CN213656805U - A large-scale thermal power unit flue gas activated coke purification system - Google Patents
A large-scale thermal power unit flue gas activated coke purification system Download PDFInfo
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- CN213656805U CN213656805U CN202022597101.5U CN202022597101U CN213656805U CN 213656805 U CN213656805 U CN 213656805U CN 202022597101 U CN202022597101 U CN 202022597101U CN 213656805 U CN213656805 U CN 213656805U
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- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 title claims abstract description 52
- 239000003546 flue gas Substances 0.000 title claims abstract description 52
- 239000000571 coke Substances 0.000 title claims abstract description 32
- 238000000746 purification Methods 0.000 title claims abstract description 14
- 238000001816 cooling Methods 0.000 claims abstract description 31
- 238000006477 desulfuration reaction Methods 0.000 claims abstract description 31
- 230000023556 desulfurization Effects 0.000 claims abstract description 31
- 239000007921 spray Substances 0.000 claims abstract description 28
- 238000007791 dehumidification Methods 0.000 claims abstract description 25
- 239000002918 waste heat Substances 0.000 claims abstract description 20
- 238000011084 recovery Methods 0.000 claims abstract 10
- 239000000428 dust Substances 0.000 claims description 19
- 238000005057 refrigeration Methods 0.000 claims description 5
- 239000000126 substance Substances 0.000 abstract description 7
- 239000012717 electrostatic precipitator Substances 0.000 abstract 2
- RAHZWNYVWXNFOC-UHFFFAOYSA-N Sulphur dioxide Chemical compound O=S=O RAHZWNYVWXNFOC-UHFFFAOYSA-N 0.000 description 18
- AKEJUJNQAAGONA-UHFFFAOYSA-N sulfur trioxide Chemical compound O=S(=O)=O AKEJUJNQAAGONA-UHFFFAOYSA-N 0.000 description 16
- 238000003795 desorption Methods 0.000 description 15
- 239000003344 environmental pollutant Substances 0.000 description 8
- 230000006872 improvement Effects 0.000 description 8
- 231100000719 pollutant Toxicity 0.000 description 8
- 238000000034 method Methods 0.000 description 7
- MWUXSHHQAYIFBG-UHFFFAOYSA-N Nitric oxide Chemical compound O=[N] MWUXSHHQAYIFBG-UHFFFAOYSA-N 0.000 description 6
- 230000007613 environmental effect Effects 0.000 description 6
- 238000001179 sorption measurement Methods 0.000 description 6
- 230000008569 process Effects 0.000 description 5
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 5
- 229910002651 NO3 Inorganic materials 0.000 description 4
- NHNBFGGVMKEFGY-UHFFFAOYSA-N Nitrate Chemical compound [O-][N+]([O-])=O NHNBFGGVMKEFGY-UHFFFAOYSA-N 0.000 description 4
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 4
- QSHDDOUJBYECFT-UHFFFAOYSA-N mercury Chemical compound [Hg] QSHDDOUJBYECFT-UHFFFAOYSA-N 0.000 description 4
- 229910052753 mercury Inorganic materials 0.000 description 4
- 239000011593 sulfur Substances 0.000 description 4
- 229910052717 sulfur Inorganic materials 0.000 description 4
- 230000009466 transformation Effects 0.000 description 3
- HGUFODBRKLSHSI-UHFFFAOYSA-N 2,3,7,8-tetrachloro-dibenzo-p-dioxin Chemical compound O1C2=CC(Cl)=C(Cl)C=C2OC2=C1C=C(Cl)C(Cl)=C2 HGUFODBRKLSHSI-UHFFFAOYSA-N 0.000 description 2
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 2
- 239000003245 coal Substances 0.000 description 2
- 239000010440 gypsum Substances 0.000 description 2
- 229910052602 gypsum Inorganic materials 0.000 description 2
- 239000010802 sludge Substances 0.000 description 2
- 235000019738 Limestone Nutrition 0.000 description 1
- XSQUKJJJFZCRTK-UHFFFAOYSA-N Urea Chemical compound NC(N)=O XSQUKJJJFZCRTK-UHFFFAOYSA-N 0.000 description 1
- 238000003915 air pollution Methods 0.000 description 1
- 229910021529 ammonia Inorganic materials 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 239000004202 carbamide Substances 0.000 description 1
- 239000003054 catalyst Substances 0.000 description 1
- 238000010531 catalytic reduction reaction Methods 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 238000002485 combustion reaction Methods 0.000 description 1
- 238000004891 communication Methods 0.000 description 1
- 238000005536 corrosion prevention Methods 0.000 description 1
- 238000013461 design Methods 0.000 description 1
- 238000011161 development Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 239000006028 limestone Substances 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 238000011160 research Methods 0.000 description 1
- 230000002195 synergetic effect Effects 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
- 239000002351 wastewater Substances 0.000 description 1
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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
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E20/00—Combustion technologies with mitigation potential
- Y02E20/30—Technologies for a more efficient combustion or heat usage
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- Treating Waste Gases (AREA)
Abstract
本实用新型公开了一种大型火电机组烟气活性焦净化系统，包括省煤器以及预热器，省煤器与预热器的入口相连，预热器的出口与分布式低温省煤器的入口相连通，分布式低温省煤器的出口分别与分室低温电除尘器的入口相连通，分室低温电除尘器的出口与余热回收器的入口相连通，余热回收器的出口与喷淋冷却塔的入口相连通，喷淋冷却塔的出口经直通烟道与多分仓流化床脱硫除湿塔的入口相连通，多分仓流化床脱硫除湿塔的出口与蒸发冷却器的入口连通，蒸发冷却器的出口与多分仓超低温流化床脱硝塔的入口相连通。本实用新型占地面积和投资非常合理，不仅可以完全脱除烟气中的NOx和SO2，还能够完全脱除SO3及Hg等有害物质，脱出效率极高。
The utility model discloses a flue gas active coke purification system for a large thermal power unit, which comprises an economizer and a preheater. The economizer is connected to the inlet of the preheater, and the outlet of the preheater is connected to the outlet of the distributed low temperature economizer. The inlet is connected, the outlet of the distributed low-temperature economizer is connected with the inlet of the sub-chamber low-temperature electrostatic precipitator, the outlet of the sub-chamber low-temperature electrostatic precipitator is communicated with the inlet of the waste heat recovery device, and the outlet of the waste heat recovery device is connected with the spray cooling tower The inlet of the spray cooling tower is connected with the inlet of the multi-silo fluidized bed desulfurization and dehumidification tower through the straight-through flue, and the outlet of the multi-segment fluidized bed desulfurization and dehumidification tower is connected with the inlet of the evaporative cooler. The outlet of the multi-silo is connected with the inlet of the ultra-low temperature fluidized bed denitrification tower. The utility model occupies a very reasonable area and investment, can not only completely remove NOx and SO2 in the flue gas, but also can completely remove harmful substances such as SO3 and Hg , and the removal efficiency is extremely high.
Description
Technical Field
The utility model belongs to the technical field of thermal power unit flue gas pollutant desorption, a active burnt clean system of large-scale thermal power unit flue gas is related to.
Background
In the field of flue gas emission control of large-scale thermal power generating units, China currently executes the strictest ultra-low emission policy in the world and requires that the emission concentration of nitrogen oxide is less than 50mg/m3(Standard, dry, 6% O)2) The emission concentration of sulfur dioxide is less than 35mg/m3(Standard, dry, 6% O)2). At present, large-scale thermal power generating units at home and abroad generally adopt an SCR (selective catalytic reduction) or SNCR + SCR denitration process and a limestone-gypsum wet desulphurization process.
However, because of the limited natural environment of China, the amount of industry is huge, the work of preventing and controlling air pollution is still far in the way, and the research on the treatment technology of flue gas pollution is endless.
The SCR mainstream process scheme adopted by the existing denitration is that a denitration device is arranged behind an economizer and in front of an air preheater, so that the operation cost is high, and a large amount of ammonia or urea is consumed; the problems that the waste generated after the service life of the catalyst generates secondary pollution to the environment and the like are urgently needed to be solved; the denitration efficiency is difficult to break through the level of 94 percent, the full-load denitration requirement cannot be met, and the like, and the new requirement of people for improving the environment cannot be met technically.
The wet desulphurization process scheme adopted by the existing desulphurization needs to consume a very large amount of limestone; the utilization rate of the byproduct gypsum is lower and lower; the treatment difficulty and the cost of the desulfurization wastewater are very high; and the sulfur dioxide can not be completely removed.
In addition, the existing denitration and desulfurization processes are completely and independently designed, the synergistic removal efficiency is very low, and the removal efficiency of harmful substances such as sulfur trioxide and mercury in the flue gas is not high.
SUMMERY OF THE UTILITY MODEL
An object of the utility model is to overcome above-mentioned prior art's shortcoming, provide a large-scale thermal power generating unit flue gas active coke clean system, can carry out the desorption to all harmful substance in the flue gas, the desorption efficiency is high.
In order to achieve the above purpose, the utility model adopts the following technical scheme:
a flue gas active coke purification system of a large thermal power generating unit comprises a distributed low-temperature economizer, a chamber-divided low-temperature dust collector, a waste heat recoverer, a spray cooling tower, a multi-chamber fluidized bed desulfurization and dehumidification tower, a multi-chamber ultralow-temperature fluidized bed denitration tower, an economizer and a preheater;
the economizer is connected with an inlet of the preheater, an outlet of the preheater is communicated with an inlet of the distributed low-temperature economizer, an outlet of the distributed low-temperature economizer is respectively communicated with an inlet of the chamber-divided low-temperature dust remover, an outlet of the chamber-divided low-temperature dust remover is communicated with an inlet of the waste heat recoverer, an outlet of the waste heat recoverer is communicated with an inlet of the spray cooling tower, an outlet of the spray cooling tower is communicated with an inlet of the multi-chamber fluidized bed desulfurization and dehumidification tower through a direct flue, an outlet of the multi-chamber fluidized bed desulfurization and dehumidification tower is communicated with an inlet of the evaporative cooler, and an outlet of the evaporative cooler is communicated with an inlet of the multi-chamber ultralow-temperature fluidized bed denitration tower.
The utility model discloses further improvement lies in, the export of pre-heater collects the flue through high temperature and is linked together with the entry of distributing type low temperature economizer.
The utility model discloses further improvement lies in, and the export of locellus low temperature dust remover is linked together with waste heat recoverer's entry after gathering the flue.
The utility model discloses further improvement lies in, waste heat recoverer's export is linked together through the entry that communicates flue and spray cooling tower.
The utility model discloses further improvement lies in, still includes cold volume recoverer, draught fan and dry chimney, and the export of many minutes storehouse ultra-low temperature fluidized bed denitration towers is linked together through the entry of ultra-clean ultra-low temperature flue with cold volume recoverer, and the play and the draught fan entry of cold volume recoverer are linked together, and the draught fan export is through the entry intercommunication of ultra-clean flue with dry chimney.
The utility model discloses further improvement lies in, and the export of dividing storehouse fluidized bed desulfurization dehumidification tower more is linked together through the entry of clean flue and evaporative cooler, and evaporative cooler's export is linked together through the entry of clean flue of ultra-low temperature and dividing storehouse ultra-low temperature fluidized bed denitration tower more.
The utility model discloses further improvement lies in, divide storehouse fluidized bed desulfurization dehumidification tower more still be connected with first active burnt warehouse, divide storehouse ultra-low temperature fluidized bed denitration tower more still to be connected with the active burnt warehouse of second.
The utility model discloses a further improvement lies in, and the spray cooling tower is connected with the spray cooling circulating pump.
The utility model discloses further improvement lies in, evaporative cooler is connected with compressor and cold water machine.
Compared with the prior art, the utility model discloses following beneficial effect has:
the utility model discloses a denitration adsorption tower arrange high temperature, high dust region before air heater unlike traditional SCR denitrification facility, but arrange behind many minutes storehouse fluidized bed desulfurization dehumidification towers, do not have special requirement to the high temperature of flue gas temperature, thoroughly solved full load denitration difficult problem.
Further, the utility model discloses a two-stage divides storehouse fluidized bed desulfurization dehumidification tower more and divides storehouse ultra-low temperature fluidized bed denitration tower to deviate from the pollutant in grades, and it is high to deviate from efficiency, divides moreWhen the bin adsorption tower works in practice, one or more sub-bins of the bin adsorption tower are in an operation mode, the other sub-bins of the adsorption tower are in an analysis mode, and the adsorption tower and a matched sulfur-containing active coke analysis tower and a matched nitrate-containing active coke analysis tower work together to realize continuous desorption and analysis treatment of flue gas and realize SO2、SO3、NOxAnd resolving and recycling harmful substances such as Hg and dioxin generated in the mixed combustion of sludge, so as to realize resource utilization.
Active burnt clean system of large-scale thermal power generating unit flue gas when concrete operation, high temperature flue gas need not through SCR denitration reactor after the economizer in proper order, and directly get into the pre-heater, all environmental protection facility equipartitions are put after the pre-heater, need not to increase any equipment or carry out any transformation at the former economizer of unit to the flue of pre-heater department. The flue gas gets into locular low temperature dust remover behind low temperature economizer and removes dust, it further reduces the flue gas temperature to above zero below the ambient temperature to go into spray cooling tower after waste heat recoverer cooling again, sulfur dioxide in the flue gas simultaneously, sulfur trioxide carries out desorption in advance, later get into many minutes storehouse fluidized bed desulfurization dehumidification tower and adsorb the desulfurization, later get into in the evaporative cooler and cool down to below zero, it adsorbs the denitration to get into many minutes storehouse ultra-low temperature fluidized bed denitration tower again, simultaneously to remaining sulfur dioxide in the flue gas, sulfur trioxide, harmful substance such as mercury adsorbs the desorption. Because the flue gas temperature drops, the flue gas volume reduces by a wide margin for pollutant desorption equipment size reduces by a wide margin, and simultaneously, the flue gas temperature reduces to below the dew point of flue gas pollutant, and the pollutant is deviate from efficiency and is improved by a wide margin, can realize the target of harmful substance zero release such as nitrogen oxide, sulfur dioxide, sulfur trioxide and mercury in the flue gas, and the desorption is efficient, and area and investment cost are low more reasonable relatively. The utility model discloses a denitration adsorption tower arrange high temperature, high dust region before air heater unlike traditional SCR denitrification facility, but arrange behind many minutes storehouse fluidized bed desulfurization dehumidification towers, do not have special requirement to the high temperature of flue gas temperature, thoroughly solved full load denitration difficult problem.
Drawings
Fig. 1 is a schematic plan view of the present invention.
Fig. 2 is a side view development flow chart of the present invention.
The system comprises a distributed low-temperature coal economizer 1, a chambered low-temperature dust remover 2, a waste heat recoverer 3, a spray cooling tower 4, a multi-bin fluidized bed desulfurization and dehumidification tower 5, an evaporative cooler 6, a multi-bin ultralow-temperature fluidized bed denitration tower 7, a cold energy recoverer 8, an induced draft fan 9, a dry chimney 10, a high-temperature collecting flue 11, a collecting flue 12, a communicating flue 13, a through flue 14, a clean flue 15, a low-temperature clean flue 16, an ultra-clean ultralow-temperature flue 18, an ultra-clean flue 21, a coal economizer 22, a preheater 23, a first active coke storage bin 24, a second active coke storage bin 24, a sulfur-containing active coke analysis tower 25, a nitrate-containing active coke analysis tower 26, a spray cooling circulating pump 27, a refrigeration compressor 28 and a water chiller 29.
Detailed Description
The present invention will be described in further detail with reference to the accompanying drawings:
referring to fig. 1 and 2, the flue gas active coke purification system of the large thermal power generating unit of the present invention includes a distributed low-temperature economizer 1, a chambered low-temperature dust remover 2, a waste heat recoverer 3, and a spray cooling tower 4; the device comprises a multi-bin fluidized bed desulfurization and dehumidification tower 5, an evaporative cooler 6, a multi-bin ultralow-temperature fluidized bed denitration tower 7, a cold energy recoverer 8, an induced draft fan 9, a dry chimney 10, a high-temperature collection chimney 11, a collection chimney 12, a communication chimney 13, a straight-through chimney 14, a clean chimney 15, a low-temperature clean chimney 16, a super-clean ultralow-temperature chimney 17, a super-clean chimney 18, an economizer 21, a preheater 22, a first active coke storage bin 23, a second active coke storage bin 24, a sulfur-containing active coke desorption tower 25, a nitrate-containing active coke desorption tower 26, a spray cooling circulating pump 27, a refrigeration compressor 28 and a water chiller 29.
Wherein, the economizer 21 is connected with the inlet of the preheater 22, the outlet of the preheater 22 is communicated with the inlet of the distributed low-temperature economizer 1 through the high-temperature collecting flue 11, the outlet of the distributed low-temperature economizer 1 is respectively communicated with the inlet of the chamber-divided low-temperature dust remover 2, the outlet of the chamber-divided low-temperature dust remover 2 is communicated with the inlet of the waste heat recoverer 3 through the collecting flue 12, the outlet of the waste heat recoverer 3 is communicated with the inlet of the spray cooling tower 4 through the communicating flue 13, the outlet of the spray cooling tower 4 is communicated with the inlet of the multi-chamber fluidized bed desulfurization and dehumidification tower 5 through the direct flue 14, the outlet of the multi-chamber fluidized bed desulfurization and dehumidification tower 5 is communicated with the inlet of the evaporative cooler 6 through the clean flue 15, the outlet of the evaporative cooler 6 is communicated with the inlet of the multi-chamber ultra-low-temperature denitration tower 7 through the ultra-clean flue 16, the outlet of the multi-chamber ultra-low-temperature fluidized bed denitration tower, the outlet of the cold energy recoverer 8 is communicated with the inlet of an induced draft fan 9, and the outlet of the induced draft fan 9 is communicated with the inlet of a dry chimney 10 through an ultra-clean flue 18.
The first active coke storage bin 23, the second active coke storage bin 24, the sulfur-containing active coke desorption tower 25 and the nitrate-containing active coke desorption tower 26 which are matched with the multi-bin fluidized bed desulfurization and dehumidification tower 5 and the multi-bin ultralow-temperature fluidized bed denitration tower 7, a spray cooling circulating pump 27 matched with the spray cooling tower 4, a refrigeration compressor 28 and a water chiller 29 matched with the evaporative cooler 6. Namely, the multi-bin fluidized bed desulfurization and dehumidification tower 5 is connected with a first active coke storage bin 23, and the multi-bin ultralow temperature fluidized bed denitration tower 7 is connected with a second active coke storage bin 24; the spray cooling tower 4 is connected with a spray cooling circulation pump 27, and the evaporative cooler 6 is connected with a refrigeration compressor 28 and a water chiller 29.
The utility model discloses in the high temperature flue gas that comes out by the boiler passes through distributed low temperature economizer 1 back in proper order, need not through SCR denitration reactor and directly gets into air heater, all environmental protection facility equipartitions are put after pre-heater 22, need not to increase any equipment or carry out any transformation at the flue of former economizer 21 to pre-heater 22 department, and all environmental protection facility equipartitions are put after the pre-heater.
The multi-bin ultra-low temperature fluidized bed denitration tower 7 is arranged behind an air preheater of a thermal power generating unit and at the position of an ultra-low temperature clean flue 16.
The induced draft fan 9 is arranged behind the desulfurization facility and the denitration facility and in front of the chimney.
The flue gas of the thermal power generating unit is the ultra-clean emission of dry flue gas, and the anticorrosion modification treatment of a dry chimney is not needed.
The purification method of the utility model is as follows: flue gas of a large thermal power generating unit sequentially passes through an economizer 21 and a preheater 22 and then passes through a high-temperature collecting flue 11 to an inlet of a distributed low-temperature economizer 1, an outlet of the distributed low-temperature economizer 1 is respectively communicated with an inlet of a chamber low-temperature dust collector 2, the flue gas is dedusted in the chamber low-temperature dust collector 2, an outlet of the chamber low-temperature dust collector 2 is communicated with an inlet of a waste heat recoverer 3 through a collecting flue 12 and is cooled in the waste heat recoverer 3, an outlet of the waste heat recoverer 3 is communicated with an inlet of a spray cooling tower 4 through a communicating flue 13, the temperature is reduced to be below zero in the spray cooling tower 4, sulfur dioxide and sulfur trioxide in the flue gas are pre-removed, an outlet of the spray cooling tower 4 is communicated with an inlet of a multi-chamber fluidized bed desulfurization and dehumidification tower 5 through a flue through a direct connection 14, and desulfurization is absorbed in the multi-chamber fluidized bed desulfurization and dehumidification, the export of many minute storehouse fluidized bed desulfurization dehumidification towers 5 communicates through the entry of clean flue 15 with evaporative cooler 6, and the flue gas continues to cool down to below zero in evaporative cooler 6, and evaporative cooler 6's export is linked together through the entry of the clean flue 16 of ultra-low temperature and the many minute storehouse ultra-low temperature fluidized bed denitration tower 7 of ultra-low temperature, adsorbs the denitration in many minute storehouse ultra-low temperature fluidized bed denitration tower 7, adsorbs the desorption to remaining sulfur dioxide, sulfur trioxide, mercury in the flue gas simultaneously. The outlet of the multi-bin ultra-low temperature fluidized bed denitration tower 7 is communicated with the inlet of the cold energy recoverer 8 through the ultra-clean ultra-low temperature flue 17, the outlet of the cold energy recoverer 8 is communicated with the inlet of the induced draft fan 9, and the outlet of the induced draft fan 9 is communicated with the inlet of the dry chimney 10 through the ultra-clean flue 18.
The utility model discloses an active burnt clean system of large-scale thermal power unit flue gas need not to increase any equipment or carry out any transformation at the flue of former economizer 21 to air heater 22 department, and all environmental protection facilities equipartition are put after air heater 22.
The ultra-low temperature fluidized bed denitration tower 7 with multiple divided bins is arranged behind an air preheater of a thermal power generating unit, and the position of an ultra-low temperature clean flue 16 thoroughly solves the problems that the SCR denitration is easy to block ash, the denitration efficiency is low, and full-load denitration cannot be solved. The induced draft fan is arranged behind the desulfurization device and the denitrification device. The flue gas of the utility model is the ultra-clean emission of dry flue gas, and the corrosion prevention treatment of a dry chimney is not needed.
The utility model provides a brand-new flue gas pollutant treatment system of large-scale thermal power generating unit, area and investment are very reasonable, not only can desorption NO in the flue gas completelyxAnd SO2And can also completely remove SO3And HgAnd harmful substances such as dioxin and the like generated when the sludge is doped and burned, the removal efficiency is extremely high, and the complete removal of pollutants can be realized theoretically. The method is suitable for the design of an environmental protection island of a newly-built large thermal power generating unit and the upgrading and reconstruction of flue gas treatment, and has good scientific and technological value and economic and environmental benefits when being popularized in a large thermal power plant.
The utility model provides a brand-new flue gas pollutant treatment system of large-scale thermal power generating unit, area and investment are very reasonable, not only can desorption NO in the flue gas completelyxAnd SO2And can also completely remove SO3And HgAnd the removal efficiency is extremely high.
Above only for explaining the technical thought of the utility model, can not prescribe a limit to with this the utility model discloses a protection scope, the fan is according to the utility model provides a technical thought, any change of doing on technical scheme basis all fall into within the protection scope of the utility model.
Claims (9)
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN112268293A (en) * | 2020-11-11 | 2021-01-26 | 西安热工研究院有限公司 | A system and method for purifying active coke from flue gas of large thermal power unit |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN112268293A (en) * | 2020-11-11 | 2021-01-26 | 西安热工研究院有限公司 | A system and method for purifying active coke from flue gas of large thermal power unit |
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