CN115025614A - Cyclic semi-dry desulfurization process - Google Patents
Cyclic semi-dry desulfurization process Download PDFInfo
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- CN115025614A CN115025614A CN202210603597.3A CN202210603597A CN115025614A CN 115025614 A CN115025614 A CN 115025614A CN 202210603597 A CN202210603597 A CN 202210603597A CN 115025614 A CN115025614 A CN 115025614A
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- flue gas
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- humidifying
- ash
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- 238000006477 desulfuration reaction Methods 0.000 title claims abstract description 60
- 230000023556 desulfurization Effects 0.000 title claims abstract description 60
- 238000000034 method Methods 0.000 title claims abstract description 26
- 230000008569 process Effects 0.000 title claims abstract description 19
- 125000004122 cyclic group Chemical group 0.000 title claims abstract description 17
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims abstract description 143
- 239000003546 flue gas Substances 0.000 claims abstract description 143
- 239000000428 dust Substances 0.000 claims abstract description 38
- 230000002745 absorbent Effects 0.000 claims abstract description 32
- 239000002250 absorbent Substances 0.000 claims abstract description 32
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 32
- 235000008733 Citrus aurantifolia Nutrition 0.000 claims abstract description 16
- 235000011941 Tilia x europaea Nutrition 0.000 claims abstract description 16
- 239000004571 lime Substances 0.000 claims abstract description 16
- 239000000463 material Substances 0.000 claims description 50
- RAHZWNYVWXNFOC-UHFFFAOYSA-N Sulphur dioxide Chemical compound O=S=O RAHZWNYVWXNFOC-UHFFFAOYSA-N 0.000 claims description 26
- 238000000227 grinding Methods 0.000 claims description 17
- XAGFODPZIPBFFR-UHFFFAOYSA-N aluminium Chemical compound [Al] XAGFODPZIPBFFR-UHFFFAOYSA-N 0.000 claims description 16
- 229910052782 aluminium Inorganic materials 0.000 claims description 16
- OSGAYBCDTDRGGQ-UHFFFAOYSA-L calcium sulfate Chemical compound [Ca+2].[O-]S([O-])(=O)=O OSGAYBCDTDRGGQ-UHFFFAOYSA-L 0.000 claims description 12
- 239000003054 catalyst Substances 0.000 claims description 11
- 238000006243 chemical reaction Methods 0.000 claims description 11
- 239000002245 particle Substances 0.000 claims description 8
- 239000007787 solid Substances 0.000 claims description 8
- AXCZMVOFGPJBDE-UHFFFAOYSA-L calcium dihydroxide Chemical compound [OH-].[OH-].[Ca+2] AXCZMVOFGPJBDE-UHFFFAOYSA-L 0.000 claims description 6
- 229910001861 calcium hydroxide Inorganic materials 0.000 claims description 6
- 235000011116 calcium hydroxide Nutrition 0.000 claims description 6
- 239000000920 calcium hydroxide Substances 0.000 claims description 6
- GBAOBIBJACZTNA-UHFFFAOYSA-L calcium sulfite Chemical compound [Ca+2].[O-]S([O-])=O GBAOBIBJACZTNA-UHFFFAOYSA-L 0.000 claims description 6
- 235000010261 calcium sulphite Nutrition 0.000 claims description 6
- 230000009467 reduction Effects 0.000 claims description 6
- 238000007599 discharging Methods 0.000 claims description 5
- 238000002156 mixing Methods 0.000 claims description 5
- 230000007246 mechanism Effects 0.000 claims description 4
- 238000003303 reheating Methods 0.000 claims description 4
- 238000003756 stirring Methods 0.000 claims description 4
- 239000004480 active ingredient Substances 0.000 claims description 3
- 229910001220 stainless steel Inorganic materials 0.000 claims description 3
- 239000010935 stainless steel Substances 0.000 claims description 3
- 230000002349 favourable effect Effects 0.000 claims description 2
- 230000000694 effects Effects 0.000 abstract description 2
- UCKMPCXJQFINFW-UHFFFAOYSA-N Sulphide Chemical compound [S-2] UCKMPCXJQFINFW-UHFFFAOYSA-N 0.000 abstract 1
- 239000002956 ash Substances 0.000 description 66
- 238000005245 sintering Methods 0.000 description 8
- 239000010881 fly ash Substances 0.000 description 6
- 239000000571 coke Substances 0.000 description 4
- 238000005516 engineering process Methods 0.000 description 4
- 238000002485 combustion reaction Methods 0.000 description 3
- 239000002994 raw material Substances 0.000 description 3
- 239000000779 smoke Substances 0.000 description 3
- GWEVSGVZZGPLCZ-UHFFFAOYSA-N Titan oxide Chemical compound O=[Ti]=O GWEVSGVZZGPLCZ-UHFFFAOYSA-N 0.000 description 2
- 239000004411 aluminium Substances 0.000 description 2
- 238000001035 drying Methods 0.000 description 2
- 230000007613 environmental effect Effects 0.000 description 2
- 239000003344 environmental pollutant Substances 0.000 description 2
- 239000002803 fossil fuel Substances 0.000 description 2
- 231100000719 pollutant Toxicity 0.000 description 2
- 239000002699 waste material Substances 0.000 description 2
- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 description 1
- 238000005299 abrasion Methods 0.000 description 1
- 239000002253 acid Substances 0.000 description 1
- 238000003916 acid precipitation Methods 0.000 description 1
- 238000003915 air pollution Methods 0.000 description 1
- 238000000889 atomisation Methods 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 239000011449 brick Substances 0.000 description 1
- 239000011575 calcium Substances 0.000 description 1
- 229910052791 calcium Inorganic materials 0.000 description 1
- JGIATAMCQXIDNZ-UHFFFAOYSA-N calcium sulfide Chemical compound [Ca]=S JGIATAMCQXIDNZ-UHFFFAOYSA-N 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000005243 fluidization Methods 0.000 description 1
- 239000007789 gas Substances 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 238000012423 maintenance Methods 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 230000020477 pH reduction Effects 0.000 description 1
- 230000035699 permeability Effects 0.000 description 1
- 238000004537 pulping Methods 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 239000002689 soil Substances 0.000 description 1
- 239000007921 spray Substances 0.000 description 1
- 238000005507 spraying Methods 0.000 description 1
- OGIDPMRJRNCKJF-UHFFFAOYSA-N titanium oxide Inorganic materials [Ti]=O OGIDPMRJRNCKJF-UHFFFAOYSA-N 0.000 description 1
- 239000011800 void 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
- B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
- B01D53/80—Semi-solid phase processes, i.e. by using slurries
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D46/00—Filters or filtering processes specially modified for separating dispersed particles from gases or vapours
- B01D46/02—Particle separators, e.g. dust precipitators, having hollow filters made of flexible material
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/46—Removing components of defined structure
- B01D53/48—Sulfur compounds
- B01D53/50—Sulfur oxides
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
- B01D53/86—Catalytic processes
- B01D53/8621—Removing nitrogen compounds
- B01D53/8625—Nitrogen oxides
-
- 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
- Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
- Y02A50/00—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE in human health protection, e.g. against extreme weather
- Y02A50/20—Air quality improvement or preservation, e.g. vehicle emission control or emission reduction by using catalytic converters
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- Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- Environmental & Geological Engineering (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Health & Medical Sciences (AREA)
- Biomedical Technology (AREA)
- Analytical Chemistry (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Treating Waste Gases (AREA)
Abstract
The invention discloses a cyclic semi-dry desulfurization process, which comprises a flue gas kiln, a high-temperature heat exchanger, an SCR denitration reactor, a low-temperature heat exchanger, a cyclic semi-dry desulfurization system, a secondary bag-type dust remover, an induced draft fan and a chimney; wherein, the circulation semidry method desulfurization system comprises: the system comprises an absorbent storage and conveying system, a reactor, a primary bag-type dust collector, a humidifying mixer, a circulating ash system, a fluidized air system, a humidifying water system, a lime conveying system and a control system; the circulating ash system is constructed among the reactor, the humidifying mixer and the primary bag-type dust collector, and transmits circulating ash to the humidifying mixer. The invention is provided with the circulating semidry desulfurization system, and the circulating ash system is respectively linked with the reactor, the humidifying mixer and the primary bag-type dust remover, so that the circulating ash and the absorbent in the reactor can be recycled, a better desulfurization effect can be achieved through circulating desulfurization, and the content of sulfide in flue gas is lower.
Description
Technical Field
The invention relates to the technical field of desulfurization equipment, in particular to a cyclic semidry desulfurization process.
Background
SO emitted from fossil fuel combustion 2 Is to cause air pollution and form acid rainOne of the main reasons for this is that acid rain can cause acidification of water and soil, endanger forests and crops, and cause serious damage to the ecological environment. With increasing emphasis on environmental issues, SO 2 The emission becomes an important index for controlling the emission of tail gas pollutants, namely, the pollutant SO of fossil fuel enterprises 2 Emissions will be severely limited. The pre-desulfurization, the middle desulfurization and the post-combustion desulfurization in the desulfurization technology are used for eliminating SO in flue gas 2 Among them, post-combustion desulfurization is currently the most effective desulfurization technique.
The semi-dry flue gas desulfurization technology is a novel semi-dry flue gas desulfurization technology developed by overcoming the defects of huge rotary spray pulping system, serious equipment abrasion, overhigh calcium-sulfur ratio of calcium spraying and humidification in a furnace and the like in the semi-dry method, and has the advantages of less investment, low operating cost, capability of making bricks by using desulfurized ash and the like.
Through massive search, the prior art is found, and the publication number is as follows: CN105731391A discloses a method for processing semi-dry desulfurized fly ash, which comprises the steps of putting semi-dry desulfurized fly ash serving as a sintering raw material instead of equal weight of lime into a sintering machine bin provided with an active coke desulfurization device to participate in batching, wherein the input amount of the semi-dry desulfurized fly ash accounts for 0.2-0.4% of the total weight of all the sintering raw materials in the bin, heating to a sintering temperature and keeping the temperature for 1-2 min during sintering, SO that SO2 is released from the semi-dry desulfurized fly ash, the sintering temperature is not lower than 850 ℃, SO2 released from the semi-dry desulfurized fly ash and flue gas enter the active coke desulfurization device, the active coke in the active coke desulfurization device can adsorb SO2 in the flue gas, and after sintering, the semi-dry desulfurized fly ash and other sintering raw materials are sintered together to form sintered ore. The treatment method of the semi-dry process desulfurization ash can quickly treat the semi-dry process desulfurization ash, and does not cause secondary pollution to the environment.
To sum up, in current deNOx systems, flue gas through desulfurization reactor all need pass through the sack cleaner, the effect that mix with the separation of solid particle thing in the flue gas after the realization reaction, but after long-time the use, solid particle thing can appear piling up in a large number in the sack cleaner, can cause the influence to the sack permeability, and then reduce the result of use of sack cleaner, and need add lime and absorbent in the reactor, lack effectual circulation feed system, and solid particle thing waste material in the sack cleaner is unfavorable for recycling, the waste of resource has been increased.
Disclosure of Invention
The invention aims to provide a circulating semidry desulfurization process to solve the problems in the background technology.
In order to achieve the purpose, the invention provides the following technical scheme: a cyclic semi-dry desulfurization process comprises a flue gas kiln, a high-temperature heat exchanger, an SCR denitration reactor, a low-temperature heat exchanger, a cyclic semi-dry desulfurization system, a secondary bag-type dust collector, an induced draft fan and a chimney;
wherein, the circulation semidry method desulfurization system comprises: the system comprises an absorbent storage and conveying system, a reactor, a primary bag-type dust collector, a humidifying mixer, a circulating ash system, a fluidized air system, a humidifying water system, a lime conveying system and a control system;
the circulating ash system is constructed among the reactor, the humidifying mixer and the primary bag-type dust collector, the circulating ash system transmits circulating ash to the humidifying mixer, the circulating ash enters the reactor after being sprayed with water and humidified by the humidifying water system, flue gas reacts with an absorbent in the circulating ash after humidification, and sulfur dioxide in the flue gas reacts with the absorbent to produce calcium sulfite and calcium sulfate under the conditions of temperature reduction and humidification.
Preferably, the circulating semidry desulfurization process flow is sequentially connected with a flue gas kiln, a high-temperature heat exchanger, an SCR denitration reactor, a low-temperature heat exchanger, a circulating semidry desulfurization system, a secondary bag-type dust collector, an induced draft fan and a chimney according to the flow direction of flue gas;
the flue gas kiln is used for communicating flue gas to the high-temperature heat exchanger, the high-temperature flue gas is in contact with the aluminum fins in the high-temperature heat exchanger to form rapid and comprehensive heat exchange, heat exchange is carried out on heat-conducting media circulating in the aluminum fins, the temperature of the high-temperature flue gas is reduced, and the temperature of the flue gas is reduced to be below 200 ℃.
Preferably, the flue gas passes through the SCR denitration reactor and is discharged into a low-temperature heat exchanger, an aluminum fin is also adopted in the low-temperature heat exchanger to be in contact with the flue gas, the temperature of the flue gas is cooled again through a heat-conducting medium circulating in the aluminum fin, and the temperature of the flue gas after denitration is reduced to be below 100 ℃.
Preferably, the flue gas passing through the high-temperature heat exchanger enters an SCR denitration reactor, the flue gas enters the SCR denitration reactor from the bottom, and a catalyst and TiO are adopted in the SCR denitration reactor 2 As a carrier, with V 2 O 5 As an active ingredient, the catalyst is designed in a honeycomb form and is used for increasing the contact area of flue gas and the catalyst, the flue gas passes through the inside of the catalyst to carry out flue gas denitration, and the reaction temperature range is 80-300 ℃.
Preferably, the low-temperature flue gas passing through the low-temperature heat exchanger enters a circulating semi-dry desulfurization system, the flue gas enters the reactor from the bottom of the reactor, the absorbent is output to a humidifying mixer from a storage by an absorbent conveying system, and water is sprayed into the humidifying mixer by a humidifying water system for humidifying the absorbent;
the circulating ash system mainly comprises a conveyor belt, a drop hopper, a screen and a grinding roller, wherein symmetrically distributed guide plates are arranged inside the conveyor belt at a material outlet and a material inlet of the humidifying mixer and used for guiding materials, the guide plates face the interior of the drop hopper, the screen is arranged at the bottom end of the interior of the drop hopper, and the grinding roller is arranged on the upper surface of the screen and used for grinding caking materials;
the material outlet and the material inlet of the humidifying mixer are respectively provided with a circulating ash conveying belt in a drop height design, a drop height hopper is arranged between the conveying belts, the drop height hopper arranged on the conveying belts is used for allowing materials to freely fall in the drop height hopper, the materials are screened by a screen after passing through a screen, the materials which do not pass through the screen are crushed by a grinding roller, the grinding roller is driven by a servo motor, the rotating speed of the grinding roller is controlled to be 300-550r/min, the screen is 30-50 meshes, and the materials are stainless steel.
The crushing mechanism in the circulating ash system is used for comprehensively crushing materials discharged from the humidifying reactor and the input humidifying reactor, can be used for crushing the humidified caking materials, and is favorable for using subsequent circulating ash.
Preferably, the reacted flue gas is discharged to a primary bag-type dust collector through the reactor, a large amount of dry solid particles are carried in the reacted flue gas, and the primary bag-type dust collector separates dry circulating ash in the flue gas from the flue gas and returns to the humidifying mixer through a circulating ash system;
the lime conveying system conveys lime into the humidifying mixer, the slaked lime is humidified and mixed and then circulated again, the humidifying and mixing stirring is circulated again, and the circulation multiplying power reaches 160 times. The cleaned flue gas is discharged into a chimney through a draught fan without reheating at the dew point temperature of more than 120 ℃.
Preferably, the flue gas passing through the circulating semidry desulfurization system is introduced into a secondary bag-type dust collector to remove dust again, so that dust in the treated flue gas is completely eliminated, and the flue gas is introduced into a chimney through an induced draft fan and is discharged.
Preferably, the control system is used for controlling the operation of the circulating ash system, and the control system is respectively connected with the reactor, the humidifying mixer, the circulating ash system, the humidifying water system and the lime conveying system and is used for adjusting the amount of water added into the mixer to ensure the reaction temperature in the reactor and the constant flue gas outlet temperature;
and meanwhile, the amount of the outlet flue gas is continuously monitored, the concentration of the outlet SO2 and the flow of the flue gas determine the addition amount of the system absorbent, and the circulating desulfurized ash in the fluidized bottom bin is discharged into a discharger through an ash discharge vertical pipe of the bottom bin after the material level of the circulating desulfurized ash is higher than the high material level for a certain time, SO that the water content of the discharged desulfurized ash is reduced to 2%, the fluidity is good, and the desulfurized ash is sent to an ash bin by a pneumatic ash conveying system.
Compared with the prior art, the invention has the beneficial effects that:
1. in the invention, flue gas enters the reactor through the bottom of the reactor and reacts with the absorbent uniformly mixed in the humidifying circulating ash. Under the conditions of temperature reduction and humidification, SO in the flue gas 2 Reacts with an absorbent to generate calcium sulfite and calcium sulfate, the desulfurization efficiency reaches 99 percent or more, and the small outlet sulfur dioxide is ensuredAt 10mg/Nm 3 And can meet increasingly strict environmental protection requirements.
2. The reaction temperature and the constant flue gas outlet temperature in the reactor are ensured by adjusting the amount of water added into the mixer through the control system, the flue gas temperature at the smoke outlet is above 120 ℃, and due to the high smoke discharge temperature, the bag pasting accident can be prevented, the smoke discharge condition of a chimney can be greatly improved, the adaptability to flue gas change is strong, and the system is stable in operation.
3. The invention adds the wet mixer and the fluidization conveying device, adds circulating ash and fresh hydrated lime into the mixer by fluidizing air to fluidize the circulating ash and add water for humidification, increases the void ratio and the mixing chance, connects the atomization humidification area to enable the moisture content of the ash to reach about 4 percent, and has the advantages of small volume, convenient maintenance and the like.
Detailed Description
The technical solutions in the embodiments of the present invention will be clearly and completely described below with reference to the embodiments of the present invention, and it is obvious that the described embodiments are only a part of the embodiments of the present invention, and not all of the embodiments. All other embodiments, which can be derived by a person skilled in the art from the embodiments given herein without making any creative effort, shall fall within the protection scope of the present invention.
In the description of the present invention, it should be noted that the terms "upper", "lower", "inner", "outer", "front", "rear", "both ends", "one end", "the other end", and the like indicate orientations or positional relationships only for convenience in describing the present invention and simplifying the description, but do not indicate or imply that the referred device or element must have a specific orientation, be constructed in a specific orientation, and be operated, and thus, should not be construed as limiting the present invention. Furthermore, the terms "first," "second," and the like are used for descriptive purposes only and are not to be construed as indicating or implying relative importance.
In the description of the present invention, it should be noted that, unless explicitly stated or limited otherwise, the terms "mounted," "disposed," "connected," and the like are to be construed broadly, such as "connected," which may be fixedly connected, detachably connected, or integrally connected; can be mechanically or electrically connected; they may be connected directly or indirectly through intervening media, or they may be interconnected between two elements. The specific meanings of the above terms in the present invention can be understood in specific cases to those skilled in the art.
The invention provides two embodiments:
the first embodiment is as follows:
a cyclic semi-dry desulfurization process comprises a flue gas kiln, a high-temperature heat exchanger, an SCR denitration reactor, a low-temperature heat exchanger, a cyclic semi-dry desulfurization system, a secondary bag-type dust collector, an induced draft fan and a chimney;
the circulating semidry desulfurization process flow is sequentially connected with a flue gas kiln, a high-temperature heat exchanger, an SCR denitration reactor, a low-temperature heat exchanger, a circulating semidry desulfurization system, a secondary bag-type dust collector, an induced draft fan and a chimney according to the flow direction of flue gas;
the flue gas kiln communicates the flue gas to high temperature heat exchanger, and the high temperature flue gas contacts with the aluminium system fin inside the high temperature heat exchanger, forms quick and comprehensive heat exchange, carries out the heat exchange to the heat-conducting medium that circulates in the aluminium system fin, reduces the temperature of high temperature flue gas, reduces the flue gas temperature to below 200 ℃. Flue gas passing through the high-temperature heat exchanger enters an SCR denitration reactor, the flue gas enters the SCR denitration reactor from the bottom, a catalyst in the SCR denitration reactor takes TiO2 as a carrier, V2O5 as an active ingredient, and the honeycomb type design is adopted for increasing the contact area of the flue gas and the catalyst, the flue gas passes through the inside of the catalyst to be subjected to flue gas denitration, and the reaction temperature range is 80-300 ℃.
The flue gas is discharged into a low-temperature heat exchanger after passing through the SCR denitration reactor, the low-temperature heat exchanger is also contacted with the flue gas by adopting an aluminum fin, the temperature of the flue gas is cooled again through a heat-conducting medium circulating in the aluminum fin, and the temperature of the flue gas after denitration is reduced to be below 100 ℃.
And introducing the flue gas passing through the circulating semidry desulfurization system into a secondary bag-type dust collector, removing dust from the flue gas again to comprehensively eliminate dust in the treated flue gas, introducing the flue gas into a chimney through an induced draft fan, and discharging. The control system ensures the reaction temperature in the reactor and the constant flue gas outlet temperature by adjusting the amount of the added water of the mixer, and simultaneously continuously monitors the outlet flue gas volume, and the concentration of the outlet SO2 and the flue gas volume determine the added amount of the absorbent of the system.
Example two:
the circulating semi-dry desulfurization system comprises: the system comprises an absorbent storage and conveying system, a reactor, a primary bag dust collector, a humidifying mixer, a circulating ash system, a fluidized air system, a humidifying water system, a lime conveying system and a control system.
The low-temperature flue gas passing through the low-temperature heat exchanger enters a circulating semi-dry desulfurization system, the flue gas enters the inside of the reactor from the bottom of the reactor, an absorbent is output into a humidifying mixer from a storage by an absorbent conveying system, and water is sprayed into the humidifying mixer by a humidifying water system for humidifying the absorbent;
the circulating ash system is constructed among the reactor, the humidifying mixer and the primary bag-type dust collector, the circulating ash system transmits circulating ash to the humidifying mixer, the circulating ash enters the reactor after being sprayed with water and humidified by the humidifying water system, flue gas reacts with an absorbent in the circulating ash after humidification, and sulfur dioxide in the flue gas reacts with the absorbent to produce calcium sulfite and calcium sulfate under the conditions of temperature reduction and humidification.
Discharging the reacted flue gas to a primary bag-type dust collector through a reactor, wherein a large amount of dry solid particles are carried in the reacted flue gas, and the primary bag-type dust collector separates dry circulating ash in the flue gas from the flue gas and returns to a humidifying mixer through a circulating ash system;
the lime delivery system delivers lime to the humidifying mixer, where the slaked lime is humidified and mixed for recirculation.
The circulating ash system mainly comprises a conveyor belt, a drop hopper, a screen and a grinding roller, wherein symmetrically distributed guide plates are arranged inside the conveyor belt at a material outlet and a material inlet of the humidifying mixer and used for guiding materials, the guide plates face the interior of the drop hopper, the screen is arranged at the bottom end of the interior of the drop hopper, and the grinding roller is arranged on the upper surface of the screen and used for crushing caking materials;
the material outlet and the material inlet of the humidifying mixer are respectively provided with a circulating ash conveying belt in a drop height design, a drop height hopper is arranged between the conveying belts, the drop height hopper arranged on the conveying belts is used for allowing materials to freely fall in the drop height hopper, the materials are screened by the screen after passing through the screen, the materials which do not pass through the screen are crushed by the grinding roller, the grinding roller is driven by a servo motor, the rotating speed of the grinding roller is controlled to be 300-550r/min, the screen is in a specification of 30-50 meshes, and the materials are stainless steel.
The crushing mechanism in the circulating ash system is used for comprehensively crushing materials input into the humidifying reactor and discharged from the humidifying reactor, and can be used for crushing the humidified caking materials, so that the subsequent circulating ash can be favorably used.
The flue gas enters the reactor through the bottom of the reactor and reacts with the absorbent uniformly mixed in the humidifying circulating ash. Under the conditions of temperature reduction and humidification, SO2 in the flue gas reacts with the absorbent to generate calcium sulfite and calcium sulfate. The flue gas after reaction carries a large amount of dry solid particles to enter a primary bag-type dust collector, dry circulating ash is separated from the flue gas by the bag-type dust collector and is conveyed to a humidifying mixer by a circulating ash system, meanwhile, slaked lime is added to the humidifying mixer, and the circulating is performed again through humidifying, mixing and stirring, wherein the circulating multiplying power reaches 160. The cleaned flue gas is discharged into a chimney through a draught fan without reheating at the dew point temperature of more than 120 ℃. The control system is used for controlling the operation of the circulating ash system, is respectively connected with the reactor, the humidifying mixer, the circulating ash system, the humidifying water system and the lime conveying system, and is used for adjusting the amount of water added into the mixer to ensure the reaction temperature in the reactor and the constant flue gas outlet temperature;
and meanwhile, the amount of the outlet flue gas is continuously monitored, the concentration of the outlet SO2 and the flow of the flue gas determine the addition amount of the system absorbent, and the circulating desulfurized ash in the fluidized bottom bin is discharged into a discharger through an ash discharge vertical pipe of the bottom bin after the material level of the circulating desulfurized ash is higher than the high material level for a certain time, SO that the water content of the discharged desulfurized ash is reduced to 2%, the fluidity is good, and the desulfurized ash is sent to an ash bin by a pneumatic ash conveying system.
The working principle is as follows: after the flue gas is discharged from the flue gas kiln, the flue gas is preferentially cooled by the high-temperature heat exchanger, the high-temperature flue gas is contacted with the aluminum fins in the high-temperature heat exchanger to form rapid and comprehensive heat exchange, heat exchange is carried out on heat-conducting media circulating in the aluminum fins, the temperature of the high-temperature flue gas is reduced, and the temperature of the flue gas is reduced to be below 200 ℃. The flue gas is discharged into a low-temperature heat exchanger after passing through an SCR denitration reactor, an aluminum fin is also adopted in the low-temperature heat exchanger to be contacted with the flue gas, the temperature of the flue gas is cooled again through a heat-conducting medium circulating in the aluminum fin, and the temperature of the flue gas after denitration is reduced to be below 100 ℃.
And introducing the flue gas passing through the circulating semidry desulfurization system into a secondary bag-type dust collector, removing dust from the flue gas again for comprehensively removing dust in the treated flue gas, and introducing the flue gas into a chimney through an induced draft fan and discharging the flue gas.
The flue gas enters the reactor through the bottom of the reactor and reacts with the absorbent uniformly mixed in the humidifying circulating ash. Under the conditions of temperature reduction and humidification, SO2 in the flue gas reacts with the absorbent to generate calcium sulfite and calcium sulfate. The reacted flue gas carries a large amount of dry solid particles to enter a primary bag-type dust collector, dry circulating ash is separated from the flue gas by the bag-type dust collector and is conveyed to a humidifying mixer by a circulating ash system, meanwhile, slaked lime is added to the humidifying mixer, the circulating multiplying power reaches 160 after humidification and mixing stirring, symmetrically distributed guide plates are arranged inside conveying belts of a material outlet and a material inlet of the humidifying mixer and used for guiding the material, and crushing rollers are arranged between the guide plates and used for crushing the caking material; the crushing mechanism in the circulating ash system is used for comprehensively crushing materials input into the humidifying reactor and discharged from the humidifying reactor, and can be used for crushing the humidified caking materials, so that the subsequent circulating ash can be favorably used.
The cleaned flue gas is discharged into a chimney through a draught fan without reheating at the dew point temperature of more than 120 ℃. The control system is used for controlling the operation of the circulating ash system, is respectively connected with the reactor, the humidifying mixer, the circulating ash system, the humidifying water system and the lime conveying system, and is used for adjusting the amount of water added into the mixer to ensure the reaction temperature in the reactor and the constant flue gas outlet temperature; and meanwhile, the amount of the outlet flue gas is continuously monitored, the concentration of the outlet SO2 and the flow of the flue gas determine the addition amount of the system absorbent, and the circulating desulfurized ash in the fluidized bottom bin is discharged into a discharger through an ash discharge vertical pipe of the bottom bin after the material level of the circulating desulfurized ash is higher than the high material level for a certain time, SO that the water content of the discharged desulfurized ash is reduced to 2%, the fluidity is good, and the desulfurized ash is sent to an ash bin by a pneumatic ash conveying system.
It will be evident to those skilled in the art that the invention is not limited to the details of the foregoing illustrative embodiments, and that the present invention may be embodied in other specific forms without departing from the spirit or essential attributes thereof. The present embodiments are therefore to be considered in all respects as illustrative and not restrictive, the scope of the invention being indicated by the appended claims rather than by the foregoing description, and all changes which come within the meaning and range of equivalency of the claims are therefore intended to be embraced therein.
Claims (8)
1. A cyclic semi-dry desulfurization process is characterized in that: the circulating semi-dry desulfurization process comprises a flue gas kiln, a high-temperature heat exchanger, an SCR denitration reactor, a low-temperature heat exchanger, a circulating semi-dry desulfurization system, a secondary bag-type dust remover, an induced draft fan and a chimney;
wherein, the circulation semidry method desulfurization system comprises: the system comprises an absorbent storage and conveying system, a reactor, a primary bag dust collector, a humidifying mixer, a circulating ash system, a fluidized air system, a humidifying water system, a lime conveying system and a control system;
the circulating ash system is constructed among the reactor, the humidifying mixer and the primary bag-type dust collector, the circulating ash system transmits circulating ash to the humidifying mixer, the circulating ash enters the reactor after being sprayed with water and humidified by the humidifying water system, flue gas reacts with an absorbent in the circulating ash after humidification, and sulfur dioxide in the flue gas reacts with the absorbent to produce calcium sulfite and calcium sulfate under the conditions of temperature reduction and humidification.
2. The cyclic semi-dry desulfurization process according to claim 1, characterized in that: the circulating semidry desulfurization process flow is sequentially connected with a flue gas kiln, a high-temperature heat exchanger, an SCR denitration reactor, a low-temperature heat exchanger, a circulating semidry desulfurization system, a secondary bag-type dust collector, an induced draft fan and a chimney according to the flow direction of flue gas;
the flue gas kiln is used for communicating flue gas to the high-temperature heat exchanger, the high-temperature flue gas is in contact with the aluminum fins in the high-temperature heat exchanger to form rapid and comprehensive heat exchange, heat exchange is carried out on heat-conducting media circulating in the aluminum fins, the temperature of the high-temperature flue gas is reduced, and the temperature of the flue gas is reduced to be below 200 ℃.
3. The cyclic semi-dry desulfurization process according to claim 1, characterized in that: the flue gas is discharged into a low-temperature heat exchanger after passing through the SCR denitration reactor, the low-temperature heat exchanger is also contacted with the flue gas by adopting an aluminum fin, the temperature of the flue gas is cooled again through a heat-conducting medium circulating in the aluminum fin, and the temperature of the flue gas after denitration is reduced to be below 100 ℃.
4. The cyclic semi-dry desulfurization process according to claim 1, wherein: the flue gas passing through the high-temperature heat exchanger enters an SCR denitration reactor, the flue gas enters the SCR denitration reactor from the bottom, and a catalyst and TiO are adopted in the SCR denitration reactor 2 As a carrier, with V 2 O 5 As an active ingredient, the catalyst is designed in a honeycomb form and is used for increasing the contact area of flue gas and the catalyst, the flue gas passes through the inside of the catalyst to carry out flue gas denitration, and the reaction temperature range is 80-300 ℃.
5. The cyclic semi-dry desulfurization process according to claim 1, characterized in that: the low-temperature flue gas passing through the low-temperature heat exchanger enters a circulating semi-dry desulfurization system, the flue gas enters the inside of the reactor from the bottom of the reactor, an absorbent is output into a humidifying mixer from a storage by an absorbent conveying system, and water is sprayed into the humidifying mixer by a humidifying water system for humidifying the absorbent;
the circulating ash system mainly comprises a conveyor belt, a drop hopper, a screen and a grinding roller, wherein symmetrically distributed guide plates are arranged inside the conveyor belt at a material outlet and a material inlet of the humidifying mixer and used for guiding materials, the guide plates face the interior of the drop hopper, the screen is arranged at the bottom end of the interior of the drop hopper, and the grinding roller is arranged on the upper surface of the screen and used for grinding caking materials;
the material outlet and the material inlet of the humidifying mixer are respectively provided with a circulating ash conveying belt in a drop height design, a drop height hopper is arranged between the conveying belts, the drop height hopper arranged on the conveying belts is used for allowing materials to freely fall in the drop height hopper, the materials are screened by a screen after passing through a screen, the materials which do not pass through the screen are crushed by a grinding roller, the grinding roller is driven by a servo motor, the rotating speed of the grinding roller is controlled to be 300-550r/min, the screen is 30-50 meshes, and the materials are stainless steel.
The crushing mechanism in the circulating ash system is used for comprehensively crushing materials discharged from the humidifying reactor and the input humidifying reactor, can be used for crushing the humidified caking materials, and is favorable for using subsequent circulating ash.
6. The cyclic semi-dry desulfurization process according to claim 1, characterized in that: discharging the reacted flue gas to a primary bag-type dust collector through a reactor, wherein a large amount of dry solid particles are carried in the reacted flue gas, and the primary bag-type dust collector separates dry circulating ash in the flue gas from the flue gas and returns to a humidifying mixer through a circulating ash system;
the lime conveying system conveys lime into the humidifying mixer, the slaked lime is humidified and mixed and then circulated again, the humidifying and mixing stirring is circulated again, and the circulation multiplying power reaches 160 times. The cleaned flue gas is discharged into a chimney through a draught fan without reheating at the dew point temperature of more than 120 ℃.
7. The cyclic semi-dry desulfurization process according to claim 1, characterized in that: and introducing the flue gas passing through the circulating semidry desulfurization system into a secondary bag-type dust collector, removing dust from the flue gas again for comprehensively removing dust in the treated flue gas, and introducing the flue gas into a chimney through an induced draft fan and discharging the flue gas.
8. The cyclic semi-dry desulfurization process according to claim 1, characterized in that: the control system is used for controlling the operation of the circulating ash system, is respectively connected with the reactor, the humidifying mixer, the circulating ash system, the humidifying water system and the lime conveying system, and is used for adjusting the amount of water added into the mixer to ensure the reaction temperature in the reactor and the constant flue gas outlet temperature;
simultaneously, the amount of the flue gas at the outlet is continuously monitored, and the SO at the outlet 2 The concentration and the flue gas flow determine the addition amount of the system absorbent, and the circulating desulfurization ash in the fluidized bottom bin is discharged into a discharger through an ash discharge vertical pipe of the bottom bin after the material level of the circulating desulfurization ash is higher than the high material level for a certain time, so that the water content of the discharged desulfurization ash is reduced to 2%, the fluidity is good, and the discharged desulfurization ash is sent to an ash silo by a pneumatic ash conveying system.
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