CN102230635B - Treatment system and method of smoke - Google Patents
Treatment system and method of smoke Download PDFInfo
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- CN102230635B CN102230635B CN2011101218749A CN201110121874A CN102230635B CN 102230635 B CN102230635 B CN 102230635B CN 2011101218749 A CN2011101218749 A CN 2011101218749A CN 201110121874 A CN201110121874 A CN 201110121874A CN 102230635 B CN102230635 B CN 102230635B
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- heat pipe
- desulfurizing tower
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- 238000000034 method Methods 0.000 title claims abstract description 33
- 239000000779 smoke Substances 0.000 title claims abstract description 20
- 239000002918 waste heat Substances 0.000 claims abstract description 22
- 239000006227 byproduct Substances 0.000 claims abstract description 19
- 230000005484 gravity Effects 0.000 claims abstract description 4
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims description 55
- 239000003546 flue gas Substances 0.000 claims description 55
- 230000003009 desulfurizing effect Effects 0.000 claims description 35
- 238000011084 recovery Methods 0.000 claims description 25
- 238000006477 desulfuration reaction Methods 0.000 claims description 19
- 239000007789 gas Substances 0.000 claims description 12
- 238000012545 processing Methods 0.000 claims description 12
- 238000006243 chemical reaction Methods 0.000 claims description 10
- FYYHWMGAXLPEAU-UHFFFAOYSA-N Magnesium Chemical compound [Mg] FYYHWMGAXLPEAU-UHFFFAOYSA-N 0.000 claims description 8
- 239000007788 liquid Substances 0.000 claims description 8
- 239000011777 magnesium Substances 0.000 claims description 8
- 229910052749 magnesium Inorganic materials 0.000 claims description 8
- 238000010521 absorption reaction Methods 0.000 claims description 6
- 238000001914 filtration Methods 0.000 claims description 6
- 238000003672 processing method Methods 0.000 claims description 6
- 239000006096 absorbing agent Substances 0.000 claims description 4
- 239000003500 flue dust Substances 0.000 claims description 4
- 238000011010 flushing procedure Methods 0.000 claims description 4
- 239000003595 mist Substances 0.000 claims description 3
- 230000001590 oxidative effect Effects 0.000 claims description 3
- 238000005201 scrubbing Methods 0.000 claims description 3
- 239000007921 spray Substances 0.000 claims description 3
- CPLXHLVBOLITMK-UHFFFAOYSA-N magnesium oxide Inorganic materials [Mg]=O CPLXHLVBOLITMK-UHFFFAOYSA-N 0.000 abstract description 15
- 230000008569 process Effects 0.000 abstract description 13
- 239000000428 dust Substances 0.000 abstract description 11
- 239000002699 waste material Substances 0.000 abstract description 9
- 239000000395 magnesium oxide Substances 0.000 abstract description 8
- 238000007599 discharging Methods 0.000 abstract description 5
- 230000009977 dual effect Effects 0.000 abstract description 2
- 238000004519 manufacturing process Methods 0.000 abstract description 2
- 239000006185 dispersion Substances 0.000 abstract 1
- WRUGWIBCXHJTDG-UHFFFAOYSA-L magnesium sulfate heptahydrate Chemical compound O.O.O.O.O.O.O.[Mg+2].[O-]S([O-])(=O)=O WRUGWIBCXHJTDG-UHFFFAOYSA-L 0.000 abstract 1
- AXZKOIWUVFPNLO-UHFFFAOYSA-N magnesium;oxygen(2-) Chemical compound [O-2].[Mg+2] AXZKOIWUVFPNLO-UHFFFAOYSA-N 0.000 abstract 1
- CSNNHWWHGAXBCP-UHFFFAOYSA-L Magnesium sulfate Chemical compound [Mg+2].[O-][S+2]([O-])([O-])[O-] CSNNHWWHGAXBCP-UHFFFAOYSA-L 0.000 description 20
- RAHZWNYVWXNFOC-UHFFFAOYSA-N Sulphur dioxide Chemical compound O=S=O RAHZWNYVWXNFOC-UHFFFAOYSA-N 0.000 description 18
- 229910052943 magnesium sulfate Inorganic materials 0.000 description 10
- 235000019341 magnesium sulphate Nutrition 0.000 description 10
- 230000023556 desulfurization Effects 0.000 description 8
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 8
- 238000005516 engineering process Methods 0.000 description 6
- 239000004744 fabric Substances 0.000 description 5
- JESHZQPNPCJVNG-UHFFFAOYSA-L magnesium;sulfite Chemical compound [Mg+2].[O-]S([O-])=O JESHZQPNPCJVNG-UHFFFAOYSA-L 0.000 description 5
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 description 4
- 239000003795 chemical substances by application Substances 0.000 description 4
- 230000009467 reduction Effects 0.000 description 4
- 230000008901 benefit Effects 0.000 description 3
- 229910002091 carbon monoxide Inorganic materials 0.000 description 3
- 239000003245 coal Substances 0.000 description 3
- 238000001816 cooling Methods 0.000 description 3
- 239000013078 crystal Substances 0.000 description 3
- 238000010586 diagram Methods 0.000 description 3
- 239000010440 gypsum Substances 0.000 description 3
- 229910052602 gypsum Inorganic materials 0.000 description 3
- 238000010438 heat treatment Methods 0.000 description 3
- VTHJTEIRLNZDEV-UHFFFAOYSA-L magnesium dihydroxide Chemical compound [OH-].[OH-].[Mg+2] VTHJTEIRLNZDEV-UHFFFAOYSA-L 0.000 description 3
- 239000000347 magnesium hydroxide Substances 0.000 description 3
- 229910001862 magnesium hydroxide Inorganic materials 0.000 description 3
- 238000012423 maintenance Methods 0.000 description 3
- 239000000463 material Substances 0.000 description 3
- 230000003647 oxidation Effects 0.000 description 3
- 238000007254 oxidation reaction Methods 0.000 description 3
- 239000000243 solution Substances 0.000 description 3
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 2
- VTYYLEPIZMXCLO-UHFFFAOYSA-L Calcium carbonate Chemical compound [Ca+2].[O-]C([O-])=O VTYYLEPIZMXCLO-UHFFFAOYSA-L 0.000 description 2
- 235000019738 Limestone Nutrition 0.000 description 2
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 2
- 239000005864 Sulphur Substances 0.000 description 2
- 238000005273 aeration Methods 0.000 description 2
- 238000004140 cleaning Methods 0.000 description 2
- 238000004891 communication Methods 0.000 description 2
- 238000011161 development Methods 0.000 description 2
- 230000007613 environmental effect Effects 0.000 description 2
- 239000003337 fertilizer Substances 0.000 description 2
- 239000013505 freshwater Substances 0.000 description 2
- 239000006028 limestone Substances 0.000 description 2
- 239000007787 solid Substances 0.000 description 2
- 238000003756 stirring Methods 0.000 description 2
- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 description 1
- 206010019233 Headaches Diseases 0.000 description 1
- CDBYLPFSWZWCQE-UHFFFAOYSA-L Sodium Carbonate Chemical compound [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 description 1
- 229910021529 ammonia Inorganic materials 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000001354 calcination Methods 0.000 description 1
- 239000011575 calcium Substances 0.000 description 1
- 229910052791 calcium Inorganic materials 0.000 description 1
- 229910000019 calcium carbonate Inorganic materials 0.000 description 1
- AXCZMVOFGPJBDE-UHFFFAOYSA-L calcium dihydroxide Chemical compound [OH-].[OH-].[Ca+2] AXCZMVOFGPJBDE-UHFFFAOYSA-L 0.000 description 1
- 239000000920 calcium hydroxide Substances 0.000 description 1
- 229910001861 calcium hydroxide Inorganic materials 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 238000002485 combustion reaction Methods 0.000 description 1
- 239000012141 concentrate Substances 0.000 description 1
- 239000004035 construction material Substances 0.000 description 1
- 238000000354 decomposition reaction Methods 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 238000001035 drying Methods 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 238000003912 environmental pollution Methods 0.000 description 1
- 239000000706 filtrate Substances 0.000 description 1
- 235000013312 flour Nutrition 0.000 description 1
- 231100000869 headache Toxicity 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 239000010842 industrial wastewater Substances 0.000 description 1
- 238000002347 injection Methods 0.000 description 1
- 239000007924 injection Substances 0.000 description 1
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- 238000004886 process control Methods 0.000 description 1
- 239000000047 product Substances 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
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- 230000000630 rising effect Effects 0.000 description 1
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- 238000004904 shortening Methods 0.000 description 1
- 239000002002 slurry Substances 0.000 description 1
- -1 stirs after 3 hours Substances 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 230000026676 system process Effects 0.000 description 1
Images
Classifications
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- 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
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
- Y02P20/129—Energy recovery, e.g. by cogeneration, H2recovery or pressure recovery turbines
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- Treating Waste Gases (AREA)
Abstract
The invention provides a treatment system and method of smoke. The method comprises the following steps: (1) introducing industrial smoke with the temperature of 120-420 DEG C into a gravity type heat pipe waste heat recovering device so as to reduce the temperature of the smoke to 100+/-10 DEG C; (2) introducing the smoke with the temperature of 100+/-10 DEG C into a low-pressure impulse bag-type dust collector for removing 95%-100% of dust, and reducing the temperature of the outlet of the dust collector to about 95+/-5 DEG C; (3) introducing the smoke with the temperature of 95+/-5 DEG C into a desulfurizer for reacting with atomized magnesium oxide; and (4) discharging the smoke after reaching a standard, and generating a desulfutation by-product MgSO4.7H2O. The system comprises the gravity type heat pipe waste heat recovering device, the low-pressure impulse bag-type dust collector and the desulfurizer, and seamless linkage is achieved through a dispersion control system. The whole process is smooth in joint and is convenient for operation, the dual purposes that energy in the smoke realizes step utilization and waste is changed into resources are achieved, and simultaneously, production and operation costs are greatly saved.
Description
Technical field
The present invention relates to field of environment protection, be specifically related to a kind of flue gas processing method and system.
Background technology
The environmental pollution of China is very serious.By coal supply, be the discharging rich and influential family of China atmosphere pollution so utilize coal-fired enterprise as power or power source due to the energy of China more than 70%.Discharging sulfur dioxide was approximately 3,000 ten thousand tons in 2003, accounted for more than 80% of national sulfur dioxide (SO2) emissions total amount.According to present discharge control level, to the year two thousand twenty, the sulfur dioxide that discharges after China's coal combustion will reach more than 4,000 ten thousand tons.If coal-fired atmosphere pollution can not get effective control, with directly having influence on the improvement of China's atmosphere quality and the sustainable development of industrial enterprise, even have influence on the sustainable development of following China economy.Wherein carbon monoxide and sulfur dioxide (SO2) emissions are one of primary pollution source of atmosphere pollution, various coal-fired furnaces (containing boiler of power plant) are the main emission sources of carbon monoxide and sulfur dioxide, the main way of administering at present this binomial discharging is residual heat integrative utilization (reducing the discharging of carbon monoxide as cogeneration) and the desulfurization of calcium method, but the work that difficulty of governance is large, initial cost is many, high these three key factors of running cost cause administering pollution runs into very large resistance, and a large amount of policies of the annual appearance of departments of government also are difficult to fundamentally address these problems.
in addition, present flue gas treatment technology, flue gas is not carried out unified planning, also not to the processing of classifying of the various compositions in flue gas, categorised collection, basically treat the head when the head aches, pin is cured the way of pin bitterly, as looking for today a technology to solve the problem of sulfur dioxide, look for again tomorrow company to solve the problem of dust pollution, the waste heat of feeling the day after tomorrow has problem, and just going for a company of doing waste heat again there emerged a scheme, the overlapping investment problem that causes is quite serious, also give follow-up smoke comprehensive utilization, the unified processing brings that the space is insufficient, corollary equipment needs the problems such as replacing back and forth.Can carry out unified planning, the unified recovery of processing, classify, utilize, turn waste into wealth step by step flue gas in the urgent need to a kind of technique in market.
Goal of the invention
In view of this, in order to overcome the deficiencies in the prior art, the invention provides a kind of flue gas processing method, the method can be carried out integrated treatment with rational step, controls substep by automation and utilizes, turns waste into wealth, and reduce running cost.
The invention provides a kind of flue gas processing method, described method comprises the steps: that the industrial smoke of (1) 120-420 ℃ enters the gravity-type heat pipe waste-heat recovery device, flue-gas temperature is down to 100 ± 10 ℃, (2) described 100 ± 10 ℃ of flue gases enter low pressure pulse bag filter and remove the 95%-100% dedusting, the deduster outlet temperature is down to 95 ± 5 ℃ of left and right, the flue gas of (3) 95 ± 5 ℃ enters desulfurizing tower and atomizing and oxidizing magnesium reacts, (4) flue gas qualified discharge, desulfuration byproduct generates MgSO47H2O; Described step is controlled by scattered control system.
The present invention also provides a kind of smoke processing system, and described system comprises: gravity-type heat pipe waste-heat recovery device, low pressure pulse bag filter and desulfurizing tower, and realize seamless link by scattered control system.
Further, described gravity-type heat pipe waste-heat recovery device adopts gravity type heat pipe, and heat pipe evaporator section is inserted in flue, and heat pipe condenser section is inserted in heat-conducting medium, by heat pipe, heat in flue gas is delivered to heat-conducting medium, 120-420 ℃ of flue-gas temperature is down to 100 ± 10 ℃.
Described gravity-type heat pipe waste-heat recovery device heat-conducting medium is the water of boiler feedwater, boiler replenishing water, heating circulation water or heat pump.
Further, described low pressure pulse bag filter is outside filtering type, dusty gas is entered the flue gas flow guiding device that is arranged in ash bucket and is passed through each filter chamber, unit by mozzle, clean gas after filtration sees through filter bag through upper box, discharged by exhaust duct through the off-line butterfly valve, the flue dust of 95%-100% in flue gas is removed.
Further, described filter bag upper end employing spring piston ring pattern.
The turn form is adopted in the filter bag upper end, and good seal performance, installation reliability are high, change bag quick.Only needing 1-2 people just can push up by machine just lifts the formula top cover and changes bag operation.The packing into and take out all and carry out at air-purifying chamber of filter bag, need not enter the deduster filter chamber.
Further, described desulfurizing tower is the countercurrent spray scrubbing tower, and described flue gas through waste heat recovery and low pressure pulse bag filter is sent into desulfurizing tower absorber portion bottom by booster fan, is discharged by top of tower.
Further, in described desulfurizing tower, column plate is from flushing type, and described desulfurizing tower is provided with three helical layer atomizer groups, and described desulfurizing tower is provided with spray-absorption liquid circulating pump and is connected with described spiral atomizer, and the demist section is set, but take off the flue gas qualified discharge after mist in tower.
Further, described smoke processing system comprises that also in desulfurizing tower, desulfuration byproduct generates MgSO
47H
2The reaction tank of O.
When the present invention reduces flue-gas temperature by heat pipe residual-heat recovery, improve the temperature of circulatory mediator, reclaimed a large amount of heat energy, saved mass energy consumption.Along with the reduction of flue-gas temperature, the operating mode exhaust gas volumn greatly reduces, and can save the materials such as flue, deduster, reduces the floor spaces such as flue, deduster, makes apparatus arrangement more compact flexibly.Flue gas is after the cooling of gravity-type heat pipe waste-heat recovery device, enter exhaust dust device with bag, because flue-gas temperature is reduced to 100 ℃ of left and right, this temperature alleviates much the infringement of cloth bag again, the raising cloth bag life-span, approximately more than 50%, efficiency of dust collection also was greatly enhanced simultaneously.
Sack cleaner has the efficiency of dust collection of the difficult analogy of other dedusters.Pure air after dedusting enters blower fan, can protect the impeller of blower fan not to be worn, and reduces the fouling of follow-up desulfurizing tower, guarantees the quality of desulfurizing byproduct.The dry ash that sack cleaner is taken off can be used as construction material and sells, and can reduce operating cost, has good economic worth.In this stage, because the present invention has dropped to flue-gas temperature below 120 ℃, so the dedusting filtrate can use cheap ordinary filter, greatly save the cost of buying high-temperature filter material cloth bag, for the user saves operation and maintenance expense.
The temperature of deduster outlet drops to 95 ℃ of left and right, the flue gas of 95 ℃ enters desulfurizing tower, temperature in this scope reacts with magnesia, the first efficient is very high, the speed of the second reaction is very fast, so greatly improve desulfuration efficiency, save the operating cost of desulfurizing tower, the desulfuration byproduct that forms after desulfurization can generate the MgSO41H2O of fertilizer grade or MgSO47H2O or the MgSO47H2O of technical grade by by-product plant.because in desulfurizing tower, byproduct provides satisfactory desulfurization waste liquor (magnesium hydroxide content 15%, the magnesium sulfite stable content is 35%, dust content is less than or equal to 10mg, waste liquid temperature is 40 ℃ of left and right), described desulfurization waste liquor is first deposited in reaction tank, and carry out secondary oxidation (aerated reaction), the air that uses during aeration reaches the air of 160 ℃ of left and right after as Steam Heating, magnesium sulfite after peroxidating, magnesium hydroxide, the adjustment that magnesium sulfate mixed solution carries out the pH value according to the size of pH value automatically by control system is adjusted to 7.8-9.2, add the mixed liquor that produces in sweetening process when high, add sulfuric acid when low.The solution that regulates carries out the nature cooling in reaction tank, and in ten minutes that lower the temperature after beginning, progressively add the magnesium sulfate crystal seed, when temperature drops to 60 ℃ of left and right, the stirring that continues prevents that in temperature-fall period, solidifying appears in solution, stirs after 3 hours, solution is imported separator, and it is the qualified epsom salt solid of output that drying is handled.
China's magnesium reserves are abundant, use magnesia as desulfurizing agent, and raw material is cheap and easy to get, meet China's actual conditions, compares with ammonia process, two alkaline process, soda method etc., and operating cost is lower, and economic advantages are obvious.Magnesium method desulfur technology is ripe, and technique is advanced, and Mg-base desulfurizing agent is to the flue gas strong adaptability, and desulfuration efficiency can reach more than 99.9%, is particularly suitable for the purification of China's sulphur coal flue gas.SO in magnesia and flue gas
2Reactivity substantially exceed calcium carbonate and calcium hydroxide, the liquid-gas ratio of tradition limestone/lime-gypsum method is many in 15 left and right, uses magnesia as desulfurizing agent, and liquid-gas ratio can be down to 2～3 left and right, can greatly save desulfurization water consumption and power consumption, the initiative and advantages of the localities that lack for water resource are more obvious.
Fouling in absorption tower and process pipe is one of problem of traditional limestone/lime-gypsum method maximum.The gypsum that oxidation generates, stable in properties is deposited in inside, absorption tower and process pipe in a large number, has greatly affected the normal operation of desulphurization system, even has an accident when serious.For solving scale problems, have to be equipped with the auxiliary device of large traffic monitoring device and other reduction scalings, technological process is very complicated.Through process modification of the present invention, because in flue-gas temperature reduction and flue gas, dirt is removed, so desulfurizing tower is wanted save area than general technology, reduce initial cost, the shortening in reaction time has reduced the power consumption of motor device such as desulfur pump, water pump etc., has saved the expenditure of the conventional energy resource expense such as electric power, water of run duration.Simultaneously, in desulfurizing tower, column plate is from flushing type, has thoroughly solved scale problems.
The byproduct magnesium sulfite that the desulfurization of magnesium method generates easily is oxidized to magnesium sulfate in air.Magnesium sulfate is important fertilizer, can be used for the multiple industries such as chemical industry, pharmacy, and approximately 3000 yuan/tons of market prices have very high economic worth.Magnesium method desulfurizing byproduct is produced magnesium sulfate and not only is recoverable to cost, also can create good economic benefit.Also can produce technical grade MgSO47HO by the byproduct recovery process, the existing market price is about 600 yuan/tons, and economic worth is very high.Magnesium sulfite also can decompose generation MgO and SO2 in 850 ℃ of heating and calcinings.MgO after decomposition can continue as the desulfurizing agent recycling, and the high concentration SO 2 of generation can sulfuric acid processed.
Complete in will be the originally single desulphurization problem of the present invention, dust removal problem, UTILIZATION OF VESIDUAL HEAT IN problem, the unification to of a byproduct recovery problem system, realize its seamless link by the DCS control system, under the technological guidance of residual heat resources cascade utilization, namely solve the problem of residual heat resources comprehensive utilization, service life is short in high temperature for a long time, the cloth bag replacing is frequent also to have solved the conventional cloth bag deduster, the higher difficult problem of the whole cost of use of deduster.Flue gas just is controlled in the optimum temperature range of sulphur and magnesia reaction through the temperature after exhaust heat stepped utilization, also reduce the initial cost of desulfurizing tower when improving desulfuration efficiency, and most suitable material proportion ratio is provided for the epsom salt conversion process of back.
Beneficial effect of the present invention is:
1. flue gas processing method of the present invention reclaims four major parts by flue gas waste heat recovery-bag-type dusting-wet-type magnesium method desulfurization-byproduct and forms that (figure one: product process flow figure).The simple science of a whole set of technique, linking smoothness, operation facilitate, applicability is strong, recovery waste heat and desulfuration byproduct when administering flue gas, make the energy in flue gas obtain cascade utilization, sensible heat and latent heat in a large amount of recovered flue gas, reach the dual purpose of energy-saving and emission-reduction, changing waste into resources, save simultaneously the operation and maintenance cost of gas cleaning (environmental protection) system to the owner, greatly saved production and operation cost.
2. smoke processing system of the present invention, realize whole method flow by integrated DCS control module, when flue-gas temperature when a certain process section is too high or too low, can realize step by step the adjusting to temperature, find that as flour bag deduster section temperature surpasses 120 ℃ or during lower than 95 ℃, DCS controls the rate-of flow that can directly strengthen the waste heat recovery section, reduction or rising that increase or minimizing by flow realizes temperature, thereby the quality of guaranteeing final byproduct epsom salt is consistent all the time, this point more has actual using value than other invention of single desulfuration byproduct recovery process on present market, also can fundamentally guarantee the stable and operation of whole system, reduce the human cost of the operation maintenance aspect of whole system, the whole system all-pass is crossed the DCS operation, manpower reduces over half than conventional system.
Description of drawings
Fig. 1: be the inventive method flow chart
Fig. 2: be gravity-type heat pipe residual-heat recovery structural representation
Fig. 3: be the low pressure pulse bag filter schematic diagram.
Fig. 4: be the low pressure pulse bag filter longitudinal sectional drawing.
Fig. 5: be the attached view of low pressure pulse bag filter.
Fig. 6: be the spring piston ring structural representation.
Fig. 7: be gravity-type heat pipe residual-heat recovery, low pressure pulse bag filter and desulfurizing tower combination assumption diagram
Fig. 8: be the Structure of Flue Gas Desulfuration Absorbing schematic diagram.
Wherein: the upper flip 12-supporting leg 13-mozzle 14-15-of the filter chamber filter bag 16-off-line valve 17-exhaust duct 18-spring piston ring 19-waste-heat recovery device 20-sack cleaner 21-booster fan 22-absorber portion bottom 23-tower top 24-atomizer 25-absorption liquid circulating pump 26-demist section 27-desulfurizing tower of casing 8-air intake 9-dusty gas 10-ash bucket 11-in 1-flue 2-heat pipe 3-heat-conducting medium 4-gas bag winding-up combination 5-lift valve combination 6-upper box 7-.
The specific embodiment
Further illustrate in the following embodiments the present invention, this does not limit the scope of the invention.
Embodiment 1
Use flue gas processing method of the present invention as example take Jincheng Paper Mill, Liaoning Prov.:
The industrial smoke of 380 ℃ enters gravity-type heat pipe waste-heat recovery device 19, and described gravity-type heat pipe waste-heat recovery device heat-conducting medium is boiler feedwater.Flue-gas temperature is down to 100 ℃, described 100 ℃ of flue gases enter low pressure pulse bag filter 20, low pressure pulse bag filter is outside filtering type, dusty gas is entered the flue gas flow guiding device that is arranged in ash bucket and is filtered by each filter chamber, unit by mozzle 13, the spring piston ring pattern is adopted in described filter bag 15 upper ends, clean gas after filtration sees through filter bag through upper box, is discharged by exhaust duct 17 through the off-line butterfly valve, and 97% flue dust in flue gas is removed.The deduster outlet temperature is down to 98 ℃ of left and right, and the dedusting flue gas of 98 ℃ enters desulfurizing tower 27 and reacts with atomizing and oxidizing magnesium.
Desulfurizing tower 27 is the countercurrent spray scrubbing tower, sends into desulfurizing tower absorber portion bottom through the flue gas of waste heat recovery and low pressure pulse bag filter by booster fan 21, is discharged by top of tower 23.In desulfurizing tower 27, column plate is from flushing type, is provided with three helical layer atomizer groups 24 in tower, and is provided with spray-absorption liquid circulating pump 25 and is connected with described spiral atomizer 24, and demist section 26 is set in tower, but takes off the flue gas qualified discharge after mist.Reaction by-product in desulfurizing tower provides satisfactory desulfurization waste liquor (magnesium hydroxide content 15%, magnesium sulfite content 35%, dust content is less than or equal to 10mg, waste liquid temperature is 40 ℃ of left and right), through aeration in reaction tank, pH is adjusted to 8.0, naturally add the magnesium sulfate crystal seed after the cooling, autocoagulation generates the epsom salt crystal grain, carries out being packaged into bag after Separation of Solid and Liquid through centrifuge.
Above-mentioned steps is controlled by scattered control system.Scattered control system is a multi-level computer system take communication network as tie that is comprised of process control level and process monitoring level, combine computer, the technology such as communication, demonstration and control, its basic thought is distributed collection switching value and analog signals, concentrates and carry out data processing, configuration demonstration, differentiated control, decentralised control, easy to operate.
First paragraph gravity-type heat pipe waste-heat recovery device is controlled electrically operated valve by temperature and feedwater flow feedback signal that collection is returned, reaches the optimum state of feed temperature value.
The second segment low pressure pulse bag filter, before the deduster of returning by collection, temperature determines whether and puts into operation, and triggers the deduster cleaning cycle according to pressure difference signal before and after deduster, and processes decentralised control pulse valve deashing by data.
The 3rd section desulphurization system by the signal that the instrument such as liquid level, pressure, flow, temperature, pH meter feed back, effectively controlled the desulfurization slurry injection rate, discharges fresh water (FW) (the industrial waste water that namely meets environmental emission standard).
The 4th section byproduct recovery system processes to realize up time by-pass valve control, dewaterer through intensive data, and the equipment such as oxidation fan, water pump produce high-quality MgSO47H2O.
Although by reference some preferred embodiment of the present invention, invention has been described, but those of ordinary skill in the art is to be understood that, can make various changes to it in the form and details, and not depart from the spirit and scope of the present invention that appended claims limits.
Claims (4)
1. flue gas processing method, it is characterized in that, described method comprises the steps: that the industrial smoke of (1) 380-420 ℃ enters the gravity-type heat pipe waste-heat recovery device, flue-gas temperature is down to 100 ± 10 ℃, (2) described 100 ± 10 ℃ of flue gases enter low pressure pulse bag filter and remove the 95%-100% flue dust, the deduster outlet temperature is down to 95 ± 5 ℃, the flue gas of (3) 95 ± 5 ℃ enters desulfurizing tower and atomizing and oxidizing magnesium reacts, (4) flue gas qualified discharge, desulfuration byproduct generates MgSO
47H
2O； Described step is controlled by scattered control system.
2. a smoke processing system, is characterized in that, described system comprises: gravity-type heat pipe waste-heat recovery device, low pressure pulse bag filter and desulfurizing tower, and realize seamless link successively by scattered control system;
Described gravity-type heat pipe waste-heat recovery device adopts gravity type heat pipe, and heat pipe evaporator section is inserted in flue, and heat pipe condenser section is inserted in heat-conducting medium, by heat pipe, heat in flue gas is delivered to heat-conducting medium, and 380-420 ℃ of flue-gas temperature is down to 100 ± 10 ℃;
Described low pressure pulse bag filter is outside filtering type, dusty gas is entered the flue gas flow guiding device that is arranged in ash bucket and is passed through each filter chamber, unit by mozzle, clean gas after filtration sees through filter bag through upper box, discharged by exhaust duct through the off-line butterfly valve again, the flue dust of 95%-100% in flue gas is removed;
Described desulfurizing tower is the countercurrent spray scrubbing tower, sends into desulfurizing tower absorber portion bottom through the flue gas of waste heat recovery and low pressure pulse bag filter by booster fan, is discharged by top of tower;
In described desulfurizing tower, column plate is from flushing type, and described desulfurizing tower is provided with three helical layer atomizer groups, and described desulfurizing tower is provided with spray-absorption liquid circulating pump and is connected with described spiral atomizer group, and the demist section is set in tower, takes off the flue gas qualified discharge after mist.
3. according to smoke processing system claimed in claim 2, it is characterized in that described filter bag upper end employing spring piston ring pattern.
4. according to smoke processing system claimed in claim 2, it is characterized in that, described smoke processing system comprises that also in desulfurizing tower, desulfuration byproduct generates MgSO
47H
2The reaction tank of O.
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| US20140072483A1 (en) * | 2012-09-10 | 2014-03-13 | Mitsubishi Heavy Industries, Ltd. | Desulfurization device and particulate collection system |
| CN113842767A (en) * | 2021-10-23 | 2021-12-28 | 安徽省华鑫铅业集团有限公司 | Tail gas treatment method based on gravity and pulse bag type dust removal |
Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1710328A (en) * | 2005-07-01 | 2005-12-21 | 煤炭科学研究总院北京煤化工研究分院 | Medium and small sized industrial pulverized-coal fired boiler |
| EP1649922A1 (en) * | 2003-07-10 | 2006-04-26 | Taiheiyo Cement Corporation | Device and method for processing combustion exhaust gas |
| CN1995823A (en) * | 2006-12-30 | 2007-07-11 | 中国科学院电工研究所 | Flue gas heater by evaporative cooling |
| CN101073744A (en) * | 2006-09-13 | 2007-11-21 | 童裳慧 | Integrating apparatus fo magnesium oxide with desulfurizing, dust-collecting and energy-saving functions and its production |
| CN101301574A (en) * | 2008-01-18 | 2008-11-12 | 北京博奇电力科技有限公司 | Multistage flue gas desulfurization spray tower |
| CN201353463Y (en) * | 2009-01-20 | 2009-12-02 | 清华同方(鞍山)环保设备股份有限公司 | Long bag low-pressure pulse bag filter |
| CN202074540U (en) * | 2011-05-11 | 2011-12-14 | 北京世能中晶能源科技有限公司 | Exhaust gas treatment system |
Family Cites Families (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS58164923A (en) * | 1982-03-24 | 1983-09-29 | Babcock Hitachi Kk | Treating device for exhaust gas |
-
2011
- 2011-05-11 CN CN2011101218749A patent/CN102230635B/en active Active
Patent Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP1649922A1 (en) * | 2003-07-10 | 2006-04-26 | Taiheiyo Cement Corporation | Device and method for processing combustion exhaust gas |
| CN1710328A (en) * | 2005-07-01 | 2005-12-21 | 煤炭科学研究总院北京煤化工研究分院 | Medium and small sized industrial pulverized-coal fired boiler |
| CN101073744A (en) * | 2006-09-13 | 2007-11-21 | 童裳慧 | Integrating apparatus fo magnesium oxide with desulfurizing, dust-collecting and energy-saving functions and its production |
| CN1995823A (en) * | 2006-12-30 | 2007-07-11 | 中国科学院电工研究所 | Flue gas heater by evaporative cooling |
| CN101301574A (en) * | 2008-01-18 | 2008-11-12 | 北京博奇电力科技有限公司 | Multistage flue gas desulfurization spray tower |
| CN201353463Y (en) * | 2009-01-20 | 2009-12-02 | 清华同方(鞍山)环保设备股份有限公司 | Long bag low-pressure pulse bag filter |
| CN202074540U (en) * | 2011-05-11 | 2011-12-14 | 北京世能中晶能源科技有限公司 | Exhaust gas treatment system |
Non-Patent Citations (1)
| Title |
|---|
| JP昭58-164923A 1983.09.29 |
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