CN108126510B - Flue gas desulfurization and denitrification equipment - Google Patents
Flue gas desulfurization and denitrification equipment Download PDFInfo
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- CN108126510B CN108126510B CN201810040815.0A CN201810040815A CN108126510B CN 108126510 B CN108126510 B CN 108126510B CN 201810040815 A CN201810040815 A CN 201810040815A CN 108126510 B CN108126510 B CN 108126510B
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- 239000003546 flue gas Substances 0.000 title claims abstract description 87
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 title claims abstract description 86
- 238000006477 desulfuration reaction Methods 0.000 title claims abstract description 58
- 230000023556 desulfurization Effects 0.000 title claims abstract description 58
- 238000010521 absorption reaction Methods 0.000 claims abstract description 139
- 239000002250 absorbent Substances 0.000 claims abstract description 111
- 230000002745 absorbent Effects 0.000 claims abstract description 109
- 238000000926 separation method Methods 0.000 claims abstract description 20
- 239000002893 slag Substances 0.000 claims abstract description 16
- 229910052602 gypsum Inorganic materials 0.000 claims abstract description 10
- 239000010440 gypsum Substances 0.000 claims abstract description 10
- 238000002156 mixing Methods 0.000 claims description 39
- 238000000034 method Methods 0.000 claims description 33
- 230000008569 process Effects 0.000 claims description 32
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 27
- 238000004519 manufacturing process Methods 0.000 claims description 17
- 239000000428 dust Substances 0.000 claims description 8
- 230000001105 regulatory effect Effects 0.000 claims description 7
- 238000003756 stirring Methods 0.000 claims description 7
- 238000007599 discharging Methods 0.000 claims description 3
- 238000011010 flushing procedure Methods 0.000 claims description 3
- 230000007423 decrease Effects 0.000 claims description 2
- 238000000746 purification Methods 0.000 abstract description 11
- 238000004064 recycling Methods 0.000 abstract description 5
- 238000001914 filtration Methods 0.000 abstract description 2
- MWUXSHHQAYIFBG-UHFFFAOYSA-N nitrogen oxide Inorganic materials O=[N] MWUXSHHQAYIFBG-UHFFFAOYSA-N 0.000 description 18
- 238000005457 optimization Methods 0.000 description 18
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 15
- 239000002002 slurry Substances 0.000 description 15
- 239000000047 product Substances 0.000 description 14
- 238000006243 chemical reaction Methods 0.000 description 12
- 239000002245 particle Substances 0.000 description 12
- 239000007789 gas Substances 0.000 description 11
- 238000000889 atomisation Methods 0.000 description 10
- 239000006096 absorbing agent Substances 0.000 description 8
- RAHZWNYVWXNFOC-UHFFFAOYSA-N Sulphur dioxide Chemical compound O=S=O RAHZWNYVWXNFOC-UHFFFAOYSA-N 0.000 description 6
- 230000000694 effects Effects 0.000 description 5
- 239000012530 fluid Substances 0.000 description 5
- 239000000203 mixture Substances 0.000 description 5
- FAPWRFPIFSIZLT-UHFFFAOYSA-M Sodium chloride Chemical compound [Na+].[Cl-] FAPWRFPIFSIZLT-UHFFFAOYSA-M 0.000 description 4
- 230000009286 beneficial effect Effects 0.000 description 4
- 230000009977 dual effect Effects 0.000 description 4
- 238000005516 engineering process Methods 0.000 description 4
- 239000003795 chemical substances by application Substances 0.000 description 3
- 238000001704 evaporation Methods 0.000 description 3
- 230000008020 evaporation Effects 0.000 description 3
- 239000007788 liquid Substances 0.000 description 3
- 239000000463 material Substances 0.000 description 3
- 238000002360 preparation method Methods 0.000 description 3
- 239000007921 spray Substances 0.000 description 3
- 150000003568 thioethers Chemical class 0.000 description 3
- 238000012546 transfer Methods 0.000 description 3
- 230000009471 action Effects 0.000 description 2
- 239000003513 alkali Substances 0.000 description 2
- 230000008901 benefit Effects 0.000 description 2
- 230000001276 controlling effect Effects 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 230000007613 environmental effect Effects 0.000 description 2
- 238000004321 preservation Methods 0.000 description 2
- 229920000742 Cotton Polymers 0.000 description 1
- YKTSYUJCYHOUJP-UHFFFAOYSA-N [O--].[Al+3].[Al+3].[O-][Si]([O-])([O-])[O-] Chemical compound [O--].[Al+3].[Al+3].[O-][Si]([O-])([O-])[O-] YKTSYUJCYHOUJP-UHFFFAOYSA-N 0.000 description 1
- 238000005299 abrasion Methods 0.000 description 1
- 239000000654 additive Substances 0.000 description 1
- 230000000996 additive effect Effects 0.000 description 1
- 238000003915 air pollution Methods 0.000 description 1
- 238000004887 air purification Methods 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 238000004140 cleaning Methods 0.000 description 1
- 230000003247 decreasing effect Effects 0.000 description 1
- 238000009826 distribution Methods 0.000 description 1
- 238000001035 drying Methods 0.000 description 1
- 230000002708 enhancing effect Effects 0.000 description 1
- 238000000605 extraction Methods 0.000 description 1
- 230000002349 favourable effect Effects 0.000 description 1
- 150000002500 ions Chemical class 0.000 description 1
- 239000003595 mist Substances 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 238000012806 monitoring device Methods 0.000 description 1
- 238000012544 monitoring process Methods 0.000 description 1
- 230000037361 pathway Effects 0.000 description 1
- 238000001556 precipitation Methods 0.000 description 1
- 230000002035 prolonged effect Effects 0.000 description 1
- 230000001737 promoting effect Effects 0.000 description 1
- 230000035484 reaction time Effects 0.000 description 1
- 238000010992 reflux Methods 0.000 description 1
- 239000000779 smoke Substances 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 238000012360 testing method Methods 0.000 description 1
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
- B01D53/80—Semi-solid phase processes, i.e. by using slurries
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- 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
- B01D53/60—Simultaneously removing sulfur oxides and nitrogen oxides
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2258/00—Sources of waste gases
- B01D2258/02—Other waste gases
- B01D2258/0283—Flue gases
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- Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- Environmental & Geological Engineering (AREA)
- Health & Medical Sciences (AREA)
- Biomedical Technology (AREA)
- Analytical Chemistry (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Treating Waste Gases (AREA)
Abstract
The invention provides flue gas desulfurization and denitrification equipment, which relates to the technical field of flue gas purification and comprises an absorption tower, a flue gas feeding device, a main absorption device, a cyclone separation device and a gypsum bin, wherein a primary absorption device is further arranged between an air inlet of the absorption tower and the main absorption device, a feed inlet of the primary absorption device is communicated with a slag outlet of the cyclone separation device, and a discharge outlet of the primary absorption device is communicated with an inner cavity of the absorption tower. According to the flue gas desulfurization and denitrification equipment provided by the invention, the desulfurization and denitrification products are introduced into the absorption tower through the primary absorption device, so that the recycling of the absorbent is realized, the absorption efficiency of the absorbent can be effectively improved, meanwhile, the absorbent sprayed out by the main absorption device can be prevented from being dried and adhered on the inner wall of the absorption tower, the service efficiency of the absorbent is improved, the cyclone separation device is combined for filtering the clean flue gas after desulfurization and denitrification, the effective purification of the flue gas is realized, and the pollution to the atmospheric environment is avoided.
Description
Technical Field
The invention belongs to the technical field of flue gas purification, and particularly relates to flue gas desulfurization and denitrification equipment.
Background
Along with the gradual increase of environmental control force, more and more enterprises can discharge the purified flue gas, and a flue gas desulfurization and denitrification technology is usually adopted. The flue gas desulfurization and denitrification technology is a flue gas purification technology applied to industries of generating nitrogen oxides, sulfides and the like, and the application of the technology has considerable benefits on environmental air purification because the nitrogen oxides and the sulfides are one of main sources of air pollution.
The existing flue gas desulfurization and denitrification generally adopts a method of introducing flue gas from the lower part of an absorption tower and absorbing nitrogen oxides and sulfides by an alkaline absorbent in the absorption tower to realize the purification of the flue gas, but the purification effect is often poor, the purification efficiency is low, the absorbent is difficult to effectively utilize, and the purification cost is high.
Disclosure of Invention
The invention aims to provide flue gas desulfurization and denitration equipment, which solves the technical problems of low flue gas purification efficiency and insufficient utilization of an absorbent in the prior art.
In order to achieve the above purpose, the invention adopts the following technical scheme: the utility model provides a flue gas desulfurization denitration equipment, including the absorption tower, set up in the flue gas feeding device of absorption tower air inlet, set up in the inside main absorbing device of absorption tower, the cyclone of air inlet and absorption tower's gas outlet intercommunication and the gypsum feed bin of slag notch and cyclone's slag notch intercommunication, still be equipped with primary absorbing device between the air inlet of absorption tower and the main absorbing device, primary absorbing device's feed inlet and cyclone's slag notch intercommunication, primary absorbing device's discharge gate and absorption tower's inner chamber intercommunication.
As a further optimization, the gas supply device comprises a dust remover and a venturi tube which are sequentially arranged along the gas flow direction of the flue gas and are used for introducing the flue gas into the absorption tower.
As a further optimization, the main absorption device is uniformly provided with at least two groups in the height direction of the absorption tower, and comprises an external mixed double-flow nozzle used for conveying process water and an internal mixed double-flow nozzle arranged below the external mixed double-flow nozzle and used for conveying absorbent, wherein the external mixed double-flow nozzle is connected with the process water tank, the internal mixed double-flow nozzle is connected with the absorbent manufacturing device, and the internal mixed double-flow nozzle and the external mixed double-flow nozzle are respectively connected with the compressed air tank.
As a further optimization, the internal mixing double-flow nozzle comprises an internal mixing nozzle body, an absorbent passage which is arranged in the center of the internal mixing nozzle body and communicated with the absorbent manufacturing device, and a second air passage which is arranged on the outer ring of the absorbent passage and is communicated with the compressed air tank at the side part, wherein the absorbent passage is communicated with the middle part of the side wall of the second air passage, the inner diameter of an outlet of the absorbent passage is gradually increased from inside to outside, and the inner diameter of an outlet of the second air passage is gradually reduced from inside to outside.
As further optimization, the external mixing double-flow nozzle comprises an external mixing nozzle body, a process water channel which is arranged in the center of the external mixing nozzle body and is communicated with the process water pipe, and a first air channel which is arranged on the outer ring of the process water channel and is communicated with the compressed air tank at the side part, wherein the inner diameter of an outlet of the process water channel is gradually increased from inside to outside, and the inner diameter of an outlet of the first air channel is gradually reduced from inside to outside.
As further optimization, the cyclone separation device comprises a primary cyclone separator, a secondary cyclone separator and a tertiary cyclone separator which are sequentially connected in series, slag outlets of the primary cyclone separator, the secondary cyclone separator and the tertiary cyclone separator are respectively communicated with the gypsum bin and the primary absorption device, an outlet for discharging flue gas is arranged at the upper end of the tertiary cyclone separator, and the primary cyclone separator, the secondary cyclone separator and the tertiary cyclone separator are further respectively connected with the primary absorption device through electromagnetic valves.
As a further optimization, the primary absorption device comprises a primary nozzle arranged in the absorption tower, a humidifying digester with a feeding hole connected with a slag outlet of the cyclone separation device and a compressed air component for feeding desulfurization and denitrification products in the humidifying digester into the absorption tower, wherein the primary nozzle is respectively communicated with a discharge hole of the humidifying digester and the compressed air component.
As a further optimization, the absorbent manufacturing device comprises a tank body, a stirring assembly arranged in the tank body, a pipeline arranged at the outlet end of the tank body and used for being connected with the absorption tower, and a secondary circuit used for communicating the middle part of the pipeline with the tank body.
As a further optimization, the pipeline is sequentially provided with an absorbent pump and an electric regulating valve along the flowing direction of the absorbent, and the inlet end of the secondary circuit is arranged between the absorbent pump and the electric regulating valve.
As a further optimization, a back flushing assembly is further arranged on the pipeline.
The flue gas desulfurization and denitrification equipment provided by the invention has the beneficial effects that: according to the flue gas desulfurization and denitrification equipment provided by the invention, the desulfurization and denitrification products are introduced into the absorption tower through the primary absorption device, so that the effect of recycling the unused absorbent is realized, the use efficiency of the absorbent can be effectively improved, the absorbent sprayed out of the main absorption device can be prevented from being dried and adhered on the inner wall of the absorption tower, the use efficiency of the absorbent is improved, the cyclone separation device is combined for filtering the clean flue gas after desulfurization and denitrification, the effective purification of the flue gas is realized, and the pollution to the atmospheric environment is avoided.
Drawings
In order to more clearly illustrate the technical solutions of the embodiments of the present invention, the drawings that are needed in the embodiments or the description of the prior art will be briefly described below, it being obvious that the drawings in the following description are only some embodiments of the present invention, and that other drawings may be obtained according to these drawings without inventive effort for a person skilled in the art.
FIG. 1 is a schematic structural diagram of a flue gas desulfurization and denitration device according to an embodiment of the present invention;
FIG. 2 is a schematic diagram of an absorbent manufacturing apparatus according to the embodiment of the present invention in FIG. 1;
FIG. 3 is a schematic cross-sectional view of an external mix dual stream spray set according to an embodiment of the present invention;
FIG. 4 is a schematic cross-sectional view of an internal mix dual stream spray assembly according to an embodiment of the present invention;
FIG. 5 is a schematic view of a venturi in an embodiment of the present invention;
wherein, each reference sign in the figure:
a 100-absorption column; 200-a primary absorber; 210-an external mix dual stream nozzle; 211-an external mixing nozzle body; 212-a process waterway; 213-a first air path; 220-an internal mixing dual flow nozzle; 221-an internal mixing nozzle body; 222-absorbent pathway; 223-a second gas path; 230-a process water tank; 240-a compressed air tank; 300-absorbent manufacturing device; 310-tank body; 320-a stirring assembly; 330-piping; 331-an absorbent pump; 332-an electric regulating valve; 333-backwash assembly; 340-a secondary circuit; 400-flue gas feeding device; 410-a dust remover; 420-venturi; 500-cyclone separation device; 510-primary cyclone separator; 520-secondary cyclone separator; 530-three stage cyclone separator; 600-gypsum bin; 800-primary absorption unit; 810-primary nozzles; 820-humidifying digester; 830-compressed air assembly.
Detailed Description
In order to make the technical problems, technical schemes and beneficial effects to be solved more clear, the invention is further described in detail below with reference to the accompanying drawings and embodiments. It should be understood that the specific embodiments described herein are for purposes of illustration only and are not intended to limit the scope of the invention.
It will be understood that when an element is referred to as being "mounted" or "disposed" on another element, it can be directly on the other element or be indirectly on the other element. When an element is referred to as being "connected to" another element, it can be directly connected to the other element or be indirectly connected to the other element.
It is to be understood that the terms "length," "width," "upper," "lower," "front," "rear," "left," "right," "vertical," "horizontal," "top," "bottom," "inner," "outer," and the like are merely for convenience in describing and simplifying the description based on the orientation or positional relationship shown in the drawings, and do not indicate or imply that the devices or elements referred to must have a particular orientation, be constructed and operated in a particular orientation, and thus are not to be construed as limiting the 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 a relative importance or implicitly indicating the number of technical features indicated. Thus, a feature defining "a first" or "a second" may explicitly or implicitly include one or more such feature. In the description of the present invention, the meaning of "a plurality" is two or more, unless explicitly defined otherwise.
Referring to fig. 1 to 5, a flue gas desulfurization and denitrification apparatus provided by the present invention will now be described. The flue gas desulfurization and denitrification equipment comprises an absorption tower 100, a flue gas feeding device 400 arranged at the air inlet of the absorption tower 100, a main absorption device 200 arranged inside the absorption tower 100, a cyclone separation device 500 with the air inlet communicated with the air outlet of the absorption tower 100, and a gypsum silo 600 with the slag inlet communicated with the slag outlet of the cyclone separation device 500, wherein a primary absorption device 800 is further arranged between the air inlet of the absorption tower 100 and the main absorption device 200, the feed inlet of the primary absorption device 800 is communicated with the slag outlet of the cyclone separation device 500, and the discharge outlet of the primary absorption device 800 is communicated with the inner cavity of the absorption tower 100.
Compared with the prior art, the flue gas desulfurization and denitrification equipment provided by the invention can effectively improve the use efficiency of the absorbent and realize the recycling of the absorbent by introducing desulfurization and denitrification products into the absorption tower 100 through the primary absorption device 800, can simultaneously avoid the slurry sprayed out of the main absorption device 200 from being dried and adhered on the inner wall of the absorption tower 100, improves the use efficiency of the absorbent, and realizes the effective purification of the flue gas and the pollution to the surrounding environment by combining the cyclone separation device 500 to filter the flue gas entering the absorption tower 100.
As a further optimization, referring to fig. 1 and 5, as a specific embodiment of the flue gas desulfurization and denitrification apparatus provided by the present invention, the gas supply device 400 includes a dust remover 410 and a venturi 420, which are sequentially arranged along the direction of the flue gas flow and are used for introducing flue gas into the absorption tower 100. The gas supply device 400 as a flue gas inlet firstly performs dust removal treatment on the passing gas through the dust remover 410 to reduce the dust content of the flue gas, and then performs deceleration on the flue gas which is about to enter the absorption tower 100 through the venturi tube 420 structure to prolong the residence time of the flue gas in the absorption tower 100. In this embodiment, the venturi 420 may be set with the following parameters, inlet diameter b=7.8m, outlet diameter d=9.2m, intermediate diameter c=5.5m, α=36.2 o ，β＝32.2 o The whole air supply device 400 is subjected to heat preservation treatment by adopting aluminum silicate heat preservation cotton with the thickness of 70mm so as to improve the temperature of a flue gas inlet, avoid the influence on the temperature of an absorbent and further avoid the influence on the absorption efficiency of the absorbent.
As a further optimization, referring to fig. 1, 3 and 4 together, as a specific embodiment of the flue gas desulfurization and denitrification apparatus provided by the present invention, the main absorption device 200 is uniformly arranged with at least two groups in the height direction of the absorption tower 100, the main absorption device 200 includes an external mixed bi-flow nozzle 210 for conveying process water and an internal mixed bi-flow nozzle 220 disposed below the external mixed bi-flow nozzle 210 and for conveying absorbent, the external mixed bi-flow nozzle 210 is connected with the process water tank 230, the internal mixed bi-flow nozzle 220 is connected with the absorbent manufacturing device 300, and the internal mixed bi-flow nozzle 220 and the external mixed bi-flow nozzle 210 are respectively connected with the compressed air tank 240. The atomization principle is that the air flow of compressed air is used to generate great friction force on the contact surface of process water or absorbent, and the process water or absorbent is spalled into slurry droplets under the action of friction force. In this embodiment, two groups of main absorption devices 200 are adopted, and are uniformly arranged in the height direction of the absorption tower 100, so that the effective reaction space in the absorption tower 100 is optimized, the contact time between the absorbent and the flue gas is prolonged, and the contact area between the absorbent and the flue gas is increased, which is beneficial to smooth ion reaction in desulfurization and denitrification reaction, provides a larger space for gas-liquid mass transfer, and can further improve the utilization efficiency of the absorbent. The gas streams ejected from the external mix bi-flow nozzle 210 and the internal mix bi-flow nozzle 220 interact with the flue gas to form entrainment, enhancing turbulence to the flue gas, which facilitates mass transfer. For easy cleaning and disassembly, the two sets of main absorbers 200 are fastened in the absorber 100 by bolts. The absorption doses of the two groups of main absorption devices 200 arranged at the upper and lower positions are 74% and 26% respectively, and the absorption of sulfur dioxide and nitrogen oxides in the flue gas occurs on the wet surface of the suspended materials of the absorbent, so that the device has higher heat and mass transfer effects than other devices. The process water in the process water tank 230 and the absorbent manufactured by the absorbent manufacturing device 300 are sprayed into the interior mixed double-flow nozzle 220 and the exterior mixed double-flow nozzle 210 respectively to be sprayed, so that a better atomization effect can be achieved by combining the use of compressed air, and the exterior mixed double-flow nozzle 210 is arranged above the interior mixed double-flow nozzle 220, so that the absorption of sulfur dioxide and nitrogen oxides in the water environment is realized, and the absorption efficiency is improved.
As a further optimization, referring to fig. 1 and 4 together, as a specific embodiment of the flue gas desulfurization and denitrification apparatus provided by the present invention, the internal mixing dual-flow nozzle 220 includes an internal mixing nozzle body 221, an absorbent passage 222 disposed in the center of the internal mixing nozzle body 221 and communicating with the absorbent manufacturing device 300, and a second air passage 223 disposed on the outer periphery of the absorbent passage 222 and having a side portion communicating with the compressed air tank 240, wherein the absorbent passage 222 communicates with the middle portion of the side wall of the second air passage 223, the inner diameter of the outlet of the absorbent passage 222 gradually increases from inside to outside, and the inner diameter of the outlet of the second air passage 223 increases from inside to outsideGradually decreasing. The atomization principle of the internal mixing type two-fluid nozzle 220 is to impact the inside absorbent by using the compressed air flow, generate a larger friction force on the contact surface of the absorbent, and spall the absorbent into absorbent fogdrops under the action of the friction force. The absorbent is often referred to as slurry in the actual production process, and the atomized particles of the absorbent after atomization are referred to as slurry droplets. The adoption of the internal mixing type double-fluid nozzle has the advantages that: the spray nozzle has a larger diameter than a centrifugal pressure nozzle, so that the possibility of nozzle blockage in the running state of the equipment is reduced. The atomization quality of the absorbent is a key factor influencing the desulfurization and denitrification efficiency of the whole device, and the atomization characteristics of the absorbent comprise slurry drop particle size, atomization angle, particle size distribution and the like. In this embodiment, the internal mixing type two-fluid nozzle atomizes the absorbent, and the gas-liquid ratio is selected to be q=0.27 to 0.35. In the reaction process, the particle size of the atomized particles is prevented from being too large or too small, and the larger the atomized particle size is, the longer the single slurry drop drying and desulfurization reaction time is, but the total surface area of the whole reaction is reduced; the smaller the atomized particle size is, the larger the total surface area of the whole reaction is, which is beneficial to improving the desulfurization efficiency of the system, but the too small particle size of slurry drops leads to the too fast evaporation, namely the flash evaporation phenomenon is generated, so that the desulfurization and denitrification efficiency is reduced. For setting the atomization angle, too large or too small is avoided, and the problem that the absorption tower 100 is corroded, slagging and the like is caused because the absorption agent can reach the wall surface of the absorption tower at a speed when the absorption agent is in full contact with the flue gas, namely an adherence phenomenon is formed; the atomization angle is too small, the contact of the flue gas and the absorbent is insufficient, and the mixing is uneven, so that not only is the energy loss caused, but also the designed desulfurization and denitrification efficiency is not achieved. The use of the internal mixing double-flow nozzle 220 improves the contact area of the flue gas to be treated and the absorbent, the desulfurization efficiency is over 99.99 percent, and the concentration of nitrogen oxides at the outlet of the absorption tower is 140mg/m 3 The following is given. Setting the feeding amount of the absorbent according to the original concentration of the flue gas entering the absorption tower 100 and the flow rate of the flue gas, wherein the monitored discharge concentration of the flue gas at the outlet of the absorption tower 100 is used as an auxiliary parameter for checking and accurately adjusting the feeding amount of the absorbent to ensure that the feeding amount of the absorbent is reachedThe desulfurization efficiency is required. A plurality of armored thermocouples on-line monitoring devices which are uniformly distributed can be arranged in the absorption tower 100, so that the internal parameters of the absorption tower 100 can be averaged conveniently, and the accuracy of the monitoring result can be further improved.
As a further optimization, referring to fig. 1 and 4 together, as a specific embodiment of the flue gas desulfurization and denitrification apparatus provided by the present invention, the external mixing dual-flow nozzle 210 includes an external mixing nozzle body 211, a process water path 212 disposed in the center of the external mixing nozzle body 211 and communicated with a process water pipe, and a first air path 213 disposed on an outer ring of the process water path 212 and having a side portion communicated with the compressed air tank 240, wherein an inner diameter of an outlet of the process water path 212 gradually increases from inside to outside, and an inner diameter of an outlet of the first air path 213 gradually decreases from inside to outside. The process water mist drops with uniform height and smaller average granularity can be generated by atomizing the process water by adopting the external mixing type double-fluid nozzle, so that a wet reaction environment is conveniently provided for the absorbent below, and the absorption efficiency of the absorbent is improved. In the process of atomizing process water by the external-mixing type two-fluid nozzle in the embodiment, the gas-liquid ratio is preferably 0.44-0.48, and the gas ratio is improved compared with the atomization of the absorbent, because the existence of the process water droplets is in order to provide an environment favorable for the reaction of the absorbent, and the water requirement is low, but the process water is required to be fully atomized by the air flow of the compressed air, so the gas ratio is improved compared with the gas ratio in the process of atomizing the absorbent.
As a further optimization, referring to fig. 1, as a specific embodiment of the flue gas desulfurization and denitrification device provided by the invention, a cyclone separation device 500 includes a primary cyclone separator 510, a secondary cyclone separator 520 and a tertiary cyclone separator 530 which are sequentially connected in series, slag outlets of the primary cyclone separator 510, the secondary cyclone separator 520 and the tertiary cyclone separator 530 are respectively communicated with a gypsum silo 600 and a primary absorption device 800, an outlet for discharging clean flue gas is arranged at the upper end of the tertiary cyclone separator 530, and the primary cyclone separator 510, the secondary cyclone separator 520 and the tertiary cyclone separator 530 are respectively connected with the primary absorption device 800 through electromagnetic valves. The absorbent is desulfurized and denitrated along with desulfurizationThe reaction proceeds gradually, and the solid particles which have been semi-dried as the absorbent leaves the absorber 100 from the upper end of the absorber 100 are sent to the primary absorber 800 to be re-introduced into the absorber 100 by three cyclone separators 500 which cyclone-separate the products with different particle diameters, wherein the product mainly comprises NaOH and Ca (OH) 2 、CaSO 4 、Na 2 SO 4 And NH 4 NO 3 The remainder is fed into gypsum silo 600 and the clean flue gas is exhausted through the chimney of tertiary cyclone 530. The quantitative supply of desulfurization and denitrification products with different particle sizes is realized by controlling the opening time of the electromagnetic valves respectively arranged on the primary cyclone separator 510, the secondary cyclone separator 520 and the tertiary cyclone separator 530, the products in the three devices are further formed to be proportioned according to the mass ratio of 4.7:2.4:1.1, then the humidity of the desulfurization and denitrification products is regulated through the primary absorption device 800 to have a proper humidity value, and then the products are sent into the absorption tower 100 to primarily absorb flue gas, so that the absorbent is recycled, the absorbent collides with each other in the cyclone separation device 500 to rub, the fresh surfaces are exposed, the absorbent can be reused in the subsequent reaction, the higher utilization rate of the absorbent can also reduce the yield of byproducts of a desulfurization and denitrification system, and the burden is reduced for the post-treatment of desulfurization ash.
As a further optimization, referring to fig. 1, as an embodiment of the flue gas desulfurization and denitrification apparatus provided by the present invention, a primary absorption device 800 includes a primary nozzle 810 disposed in an absorption tower 100, a humidifying digester 820 with a feed inlet connected to a slag outlet of a cyclone separation device 500, and a compressed air assembly 830 for feeding desulfurization and denitrification products in the humidifying digester 820 into the absorption tower 100, wherein the primary nozzle 810 is respectively communicated with a discharge outlet of the humidifying digester 820 and the compressed air assembly 830. In order to enable the desulfurization and denitrification products to smoothly pass through the primary absorption device 800 and enter the absorption tower 100, the recycling in the absorption tower 100 is realized. After the humidity of the partial desulfurization and denitrification product in the cyclone 500 is adjusted by the humidifying digester 820, the partial desulfurization and denitrification product is sent to the absorption tower 100 through the primary nozzle 810 by adopting the compressed air assembly 830, and the use of the compressed air assembly 830 can overcome the blockage of the absorbent in the conveying pipeline and reduce the abrasion of the primary nozzle 810.
As a further optimization, referring to fig. 1 and 2 together, as a specific embodiment of the flue gas desulfurization and denitrification apparatus provided by the present invention, the absorbent manufacturing device 300 includes a tank 310, a stirring assembly 320 disposed inside the tank 310, a pipeline 330 disposed at an outlet end of the tank 310 and used for connecting with the absorption tower 100, and a secondary circuit 340 used for communicating the middle part of the pipeline 330 with the tank 310. The amount of water sprayed in each layer in the height direction is controlled according to the temperature of the flue gas at the outlet of the absorption tower 100 to ensure that the temperature of the flue gas of the absorption tower 100 is as much as possible within the optimal reaction temperature range above the dew point. In the absorber, the absorbent is combined with all SO2 and most NO X The reaction takes place as follows:
NaOH+SO 2 →Na 2 SO 3 +H 2 O
Na 2 SO 3 +O 2 →Na 2 SO 4
Ca(OH) 2 +SO 2 →CaSO 3 +H 2 O
CaSO 3 +O 2 →CaSO 4
NO X +H 2 O 2 →NO 2 +H 2 O
NaOH+NO 2 →NaNO 3 +H 2 O
NH 3 ·H 2 O+NO 2 →NH 4 NO 3 +H 2 O
the device adopts Ca (OH) 2 And NaOH double alkali absorbent, and H with the addition concentration of 20.5% is added simultaneously 2 O 2 And NaCL in which Ca (OH) 2 、NaOH、H 2 O 2 And NaCL in a mass ratio of 62.2%, 35.1% and 2.6%, 1.1%, H is added 2 O 2 And the NaCL can improve the desulfurization and denitrification efficiency and the utilization rate of the desulfurization and denitrification agent, and the additive NaCL can delay the evaporation time of slurry drops. In order to prevent the absorbent from being non-uniform or generating precipitation during the absorbent preparation process, a stirring assembly 320 is installed in the tank 310, the absorbentIn the manufacturing process of (2), the mass of the double-alkali absorbent and the water amount added into the tank 310 are changed to prepare the absorbent with different concentrations so as to match the absorption of the smoke with different components, and the stirring assembly 320 automatically stirs at a uniform speed in the preparation process and the production process of the absorbent, so that the uniformity of the slurry preparation is realized. At the same time, in order to ensure that the absorbent particles are not deposited in the pipeline 330, the flow rate of the absorbent should be not lower than 1.8m/s, and the flow rate of the absorbent should be set so that the flow rate of the absorbent is far higher than the actually required flow rate, so that the secondary circuit 340 is adopted to realize the reflux of the absorbent, namely, a large part of the absorbent in the pipeline 330 flows back into the tank 310 through the secondary circuit 340, and only a small part enters the absorption tower 100 through the electric regulating valve 332 arranged on the pipeline 330 and is supplied to the two internal mixing double-flow nozzles 220.
As a further optimization, referring to fig. 1 and fig. 2 together, as a specific embodiment of the flue gas desulfurization and denitrification apparatus provided by the present invention, an absorbent pump 331 and an electric control valve 332 are sequentially disposed on a pipeline 330 along the flow direction of the absorbent, and an inlet end of a secondary circuit 340 is disposed between the absorbent pump 331 and the electric control valve 332. To prevent the absorbent from settling in the pipeline, the backwash assembly 333 is periodically activated to flush the pipeline. The electric control valve 332 is used for controlling the amount of the absorbent in the tank 310 entering the slurry in the absorption tower 100, the absorbent pump 331 is used for promoting the flow of the slurry in the pipeline 330, and the inlet end of the secondary circuit 340 is arranged between the absorbent pump 331 and the electric control valve 332, so as to realize the effect of most of the slurry backflow in the pipeline 330.
As a further optimization, referring to fig. 1 and fig. 2 together, as a specific embodiment of the flue gas desulfurization and denitrification apparatus provided by the present invention, a backwash assembly 333 is further provided on the pipeline 330. The backwash assembly 333 is configured to be conveniently and periodically opened for flushing the pipeline during service, and the backwash assembly 333 is configured to be conveniently and periodically cleaned to ensure good absorbent manufacturing quality because the absorbent is easily attached to the pipeline 330 during delivery.
Embodiment one:
the absorption tower 100 is a cuboid, the material of the absorption tower 100 is a rigid material, the tower height is 39.4m, three layers of a primary absorption device 800, a main absorption device 200 and a main absorption device 200 are sequentially arranged from bottom to top, the three layers of the primary absorption device 800, the main absorption device 200 and the main absorption device 200 are respectively arranged at positions of 7.2m, 22.8m and 31.6m of the tower height in the absorption tower 100, the primary absorption device 800 is connected with a gypsum silo 600 through pipelines, and the two main absorption devices 200 are respectively connected with a process water tank 230, a compressed air tank 240 and an absorbent manufacturing device 300 through pipelines. The absorption tower 100 is provided with 6 visible holes which are respectively arranged at the positions of 1.9m of the flue gas inlet of the absorption tower 100, the effective heights of 6.3m, 12.6m, 18.9m, 25.2m and 38.4m of the outlet of the absorption tower 100. The temperature measuring area in the absorption tower 100 is divided into a slurry-free area and a flue gas slurry mixing area, wherein the slurry-free area is an area above two main absorption devices 200, the flue gas slurry mixing area is an area below the main absorption device 200 which is relatively upper, the flue gas temperature in the slurry-free area is monitored on line by five armored thermocouples uniformly arranged at the heights of 26.8m and 35.6m of the absorption tower 100, the temperature in the flue gas slurry mixing area is monitored on line by five air extraction thermocouples uniformly arranged at the heights of 23.8m and 32.6m of the absorption tower 100, and the test results are all averaged.
According to the flue gas desulfurization and denitrification equipment provided by the invention, the desulfurization and denitrification products are introduced into the absorption tower through the primary absorption device, so that the recycling of the absorbent is realized, the absorption efficiency of the absorbent can be effectively improved, meanwhile, the absorbent can be prevented from being dried and adhered on the inner wall of the absorption tower, the service efficiency of the absorbent is improved, and the flue gas after entering the absorption tower is filtered by combining with the cyclone separation device, so that the effective dust removal of the flue gas is realized, and the pollution to the surrounding environment is avoided.
The foregoing description of the preferred embodiments of the invention is not intended to be limiting, but rather is intended to cover all modifications, equivalents, and alternatives falling within the spirit and principles of the invention.
Claims (6)
1. The flue gas desulfurization and denitrification equipment is characterized in that: the device comprises an absorption tower (100), a flue gas feeding device (400) arranged at the air inlet of the absorption tower (100), a main absorption device (200) arranged inside the absorption tower (100), a cyclone separation device (500) with the air inlet communicated with the air outlet of the absorption tower (100) and a gypsum bin (600) with the slag inlet communicated with the slag outlet of the cyclone separation device (500), wherein a primary absorption device (800) is further arranged between the air inlet of the absorption tower (100) and the main absorption device (200), the feed inlet of the primary absorption device (800) is communicated with the slag outlet of the cyclone separation device (500), and the discharge outlet of the primary absorption device (800) is communicated with the inner cavity of the absorption tower (100);
the main absorption device (200) is uniformly provided with at least two groups in the height direction of the absorption tower (100), the main absorption device (200) comprises an external mixing double-flow nozzle (210) for conveying process water and an internal mixing double-flow nozzle (220) which is arranged below the external mixing double-flow nozzle (210) and is used for conveying absorbent, the external mixing double-flow nozzle (210) is connected with a process water tank (230), the internal mixing double-flow nozzle (220) is connected with an absorbent manufacturing device (300), and the internal mixing double-flow nozzle (220) and the external mixing double-flow nozzle (210) are respectively connected with a compressed air tank (240);
the internal mixing double-flow nozzle (220) comprises an internal mixing nozzle body (221), an absorbent passage (222) which is arranged in the center of the internal mixing nozzle body (221) and communicated with the absorbent manufacturing device (300), and a second air passage (223) which is arranged on the outer ring of the absorbent passage (222) and the side part of which is communicated with the compressed air tank (240), wherein the absorbent passage (222) is communicated with the middle part of the side wall of the second air passage (223), the inner diameter of an outlet of the absorbent passage (222) is gradually increased from inside to outside, and the inner diameter of an outlet of the second air passage (223) is gradually reduced from inside to outside;
the external mixing double-flow nozzle (210) comprises an external mixing nozzle body (211), a process water channel (212) which is arranged in the center of the external mixing nozzle body (211) and is communicated with a process water pipe, and a first air channel (213) which is arranged on the outer ring of the process water channel (212) and is communicated with a compressed air tank (240) on the side part, wherein the inner diameter of an outlet of the process water channel (212) gradually increases from inside to outside, and the inner diameter of an outlet of the first air channel (213) gradually decreases from inside to outside;
the primary absorption device (800) comprises a primary nozzle (810) arranged in the absorption tower (100), a humidifying digester (820) with a feeding hole connected with a slag outlet of the cyclone separation device (500) and a compressed air component (830) for feeding desulfurization and denitrification products in the humidifying digester (820) into the absorption tower (100), wherein the primary nozzle (810) is respectively communicated with a discharge hole of the humidifying digester (820) and the compressed air component (830).
2. A flue gas desulfurization and denitrification device according to claim 1, wherein: the flue gas feeding device (400) comprises a dust remover (410) and a venturi tube (420) which are sequentially arranged along the direction of the flue gas flow and are used for introducing the flue gas into the absorption tower (100).
3. A flue gas desulfurization and denitrification device according to claim 1, wherein: the cyclone separation device (500) comprises a primary cyclone separator (510), a secondary cyclone separator (520) and a tertiary cyclone separator (530) which are sequentially connected in series, slag outlets of the primary cyclone separator (510), the secondary cyclone separator (520) and the tertiary cyclone separator (530) are respectively communicated with the gypsum bin (600) and the primary absorption device (800), an outlet for discharging clean flue gas is formed in the upper end of the tertiary cyclone separator (530), and the primary cyclone separator (510), the secondary cyclone separator (520) and the tertiary cyclone separator (530) are also respectively connected with the primary absorption device (800) through electromagnetic valves.
4. A flue gas desulfurization and denitrification device according to claim 1, wherein: the absorbent manufacturing device (300) comprises a tank body (310), a stirring assembly (320) arranged in the tank body (310), a pipeline (330) arranged at the outlet end of the tank body (310) and used for being connected with the absorption tower (100), and a secondary circuit (340) used for communicating the middle part of the pipeline (330) with the tank body (310).
5. A flue gas desulfurization and denitrification apparatus according to claim 4, wherein: the pipeline (330) is sequentially provided with an absorbent pump (331) and an electric regulating valve (332) along the flowing direction of the absorbent, and the inlet end of the secondary circuit (340) is arranged between the absorbent pump (331) and the electric regulating valve (332).
6. A flue gas desulfurization and denitrification device as set forth in claim 5, wherein: and a back flushing assembly (333) is further arranged on the pipeline (330).
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