CN109464897B - Comprehensive application system for flue gas desulfurization and denitrification waste heat recovery of coke oven - Google Patents
Comprehensive application system for flue gas desulfurization and denitrification waste heat recovery of coke oven Download PDFInfo
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- CN109464897B CN109464897B CN201811251718.2A CN201811251718A CN109464897B CN 109464897 B CN109464897 B CN 109464897B CN 201811251718 A CN201811251718 A CN 201811251718A CN 109464897 B CN109464897 B CN 109464897B
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- 239000002918 waste heat Substances 0.000 title claims abstract description 116
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 title claims abstract description 95
- 239000003546 flue gas Substances 0.000 title claims abstract description 95
- 238000011084 recovery Methods 0.000 title claims abstract description 88
- 238000006477 desulfuration reaction Methods 0.000 title claims abstract description 53
- 230000023556 desulfurization Effects 0.000 title claims abstract description 53
- 239000000571 coke Substances 0.000 title claims abstract description 48
- 238000005235 decoking Methods 0.000 claims abstract description 36
- 239000003795 chemical substances by application Substances 0.000 claims abstract description 32
- 238000000034 method Methods 0.000 claims abstract description 19
- 238000004064 recycling Methods 0.000 claims abstract description 19
- 239000000428 dust Substances 0.000 claims abstract description 10
- 238000001914 filtration Methods 0.000 claims abstract description 7
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 claims description 76
- 229910052717 sulfur Inorganic materials 0.000 claims description 76
- 239000011593 sulfur Substances 0.000 claims description 76
- 239000007788 liquid Substances 0.000 claims description 53
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 claims description 28
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 27
- 239000007789 gas Substances 0.000 claims description 19
- 229910021536 Zeolite Inorganic materials 0.000 claims description 14
- 229960000892 attapulgite Drugs 0.000 claims description 14
- HNPSIPDUKPIQMN-UHFFFAOYSA-N dioxosilane;oxo(oxoalumanyloxy)alumane Chemical compound O=[Si]=O.O=[Al]O[Al]=O HNPSIPDUKPIQMN-UHFFFAOYSA-N 0.000 claims description 14
- 239000000395 magnesium oxide Substances 0.000 claims description 14
- CPLXHLVBOLITMK-UHFFFAOYSA-N magnesium oxide Inorganic materials [Mg]=O CPLXHLVBOLITMK-UHFFFAOYSA-N 0.000 claims description 14
- AXZKOIWUVFPNLO-UHFFFAOYSA-N magnesium;oxygen(2-) Chemical compound [O-2].[Mg+2] AXZKOIWUVFPNLO-UHFFFAOYSA-N 0.000 claims description 14
- 229910052751 metal Inorganic materials 0.000 claims description 14
- 239000002184 metal Substances 0.000 claims description 14
- TWNQGVIAIRXVLR-UHFFFAOYSA-N oxo(oxoalumanyloxy)alumane Chemical compound O=[Al]O[Al]=O TWNQGVIAIRXVLR-UHFFFAOYSA-N 0.000 claims description 14
- 229910052625 palygorskite Inorganic materials 0.000 claims description 14
- 239000000377 silicon dioxide Substances 0.000 claims description 14
- 239000010457 zeolite Substances 0.000 claims description 14
- DGAQECJNVWCQMB-PUAWFVPOSA-M Ilexoside XXIX Chemical compound C[C@@H]1CC[C@@]2(CC[C@@]3(C(=CC[C@H]4[C@]3(CC[C@@H]5[C@@]4(CC[C@@H](C5(C)C)OS(=O)(=O)[O-])C)C)[C@@H]2[C@]1(C)O)C)C(=O)O[C@H]6[C@@H]([C@H]([C@@H]([C@H](O6)CO)O)O)O.[Na+] DGAQECJNVWCQMB-PUAWFVPOSA-M 0.000 claims description 13
- 229920003063 hydroxymethyl cellulose Polymers 0.000 claims description 13
- 229940031574 hydroxymethyl cellulose Drugs 0.000 claims description 13
- 239000011734 sodium Substances 0.000 claims description 13
- 229910052708 sodium Inorganic materials 0.000 claims description 13
- 239000007787 solid Substances 0.000 claims description 13
- 239000004343 Calcium peroxide Substances 0.000 claims description 12
- VSGNNIFQASZAOI-UHFFFAOYSA-L calcium acetate Chemical compound [Ca+2].CC([O-])=O.CC([O-])=O VSGNNIFQASZAOI-UHFFFAOYSA-L 0.000 claims description 12
- 239000001639 calcium acetate Substances 0.000 claims description 12
- 235000011092 calcium acetate Nutrition 0.000 claims description 12
- 229960005147 calcium acetate Drugs 0.000 claims description 12
- LHJQIRIGXXHNLA-UHFFFAOYSA-N calcium peroxide Chemical compound [Ca+2].[O-][O-] LHJQIRIGXXHNLA-UHFFFAOYSA-N 0.000 claims description 12
- 235000019402 calcium peroxide Nutrition 0.000 claims description 12
- 238000010438 heat treatment Methods 0.000 claims description 12
- 239000002808 molecular sieve Substances 0.000 claims description 12
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 claims description 12
- 239000000725 suspension Substances 0.000 claims description 12
- 238000007789 sealing Methods 0.000 claims description 9
- 239000000779 smoke Substances 0.000 claims description 9
- 239000007921 spray Substances 0.000 claims description 9
- 239000000843 powder Substances 0.000 claims description 8
- 235000012239 silicon dioxide Nutrition 0.000 claims description 7
- 238000001179 sorption measurement Methods 0.000 claims description 7
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 7
- 239000004215 Carbon black (E152) Substances 0.000 claims description 6
- 238000010285 flame spraying Methods 0.000 claims description 6
- 229930195733 hydrocarbon Natural products 0.000 claims description 6
- 150000002430 hydrocarbons Chemical class 0.000 claims description 6
- 239000002893 slag Substances 0.000 claims description 6
- 239000002002 slurry Substances 0.000 claims description 6
- FYIRUPZTYPILDH-UHFFFAOYSA-N 1,1,1,2,3,3-hexafluoropropane Chemical compound FC(F)C(F)C(F)(F)F FYIRUPZTYPILDH-UHFFFAOYSA-N 0.000 claims description 3
- 238000007599 discharging Methods 0.000 claims description 3
- 239000000203 mixture Substances 0.000 claims description 3
- 230000003009 desulfurizing effect Effects 0.000 abstract description 5
- 230000000694 effects Effects 0.000 abstract description 5
- 239000010410 layer Substances 0.000 description 17
- 238000004939 coking Methods 0.000 description 9
- MWUXSHHQAYIFBG-UHFFFAOYSA-N nitrogen oxide Inorganic materials O=[N] MWUXSHHQAYIFBG-UHFFFAOYSA-N 0.000 description 9
- 239000011269 tar Substances 0.000 description 8
- 239000011777 magnesium Substances 0.000 description 7
- 241000196324 Embryophyta Species 0.000 description 6
- RAHZWNYVWXNFOC-UHFFFAOYSA-N Sulphur dioxide Chemical compound O=S=O RAHZWNYVWXNFOC-UHFFFAOYSA-N 0.000 description 6
- 238000004321 preservation Methods 0.000 description 6
- 229910000831 Steel Inorganic materials 0.000 description 5
- 239000003921 oil Substances 0.000 description 5
- 239000010959 steel Substances 0.000 description 5
- 238000006243 chemical reaction Methods 0.000 description 4
- 230000007613 environmental effect Effects 0.000 description 4
- UHOVQNZJYSORNB-UHFFFAOYSA-N Benzene Chemical compound C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 description 3
- 239000003245 coal Substances 0.000 description 3
- 239000012530 fluid Substances 0.000 description 3
- 239000007791 liquid phase Substances 0.000 description 3
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 2
- VHUUQVKOLVNVRT-UHFFFAOYSA-N Ammonium hydroxide Chemical compound [NH4+].[OH-] VHUUQVKOLVNVRT-UHFFFAOYSA-N 0.000 description 2
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 2
- CSNNHWWHGAXBCP-UHFFFAOYSA-L Magnesium sulfate Chemical compound [Mg+2].[O-][S+2]([O-])([O-])[O-] CSNNHWWHGAXBCP-UHFFFAOYSA-L 0.000 description 2
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 description 2
- 239000003463 adsorbent Substances 0.000 description 2
- 235000011114 ammonium hydroxide Nutrition 0.000 description 2
- BRPQOXSCLDDYGP-UHFFFAOYSA-N calcium oxide Chemical compound [O-2].[Ca+2] BRPQOXSCLDDYGP-UHFFFAOYSA-N 0.000 description 2
- 239000000292 calcium oxide Substances 0.000 description 2
- ODINCKMPIJJUCX-UHFFFAOYSA-N calcium oxide Inorganic materials [Ca]=O ODINCKMPIJJUCX-UHFFFAOYSA-N 0.000 description 2
- 239000011280 coal tar Substances 0.000 description 2
- 230000000052 comparative effect Effects 0.000 description 2
- 238000001816 cooling Methods 0.000 description 2
- 238000004821 distillation Methods 0.000 description 2
- 239000000463 material Substances 0.000 description 2
- 239000011241 protective layer Substances 0.000 description 2
- 229910000851 Alloy steel Inorganic materials 0.000 description 1
- 240000000233 Melia azedarach Species 0.000 description 1
- QAOWNCQODCNURD-UHFFFAOYSA-L Sulfate Chemical compound [O-]S([O-])(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-L 0.000 description 1
- LSNNMFCWUKXFEE-UHFFFAOYSA-N Sulfurous acid Chemical compound OS(O)=O LSNNMFCWUKXFEE-UHFFFAOYSA-N 0.000 description 1
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 description 1
- DIZPMCHEQGEION-UHFFFAOYSA-H aluminium sulfate (anhydrous) Chemical compound [Al+3].[Al+3].[O-]S([O-])(=O)=O.[O-]S([O-])(=O)=O.[O-]S([O-])(=O)=O DIZPMCHEQGEION-UHFFFAOYSA-H 0.000 description 1
- 229910021529 ammonia Inorganic materials 0.000 description 1
- 230000001174 ascending effect Effects 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 238000003763 carbonization Methods 0.000 description 1
- 238000007600 charging Methods 0.000 description 1
- 230000008602 contraction Effects 0.000 description 1
- 230000007797 corrosion Effects 0.000 description 1
- 238000005260 corrosion Methods 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000003795 desorption Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000001035 drying Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 238000001704 evaporation Methods 0.000 description 1
- 230000008020 evaporation Effects 0.000 description 1
- XEEYBQQBJWHFJM-UHFFFAOYSA-N iron Substances [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 1
- 229910052742 iron Inorganic materials 0.000 description 1
- 229910052943 magnesium sulfate Inorganic materials 0.000 description 1
- 235000019341 magnesium sulphate Nutrition 0.000 description 1
- 229910052757 nitrogen Inorganic materials 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 238000005507 spraying Methods 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 238000009834 vaporization Methods 0.000 description 1
- 230000008016 vaporization Effects 0.000 description 1
- 239000002699 waste material Substances 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
- B01D53/46—Removing components of defined structure
- B01D53/48—Sulfur compounds
- B01D53/50—Sulfur oxides
- B01D53/507—Sulfur oxides by treating the gases with other liquids
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F22—STEAM GENERATION
- F22B—METHODS OF STEAM GENERATION; STEAM BOILERS
- F22B1/00—Methods of steam generation characterised by form of heating method
- F22B1/02—Methods of steam generation characterised by form of heating method by exploitation of the heat content of hot heat carriers
- F22B1/18—Methods of steam generation characterised by form of heating method by exploitation of the heat content of hot heat carriers the heat carrier being a hot gas, e.g. waste gas such as exhaust gas of internal-combustion engines
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F27—FURNACES; KILNS; OVENS; RETORTS
- F27D—DETAILS OR ACCESSORIES OF FURNACES, KILNS, OVENS, OR RETORTS, IN SO FAR AS THEY ARE OF KINDS OCCURRING IN MORE THAN ONE KIND OF FURNACE
- F27D17/00—Arrangements for using waste heat; Arrangements for using, or disposing of, waste gases
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F27—FURNACES; KILNS; OVENS; RETORTS
- F27D—DETAILS OR ACCESSORIES OF FURNACES, KILNS, OVENS, OR RETORTS, IN SO FAR AS THEY ARE OF KINDS OCCURRING IN MORE THAN ONE KIND OF FURNACE
- F27D17/00—Arrangements for using waste heat; Arrangements for using, or disposing of, waste gases
- F27D17/004—Systems for reclaiming waste heat
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P10/00—Technologies related to metal processing
- Y02P10/25—Process efficiency
Landscapes
- Engineering & Computer Science (AREA)
- Environmental & Geological Engineering (AREA)
- Mechanical Engineering (AREA)
- General Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- Combustion & Propulsion (AREA)
- Life Sciences & Earth Sciences (AREA)
- Sustainable Development (AREA)
- Sustainable Energy (AREA)
- Physics & Mathematics (AREA)
- Thermal Sciences (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 provides a comprehensive application system for desulfurization and denitration of coke oven flue gas, which comprises a coke oven (1), a bag-type dust collector (2), a decoking device (3), an SCR denitration device (4), a waste heat recycling device (5), a desulfurization device (6), a filtering device (7) and a chimney (8); the waste heat recycling device (5) comprises a high-grade waste heat recycling loop and a low-grade waste heat recycling loop. The invention also provides a comprehensive application method of the flue gas desulfurization and denitration of the coke oven. The comprehensive application system for desulfurizing and denitrating the flue gas of the coke oven firstly uses high-temperature waste heat recovery for acting, and then preheats desulfurizing agent for desulfurizing by using low-temperature waste heat recovery, thereby greatly improving the utilization efficiency and effect of the waste heat.
Description
Technical Field
The invention belongs to the field of coke oven equipment, and particularly relates to a comprehensive application system for desulfurization and denitrification of coke oven flue gas.
Background
In recent years, in northern areas, particularly in Jing Ji areas, severe haze weather frequently occurs, and the increasingly severe atmospheric pollution is paid attention to the state and the whole society, so that effective treatment of the atmospheric pollution is a consensus and expected in all the communities. During the period of twelve, five and thirteen, china comes out of the counter and a great deal of current environmental protection regulations are modified, so that the atmospheric pollution emission standards of all fields are becoming stricter. Against this large background, the coking industry, which was previously substantially in a disordered discharge state, has also received particular attention. The department of environmental protection issued in 2012 a new "pollution emission standards for coking chemistry industry" (GB 16171-2012), which specifies that all businesses should perform according to the new atmospheric emission standards since 1 month 1 of 2015. This requires each coking enterprise to build new desulfurization and denitrification facilities to ensure the standard discharge of flue gas.
At present, desulfurization and denitrification treatment of domestic coke oven flue gas is still in a starting stage, and most coke oven flue gas of coking plants and steel plants is still directly discharged into the atmosphere without treatment. The method seriously affects the local atmosphere environment, and brings great hidden trouble to the health of people. With the discharge of the stricter coke oven flue gas emission standard GB16171-2012, the desulfurization and denitration of the coke oven flue gas become the necessary process of all domestic coking factories. It is expected that future emission standards of flue gas will be closer to stricter international environmental standards to adapt to international energy-saving environmental trends. Therefore, a reliable system and process are needed to realize the purposes of desulfurization and denitrification of the coke oven flue gas and waste heat recovery.
The coke oven can carry out high-temperature carbonization treatment on coal, and can efficiently convert the coal into products such as coke, coke oven gas, coal tar, crude benzene and the like, thereby being an efficient energy conversion kiln. In the heat of the coke oven expenditure, the heat of the crude gas at 650-700 ℃ is about 36%, and the recovery and utilization value is extremely high. At present, a cooling treatment process is generally adopted to realize industrial application of raw gas, and the traditional process is as follows: spraying a large amount of circulating ammonia water at 70-75 ℃ to the high-temperature raw gas to cool the high-temperature raw gas, so as to realize waste heat recovery, however, the waste of heat brought out by the high-temperature raw gas due to the large amount of evaporation of the circulating ammonia water is caused.
In the 80 s of the 20 th century, most coking plants in japan have used conduction oil for riser recovery of raw gas carry-over heat: they make the riser into a jacket pipe, and the heat transfer oil indirectly exchanges heat with the high temperature raw gas through the jacket pipe, so that the heated high temperature heat transfer oil can be used for various purposes, such as ammonia distillation, coal tar distillation, drying and charging coal, etc. Later, the economic steel in China has been subjected to similar tests on a five-hole riser; many enterprises in China such as Wu Steel, ma Steel, saddle Steel, lian Steel, beijing coking plant, shenyang gas two plant, yi-Tien-iron, pingshan coking plant and the like use a water vaporization cooling technology to recover the heat in a riser; in addition, enterprises adopt a method of indirectly exchanging heat with high-temperature raw gas by taking nitrogen as a medium.
The structure of the traditional coke oven riser raw gas waste heat recovery heat device is an overall inner, middle and outer three-layer basic structure. The inner layer is a cylinder made of high-temperature-resistant and corrosion-resistant alloy steel, and raw gas flows through the cylinder from bottom to top. The middle is a core heat transfer layer, a high-temperature-resistant solid medium layer with high heat conduction capability and a certain thickness is closely attached to the outer wall of the inner cylinder, a heat transfer pipe passes through the solid medium layer and is closely contacted with the solid medium layer, a heat taking medium flows through the heat transfer pipe, the heat taking medium absorbs the heat release quantity of raw gas in the inner cylinder in the flowing process, and the temperature is increased in the flowing process from bottom to top. The heat transfer pipe or the spiral ascending spiral is arranged in the solid medium layer or is vertically arranged on the solid medium layer from bottom to top, and the solid medium layer needs to cover the outer surface of the whole heat transfer pipe; the outer layer is a heat preservation protective layer, the metal cylinder body is made of metal, a heat preservation material is stuck on the inner wall surface, the heat preservation and protection effects on the inner cylinder and the middle core heat transfer layer are achieved, heat loss is reduced, and the heat preservation protective layer is free from impact.
However, the prior art coke oven riser raw gas waste heat recovery heat device has more or less the following problems: the heat transfer process has unreasonable structural design, unsmooth circulation and low heat exchange efficiency, and tar adhesion on the side wall surface of raw gas causes blockage of a raw gas channel, coking of heat conduction oil causes blockage of a heat conduction oil channel, and is easy to corrode by media and the like or can not effectively solve the problems of thermal expansion and cold contraction in the starting, stopping and running processes, so that the method is difficult to implement successfully or has a satisfactory effect.
Disclosure of Invention
Technical problems: in order to solve the defects of the prior art, the invention provides a comprehensive application system for desulfurization and denitrification of coke oven flue gas.
The technical scheme is as follows: the invention provides a comprehensive application system for desulfurization and denitration of coke oven flue gas, which comprises a coke oven (1), a bag-type dust collector (2), a decoking device (3), an SCR denitration device (4), a waste heat recycling device (5), a desulfurization device (6), a filtering device (7) and a chimney (8); the waste heat recycling device (5) comprises a high-grade waste heat recycling loop and a low-grade waste heat recycling loop; the high-grade waste heat recovery loop comprises a first auxiliary heating device (53), a steam turbine (54), a high-temperature working medium pump (55), a working medium pipeline of a first high-temperature waste heat recovery device (51) and a working medium pipeline of a second high-temperature waste heat recovery device (52) which are connected in sequence; the low-grade waste heat recovery loop comprises a working medium pipeline of a heat exchanger (58), a low-temperature working medium pump (59), a working medium pipeline of a first low-temperature waste heat recovery device (56) and a second low-temperature waste heat recovery device (57) which are connected in parallel in sequence; the flue gas pipeline of the first high-temperature waste heat recovery device (51) and the flue gas pipeline of the first low-temperature waste heat recovery device (56) are connected in series with the flue gas pipeline of the second high-temperature waste heat recovery device (52) and the flue gas pipeline of the second low-temperature waste heat recovery device (57) in parallel, one end of each parallel pipeline is connected in series with the flue gas outlets of the SCR denitration device (4), the decoking device (3), the bag-type dust collector (2) and the coke oven (1) in sequence, and the other end of each parallel pipeline is connected in series with the desulfurization device (6), the filtering device (7) and the chimney (8) in sequence; the bottom of the sulfur removal device (6) is provided with a slurry tank (61) and a sulfur removal liquid spray head (66) at the top, the bottom of the slurry tank (61) is connected with a first sulfur removal liquid pump (62), a sulfur removal liquid pool (63) is connected with a second sulfur removal liquid pump (64), and a liquid outlet of the first sulfur removal liquid pump (62) and a liquid outlet of the second sulfur removal liquid pump (64) are respectively connected with a sulfur removal liquid pipeline of the heat exchanger (58), a second auxiliary heater (65) and the sulfur removal liquid spray head (66) in sequence.
The decoking device (3) comprises an equipment room (31), an adsorption room (32), a decoking room (33) and an ash room (34) which are sequentially connected from top to bottom, a driving wheel (35) connected with a driving motor is arranged in the equipment room (31), a driven wheel (36) and a group of flame spraying devices (37) are arranged in the decoking room (33), a metal net (38) capable of rotating around the driving wheel (35) and the driven wheel (36) is arranged between the driving wheel (35) and the driven wheel (36), a slag storage box (39) is arranged in the ash room (34), and a movable sealing door (30) is arranged between the decoking room (33) and the ash room (34).
The waste heat recovery device (1) comprises a flue gas pipeline (11) and a working medium pipeline (15), the side wall of the flue gas pipeline (11) sequentially comprises an outer cylinder wall (12), a heat preservation layer (13), a solid medium layer (14) and an inner cylinder wall (16) from outside to inside, the working medium pipeline (15) is spirally arranged in the solid medium layer (14), a group of fins (17) are arranged in the inner cylinder wall (16), a group of turbulent flow rings (18) are arranged in the flue gas pipeline (11), and an expansion joint (19) is arranged in the middle of the outer cylinder wall (12).
The high-grade waste heat recovery loop adopts water as working medium.
The low-grade waste heat recovery loop adopts Hydrofluorocarbon (HFC) or Hydrocarbon (HC) with the critical temperature below 100 ℃ as R23, R32, R41, R116, R125, R134A, R143A, R152A, R218, R227ea, R236ea, R236fa, RC318, R404A, R407A, R407B, R407C, R407D, R407E, R410A, R410B, R413A, R417A, R419A, R421A, R421B, R422A, R422B, R422C, R422D, R423A, R424A, R425A, R427A, R428A, R507A, R1150, R170, R1270, R290 and R744 as a circulating working medium or a multi-component mixture of the working mediums as the circulating working mediums. .
The sulfur removal liquid pool (63) is internally provided with sulfur removal agent suspension.
The sulfur removing agent comprises the following components in parts by weight: 20-30 parts of aluminum oxide, 10-20 parts of magnesium oxide, 20-30 parts of attapulgite, 10-20 parts of activated carbon, 4-10 parts of zeolite molecular sieve, 4-10 parts of silica micropowder, 10-20 parts of calcium peroxide, 4-10 parts of sodium hydroxymethyl cellulose and 6-12 parts of calcium acetate.
The sulfur removing agent comprises the following components in parts by weight: 24-26 parts of aluminum oxide, 14-16 parts of magnesium oxide, 24-26 parts of attapulgite, 14-16 parts of activated carbon, 6-8 parts of zeolite molecular sieve, 6-8 parts of silica micropowder, 14-16 parts of calcium peroxide, 6-8 parts of sodium hydroxymethyl cellulose and 8-10 parts of calcium acetate.
The sulfur removing agent comprises the following components in parts by weight: 25 parts of aluminum oxide, 15 parts of magnesium oxide, 25 parts of attapulgite, 15 parts of activated carbon, 7 parts of zeolite molecular sieve, 7 parts of silicon dioxide micro powder, 15 parts of calcium peroxide, 7 parts of sodium hydroxymethyl cellulose and 9 parts of calcium acetate.
The invention also provides a comprehensive application method of the flue gas desulfurization and denitration of the coke oven, which comprises the following steps of:
the method comprises the steps of (1) discharging smoke of a coke oven (1) from an outlet, dedusting the smoke, entering a bag-type dust remover (2), entering a decoking device (3), decoking, enriching tar contained in the smoke on a metal net (38) in the decoking device (3), rotating a driving wheel (35) to enable the metal net (38) to enter a decoking chamber (33) if the metal net (38) is enriched with more tar, starting a flame spraying device (37) to enable the tar to burn and fall to the bottom, opening a sealing door (30), enabling ash to fall into a slag storage box (39), and closing the sealing door (30);
(2) The flue gas after the decoking enters an SCR denitration device (4) for denitration;
(3) The flue gas after denitration enters a waste heat recycling device (5) to recycle waste heat:
the flue gas firstly exchanges heat with working media in a first high-temperature waste heat recovery device (51) and a second high-temperature waste heat recovery device (52), so that waste heat of the flue gas is recovered, the working media enter a first auxiliary heater (53) after being heated, the first auxiliary heater (53) is started when the temperature is insufficient, the first auxiliary heater (53) is closed when the temperature is sufficient, high-temperature gas enters a steam turbine (54) again to do work to form exhaust steam or liquid, and the exhaust steam or liquid after heat exchange is pumped into a working media pipeline of the high-temperature waste heat recovery device (51) and a working media pipeline of the second high-temperature waste heat recovery device (52) through a high-temperature working media pump (55);
the flue gas exchanges heat with working media in a second high-temperature waste heat recovery device (52) and a second low-temperature waste heat recovery device (57), so that the waste heat of the flue gas is recovered, after the working media are heated, the working media enter a working media pipeline of a heat exchanger 586) to exchange heat with a sulfur removal agent suspension liquid in a sulfur removal liquid pipeline of the heat exchanger (58), the sulfur removal agent suspension liquid is heated, when the heating temperature is insufficient, a second auxiliary heater (65) is started, when the heating temperature is sufficient, the second auxiliary heater (65) is closed, and the working media after heat exchange are pumped into the working media pipeline of the second high-temperature waste heat recovery device (52) and the second low-temperature waste heat recovery device (57) through a low-temperature working media pump (59);
(4) The flue gas after the waste heat recovery enters a sulfur removal device (6), and reacts with sulfur removal agent suspension liquid sprayed from a sulfur removal liquid spray head (66) in the sulfur removal device (6) to realize sulfur removal;
(5) And the flue gas after sulfur removal is discharged after being filtered.
The beneficial effects are that: the comprehensive application system for desulfurization and denitration of the coke oven flue gas firstly uses the high-temperature waste heat recovery for acting, and then preheats the desulfurizing agent for desulfurization by using the low-temperature waste heat recovery, thereby greatly improving the utilization efficiency and effect of the waste heat.
Meanwhile, the invention uses the decoking system with a special structure to decoke the flue gas before treatment, thereby greatly avoiding the influence on the service life of the equipment due to the enrichment of tar in the flue gas in the equipment in the follow-up denitration, waste heat recovery and desulfurization.
Meanwhile, the method uses the special sulfur removal agent, the sulfur removal agent has rich raw material sources and low cost, sulfur dioxide and nitrogen oxides in the flue gas are removed by physical adsorption and chemical sulfur removal methods, and the flue gas is easy to regenerate and can be reused after desorption, so that the consumption of the adsorbent is greatly reduced.
Because calcium oxide, aluminum oxide and magnesium oxide are difficult to dissolve in water, the desulfurization efficiency is low; the desulfurization adsorbent of the invention utilizes the different adsorption effects of alumina, attapulgite, activated carbon, zeolite molecules and silica micro powder on sulfur dioxide and nitrogen oxides in the flue gas, and the adsorption rate of the sulfur dioxide and the nitrogen oxides in the flue gas is greatly improved by cooperative work, and the adsorption is released in water; meanwhile, the calcium peroxide slowly releases oxygen to oxidize sulfurous acid into sulfuric acid on one hand, and generates calcium oxide to participate in the reaction on the other hand; the sulfate reacts with aluminum oxide and magnesium oxide to form aluminum sulfate and magnesium sulfate which are easy to dissolve in water; the calcium acetate in the liquid phase makes the whole liquid phase weak alkaline, so that the reaction is accelerated; the addition of the sodium hydroxymethyl cellulose can lead the components to be matched and reacted in the liquid phase, and if the pH is too low, the viscosity is higher, and the sodium hydroxymethyl cellulose can also be used for indicating a reaction system; the rest solid is attapulgite, active carbon, zeolite molecules and silica micropowder.
Drawings
Fig. 1 is a schematic structural diagram of a comprehensive application system for desulfurizing and denitrating coke oven flue gas.
Fig. 2 is a schematic structural view of a decoking device.
Fig. 3 is a schematic structural view of the waste heat recovery device.
Fig. 4 is a partial enlarged view of the waste heat recovery device.
Detailed Description
The present invention will be further described below.
Example 1
The coke oven flue gas sulfur remover comprises the following components in parts by weight: 20 parts of aluminum oxide, 20 parts of magnesium oxide, 20 parts of attapulgite, 20 parts of activated carbon, 4 parts of zeolite molecular sieve, 10 parts of silicon dioxide micro powder, 10 parts of calcium peroxide, 10 parts of sodium hydroxymethyl cellulose and 6 parts of calcium acetate.
The flue gas desulfurization agent is used for wet desulfurization, n (2/3Al+Mg): when S is 1.2, the desulfurization efficiency is 99.1%.
Example 2
The coke oven flue gas sulfur remover comprises the following components in parts by weight: 30 parts of aluminum oxide, 10 parts of magnesium oxide, 30 parts of attapulgite, 10 parts of activated carbon, 10 parts of zeolite molecular sieve, 4 parts of silicon dioxide micro powder, 20 parts of calcium peroxide, 4 parts of sodium hydroxymethyl cellulose and 12 parts of calcium acetate.
The flue gas desulfurization agent is used for wet desulfurization, n (2/3Al+Mg): when S is 1.2, the desulfurization efficiency is 97.4%.
Example 3
The coke oven flue gas sulfur removal agent comprises the following components in parts by weight: 24 parts of aluminum oxide, 16 parts of magnesium oxide, 24 parts of attapulgite, 16 parts of activated carbon, 6 parts of zeolite molecular sieve, 8 parts of silicon dioxide micro powder, 14 parts of calcium peroxide, 8 parts of hydroxymethyl cellulose sodium and 8 parts of calcium acetate.
The flue gas desulfurization agent is used for wet desulfurization, n (2/3Al+Mg): when S is 1.2, the desulfurization efficiency is 97.6%.
Example 4
The coke oven flue gas sulfur removal agent comprises the following components in parts by weight: 26 parts of aluminum oxide, 14 parts of magnesium oxide, 26 parts of attapulgite, 14 parts of activated carbon, 8 parts of zeolite molecular sieve, 6 parts of silicon dioxide micro powder, 16 parts of calcium peroxide, 6 parts of sodium hydroxymethyl cellulose and 10 parts of calcium acetate.
The flue gas desulfurization agent is used for wet desulfurization, n (2/3Al+Mg): when S is 1.2, the desulfurization efficiency is 95.9%.
Example 5
The coke oven flue gas sulfur removal agent comprises the following components in parts by weight: 25 parts of aluminum oxide, 15 parts of magnesium oxide, 25 parts of attapulgite, 15 parts of activated carbon, 7 parts of zeolite molecular sieve, 7 parts of silicon dioxide micro powder, 15 parts of calcium peroxide, 7 parts of sodium hydroxymethyl cellulose and 9 parts of calcium acetate.
The flue gas desulfurization agent is used for wet desulfurization, n (2/3Al+Mg): when S is 1.2, the desulfurization efficiency is 95.8%. Comparative example 1
The coke oven flue gas sulfur remover comprises the following components in parts by weight: 20 parts of aluminum oxide and 20 parts of magnesium oxide.
The flue gas desulfurization agent is used for wet desulfurization, n (2/3Al+Mg): when S is 1.2, the desulfurization efficiency is 89.1%.
Comparative example 2
The coke oven flue gas sulfur remover comprises the following components in parts by weight: 20 parts of attapulgite, 20 parts of activated carbon, 4 parts of zeolite molecular sieve and 10 parts of silica micropowder.
The flue gas desulfurization agent is used for wet desulfurization, n (2/3Al+Mg): when S is 1.2, the desulfurization efficiency is 88.2%.
Example 6
The comprehensive application system for the desulfurization and the denitrification of the coke oven flue gas comprises a coke oven (1), a bag-type dust collector (2), a decoking device (3), an SCR denitration device (4), a waste heat recycling device (5), a desulfurization device (6), a filtering device (7) and a chimney (8); the waste heat recycling device (5) comprises a high-grade waste heat recycling loop and a low-grade waste heat recycling loop; the high-grade waste heat recovery loop comprises a first auxiliary heating device (53), a steam turbine (54), a high-temperature working medium pump (55), a working medium pipeline of a first high-temperature waste heat recovery device (51) and a working medium pipeline of a second high-temperature waste heat recovery device (52) which are connected in sequence; the low-grade waste heat recovery loop comprises a working medium pipeline of a heat exchanger (58), a low-temperature working medium pump (59), a working medium pipeline of a first low-temperature waste heat recovery device (56) and a second low-temperature waste heat recovery device (57) which are connected in parallel in sequence; the flue gas pipeline of the first high-temperature waste heat recovery device (51) and the flue gas pipeline of the first low-temperature waste heat recovery device (56) are connected in series with the flue gas pipeline of the second high-temperature waste heat recovery device (52) and the flue gas pipeline of the second low-temperature waste heat recovery device (57) in parallel, one end of each parallel pipeline is connected in series with the flue gas outlets of the SCR denitration device (4), the decoking device (3), the bag-type dust collector (2) and the coke oven (1) in sequence, and the other end of each parallel pipeline is connected in series with the desulfurization device (6), the filtering device (7) and the chimney (8) in sequence; the bottom of the sulfur removal device (6) is provided with a slurry tank (61) and a sulfur removal liquid spray head (66) at the top, the bottom of the slurry tank (61) is connected with a first sulfur removal liquid pump (62), a sulfur removal liquid pool (63) is connected with a second sulfur removal liquid pump (64), and a liquid outlet of the first sulfur removal liquid pump (62) and a liquid outlet of the second sulfur removal liquid pump (64) are respectively connected with a sulfur removal liquid pipeline of the heat exchanger (58), a second auxiliary heater (65) and the sulfur removal liquid spray head (66) in sequence.
The waste heat recovery device (1) comprises a flue gas pipeline (11) and a working medium pipeline (15), the side wall of the flue gas pipeline (11) sequentially comprises an outer cylinder wall (12), a heat preservation layer (13), a solid medium layer (14) and an inner cylinder wall (16) from outside to inside, the working medium pipeline (15) is spirally arranged in the solid medium layer (14), a group of fins (17) are arranged in the inner cylinder wall (16), a group of turbulent flow rings (18) are arranged in the flue gas pipeline (11), and an expansion joint (19) is arranged in the middle of the outer cylinder wall (12).
The decoking device (3) comprises an equipment room (31), an adsorption room (32), a decoking room (33) and an ash room (34) which are sequentially connected from top to bottom, a driving wheel (35) connected with a driving motor is arranged in the equipment room (31), a driven wheel (36) and a group of flame spraying devices (37) are arranged in the decoking room (33), a metal net (38) capable of rotating around the driving wheel (35) and the driven wheel (36) is arranged between the driving wheel (35) and the driven wheel (36), a slag storage box (39) is arranged in the ash room (34), and a movable sealing door (30) is arranged between the decoking room (33) and the ash room (34).
The high-grade waste heat recovery loop adopts water as working medium.
The low grade waste heat recovery circuit adopts Hydrofluorocarbon (HFC) or Hydrocarbon (HC) of R23, R32, R41, R116, R125, R134A, R143A, R152A, R218, R227ea, R236ea, R236fa, RC318, R404A, R407A, R407B, R407C, R407D, R407E, R410A, R410B, R413A, R417A, R419A, R421A, R421B, R422A, R422B, R422C, R422D, R423A, R424A, R425A, R427A, R428A, R507A, R1150, R170, R1270, R290, R744 as a cycle fluid or a multi-component mixture of the above working fluids as the cycle fluid. The recovery efficiency of waste heat can be greatly improved by adopting the materials.
The sulfur removal liquid bath (63) is provided with the sulfur removal agent suspension described in embodiments 1 to 5.
The device is utilized to comprehensively utilize the flue gas desulfurization and denitration of the coke oven, and comprises the following steps:
the method comprises the steps of (1) discharging smoke of a coke oven (1) from an outlet, dedusting the smoke, entering a bag-type dust remover (2), entering a decoking device (3), decoking, enriching tar contained in the smoke on a metal net (38) in the decoking device (3), rotating a driving wheel (35) to enable the metal net (38) to enter a decoking chamber (33) if the metal net (38) is enriched with more tar, starting a flame spraying device (37) to enable the tar to burn and fall to the bottom, opening a sealing door (30), enabling ash to fall into a slag storage box (39), and closing the sealing door (30);
(2) The flue gas after the decoking enters an SCR denitration device (4) for denitration;
(3) The flue gas after denitration enters a waste heat recycling device (5) to recycle waste heat:
the flue gas firstly exchanges heat with working media in a first high-temperature waste heat recovery device (51) and a second high-temperature waste heat recovery device (52), so that waste heat of the flue gas is recovered, the working media enter a first auxiliary heater (53) after being heated, the first auxiliary heater (53) is started when the temperature is insufficient, the first auxiliary heater (53) is closed when the temperature is sufficient, high-temperature gas enters a steam turbine (54) again to do work to form exhaust steam or liquid, and the exhaust steam or liquid after heat exchange is pumped into a working media pipeline of the high-temperature waste heat recovery device (51) and a working media pipeline of the second high-temperature waste heat recovery device (52) through a high-temperature working media pump (55);
the flue gas exchanges heat with working media in a second high-temperature waste heat recovery device (52) and a second low-temperature waste heat recovery device (57), so that the waste heat of the flue gas is recovered, after the working media are heated, the working media enter a working media pipeline of a heat exchanger 586) to exchange heat with a sulfur removal agent suspension liquid in a sulfur removal liquid pipeline of the heat exchanger (58), the sulfur removal agent suspension liquid is heated, when the heating temperature is insufficient, a second auxiliary heater (65) is started, when the heating temperature is sufficient, the second auxiliary heater (65) is closed, and the working media after heat exchange are pumped into the working media pipeline of the second high-temperature waste heat recovery device (52) and the second low-temperature waste heat recovery device (57) through a low-temperature working media pump (59);
(4) The flue gas after the waste heat recovery enters a sulfur removal device (6), and reacts with sulfur removal agent suspension liquid sprayed from a sulfur removal liquid spray head (66) in the sulfur removal device (6) to realize sulfur removal;
(5) And the flue gas after sulfur removal is discharged after being filtered.
Claims (6)
1. A comprehensive application system for desulfurization and denitrification of coke oven flue gas is characterized in that: comprises a coke oven (1), a bag-type dust collector (2), a decoking device (3), an SCR denitration device (4), a waste heat recycling device (5), a desulfurization device (6), a filtering device (7) and a chimney (8); the waste heat recycling device (5) comprises a high-grade waste heat recycling loop and a low-grade waste heat recycling loop; the high-grade waste heat recovery loop comprises a first auxiliary heating device (53), a steam turbine (54), a high-temperature working medium pump (55), a working medium pipeline of a first high-temperature waste heat recovery device (51) and a working medium pipeline of a second high-temperature waste heat recovery device (52) which are connected in sequence; the low-grade waste heat recovery loop comprises a working medium pipeline of a heat exchanger (58), a low-temperature working medium pump (59), a working medium pipeline of a first low-temperature waste heat recovery device (56) and a second low-temperature waste heat recovery device (57) which are connected in parallel in sequence; the flue gas pipeline of the first high-temperature waste heat recovery device (51) and the flue gas pipeline of the first low-temperature waste heat recovery device (56) are connected in series with the flue gas pipeline of the second high-temperature waste heat recovery device (52) and the flue gas pipeline of the second low-temperature waste heat recovery device (57) in parallel, one end of each parallel pipeline is connected in series with the flue gas outlets of the SCR denitration device (4), the decoking device (3), the bag-type dust collector (2) and the coke oven (1) in sequence, and the other end of each parallel pipeline is connected in series with the desulfurization device (6), the filtering device (7) and the chimney (8) in sequence; the bottom of the sulfur removal device (6) is provided with a slurry tank (61) and a sulfur removal liquid spray head (66) at the top, the bottom of the slurry tank (61) is connected with a first sulfur removal liquid pump (62), the sulfur removal liquid pool (63) is connected with a second sulfur removal liquid pump (64), and the liquid outlets of the first sulfur removal liquid pump (62) and the second sulfur removal liquid pump (64) are respectively connected with a sulfur removal liquid pipeline of the heat exchanger (58), a second auxiliary heater (65) and the sulfur removal liquid spray head (66) in sequence;
the decoking device (3) comprises an equipment room (31), an adsorption room (32), a decoking room (33) and an ash room (34) which are sequentially connected from top to bottom, wherein a driving wheel (35) connected with a driving motor is arranged in the equipment room (31), a driven wheel (36) and a group of flame spraying devices (37) are arranged in the decoking room (33), a metal net (38) capable of rotating around the driving wheel (35) and the driven wheel (36) is arranged between the driving wheel (35) and the driven wheel (36), a slag storage box (39) is arranged in the ash room (34), and a movable sealing door (30) is arranged between the decoking room (33) and the ash room (34);
the high-grade waste heat recovery loop adopts water as working medium;
the low-grade waste heat recovery loop adopts Hydrofluorocarbon (HFC) or Hydrocarbon (HC) with the critical temperature below 100 ℃ as R23, R32, R41, R116, R125, R134A, R143A, R152A, R218, R227ea, R236ea, R236fa, RC318, R404A, R407A, R407B, R407C, R407D, R407E, R410A, R410B, R413A, R417A, R419A, R421A, R421B, R422A, R422B, R422C, R422D, R423A, R424A, R425A, R427A, R428A, R507A, R1150, R170, R0, R290 and R744 as a circulating working medium or a multi-component mixture of the working mediums as the circulating working mediums;
the sulfur removing agent comprises the following components in parts by weight: 20-30 parts of aluminum oxide, 10-20 parts of magnesium oxide, 20-30 parts of attapulgite, 10-20 parts of activated carbon, 4-10 parts of zeolite molecular sieve, 4-10 parts of silica micropowder, 10-20 parts of calcium peroxide, 4-10 parts of sodium hydroxymethyl cellulose and 6-12 parts of calcium acetate.
2. The integrated application system for desulfurization and denitrification of flue gas of a coke oven according to claim 1, wherein: the low-temperature waste heat recovery device comprises a first low-temperature waste heat recovery device (56), a second high-temperature waste heat recovery device (52), a first low-temperature waste heat recovery device (56) and a second low-temperature waste heat recovery device (57), wherein the low-temperature waste heat recovery device and the second low-temperature waste heat recovery device (57) respectively and independently comprise a flue gas pipeline (11) and a working medium pipeline (15), the side wall of the flue gas pipeline (11) sequentially comprises an outer cylinder wall (12), an insulating layer (13), a solid medium layer (14) and an inner cylinder wall (16) from outside to inside, the working medium pipeline (15) is spirally arranged in the solid medium layer (14), a group of fins (17) are arranged in the inner cylinder wall (16), a group of vortex rings (18) are arranged in the flue gas pipeline (11), and an expansion joint (19) is arranged in the middle of the outer cylinder wall (12).
3. The integrated application system for desulfurization and denitrification of flue gas of a coke oven according to claim 1, wherein: the sulfur removal liquid pool (63) is internally provided with sulfur removal agent suspension.
4. The integrated application system for desulfurization and denitrification of flue gas of a coke oven according to claim 1, wherein: the sulfur removing agent comprises the following components in parts by weight: 24-26 parts of aluminum oxide, 14-16 parts of magnesium oxide, 24-26 parts of attapulgite, 14-16 parts of activated carbon, 6-8 parts of zeolite molecular sieve, 6-8 parts of silica micropowder, 14-16 parts of calcium peroxide, 6-8 parts of sodium hydroxymethyl cellulose and 8-10 parts of calcium acetate.
5. The integrated application system for desulfurization and denitrification of flue gas of a coke oven according to claim 1, wherein: the sulfur removing agent comprises the following components in parts by weight: 25 parts of aluminum oxide, 15 parts of magnesium oxide, 25 parts of attapulgite, 15 parts of activated carbon, 7 parts of zeolite molecular sieve, 7 parts of silicon dioxide micro powder, 15 parts of calcium peroxide, 7 parts of sodium hydroxymethyl cellulose and 9 parts of calcium acetate.
6. A comprehensive application method for desulfurization and denitrification of coke oven flue gas is characterized by comprising the following steps: use of a system according to any one of claims 1 to 5, comprising the steps of:
the method comprises the steps of (1) discharging smoke of a coke oven (1) from an outlet, dedusting the smoke, entering a bag-type dust remover (2), entering a decoking device (3), decoking, enriching tar contained in the smoke on a metal net (38) in the decoking device (3), rotating a driving wheel (35) to enable the metal net (38) to enter a decoking chamber (33) if the metal net (38) is enriched with more tar, starting a flame spraying device (37) to enable the tar to burn and fall to the bottom, opening a sealing door (30), enabling ash to fall into a slag storage box (39), and closing the sealing door (30);
(2) The flue gas after the decoking enters an SCR denitration device (4) for denitration;
(3) The flue gas after denitration enters a waste heat recycling device (5) to recycle waste heat:
the flue gas firstly exchanges heat with working media in a first high-temperature waste heat recovery device (51) and a second high-temperature waste heat recovery device (52), so that waste heat of the flue gas is recovered, the working media enter a first auxiliary heating device (53) after being heated, the first auxiliary heating device (53) is started when the temperature is insufficient, the first auxiliary heating device (53) is closed when the temperature is sufficient, high-temperature gas enters a steam turbine (54) again to do work to form exhaust steam or liquid, and the exhaust steam or liquid after heat exchange is pumped into a working media pipeline of the high-temperature waste heat recovery device (51) and a working media pipeline of the second high-temperature waste heat recovery device (52) through a high-temperature working media pump (55);
the flue gas exchanges heat with working media in a second high-temperature waste heat recovery device (52) and a second low-temperature waste heat recovery device (57), so that the waste heat of the flue gas is recovered, after the working media are heated, the flue gas enters a working media pipeline of a heat exchanger (58) to exchange heat with a sulfur removal agent suspension liquid in a sulfur removal liquid pipeline of the heat exchanger (58), the sulfur removal agent suspension liquid is heated, when the heating temperature is insufficient, a second auxiliary heater (65) is started, when the heating temperature is sufficient, the second auxiliary heater (65) is closed, and the working media after heat exchange are pumped into the working media pipelines of the second high-temperature waste heat recovery device (52) and the second low-temperature waste heat recovery device (57) through a low-temperature working media pump (59);
(4) The flue gas after the waste heat recovery enters a sulfur removal device (6), and reacts with sulfur removal agent suspension liquid sprayed from a sulfur removal liquid spray head (66) in the sulfur removal device (6) to realize sulfur removal;
(5) And the flue gas after sulfur removal is discharged after being filtered.
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| CN111664603A (en) * | 2020-06-12 | 2020-09-15 | 柴皓静 | Waste heat collecting and utilizing device of hydrated lime production equipment |
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| CN205832922U (en) * | 2016-05-03 | 2016-12-28 | 湖北思搏盈环保科技股份有限公司 | A kind of coalitenessity kiln gas Environmental-protection comprehensive processing system |
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| CN107418599A (en) * | 2017-08-31 | 2017-12-01 | 南京沪友冶金机械制造有限公司 | The coke oven coke oven uprising tube waste heat recovery device of integration desulfurization denitration |
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