CN112546825A - Device and method for reducing and zero-discharging desulfurization wastewater and reducing emission of acid gas - Google Patents
Device and method for reducing and zero-discharging desulfurization wastewater and reducing emission of acid gas Download PDFInfo
- Publication number
- CN112546825A CN112546825A CN202011242787.4A CN202011242787A CN112546825A CN 112546825 A CN112546825 A CN 112546825A CN 202011242787 A CN202011242787 A CN 202011242787A CN 112546825 A CN112546825 A CN 112546825A
- Authority
- CN
- China
- Prior art keywords
- absorbent
- slurry
- flue gas
- desulfurization
- waste water
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Pending
Links
- 238000006477 desulfuration reaction Methods 0.000 title claims abstract description 101
- 230000023556 desulfurization Effects 0.000 title claims abstract description 101
- 239000002351 wastewater Substances 0.000 title claims abstract description 83
- 238000000034 method Methods 0.000 title claims abstract description 50
- 239000002253 acid Substances 0.000 title claims abstract description 23
- 230000001603 reducing effect Effects 0.000 title claims abstract description 21
- 238000007599 discharging Methods 0.000 title claims abstract description 13
- 239000003546 flue gas Substances 0.000 claims abstract description 115
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims abstract description 112
- 239000002002 slurry Substances 0.000 claims abstract description 99
- 230000002745 absorbent Effects 0.000 claims abstract description 96
- 239000002250 absorbent Substances 0.000 claims abstract description 96
- 238000000889 atomisation Methods 0.000 claims abstract description 59
- 238000010521 absorption reaction Methods 0.000 claims abstract description 49
- 238000001035 drying Methods 0.000 claims abstract description 48
- 239000007789 gas Substances 0.000 claims abstract description 43
- 239000007921 spray Substances 0.000 claims abstract description 37
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 36
- 238000000746 purification Methods 0.000 claims abstract description 27
- 230000009467 reduction Effects 0.000 claims abstract description 26
- 230000029087 digestion Effects 0.000 claims abstract description 23
- 230000002378 acidificating effect Effects 0.000 claims abstract description 22
- 239000000706 filtrate Substances 0.000 claims abstract description 20
- 239000000428 dust Substances 0.000 claims description 31
- 230000008569 process Effects 0.000 claims description 25
- 239000002245 particle Substances 0.000 claims description 11
- 238000005507 spraying Methods 0.000 claims description 10
- HEMHJVSKTPXQMS-UHFFFAOYSA-M sodium hydroxide Inorganic materials [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 claims description 8
- 239000007787 solid Substances 0.000 claims description 8
- 238000004140 cleaning Methods 0.000 claims description 4
- 238000001914 filtration Methods 0.000 claims description 4
- 239000012530 fluid Substances 0.000 claims description 4
- 239000000347 magnesium hydroxide Substances 0.000 claims description 4
- 229910001862 magnesium hydroxide Inorganic materials 0.000 claims description 4
- CDBYLPFSWZWCQE-UHFFFAOYSA-L sodium carbonate Substances [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 claims description 4
- 229910000029 sodium carbonate Inorganic materials 0.000 claims description 4
- 238000003756 stirring Methods 0.000 claims description 3
- 238000004065 wastewater treatment Methods 0.000 abstract description 18
- 230000002195 synergetic effect Effects 0.000 abstract description 3
- TXKMVPPZCYKFAC-UHFFFAOYSA-N disulfur monoxide Inorganic materials O=S=S TXKMVPPZCYKFAC-UHFFFAOYSA-N 0.000 description 17
- XTQHKBHJIVJGKJ-UHFFFAOYSA-N sulfur monoxide Chemical compound S=O XTQHKBHJIVJGKJ-UHFFFAOYSA-N 0.000 description 17
- 238000005245 sintering Methods 0.000 description 11
- 238000006722 reduction reaction Methods 0.000 description 10
- 239000010440 gypsum Substances 0.000 description 7
- 229910052602 gypsum Inorganic materials 0.000 description 7
- 150000002500 ions Chemical class 0.000 description 7
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 description 6
- 238000005260 corrosion Methods 0.000 description 6
- 230000007797 corrosion Effects 0.000 description 6
- 238000001704 evaporation Methods 0.000 description 6
- 230000008020 evaporation Effects 0.000 description 6
- 239000000779 smoke Substances 0.000 description 6
- 239000000126 substance Substances 0.000 description 6
- 230000003197 catalytic effect Effects 0.000 description 5
- 238000006243 chemical reaction Methods 0.000 description 5
- 239000012528 membrane Substances 0.000 description 5
- VEXZGXHMUGYJMC-UHFFFAOYSA-M Chloride anion Chemical compound [Cl-] VEXZGXHMUGYJMC-UHFFFAOYSA-M 0.000 description 4
- 239000011575 calcium Substances 0.000 description 4
- 238000010586 diagram Methods 0.000 description 4
- 150000003839 salts Chemical class 0.000 description 4
- 235000019738 Limestone Nutrition 0.000 description 3
- 239000000443 aerosol Substances 0.000 description 3
- 230000000694 effects Effects 0.000 description 3
- 238000005265 energy consumption Methods 0.000 description 3
- 239000006028 limestone Substances 0.000 description 3
- 230000001105 regulatory effect Effects 0.000 description 3
- 239000002918 waste heat Substances 0.000 description 3
- UXVMQQNJUSDDNG-UHFFFAOYSA-L Calcium chloride Chemical compound [Cl-].[Cl-].[Ca+2] UXVMQQNJUSDDNG-UHFFFAOYSA-L 0.000 description 2
- JLVVSXFLKOJNIY-UHFFFAOYSA-N Magnesium ion Chemical compound [Mg+2] JLVVSXFLKOJNIY-UHFFFAOYSA-N 0.000 description 2
- 239000003513 alkali Substances 0.000 description 2
- 229910001424 calcium ion Inorganic materials 0.000 description 2
- 238000010531 catalytic reduction reaction Methods 0.000 description 2
- 239000003245 coal Substances 0.000 description 2
- 238000002485 combustion reaction Methods 0.000 description 2
- 238000002425 crystallisation Methods 0.000 description 2
- 230000008025 crystallization Effects 0.000 description 2
- 230000008021 deposition Effects 0.000 description 2
- 210000003746 feather Anatomy 0.000 description 2
- 229910001385 heavy metal Inorganic materials 0.000 description 2
- 229910001425 magnesium ion Inorganic materials 0.000 description 2
- 239000000203 mixture Substances 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 239000000843 powder Substances 0.000 description 2
- 238000004064 recycling Methods 0.000 description 2
- 238000000926 separation method Methods 0.000 description 2
- 238000006467 substitution reaction Methods 0.000 description 2
- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 description 1
- BHPQYMZQTOCNFJ-UHFFFAOYSA-N Calcium cation Chemical compound [Ca+2] BHPQYMZQTOCNFJ-UHFFFAOYSA-N 0.000 description 1
- 229910000831 Steel Inorganic materials 0.000 description 1
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 1
- 238000009825 accumulation Methods 0.000 description 1
- 238000003916 acid precipitation Methods 0.000 description 1
- 230000002411 adverse Effects 0.000 description 1
- 230000033228 biological regulation Effects 0.000 description 1
- AXCZMVOFGPJBDE-UHFFFAOYSA-L calcium dihydroxide Chemical compound [OH-].[OH-].[Ca+2] AXCZMVOFGPJBDE-UHFFFAOYSA-L 0.000 description 1
- 239000000920 calcium hydroxide Substances 0.000 description 1
- 229910001861 calcium hydroxide Inorganic materials 0.000 description 1
- 239000003054 catalyst Substances 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 239000003814 drug Substances 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 239000003500 flue dust Substances 0.000 description 1
- 239000011521 glass Substances 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 206010022000 influenza Diseases 0.000 description 1
- JEIPFZHSYJVQDO-UHFFFAOYSA-N iron(III) oxide Inorganic materials O=[Fe]O[Fe]=O JEIPFZHSYJVQDO-UHFFFAOYSA-N 0.000 description 1
- 239000007788 liquid Substances 0.000 description 1
- 230000007774 longterm Effects 0.000 description 1
- 230000014759 maintenance of location Effects 0.000 description 1
- 238000001471 micro-filtration Methods 0.000 description 1
- 238000010992 reflux Methods 0.000 description 1
- 238000001223 reverse osmosis Methods 0.000 description 1
- 230000001568 sexual effect Effects 0.000 description 1
- 239000010959 steel Substances 0.000 description 1
- 239000011593 sulfur Substances 0.000 description 1
- 229910052717 sulfur Inorganic materials 0.000 description 1
Images
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
- B01D53/38—Removing components of undefined structure
- B01D53/40—Acidic components
-
- 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
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/02—Treatment of water, waste water, or sewage by heating
- C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
- C02F1/043—Details
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/02—Treatment of water, waste water, or sewage by heating
- C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
- C02F1/10—Treatment of water, waste water, or sewage by heating by distillation or evaporation by direct contact with a particulate solid or with a fluid, as a heat transfer medium
- C02F1/12—Spray evaporation
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/02—Treatment of water, waste water, or sewage by heating
- C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
- C02F1/16—Treatment of water, waste water, or sewage by heating by distillation or evaporation using waste heat from other processes
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2251/00—Reactants
- B01D2251/30—Alkali metal compounds
- B01D2251/304—Alkali metal compounds of sodium
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2251/00—Reactants
- B01D2251/40—Alkaline earth metal or magnesium compounds
- B01D2251/402—Alkaline earth metal or magnesium compounds of magnesium
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2251/00—Reactants
- B01D2251/40—Alkaline earth metal or magnesium compounds
- B01D2251/404—Alkaline earth metal or magnesium compounds of calcium
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2251/00—Reactants
- B01D2251/60—Inorganic bases or salts
- B01D2251/602—Oxides
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2251/00—Reactants
- B01D2251/60—Inorganic bases or salts
- B01D2251/604—Hydroxides
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2251/00—Reactants
- B01D2251/60—Inorganic bases or salts
- B01D2251/606—Carbonates
-
- 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
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2103/00—Nature of the water, waste water, sewage or sludge to be treated
- C02F2103/18—Nature of the water, waste water, sewage or sludge to be treated from the purification of gaseous effluents
Abstract
The invention relates to the technical field of wastewater treatment, and discloses a device and a method for reducing and zero-discharging desulfurization wastewater and acidic gas, wherein the device for treating the desulfurization wastewater is connected with a flue gas purification system and comprises the following components: the device comprises an absorbent storage bin, a digestion tank, a deacidification slurry tank, a slurry conveying device and an atomization spray gun which are connected in sequence, wherein the absorbent storage bin is used for storing an alkaline absorbent; the digestion tank is also connected with a filtrate storage device so as to enable the desulfurization waste water to react with the alkaline absorbent to form deacidified absorbent slurry; and the atomized deacidified absorbent slurry is sprayed into the atomization drying and absorption device by the atomization spray gun so as to react with the acid gas in the flue gas entering the atomization drying and absorption device. The invention not only solves the problem of desulfurization waste water discharge, but also recycles the water resource in the desulfurization waste water, saves the water consumption of a wet desulfurization system, and realizes the zero discharge of the desulfurization waste water and the synergistic emission reduction of the acid gas in the flue gas.
Description
Technical Field
The invention relates to the technical field of wastewater treatment, in particular to a method for realizing reduction and zero discharge of desulfurization wastewater and realizing cooperative emission reduction of SO3The device and the method for treating the flue gas desulfurization wastewater of the acidic gas.
Background
The limestone-gypsum wet flue gas desulfurization technology can efficiently remove SO in flue gas2And has the characteristic of high system reliability, and is the most widely used method in the current flue gas desulfurization engineering. The impurities in the waste water in the wet desulfurization (limestone-gypsum method) mainly come from flue gas and desulfurizer, and the Cl ions in the flue gas mainly come from the combustion of coal/ore, etc., Cl ions in the desulfurizer limestone and Cl ions in the process waterAnd (4) Cl ions. During the wet desulphurization process of the flue gas, the system can gradually enrich Cl ions, heavy metal ions and the like, and can have adverse effects on the desulphurization system, such as: affecting the desulfurization efficiency, accelerating the corrosion of equipment, and having poor gypsum quality, etc. It is often necessary to discharge a certain amount of wastewater from the system to maintain a long-term stable operation of the desulfurization unit. Along with the continuous improvement of environmental protection requirement, especially to the restriction of waste water discharge more and more tight, desulfurization waste water must just can discharge through handling, and conventional desulfurization waste water is the triplex case chemical treatment, and this treatment mode consumes the medicament great, and difficult up to standard, even up to standard, because of the higher content of Cl ion that contains in the waste water, still can not recycle again.
At present, the flue gas desulfurization wastewater treatment method mainly comprises the following steps: membrane concentration, crystallization evaporation and direct flue evaporation.
Wherein, the membrane concentration + evaporative crystallization (MVR) mode is as follows: removing heavy metals, calcium ions, magnesium ions, suspended matters and the like in water through chemical softening and a microfiltration membrane; through membrane advanced treatment, reverse osmosis produced water reaches the standard of recycled water, and the concentrated solution can be subjected to MVR evaporation to obtain salt. The method can realize zero discharge of the desulfurization wastewater, but because the content of calcium and magnesium ions in the desulfurization wastewater is higher, the consumption of a membrane advanced treatment agent is higher, the energy consumption is higher, the process is complex, the investment cost is high, and the operating cost is high.
The direct evaporation mode of the flue is as follows: the desulfurization waste water is atomized and sprayed in the flue, and can be dried and evaporated by utilizing the heat of the flue gas to be converted into solid matters, so that zero emission of the desulfurization waste water can be realized. However, the following problems may occur: desulfurization wastewater is directly evaporated without reduction, incomplete evaporation is probably caused by large spraying amount, the humidity of flue gas is increased, and low-temperature corrosion perforation is caused to a flue and a dust removal system; in particular, coarse liquid drops exist due to poor atomization of the waste water, and flue dust deposition is easy to occur; the atomization performance is deteriorated under the conditions of unstable smoke amount and low load smoke temperature and smoke flow velocity, and smoke dust deposition and equipment corrosion are possible to occur.
In addition, boiler flue gas is subjected to Selective Catalytic reduction (Selective Catalytic reduction)on, SCR) denitration system, SO in flue gas2Will convert a certain amount into SO3(ii) a In the sintering process, because of the existence of Fe2O3Presence of SO in flue gas at higher temperatures2Can be converted into SO3. With the comprehensive entering of power plant and steel plant for ultra-clean discharge, wet desulphurization is used for SO2Has a higher removal rate but to SO3The removal rate of the limestone desulfurization slurry is not high, and SO is removed by the limestone desulfurization slurry2Has an absorption rate greater than SO3The absorption rate of (2) and the retention time of the flue gas in the absorption tower is short, SO the absorption tower has poor effect of removing sulfuric acid aerosol, usually SO3The removal efficiency of (A) is about 30 percent, and SO3And finally discharged through a chimney in the form of sulfuric acid aerosol. After the sulfuric acid aerosol enters the atmospheric environment, haze weather, acid rain and the like are caused, the transparency of smoke is reduced, and SO in the smoke is discharged3Higher than 16mg/Nm3The appearance of "blue feather". Therefore, SO3The problem of emission reduction is also very much regarded at present.
Therefore, there is a need for a method capable of simultaneously realizing zero discharge of desulfurization wastewater and removal of SO3The flue gas desulfurization wastewater treatment device.
Disclosure of Invention
In view of the above problems, the present invention aims to provide a device and a method for reducing desulfurization wastewater, zero emission and acid gas emission, SO as to solve the problems of high cost, easy corrosion and difficulty in realizing zero emission of desulfurization wastewater by using the existing flue gas desulfurization wastewater treatment device3Emission reduction and the like.
In order to achieve the above object, an aspect of the present invention provides a device for reducing and zero-discharging desulfurization wastewater and acid gas, which is connected to a flue gas purification system, the flue gas purification system comprising: the device comprises a flue gas generating device, an atomization drying and absorption device, a dust remover and a filtrate storage device, wherein the atomization drying and absorption device is connected between the flue gas generating device and the dust remover, and the filtrate storage device is arranged at the tail end of the flue gas purification system to store desulfurization wastewater;
flue gas desulfurization effluent treatment plant includes: the device comprises an absorbent storage bin, a digestion tank, a deacidification slurry tank, a slurry conveying device and an atomization spray gun which are connected in sequence, wherein the absorbent storage bin is used for storing an alkaline absorbent; the digestion tank is also connected with the filtrate storage device so as to enable the desulfurization wastewater to react with an alkaline absorbent to form deacidified absorbent slurry;
and the atomized deacidified absorbent slurry is sprayed into the atomization drying and absorption device by the atomization spray gun so as to react with the acidic gas in the flue gas entering the atomization drying and absorption device.
Preferably, the flue gas desulfurization wastewater treatment device further comprises a filter arranged between the slurry conveying device and the atomizing spray gun.
Preferably, a stirring device is arranged in each of the digestion tank and the deacidification slurry tank.
Preferably, the atomizing spray gun is a three-fluid atomizing spray gun, and is provided with a slurry conveying pipeline, a process water conveying pipeline and a compressed air conveying pipeline, and the slurry conveying pipeline and the process water conveying pipeline are both provided with a flow meter and an adjusting valve.
Preferably, the particle size of the atomized deacidification absorbent slurry is 10-60 mu m.
Preferably, the alkaline absorbent comprises: CaO, Ca (OH)2、MgO、Mg(OH)2NaOH and Na2CO3One or more of (a).
In order to achieve the above object, another aspect of the present invention provides a method for reducing and zero-discharging desulfurized wastewater and acid gas, comprising:
adding set amounts of desulfurization waste water and an alkaline absorbent into a digestion tank, wherein the desulfurization waste water and the alkaline absorbent react in the digestion tank to generate a deacidification absorbent slurry, and the desulfurization waste water is generated by a flue gas purification system;
conveying the deacidified absorbent slurry, water and compressed air to an atomizing spray gun, and atomizing the deacidified absorbent slurry in the atomizing spray gun;
and spraying the atomized deacidified absorbent slurry into an atomization drying and absorption device to enable the atomized deacidified absorbent slurry to react with the acidic gas in the flue gas entering the atomization drying and absorption device to generate solid particles.
Preferably, before the deacidified absorbent slurry is conveyed to the atomizing spray gun, the method further comprises the following steps: and filtering the deacidification absorbent slurry.
Preferably, the particle size of the atomized deacidification absorbent slurry is 10-60 mu m.
Preferably, the spraying amount of the atomized deacidified absorbent slurry sprayed into the atomization drying and absorption device is adjusted according to the temperature of the flue gas at the outlet of the atomization drying and absorption device.
Compared with the prior art, the device and the method for reducing and zero-discharging the desulfurization wastewater and the acidic gas have the advantages that:
the invention utilizes the desulfurization waste water to prepare absorbent slurry, and the absorbent slurry is sprayed into the atomization drying absorption device to be fully contacted with the flue gas, so that the acidic gas in the flue gas can be absorbed. Not only solves the problem of the discharge of the desulfurization waste water, but also recovers the water resource in the desulfurization waste water, saves the water consumption of a wet desulfurization system, realizes the zero discharge of the desulfurization waste water, and simultaneously reduces the emission of acid gas, especially SO, in the flue gas in a synergic manner3And PM2.5 emission reduction is achieved.
The invention can utilize the waste heat of the flue gas as a steam heating source in the atomization drying absorption device, does not need additional steam and reduces the energy consumption.
The method has the advantages of simple process flow, convenient operation and small occupied area; the investment and the operating cost are low.
Drawings
FIG. 1 is a schematic structural diagram of a flue gas desulfurization wastewater treatment device applied to a boiler flue gas purification system according to an embodiment of the present invention;
FIG. 2 is a schematic structural diagram of a flue gas desulfurization wastewater treatment device applied to a flue gas purification system of a sintering machine according to an embodiment of the invention;
in the figure, 1, a boiler; 2. an atomization drying absorption device; 3. a flue; 4. a flapper door; 5. a dust remover; 6. a dust remover ash discharging and pneumatic ash conveying system; 7. an induced draft fan; 8. a wet desulfurization tower; 9. A vacuum belt dehydrator; 10. a filtrate storage device; 11. a digestion tank; 12. an absorbent storage bin; 13. a deacidification slurry tank; 14. a slurry delivery device; 15. a filter; 16. an atomizing spray gun; 17. a slurry flow meter; 18. a process water flow meter; 19. a slurry regulating valve; 20. a process water regulating valve; 21. an SCR denitration catalytic reactor; 22. sintering machine; 23. a machine head dust remover; 24. a main exhaust fan.
Detailed Description
The following detailed description of embodiments of the present invention is provided in connection with the accompanying drawings and examples. The following examples are intended to illustrate the invention but are not intended to limit the scope of the invention.
Example 1
As shown in fig. 1, a schematic structural diagram of an application of a device for reducing desulfurization wastewater, realizing zero emission and reducing emission of acid gas (hereinafter referred to as "flue gas desulfurization wastewater treatment device") in a boiler flue gas purification system according to an embodiment of the present invention is shown, the flue gas desulfurization wastewater treatment device is connected to the boiler flue gas purification system, wherein the boiler flue gas purification system includes: the system comprises a flue gas generating device, an atomization drying and absorption device 2, a dust remover 5, an induced draft fan 7, a wet desulphurization tower 8 (wet desulphurization is carried out by limestone-gypsum in the wet desulphurization tower 8), a chimney, a vacuum belt dehydrator and a filtrate storage device 10, wherein the flue gas generating device comprises a boiler 1 and an SCR denitration catalytic reactor 21, the atomization drying and absorption device 2 is connected between the SCR denitration catalytic reactor 21 and the dust remover 5 and is used for carrying out atomization drying on flue gas, a flue 3 between the atomization drying and absorption device 2 and the dust remover 5 needs to be close to the dust remover 5 as much as possible, and the flue 3 cannot form a U-shaped bend to prevent dust from accumulating to block the flue 3 and influence normal operation; a baffle door 4 is arranged on a flue between the SCR denitration catalytic reactor 21 and the dust remover 5 and close to the dust remover 5, so that the flue gas completely enters the atomization drying absorption device 2; the filtrate storage device 10 is arranged at the tail end of the boiler flue gas purification system and used for storing desulfurization wastewater generated by the flue gas purification system.
Flue gas desulfurization effluent treatment plant includes: the device comprises an absorbent storage bin 12, a digestion tank 11, a deacidification slurry tank 13, a slurry conveying device 14 and an atomizing spray gun 16 which are sequentially connected, wherein the absorbent storage bin 12 is used for storing an alkaline absorbent, the alkaline absorbent is in a dry powder shape, and the size of the absorbent storage bin 12 can be determined according to the amount of desulfurization wastewater, the amount of flue gas acidic gas and the like; the digestion tank 11 is also connected with the filtrate storage device 10 to receive the desulfurization wastewater and the alkaline absorbent, so that the desulfurization wastewater and the alkaline absorbent react to form deacidified absorbent slurry; the deacidification slurry tank 13 is connected with the digestion tank 11 to buffer deacidification absorbent slurry; the slurry conveying device 14 is connected with the deacidification slurry tank 13 and is used for conveying the deacidification absorbent slurry to an atomization spray gun 16; the atomizing spray gun 16 is used for atomizing the deacidified absorbent slurry, and spraying the atomized deacidified absorbent slurry into the atomizing, drying and absorbing device 2, so that the atomized deacidified absorbent slurry reacts with the acidic gas in the flue gas entering the atomizing, drying and absorbing device 2.
The boiler generates flue gas containing acidic gases (HCl, HF, SO) from coal combustion2、SO3Etc.), the flue gas that comes out from boiler 1 loops through the flue and gets into SCR denitration catalytic reactor 21, atomizing drying absorbing device 2, dust remover 5, draught fan 7, wet flue gas desulfurization tower 8, vacuum belt hydroextractor 9 and chimney. The desulfurization wastewater is obtained from filtrate water obtained after gypsum is separated from a vacuum belt dehydrator 9 and cached in a filtrate storage device 10; separating gypsum from filtrate water in a wet desulphurization tower 8, and storing the gypsum in a filtrate caching device when the content of chloride ions in the filtrate water reaches 15000-; and when the content of chloride ions in the filtrate water does not reach 15000mg/L, refluxing the filtrate water to the wet desulphurization tower 8 for reuse. A certain amount of SO is generated at the outlet of the SCR denitration catalyst reactor 212Conversion to SO3The flue gas enters an atomization drying absorption device 2 along with the flue gas, fog drops of deacidification absorbent slurry are sprayed out to the atomization drying absorption device 2 through an atomization spray gun 16 and are fully contacted with high-temperature flue gas containing acidic gas, so that acidic components in the flue gas are absorbed and reacted, and meanwhile, the fog drops in the deacidification absorbent slurryThe water is evaporated, the water enters the flue gas, the dried substances such as salts and the like generated by the reaction enter the dust remover 5 along with the flue gas for gas-solid separation treatment, and the dried substances are separated and collected by the dust remover ash discharging and pneumatic ash conveying system 6 connected with the dust remover 5.
The flue gas desulfurization wastewater treatment device provided by the invention utilizes desulfurization wastewater as a part of deacidification absorbent slurry, and sprays the desulfurization wastewater into the atomization drying absorption device 2 to react with flue gas, SO that acidic gas in the flue gas can be absorbed, and the reduction and zero emission of the desulfurization wastewater can be realized, and the synergistic emission reduction of SO (sulfur oxide) can be realized3、HCl、SO2And reducing PM2.5 emission.
In addition, the invention can reduce SO entering the wet desulphurization tower 8 by adding the deacidification absorbent slurry into the atomization drying absorption device 2 to absorb a part of acid gas, which is equivalent to primary desulphurization in a flue gas purification system2Content, thereby ensuring that the emission of the flue gas purification system meets the ultra-clean requirement.
In addition, taking the alkaline absorbent as calcium hydroxide as an example, the deacidification absorbent slurry reacts with HCl in the atomization drying absorption device 2 to generate calcium chloride salt and the like, and the calcium chloride salt and the like are separated from the flue gas in the dust remover 5, so that the HCl in the flue gas can be reduced to enter the wet desulphurization tower 8, the total chloride ion entering amount in the wet desulphurization tower 8 is reduced, the discharge amount of the desulphurization waste water is reduced, and the desulphurization waste water reducing effect is also achieved.
In addition, in the atomization drying absorption device 2, because the temperature of the flue gas entering the atomization drying absorption device is higher, generally about 130-170 ℃, the flue gas can be used as a heat source for evaporation by using the waste heat of the flue gas, no extra steam is needed, the energy consumption is reduced, and the operation cost is reduced. In the atomization drying absorption device 2, the acid absorbent slurry and the acidic gas (SO) in the flue gas are removed3、HCl、HF、SO2Etc.) enters a dust remover 5 in the flue gas purification system through the flue after the reaction, and the generated solid particle salt is collected and separated by the dust remover 5, thereby achieving the purpose of reducing the emission of SO3The function of (1); the generated steam enters the wet desulphurization system along with the flue gas for recycling, thereby reducing the process water consumption in the wet desulphurization.
Preferably, the flue gas desulfurization wastewater treatment device further comprises a filter 15, which is arranged between the slurry conveying device 14 and the atomizing spray gun 16, and is used for filtering the deacidification absorbent slurry. The filter 15 is preferably a self-cleaning filter or a blue filter, using an 80 mesh screen.
In order to better contact reaction between the desulfurization waste water and the alkaline absorbent, it is preferable that stirring devices be provided in both the digestion tank 11 and the deacidification slurry tank 13. And, glass flake is set in digestion tank 11 and deacidification slurry tank 13 to prevent corrosion.
The slurry delivery device 14 employs a slurry feed pump and a regulating valve is provided at the outlet of the pump to control the flow of the deacidified absorbent slurry into the atomizing spray gun 16.
The atomization spray gun 16 adopts a three-fluid atomization spray gun 16 and is provided with a slurry conveying pipeline, a process water conveying pipeline and a compressed air conveying pipeline, deacidified absorbent slurry, water and compressed air are simultaneously input, a slurry flow meter 17 and a slurry adjusting valve 19 are arranged on the slurry conveying pipeline to measure and control the flow of the slurry, a process water flow meter 18 and a process water adjusting valve 20 are arranged on the water conveying pipeline to measure and control the flow of the process water, so that the outlet flue gas temperature of the atomization drying and absorption device 2 is controlled, the inlet flue gas temperature of the dust remover 5 is further controlled, the inlet flue gas temperature of the dust remover 5 is 15-20 ℃ higher than the acid dew point temperature, and the pressure flow of the slurry absorbent, the water and the compressed air is required to meet the requirements of the atomization spray gun 16 so as to achieve the atomization effect. Preferably, the particle size of the atomized deacidification absorbent slurry is 10-60 mu m. Further, the atomizing spray guns 16 may have one or more groups, which may be determined according to different desulfurization waste water flow rates, flue gas loads, flue gas sulfur contents, and the like.
Preferably, the alkaline absorbent comprises: CaO, Ca (OH)2、MgO、Mg(OH)2NaOH and Na2CO3One or more of (a). The alkaline absorbent is not limited to the above-mentioned ones, and may be other alkaline substances as long as it is resistant to SO3And the acid gas can be better absorbed. Further, preferably, the alkali in the alkali absorbentThe content of sexual substance is above 90% and above 300 mesh.
It should be noted that the above description is only given by taking the application of the present invention in a boiler flue gas purification system as an example, and the boiler 1 may be replaced by a rotary kiln, a gas furnace, a shaft furnace, etc.
Example 2
As shown in fig. 2, a schematic structural diagram of an application of the flue gas desulfurization wastewater treatment device of the embodiment of the invention in a flue gas purification system of a sintering machine is shown. The structural composition of the flue gas desulfurization wastewater treatment device is the same as that in example 1, the difference from example 1 is that the flue gas purification system applied to the flue gas desulfurization wastewater treatment device is different, and in example 2, the flue gas desulfurization wastewater treatment device is applied to the flue gas purification system of a sintering machine.
The flue gas purification system of the sintering machine comprises: the device comprises a sintering machine 22, a machine head dust remover 23, a main exhaust fan 24, an atomization drying absorption device 2, a dust remover 5, an induced draft fan 7, a wet desulphurization tower 8, a chimney, a vacuum belt dehydrator 9 and a filtrate storage device 10 which are connected in sequence.
The sintering machine 22 generates flue gas, and the sintering machine 22 has Fe in the sintering process2O3Presence of SO in flue gas at higher temperatures2Can be converted into SO3The flue gas also contains HCl, HF and SO2、SO3And the like. The flue gas enters the atomizing, drying and absorbing device 2 after passing through the nose dust remover 23 and the main exhaust fan 24, the treatment process of the flue gas from the atomizing, drying and absorbing device 2 to the chimney or the vacuum belt dehydrator 9 is the same as that in the embodiment 1, until the generated desulfurization wastewater is buffered in the filtrate storage device 10, and the detailed description is omitted here.
In this embodiment, the process of treating the desulfurization wastewater by using the desulfurization wastewater treatment device to generate the deacidification absorbent slurry and spraying the deacidification absorbent slurry to the atomization drying absorption device 2 to absorb the acid gas in the flue gas is the same as that in embodiment 1, and the detailed description of the process is omitted here.
The flue gas desulfurization wastewater treatment device can be applied to treatment of desulfurization wastewater and high-salinity wastewater, so that zero discharge of the high-salinity wastewater is realized.
Example 3
The invention also provides a method for reducing and zero-discharging the desulfurization wastewater and acidic gas, which comprises the following steps:
step S1, adding a set amount of desulfurization waste water and alkaline absorbent into the digestion tank 11, wherein the desulfurization waste water and the alkaline absorbent react in the digestion tank 11 to generate a deacidification absorbent slurry, and the desulfurization waste water and the alkaline absorbent are preferably used in an amount of 100: (5-25) adding the mixture into a digestion tank; the desulfurization wastewater is generated by a flue gas purification system, and the flue gas purification system can be the boiler flue gas purification system or the sintering machine flue gas purification system; wherein the alkaline absorbent is in dry powder form, and can be CaO, Ca (OH)2、MgO、Mg(OH)2NaOH and Na2CO3One or more of; when the method is applied, the desulfurization wastewater firstly enters the digestion tank 11, and a certain amount of alkaline absorbent can be added into the digestion tank 11 according to the amount of the desulfurization wastewater;
step S2, delivering the deacidified absorbent slurry, water and compressed air to an atomizing spray gun 16, and atomizing the deacidified absorbent slurry in the atomizing spray gun 16, wherein the slurry flow and the process water flow are measured by a slurry flow meter 17 and a process water flow meter 18 which are arranged on a pipeline, and the slurry flow and the process water flow entering the atomizing spray gun 16 are adjusted by a slurry adjusting valve 19 and a process water adjusting valve 20 so that the slurry, the process water and the like entering the atomizing spray gun 16 meet the process requirements of the atomizing spray gun 16; preferably, the particle size of the atomized deacidification absorbent slurry is 10-60 μm;
step S3, spraying the atomized deacidified absorbent slurry into the atomization drying absorption device 2, so that the atomized deacidified absorbent slurry reacts with the acidic gas in the flue gas entering the atomization drying absorption device 2 to generate solid particles. The generated solid particle salt is collected and separated by a dust remover in the flue gas purification system, and the generated steam enters the wet desulphurization system along with the flue gas for recycling.
Preferably, before the delivering the deacidified absorbent slurry to the atomizing spray gun 16, the method further comprises: and filtering the deacidification absorbent slurry by adopting a blue filter or a self-cleaning filter and an 80-mesh filter screen.
Preferably, the spraying amount of the atomized deacidification absorbent slurry sprayed into the atomization drying absorption device 2 is adjusted according to the temperature of the flue gas at the outlet of the atomization drying absorption device 2, so that the dust remover 5 is ensured to operate at 15-20 ℃ above the dew point temperature of acid, the full automation of atomization spraying is realized, and the corrosion of subsequent flues and equipment is avoided. Further, the spraying amount of the deacidification absorbent slurry is adjusted according to the temperature of the inlet flue gas of the dust remover 5. Preferably, the regulation can be achieved using a PID controller.
In summary, the embodiment of the invention provides a method for reducing and zero-discharging desulfurization wastewater and cooperatively reducing SO3The device and the method for treating the acidic gas utilize desulfurization waste water and an alkaline absorbent to prepare deacidification absorbent slurry, and spray the slurry into an atomization drying absorption device 2 by using a three-fluid atomization spray gun 16, realize atomization drying absorption by using waste heat flue gas, complete liquid-solid separation, and realize zero emission of the desulfurization waste water and absorption of the acidic gas. The desulfurization waste water is added with alkaline absorbent as deacidification absorbent slurry which can treat SO in flue gas3、HCl、HF、SO2Absorption reaction of acidic gases, SO3The emission reduction can eliminate blue feather at the outlet of the chimney, reduce the accumulation of chloride ions in wet desulphurization by the reaction absorption of HCl, thereby reducing the discharge of desulphurization waste water and realizing the reduction of the desulphurization waste water.
The above description is only a preferred embodiment of the present invention, and it should be noted that, for those skilled in the art, various modifications and substitutions can be made without departing from the technical principle of the present invention, and these modifications and substitutions should also be regarded as the protection scope of the present invention.
Claims (10)
1. The utility model provides a desulfurization waste water minimizing and zero release and reduce discharging acid gas's device which characterized in that is connected with the gas cleaning system, the gas cleaning system includes: the device comprises a flue gas generating device, an atomization drying and absorption device, a dust remover and a filtrate storage device, wherein the atomization drying and absorption device is connected between the flue gas generating device and the dust remover, and the filtrate storage device is arranged at the tail end of the flue gas purification system to store desulfurization wastewater;
flue gas desulfurization effluent treatment plant includes: the device comprises an absorbent storage bin, a digestion tank, a deacidification slurry tank, a slurry conveying device and an atomization spray gun which are connected in sequence, wherein the absorbent storage bin is used for storing an alkaline absorbent; the digestion tank is also connected with the filtrate storage device so as to enable the desulfurization wastewater to react with an alkaline absorbent to form deacidified absorbent slurry;
and the atomized deacidified absorbent slurry is sprayed into the atomization drying and absorption device by the atomization spray gun so as to react with the acidic gas in the flue gas entering the atomization drying and absorption device.
2. The apparatus for desulfurization waste water reduction and zero emission and acid gas reduction of claim 1, further comprising a filter disposed between the slurry delivery device and the atomizing lances.
3. The apparatus for desulfurization wastewater reduction and zero discharge and acid gas emission reduction of claim 1, wherein stirring devices are disposed in the digestion tank and the deacidification slurry tank.
4. The apparatus for desulfurization wastewater reduction and zero discharge and acid gas emission reduction of claim 1, wherein the atomizing spray gun is a three-fluid atomizing spray gun, and is provided with a slurry conveying pipeline, a process water conveying pipeline and a compressed air conveying pipeline, and the slurry conveying pipeline and the process water conveying pipeline are both provided with a flow meter and an adjusting valve.
5. The apparatus for desulfurization wastewater reduction and zero discharge and acid gas emission reduction of claim 4, wherein the particle size of the atomized deacidification absorbent slurry is 10-60 μm.
6. The apparatus for desulfurization waste water reduction and zero emission and acid gas emission reduction of claim 1, wherein the alkaline absorbent comprises: CaO, Ca (OH)2、MgO、Mg(OH)2NaOH and Na2CO3One or more of (a).
7. A method for reducing and zero-discharging desulfurization wastewater and acidic gas is characterized by comprising the following steps:
adding set amounts of desulfurization waste water and an alkaline absorbent into a digestion tank, wherein the desulfurization waste water and the alkaline absorbent react in the digestion tank to generate a deacidification absorbent slurry, and the desulfurization waste water is generated by a flue gas purification system;
conveying the deacidified absorbent slurry, water and compressed air to an atomizing spray gun, and atomizing the deacidified absorbent slurry in the atomizing spray gun;
and spraying the atomized deacidified absorbent slurry into an atomization drying and absorption device to enable the atomized deacidified absorbent slurry to react with the acidic gas in the flue gas entering the atomization drying and absorption device to generate solid particles.
8. The method for reducing and zero-discharging desulfurization waste water and acidic gas emission reduction according to claim 7, wherein before the delivering the deacidified absorbent slurry to the atomizing spray gun, the method further comprises:
and filtering the deacidification absorbent slurry.
9. The method for desulfurization wastewater reduction and zero discharge and acid gas emission reduction of claim 7, wherein the particle size of the atomized deacidification absorbent slurry is 10-60 μm.
10. The method for desulfurization wastewater reduction and zero discharge and acid gas emission reduction of claim 7, wherein the amount of the atomized deacidification absorbent slurry sprayed into the atomization drying absorption device is adjusted according to the temperature of the outlet flue gas of the atomization drying absorption device.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202011242787.4A CN112546825A (en) | 2020-11-09 | 2020-11-09 | Device and method for reducing and zero-discharging desulfurization wastewater and reducing emission of acid gas |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202011242787.4A CN112546825A (en) | 2020-11-09 | 2020-11-09 | Device and method for reducing and zero-discharging desulfurization wastewater and reducing emission of acid gas |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN112546825A true CN112546825A (en) | 2021-03-26 |
Family
ID=75042915
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202011242787.4A Pending CN112546825A (en) | 2020-11-09 | 2020-11-09 | Device and method for reducing and zero-discharging desulfurization wastewater and reducing emission of acid gas |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN112546825A (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113209790A (en) * | 2021-05-28 | 2021-08-06 | 沈阳东大山汇环境科技有限公司 | Treatment system and method for preventing corrosion and scaling of equipment acid dew in flue gas treatment process |
Citations (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105854575A (en) * | 2016-04-26 | 2016-08-17 | 华北电力大学（保定） | Method for simultaneously treating SO3 and desulfurization waste water in exhaust gas of coal-fired power plant |
| CN106076100A (en) * | 2016-08-08 | 2016-11-09 | 浙江大学 | A kind of coal-fired flue-gas semidry method takes off the desulfurization wastewater Zero discharging system of fluorine and chlorine removal |
| CN205867988U (en) * | 2016-08-02 | 2017-01-11 | 山东大学 | Wet flue gas desulfurization result dry state is handled and zero discharge system of waste water |
| CN106474908A (en) * | 2016-09-22 | 2017-03-08 | 上海交通大学 | A kind of flue gas desulfurization waste-water Zero discharging system and method |
| CN107596883A (en) * | 2017-09-22 | 2018-01-19 | 华电电力科学研究院 | A kind of desulfurization wastewater Zero discharging system and its method of work |
| CN107697967A (en) * | 2017-10-11 | 2018-02-16 | 江苏中建材环保研究院有限公司 | A kind of Desulphurization for Coal-fired Power Plant wastewater zero discharge system and method |
| CN207102319U (en) * | 2017-07-25 | 2018-03-16 | 无锡市华星电力环保修造有限公司 | SDA alkali adding method deep desulfuration dedustings and wastewater zero discharge flue gas processing device |
| CN208839340U (en) * | 2018-06-22 | 2019-05-10 | 西安西矿环保科技有限公司 | A kind of deep desulfuration demisting dust separation system for cement kiln end flue gas |
-
2020
- 2020-11-09 CN CN202011242787.4A patent/CN112546825A/en active Pending
Patent Citations (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105854575A (en) * | 2016-04-26 | 2016-08-17 | 华北电力大学（保定） | Method for simultaneously treating SO3 and desulfurization waste water in exhaust gas of coal-fired power plant |
| CN205867988U (en) * | 2016-08-02 | 2017-01-11 | 山东大学 | Wet flue gas desulfurization result dry state is handled and zero discharge system of waste water |
| CN106076100A (en) * | 2016-08-08 | 2016-11-09 | 浙江大学 | A kind of coal-fired flue-gas semidry method takes off the desulfurization wastewater Zero discharging system of fluorine and chlorine removal |
| CN106474908A (en) * | 2016-09-22 | 2017-03-08 | 上海交通大学 | A kind of flue gas desulfurization waste-water Zero discharging system and method |
| CN207102319U (en) * | 2017-07-25 | 2018-03-16 | 无锡市华星电力环保修造有限公司 | SDA alkali adding method deep desulfuration dedustings and wastewater zero discharge flue gas processing device |
| CN107596883A (en) * | 2017-09-22 | 2018-01-19 | 华电电力科学研究院 | A kind of desulfurization wastewater Zero discharging system and its method of work |
| CN107697967A (en) * | 2017-10-11 | 2018-02-16 | 江苏中建材环保研究院有限公司 | A kind of Desulphurization for Coal-fired Power Plant wastewater zero discharge system and method |
| CN208839340U (en) * | 2018-06-22 | 2019-05-10 | 西安西矿环保科技有限公司 | A kind of deep desulfuration demisting dust separation system for cement kiln end flue gas |
Non-Patent Citations (3)
| Title |
|---|
| 叶恒棣等: "《钢铁烧结烟气全流程减排技术》", 31 May 2019, 冶金工业出版社, pages: 191 - 193 * |
| 广东省电力设计研究院: "《电力设计技术优秀论文集（上）》", 中国地质大学出版社, pages: 139 - 141 * |
| 杨飏: "《二氧化硫减排技术与烟气脱硫工程》", 31 January 2004, 冶金工业出版社, pages: 324 * |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113209790A (en) * | 2021-05-28 | 2021-08-06 | 沈阳东大山汇环境科技有限公司 | Treatment system and method for preventing corrosion and scaling of equipment acid dew in flue gas treatment process |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN110756033A (en) | Deep purification treatment system and process for waste incineration power station flue gas | |
| CN211886232U (en) | Sodium-based dry desulfurization system applied to low-sulfur flue gas working condition | |
| CN105214478A (en) | The integral process of a kind of coke oven flue exhuast gas desulfurization denitration and waste heat recovery | |
| CN105477995A (en) | Method for removing sulfur trioxide from coal-fired flue gas | |
| CN108043210A (en) | A kind of desulfurization of coke oven flue gas and dedusting denitrification integral system | |
| CN106582286B (en) | Flue gas purification device and method | |
| CN107551778B (en) | Flue gas denitration desulfurization dust removal process method | |
| CN103007718A (en) | Wet redox, desulfuration and resource utilization method for flue gas | |
| CN210631915U (en) | Cement kiln desulfurization system | |
| CN202387362U (en) | Semi-dry low temperature flue gas denitrification system | |
| CN116262198A (en) | Two-stage dry desulfurization deacidification dust removal process for waste incineration flue gas | |
| CN106178877A (en) | A kind of coke oven flue waste gas purification waste heat recovery apparatus and technique | |
| CN206762618U (en) | A kind of dry-wet integratedization desulfuring and denitrifying apparatus | |
| CN112546825A (en) | Device and method for reducing and zero-discharging desulfurization wastewater and reducing emission of acid gas | |
| CN211358331U (en) | Wet desulfurization quenching equipment in hazardous waste incineration treatment system | |
| CN111715069A (en) | Ultra-clean discharge system and method for desulfurization and denitrification of sintering flue gas by using spray drying method | |
| CN217220890U (en) | Domestic waste burns flue gas denitration deacidification dust removal integration system of optimization | |
| CN207722616U (en) | A kind of ultra-clean zero waste liquid dust arrester installation of discharge desulfurization of flue gas | |
| CN110548387A (en) | integrated treatment device and process for ion denitration, desulfurization and dust removal by semidry method | |
| CN108636037A (en) | A kind of catalytic cracking flue gas wet desulphurization denitration dust collecting technique and system and device | |
| CN110787617B (en) | Sintering flue gas semi-dry desulfurization and denitrification integrated device and method | |
| CN211328914U (en) | Composite catalytic desulfurization system | |
| CN210934428U (en) | Integrated treatment device for ion denitration, desulfurization and dust removal by semidry method | |
| CN211770757U (en) | Tail gas purification and waste heat utilization device of hot blast stove for active carbon desorption | |
| CN102350189B (en) | Half-dry low-temperature smoke denitrification system |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| RJ01 | Rejection of invention patent application after publication |
Application publication date: 20210326 |
|
| RJ01 | Rejection of invention patent application after publication |