denitrification process special for a lime kiln specifically comprises the following steps:
1. Low temperature SCR denitration: the flue gas of the lime kiln enters an SCR reactor to be denitrated after passing through a blower, the rotating speed of the blower is controlled to be 32Hz, the air quantity is controlled to be 20000m 3/h, the calcining zone of the SCR reactor is moved to 27 m, the coal ratio is controlled to be 7.5%, and the calcining temperature is controlled to be 180 ℃; and (3) carrying out periodic continuous feeding, namely carrying out stone feeding for 3 times in one hour, wherein six vehicles are used each time, each vehicle is 1.6 tons, and the low-temperature SCR denitration is finished, so that the lime kiln flue gas after denitration is obtained.
The temperature of the lime kiln flue gas is maintained at 160 ℃, the content of particles is 5g/m 3, the content of sulfur dioxide is 200mg/m 3, the content of nitrogen oxides is 200mg/m 3, and the flow is 75000Nm 3/h;
The catalyst in the SCR reactor is of the type of honeycomb WDSCR-22, the manufacturer is Shanghai compound wing environmental protection technology Co., ltd, the initial catalyst volume is 14.9m 3, the catalyst pore number is 22 pores, the catalyst monomer length is 150mm, the monomer width is 150mm, the monomer height is 1150mm, the specific surface area is 527m 2/m3, the volume density is 450mg/cm 3, and the void ratio is 74.88%.
The content of particles in the flue gas of the lime kiln after denitration is 10mg/m 3, the content of sulfur dioxide is 190mg/m 3, and the content of nitrogen oxides is 10mg/m 3.
SDS dry desulfurization: heating the denitrated lime kiln flue gas to 125 ℃, then introducing the flue gas into a dust remover, controlling the temperature of the dust remover to be 110 ℃, spraying a desulfurizing agent on a front flue of the dust remover, and absorbing and purifying SO 2 and other acidic media in the lime kiln flue gas by the desulfurizing agent to obtain desulfurized lime kiln flue gas;
The preparation method of the desulfurizing agent comprises the following steps: mixing calcium bentonite, magnesium oxide and zeolite powder, performing first ball milling, controlling the ball-material ratio at 10:1, the rotation speed at 320rpm and the time at 28min, obtaining mixed powder after ball milling, adding the mixed powder into surface modification liquid, soaking, controlling the temperature at 50 ℃ and the time at 40min, filtering after soaking, freezing filter residues at-30 ℃ for 35min, drying at 120 ℃ to obtain a matrix, mixing the matrix, calcium gluconate, calcium citrate, calcium phytate, calcium sulfate, sodium bicarbonate and sodium lignin sulfonate, performing second ball milling, controlling the ball-material ratio at 12:1, the rotation speed at 300rpm and the time at 38min, and obtaining a desulfurizing agent after the second ball milling;
The surface modification liquid comprises the following components in parts by weight: 4 parts of sodium dodecyl benzene sulfonate, 3 parts of zwitterionic polyacrylamide, 5 parts of stearic acid and 50 parts of deionized water.
Wherein the weight ratio of the calcium bentonite to the magnesia to the zeolite powder is 50:3:6;
Wherein, the weight ratio of the matrix to the calcium gluconate to the calcium citrate to the calcium phytate to the calcium sulfate to the sodium bicarbonate to the sodium lignin sulfonate is 50:7:12:10:5:9:3.
The content of particles in the flue gas of the lime kiln after desulfurization is 6mg/m 3, the content of sulfur dioxide is 12mg/m 3, and the content of nitrogen oxides is 7mg/m 3.
Example 2
An ultralow temperature desulfurization and denitrification process special for a lime kiln specifically comprises the following steps:
1. Low temperature SCR denitration: the flue gas of the lime kiln enters an SCR reactor for denitration after passing through a blower, the rotating speed of the blower is controlled to be 33Hz, the air quantity is controlled to be 21000m 3/h, the calcining zone of the SCR reactor is moved to 27.1 m, the coal ratio is controlled to be 7.6%, and the calcining temperature is controlled to be 182 ℃; and (3) carrying out periodic continuous feeding, namely carrying out stone feeding for 3 times in one hour, wherein six vehicles are used each time, each vehicle is 1.6 tons, and the low-temperature SCR denitration is finished, so that the lime kiln flue gas after denitration is obtained.
The temperature of the lime kiln flue gas is maintained at 163 ℃, the content of particulate matters is 5.2g/m 3, the content of sulfur dioxide is 650mg/m 3, the content of nitrogen oxides is 240mg/m 3, and the flow is 75100Nm 3/h;
The catalyst in the SCR reactor is of the type of honeycomb WDSCR-22, the manufacturer is Shanghai compound wing environmental protection technology Co., ltd, the initial catalyst volume is 15.1m 3, the catalyst hole number is 22 holes, the catalyst monomer length is 152mm, the monomer width is 151mm, the monomer height is 1160mm, the specific surface area is 528m 2/m3, the volume density is 451mg/cm 3, and the void ratio is 74.92%.
The content of particles in the flue gas of the lime kiln after denitration is 11mg/m 3, the content of sulfur dioxide is 634mg/m 3, and the content of nitrogen oxides is 11mg/m 3.
SDS dry desulfurization: heating the denitrated lime kiln flue gas to 128 ℃, then introducing the flue gas into a dust remover, controlling the temperature of the dust remover to 130 ℃, spraying a desulfurizing agent on a front flue of the dust remover, and absorbing and purifying SO 2 and other acidic media in the lime kiln flue gas by the desulfurizing agent to obtain desulfurized lime kiln flue gas;
The preparation method of the desulfurizing agent comprises the following steps: mixing calcium bentonite, magnesium oxide and zeolite powder, performing first ball milling, controlling the ball-material ratio at 11:1, the rotation speed at 330rpm and the time at 29min, obtaining mixed powder after ball milling, adding the mixed powder into surface modification liquid, soaking, controlling the temperature at 51 ℃ for 41min, filtering after soaking, freezing filter residues at-30 ℃ for 36min, drying at 122 ℃ to obtain a matrix, mixing the matrix, calcium gluconate, calcium citrate, calcium phytate, calcium sulfate, sodium bicarbonate and sodium lignin sulfonate, performing second ball milling, controlling the ball-material ratio at 13:1, the rotation speed at 310rpm and the time at 39min, and obtaining a desulfurizing agent after the second ball milling;
The surface modification liquid comprises the following components in parts by weight: 5 parts of sodium dodecyl benzene sulfonate, 3.2 parts of zwitterionic polyacrylamide, 6 parts of stearic acid and 51 parts of deionized water.
Wherein the weight ratio of the calcium bentonite to the magnesia to the zeolite powder is 51:4:7;
Wherein, the weight ratio of the matrix to the calcium gluconate to the calcium citrate to the calcium phytate to the calcium sulfate to the sodium bicarbonate to the sodium lignin sulfonate is 51:7.5:13:11:6:9.5:3.5.
The content of particles in the flue gas of the lime kiln after desulfurization is 6.2mg/m 3, the content of sulfur dioxide is 25.5mg/m 3, and the content of nitrogen oxides is 7.2mg/m 3.
Example 3
An ultralow temperature desulfurization and denitrification process special for a lime kiln specifically comprises the following steps:
1. Low temperature SCR denitration: the flue gas of the lime kiln enters an SCR reactor to be denitrated after passing through a blower, the rotating speed of the blower is controlled to be 34Hz, the air quantity is controlled to be 21500m 3/h, the calcining zone of the SCR reactor is moved to 27.2 m, the coal ratio is controlled to be 7.7%, and the calcining temperature is controlled to be 184 ℃; and (3) carrying out periodic continuous feeding, namely carrying out stone feeding for 3 times in one hour, wherein six vehicles are used each time, each vehicle is 1.7 tons, and the low-temperature SCR denitration is finished, so that the lime kiln flue gas after denitration is obtained.
The temperature of the lime kiln flue gas is maintained at 165 ℃, the content of particulate matters is 5.3g/m 3, the content of sulfur dioxide is 900mg/m 3, the content of nitrogen oxides is 280mg/m 3, and the flow is 75200Nm 3/h;
The catalyst in the SCR reactor is of the type of honeycomb WDSCR-22, the manufacturer is Shanghai compound wing environmental protection technology Co., ltd, the initial catalyst volume is 15.3m 3, the catalyst pore number is 24 pores, the catalyst monomer length is 153mm, the monomer width is 152mm, the monomer height is 1170mm, the specific surface area is 529m 2/m3, the volume density is 452mg/cm 3, and the void ratio is 74.93%.
The content of particles in the flue gas of the lime kiln after denitration is 13mg/m 3, the content of sulfur dioxide is 875mg/m 3, and the content of nitrogen oxides is 12mg/m 3.
SDS dry desulfurization: heating the denitrated lime kiln flue gas to 130 ℃, then introducing the flue gas into a dust remover, controlling the temperature of the dust remover to be 200 ℃, spraying a desulfurizing agent on a front flue of the dust remover, and absorbing and purifying SO 2 and other acidic media in the lime kiln flue gas by the desulfurizing agent to obtain desulfurized lime kiln flue gas;
The preparation method of the desulfurizing agent comprises the following steps: mixing calcium bentonite, magnesium oxide and zeolite powder, performing first ball milling, controlling the ball-material ratio at 11:1, the rotating speed at 340rpm, and the time at 30min, obtaining mixed powder after ball milling, adding the mixed powder into surface modification liquid, soaking, controlling the temperature at 53 ℃ for 43min, filtering after soaking, freezing filter residues at-28 ℃ for 37min, drying at 124 ℃ to obtain a matrix, mixing the matrix, calcium gluconate, calcium citrate, calcium phytate, calcium sulfate, sodium bicarbonate and sodium lignin sulfonate, performing second ball milling, controlling the ball-material ratio at 14:1, the rotating speed at 315rpm, and the time at 40min, and obtaining the desulfurizing agent after the second ball milling;
the surface modification liquid comprises the following components in parts by weight: 5.5 parts of sodium dodecyl benzene sulfonate, 3.5 parts of zwitterionic polyacrylamide, 7 parts of stearic acid and 51.5 parts of deionized water.
Wherein the weight ratio of the calcium bentonite to the magnesia to the zeolite powder is 51.5:4.5:8;
Wherein, the weight ratio of the matrix to the calcium gluconate to the calcium citrate to the calcium phytate to the calcium sulfate to the sodium bicarbonate to the sodium lignin sulfonate is 53:9:15:12:7:11:5.
The content of particles in the flue gas of the lime kiln after desulfurization is 5.2mg/m 3, the content of sulfur dioxide is 27.5mg/m 3, and the content of nitrogen oxides is 6.7mg/m 3.
Example 4
An ultralow temperature desulfurization and denitrification process special for a lime kiln specifically comprises the following steps:
1. Low temperature SCR denitration: the flue gas of the lime kiln enters an SCR reactor for denitration after passing through a blower, the rotating speed of the blower is controlled to be 35Hz, the air quantity is controlled to be 22000m 3/h, the calcining zone of the SCR reactor is moved to be 27.5 m, the coal ratio is controlled to be 7.8%, and the calcining temperature is controlled to be 185 ℃; and (3) carrying out periodic continuous feeding, namely carrying out stone feeding for 3 times in one hour, wherein six vehicles are used each time, each vehicle is 1.8 tons, and the low-temperature SCR denitration is finished, so that the lime kiln flue gas after denitration is obtained.
The temperature of the lime kiln flue gas is maintained at 170 ℃, the content of particulate matters is 5.6g/m 3, the content of sulfur dioxide is 1100mg/m 3, the content of nitrogen oxides is 350mg/m 3, and the flow is 75500Nm 3/h;
The catalyst in the SCR reactor is of the type of honeycomb WDSCR-22, the manufacturer is Shanghai compound wing environmental protection technology Co., ltd, the initial catalyst volume is 15.5m 3, the catalyst hole number is 25 holes, the catalyst monomer length is 155mm, the monomer width is 155mm, the monomer height is 1180mm, the specific surface area is 530m 2/m3, the volume density is 455mg/cm 3, and the void ratio is 74.95%.
The content of particles in the flue gas of the lime kiln after denitration is 15mg/m 3, the content of sulfur dioxide is 1054mg/m 3, and the content of nitrogen oxides is 14mg/m 3.
SDS dry desulfurization: heating the denitrated lime kiln flue gas to 135 ℃, then introducing the flue gas into a dust remover, controlling the temperature of the dust remover to 270 ℃, spraying a desulfurizing agent on a front flue of the dust remover, and absorbing and purifying SO 2 and other acidic media in the lime kiln flue gas by the desulfurizing agent to obtain desulfurized lime kiln flue gas;
The preparation method of the desulfurizing agent comprises the following steps: mixing calcium bentonite, magnesium oxide and zeolite powder, performing first ball milling, controlling the ball-material ratio at 12:1, the rotation speed at 350rpm and the time at 32min, obtaining mixed powder after ball milling, adding the mixed powder into surface modification liquid, soaking, controlling the temperature at 55 ℃ and the time at 45min, filtering after soaking, freezing filter residues at-25 ℃ for 40min, drying at 125 ℃ to obtain a matrix, mixing the matrix, calcium gluconate, calcium citrate, calcium phytate, calcium sulfate, sodium bicarbonate and sodium lignin sulfonate, performing second ball milling, controlling the ball-material ratio at 15:1, the rotation speed at 320rpm and the time at 42min, and obtaining a desulfurizing agent after the second ball milling;
The surface modification liquid comprises the following components in parts by weight: 6 parts of sodium dodecyl benzene sulfonate, 4 parts of zwitterionic polyacrylamide, 8 parts of stearic acid and 52 parts of deionized water.
Wherein the weight ratio of the calcium bentonite to the magnesia to the zeolite powder is 52:5:9;
Wherein, the weight ratio of the matrix to the calcium gluconate to the calcium citrate to the calcium phytate to the calcium sulfate to the sodium bicarbonate to the sodium lignin sulfonate is 55:10:16:13:8:12:6.
The content of particles in the flue gas of the lime kiln after desulfurization is 6.9mg/m 3, the content of sulfur dioxide is 30.4mg/m 3, and the content of nitrogen oxides is 7.5mg/m 3.
The percentages used in the present invention are mass percentages unless otherwise indicated.
Finally, it should be noted that: the foregoing description is only a preferred embodiment of the present invention, and the present invention is not limited thereto, but it is to be understood that modifications and equivalents of some of the technical features described in the foregoing embodiments may be made by those skilled in the art, although the present invention has been described in detail with reference to the foregoing embodiments. Any modification, equivalent replacement, improvement, etc. made within the spirit and principle of the present invention should be included in the protection scope of the present invention.
Claims (4)
1. The ultralow-temperature desulfurization and denitrification process special for the lime kiln is characterized by comprising low-temperature SCR denitration and SDS dry desulfurization;
the low-temperature SCR denitration is carried out, and the lime kiln flue gas enters an SCR reactor for denitration after passing through a blower; after the low-temperature SCR denitration is finished, lime kiln flue gas after denitration is obtained;
The temperature of the lime kiln flue gas is maintained at 160-170 ℃, the content of particles is 5-5.6g/m 3, the content of sulfur dioxide is 200-1100mg/m 3, the content of nitrogen oxides is 200-350mg/m 3, and the flow is 75000-75500Nm 3/h;
the SCR reactor is internally provided with a honeycomb catalyst, the volume of the initial catalyst is 14.9-15.5m 3, the number of catalyst holes is 22-25 holes, the length of a catalyst monomer is 150-155mm, the width of the monomer is 150-155mm, the height of the monomer is 1150-1180mm, the specific surface area is 527-530m 2/m3, the volume density is 450-455mg/cm 3, and the void ratio is 74.88-74.95%;
heating the flue gas of the lime kiln after denitration to 125-135 ℃, then introducing the flue gas into a dust remover, controlling the temperature of the dust remover to be 110-270 ℃, spraying a desulfurizing agent on a flue before the dust remover, and obtaining the flue gas of the lime kiln after desulfurization;
The preparation method of the desulfurizing agent comprises the following steps: mixing calcium bentonite, magnesium oxide and zeolite powder, performing first ball milling, controlling the ball-material ratio at 10-12:1, the rotation speed at 320-350rpm, the time at 28-32min, obtaining mixed powder after ball milling, adding the mixed powder into surface modification liquid, soaking, controlling the temperature at 50-55 ℃ for 40-45min, filtering after soaking, freezing filter residues at-30 ℃ to-25 ℃ for 35-40min, drying at 120-125 ℃ to obtain a matrix, mixing the matrix, calcium gluconate, calcium citrate, calcium phytate, calcium sulfate, sodium bicarbonate and sodium lignin sulfonate, performing second ball milling, controlling the ball-material ratio at 12-15:1, the rotation speed at 300-320rpm, and the time at 38-42min, and obtaining the desulfurizing agent after the second ball milling;
The surface modification liquid comprises the following components in parts by weight: 4-6 parts of sodium dodecyl benzene sulfonate, 3-4 parts of zwitterionic polyacrylamide, 5-8 parts of stearic acid and 50-52 parts of deionized water.
2. The ultralow temperature desulfurization and denitrification process special for the lime kiln according to claim 1, wherein the rotating speed of the air blower is 32-35Hz, and the air quantity is 20000-22000m 3/h.
3. The ultralow temperature desulfurization and denitrification process special for a lime kiln according to claim 1, wherein the weight ratio of the calcium bentonite to the magnesia to the zeolite powder is 50-52:3-5:6-9.
4. The ultralow temperature desulfurization and denitrification process special for a lime kiln according to claim 1, wherein the weight ratio of the matrix to the calcium gluconate to the calcium citrate to the calcium phytate to the calcium sulfate to the sodium bicarbonate to the sodium lignin sulfonate is 50-55:7-10:12-16:10-13:5-8:9-12:3-6.
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