CN113230831A - System and method for washing, arsenic removal and purification of nonferrous smelting flue gas through adiabatic evaporation and cooling - Google Patents
System and method for washing, arsenic removal and purification of nonferrous smelting flue gas through adiabatic evaporation and cooling Download PDFInfo
- Publication number
- CN113230831A CN113230831A CN202110511728.0A CN202110511728A CN113230831A CN 113230831 A CN113230831 A CN 113230831A CN 202110511728 A CN202110511728 A CN 202110511728A CN 113230831 A CN113230831 A CN 113230831A
- Authority
- CN
- China
- Prior art keywords
- flue gas
- acid
- pipeline
- arsenic
- liquid
- 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
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 title claims abstract description 129
- 239000003546 flue gas Substances 0.000 title claims abstract description 129
- 229910052785 arsenic Inorganic materials 0.000 title claims abstract description 67
- RQNWIZPPADIBDY-UHFFFAOYSA-N arsenic atom Chemical compound [As] RQNWIZPPADIBDY-UHFFFAOYSA-N 0.000 title claims abstract description 67
- 238000005406 washing Methods 0.000 title claims abstract description 63
- 238000000034 method Methods 0.000 title claims abstract description 47
- 238000001816 cooling Methods 0.000 title claims abstract description 22
- 238000003723 Smelting Methods 0.000 title claims abstract description 20
- 238000000746 purification Methods 0.000 title claims abstract description 17
- 238000001704 evaporation Methods 0.000 title claims abstract description 14
- 230000008020 evaporation Effects 0.000 title claims abstract description 14
- 239000002253 acid Substances 0.000 claims abstract description 159
- 239000007788 liquid Substances 0.000 claims abstract description 98
- 239000007921 spray Substances 0.000 claims abstract description 71
- 239000000428 dust Substances 0.000 claims abstract description 58
- 238000004062 sedimentation Methods 0.000 claims abstract description 48
- 239000002699 waste material Substances 0.000 claims abstract description 44
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 25
- CWYNVVGOOAEACU-UHFFFAOYSA-N Fe2+ Chemical compound [Fe+2] CWYNVVGOOAEACU-UHFFFAOYSA-N 0.000 claims abstract description 9
- 229910000975 Carbon steel Inorganic materials 0.000 claims abstract description 8
- 239000010962 carbon steel Substances 0.000 claims abstract description 8
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 claims description 66
- GOLCXWYRSKYTSP-UHFFFAOYSA-N Arsenious Acid Chemical compound O1[As]2O[As]1O2 GOLCXWYRSKYTSP-UHFFFAOYSA-N 0.000 claims description 64
- 239000000243 solution Substances 0.000 claims description 36
- 239000013078 crystal Substances 0.000 claims description 28
- 239000000706 filtrate Substances 0.000 claims description 17
- 238000005554 pickling Methods 0.000 claims description 15
- 238000005507 spraying Methods 0.000 claims description 15
- 238000001914 filtration Methods 0.000 claims description 14
- 239000002245 particle Substances 0.000 claims description 12
- 239000007787 solid Substances 0.000 claims description 12
- 238000009413 insulation Methods 0.000 claims description 11
- 238000005352 clarification Methods 0.000 claims description 10
- 239000007789 gas Substances 0.000 claims description 10
- 239000012530 fluid Substances 0.000 claims description 9
- 238000002347 injection Methods 0.000 claims description 9
- 239000007924 injection Substances 0.000 claims description 9
- 238000000926 separation method Methods 0.000 claims description 9
- 229960002594 arsenic trioxide Drugs 0.000 claims description 7
- 239000000498 cooling water Substances 0.000 claims description 7
- 230000005484 gravity Effects 0.000 claims description 6
- 238000003825 pressing Methods 0.000 claims description 6
- 229910000413 arsenic oxide Inorganic materials 0.000 claims description 3
- 238000005245 sintering Methods 0.000 claims description 2
- KTTMEOWBIWLMSE-UHFFFAOYSA-N diarsenic trioxide Chemical compound O1[As](O2)O[As]3O[As]1O[As]2O3 KTTMEOWBIWLMSE-UHFFFAOYSA-N 0.000 claims 1
- IKWTVSLWAPBBKU-UHFFFAOYSA-N a1010_sial Chemical compound O=[As]O[As]=O IKWTVSLWAPBBKU-UHFFFAOYSA-N 0.000 description 6
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 description 4
- 229910000037 hydrogen sulfide Inorganic materials 0.000 description 4
- 238000002360 preparation method Methods 0.000 description 4
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 description 3
- 238000010586 diagram Methods 0.000 description 3
- 239000011521 glass Substances 0.000 description 3
- 238000010791 quenching Methods 0.000 description 3
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 2
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 2
- 238000006243 chemical reaction Methods 0.000 description 2
- 238000009833 condensation Methods 0.000 description 2
- 230000005494 condensation Effects 0.000 description 2
- 239000001257 hydrogen Substances 0.000 description 2
- 229910052739 hydrogen Inorganic materials 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- 230000000171 quenching effect Effects 0.000 description 2
- 239000002994 raw material Substances 0.000 description 2
- 238000010583 slow cooling Methods 0.000 description 2
- 239000000779 smoke Substances 0.000 description 2
- 238000005987 sulfurization reaction Methods 0.000 description 2
- 239000001117 sulphuric acid Substances 0.000 description 2
- 235000011149 sulphuric acid Nutrition 0.000 description 2
- 239000002351 wastewater Substances 0.000 description 2
- RYGMFSIKBFXOCR-UHFFFAOYSA-N Copper Chemical compound [Cu] RYGMFSIKBFXOCR-UHFFFAOYSA-N 0.000 description 1
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 1
- HCHKCACWOHOZIP-UHFFFAOYSA-N Zinc Chemical compound [Zn] HCHKCACWOHOZIP-UHFFFAOYSA-N 0.000 description 1
- CUGMJFZCCDSABL-UHFFFAOYSA-N arsenic(3+);trisulfide Chemical compound [S-2].[S-2].[S-2].[As+3].[As+3] CUGMJFZCCDSABL-UHFFFAOYSA-N 0.000 description 1
- 238000000889 atomisation Methods 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 239000001569 carbon dioxide Substances 0.000 description 1
- 229910002092 carbon dioxide Inorganic materials 0.000 description 1
- 239000003054 catalyst Substances 0.000 description 1
- 229910052802 copper Inorganic materials 0.000 description 1
- 239000010949 copper Substances 0.000 description 1
- 230000007797 corrosion Effects 0.000 description 1
- 238000005260 corrosion Methods 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000001035 drying Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 239000008187 granular material Substances 0.000 description 1
- 239000011133 lead Substances 0.000 description 1
- 239000003595 mist Substances 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 230000003020 moisturizing effect Effects 0.000 description 1
- 238000009856 non-ferrous metallurgy Methods 0.000 description 1
- 239000000047 product Substances 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 238000010992 reflux Methods 0.000 description 1
- 239000002893 slag Substances 0.000 description 1
- 230000003068 static effect Effects 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 229910052717 sulfur Inorganic materials 0.000 description 1
- 239000011593 sulfur Substances 0.000 description 1
- XTQHKBHJIVJGKJ-UHFFFAOYSA-N sulfur monoxide Chemical class S=O XTQHKBHJIVJGKJ-UHFFFAOYSA-N 0.000 description 1
- 229910052815 sulfur oxide Inorganic materials 0.000 description 1
- 229910052720 vanadium Inorganic materials 0.000 description 1
- LEONUFNNVUYDNQ-UHFFFAOYSA-N vanadium atom Chemical compound [V] LEONUFNNVUYDNQ-UHFFFAOYSA-N 0.000 description 1
- 238000004073 vulcanization Methods 0.000 description 1
- 239000002912 waste gas Substances 0.000 description 1
- 239000011701 zinc Substances 0.000 description 1
- 229910052725 zinc 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
- B01D53/14—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 by absorption
- B01D53/1406—Multiple stage absorption
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D50/00—Combinations of methods or devices for separating particles from gases or vapours
- B01D50/10—Combinations of devices covered by groups B01D45/00, B01D46/00 and B01D47/00
-
- 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
- B01D53/14—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 by absorption
- B01D53/18—Absorbing units; Liquid distributors therefor
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F27—FURNACES; KILNS; OVENS; RETORTS
- F27D—DETAILS OR ACCESSORIES OF FURNACES, KILNS, OVENS, OR RETORTS, IN SO FAR AS THEY ARE OF KINDS OCCURRING IN MORE THAN ONE KIND OF FURNACE
- F27D17/00—Arrangements for using waste heat; Arrangements for using, or disposing of, waste gases
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F27—FURNACES; KILNS; OVENS; RETORTS
- F27D—DETAILS OR ACCESSORIES OF FURNACES, KILNS, OVENS, OR RETORTS, IN SO FAR AS THEY ARE OF KINDS OCCURRING IN MORE THAN ONE KIND OF FURNACE
- F27D17/00—Arrangements for using waste heat; Arrangements for using, or disposing of, waste gases
- F27D17/008—Arrangements for using waste heat; Arrangements for using, or disposing of, waste gases cleaning gases
-
- 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
Landscapes
- Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Environmental & Geological Engineering (AREA)
- Mechanical Engineering (AREA)
- General Engineering & Computer Science (AREA)
- Analytical Chemistry (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Treating Waste Gases (AREA)
- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
Abstract
The invention discloses a non-ferrous smelting flue gas adiabatic evaporation cooling acid washing arsenic removal purification system and a method thereof, and the system comprises a factory, an adiabatic evaporator, an acid liquor spray tower, a rotary dust collector, a demister, a plate-and-frame filter press, an inclined plate sedimentation separator, a liquid heat exchanger, a plastic burning plate dust collector, a water spray tower and a waste collection pool, wherein a carbon steel flue is arranged between the exhaust end of the factory and the air inlet end of the adiabatic evaporator, the air outlet end of the adiabatic evaporator is connected with the air inlet end of the rotary dust collector through a pipeline, the waste end of the rotary dust collector is connected with the feed end of the waste collection pool through a pipeline, the air outlet end of the rotary dust collector is connected with the air inlet end of the acid liquor spray tower through an air pressure pump and a pipeline, and the exhaust end of the acid liquor spray tower is connected with the air inlet end of the demister through an air pressure pump and a pipeline. The invention solves the problems of more complicated process and higher operation cost of the traditional arsenic removal process of the flue gas in the prior art. The method has the advantages of simple steps, low cost and the like.
Description
Technical Field
The invention relates to the field of non-ferrous smelting waste gas treatment, in particular to a non-ferrous smelting flue gas adiabatic evaporation cooling acid washing arsenic removal purification system and a method thereof.
Background
In the process of nonferrous metallurgy of copper, lead, zinc and the like, arsenic contained in ores is converted into arsenic trioxide to enter flue gas after being roasted, smelting flue gas also contains high-concentration sulfur oxides, the high-concentration dioxide is generally used for preparing sulfuric acid by adopting a conversion method, and the arsenic is recovered along with the purification process of acid preparation, so that a vanadium catalyst for acid preparation is poisoned and ineffective by the arsenic, and therefore the flue gas acid preparation needs to be purified and dearsenified. The processes for recovering arsenic from flue gas to prepare acid mainly comprise a wet process and a dry process. The wet process currently and generally adopts a dilute acid washing method: roasting the ore, volatilizing most arsenic into flue gas As As2O3, dedusting the generated flue gas, removing most dust, performing acid preparation purification process, washing with 3-20% dilute sulfuric acid in multiple stages, and preparing sulfuric acid product, as2O3 enters the washing waste acid, at present, the sulfuration method is commonly applied in various countries around the world to treat the arsenic-containing waste acid, the arsenic removal efficiency is more than 90 percent, and form arsenic sulfide slag, CN111018188A discloses a method for treating waste acid wastewater by using hydrogen sulfide and carbon dioxide generated in the production process of the hydrogen sulfide, hydrogen sulfide gas is introduced into the waste acid wastewater for sulfuration reaction, the hydrogen sulfide gas is prepared by reacting hydrogen and liquid sulfur serving as raw materials, and the hydrogen is prepared by reacting methanol and water serving as raw materials. There are two methods for dry arsenic recovery, namely, a quenching method: the process has the problems that a large amount of water vapor is brought into the flue gas, the dew point of the flue gas is raised to about 165 ℃, the flue gas can be subjected to condensation in the cooling process, and a small amount of SO3 in the flue gas is dissolved in the condensed water to form acid mist condensation corrosion equipment and a pipeline, SO that unstable operation of a system is guided. Slow cooling method: the method is characterized in that high-temperature high-arsenic smelting flue gas is sent into a slow cooler, the temperature of the flue gas is slowly reduced to 120 ℃ through the ambient temperature, gaseous arsenic trioxide in the flue gas is completely condensed and then sent into a next flue gas treatment system, and the slow cooling method has the defect that the gaseous arsenic trioxide can be condensed into glass arsenic at the temperature of 150 ℃ plus 170 ℃, and the arsenic trioxide with a glass arsenic structure is a substance with very high viscosity and can scale in the slow cooler to influence the production process. The patent CN109553131A discloses a method for recovering arsenic from smelting flue gas by a dry method, which comprises the steps of indirectly quenching high-temperature flue gas containing arsenic, and then recovering arsenic by settling and static dry methods.
Therefore, for the nonferrous smelting flue gas with complex working conditions, a treatment process for efficiently removing arsenic and deeply purifying the nonferrous smelting flue gas to meet the requirement of flue gas acid making is urgently needed to be developed.
Disclosure of Invention
The invention aims to solve the problems of complicated arsenic removal process and high operation cost of the traditional nonferrous smelting flue gas in the prior art, and provides a nonferrous smelting flue gas adiabatic evaporation cooling acid washing arsenic removal purification system and a method thereof, which have the advantages of simple arsenic removal process, low operation cost and the like.
The invention relates to a nonferrous smelting flue gas heat-insulation evaporation cooling acid washing arsenic-removing purification system and a method thereof, which comprises a factory, a heat-insulation evaporator, an acid liquor spray tower, a rotary dust collector, a demister, a plate-and-frame filter press, an inclined plate sedimentation separator, a liquid heat exchanger, a plastic-fired plate dust collector, a water spray tower and a waste collecting pool, wherein a carbon steel flue is arranged between the exhaust end of the factory and the air inlet end of the heat-insulation evaporator, the air outlet end of the heat-insulation evaporator is connected with the air inlet end of the rotary dust collector through a pipeline, the waste end of the rotary dust collector is connected with the air inlet end of the waste collecting pool through a pipeline, the air outlet end of the rotary dust collector is connected with the air inlet end of the acid liquor spray tower through an air pressure pump and a pipeline, the air outlet end of the demister is connected with the air inlet end of the plastic-fired plate dust collector through a pipeline, the waste end of the demister and the waste end of the plastic burning plate dust remover are respectively connected with the feed end of the waste collecting tank through pipelines, the air outlet end of the plastic burning plate dust remover is connected with the air inlet end of the water spray tower through a pneumatic pump and a pipeline, the liquid outlet end of the acid liquor spray tower is connected with the liquid inlet end of the inclined plate sedimentation separator through a hydraulic pump and a pipeline, the liquid outlet end of the inclined plate sedimentation separator is connected with the liquid inlet end of the liquid heat exchanger through a pipeline, the liquid outlet end of the liquid heat exchanger is connected with the liquid inlet end of the acid liquor spray tower through a hydraulic pump and a pipeline, the waste end of the inclined plate sedimentation separator is connected with the liquid inlet end of the plate-and-frame filter press through a hydraulic pump and a pipeline, the liquid outlet end of the plate-and-frame filter press is connected with the liquid inlet end pipeline of the inclined plate sedimentation separator, and the waste end of the plate-and-frame filter press is connected with the feed end pipeline of the waste collecting tank.
The high-efficiency atomizing spray head is arranged in the heat-insulating evaporator, the smoke can be quickly cooled by atomizing and spraying, in order to enhance the cooling effect and reduce the water expansion of the whole system, the low-temperature water with the temperature of 5-10 ℃ can be used for heat exchange, the temperature of the smoke is reduced to about 79-90 ℃, and the cooling water in the heat-insulating evaporator can be prepared by a cold water precooler.
Preferably, the acid liquor spray tower comprises a tower body, an acid washing pipeline is arranged on the left side of the tower body, a reverse spray nozzle is arranged in the acid washing pipeline, an acid liquor pool is arranged at the bottom in the tower body, acid liquor in the acid liquor pool is sulfuric acid solution with the concentration of 50-60%, a first spray layer is arranged above the acid liquor pool, a second spray layer is arranged above the first spray layer, and a tower top exhaust port is arranged above the second spray layer.
The prior arsenic removal process is washed by 5-20% dilute acid, the invention adopts 50-60% sulfuric acid, the solubility of As2O3 in the acid washing environment is lowest, and As2O3 crystals can be separated out to a greater extent when the temperature of flue gas is reduced, thereby removing arsenic element in the flue gas to a greater extent.
Preferably, the acid liquid pool is filled with 50-60% sulfuric acid solution, the left end of the bottom of the tower body is provided with an arsenic filtering port, the tower body above the arsenic filtering port is provided with a primary acid liquid port, the right end of the tower body is provided with an acid liquor return port, a third-stage acid liquor port is arranged above the acid liquor return port, a second-stage acid liquid port is arranged above the third-stage acid liquid port, the arsenic filtering port is connected with the inclined plate sedimentation separator through a hydraulic pump and a pipeline, the first-stage acid liquid port is connected with the liquid injection end of the reverse spray nozzle through a hydraulic pump and a pipeline, the third-stage acid liquid port is connected with the liquid injection end of the second spray layer through a hydraulic pump and a pipeline, the second-stage acid liquid port is connected with the liquid injection end of the first spraying layer through a hydraulic pump and a pipeline, and the acid liquid return port is connected with the liquid heat exchanger through the hydraulic pump and the pipeline.
Preferably, the inclined plate sedimentation separator comprises a sedimentation tank as a main body, an inclined filter plate is arranged in the sedimentation tank, the inclination of the inclined filter plate is 45-60 degrees, the inclined filter plate is provided with a plurality of uniformly distributed filter holes with the diameter of 1mm, the left side of the inclined filter plate is a sedimentation area, the right side of the inclined filter plate is a clarification area, the bottom of the sedimentation area is provided with an arsenic removal port, the left side of the sedimentation area is provided with a filtrate inlet, a secondary liquid inlet is arranged below the filtrate inlet, the right side of the clarification area is provided with a filtrate outlet, the arsenic removal port is connected with the filtrate inlet through a hydraulic pump and a pipeline, the arsenic removal port is connected with the liquid inlet end of the plate-and-frame filter press through a hydraulic pump and a pipeline, and the liquid outlet end of the secondary plate-and-frame filter press is connected with the pipeline through a hydraulic pump, the filtrate outlet is connected with the liquid heat exchanger through a hydraulic pump and a pipeline.
The purification method comprises the following steps:
1. the flue gas that discharges from the mill earlier carries out preliminary cooling in the heat-insulating evaporator through carbon steel flue input, and during preliminary cooling, atomizing shower nozzle can spout atomizing cooling water in heat-insulating evaporator, carries out adiabatic evaporation heat transfer to the flue gas through spraying atomizing cooling water, makes the flue gas temperature drop to about 90 ℃ from 300 ℃, and the arsenic element that contains in this in-process flue gas becomes solid-state arsenic oxide from the gaseous state.
2. The flue gas passing through the heat insulation evaporator is input into a rotary dust remover, solid dust particles in the flue gas are separated from the gas flow by means of centrifugal force and collected on the wall of the rotary dust remover in the rotating process of the rotary dust remover, then the solid dust particles fall into a waste collecting pool under the action of gravity, and after the flue gas is treated by the rotary dust remover, the content of the solid particles in the flue gas is less than 1500mg/Nm 3.
3. After being treated by a rotary dust remover, flue gas is input into an acid liquor spray tower for acid washing treatment, during acid washing treatment, the flue gas is input into an acid washing pipeline firstly, a reverse spray nozzle can carry out primary acid washing on the flue gas in the acid washing pipeline, the flue gas after the primary acid washing can be continuously introduced into a tower body, the temperature of the flue gas is 65-70 ℃, a first spray layer in the tower body can carry out secondary acid washing on the flue gas, the flue gas after the secondary acid washing rises in the tower body, a second spray layer can carry out tertiary acid washing on the flue gas after the secondary acid washing, the flue gas after the tertiary acid washing can be discharged from an exhaust port at the top of the tower, and the temperature of the flue gas is 50-55 ℃.
4. When primary pickling is carried out, the temperature of the flue gas is reduced, and at the moment, part of arsenic element in the flue gas enters a sulfuric acid solution in the form of As2O3 crystals and flows into an acid liquor pool along a pickling pipeline along with the sulfuric acid solution; after the secondary pickling and the tertiary pickling are respectively carried out, the temperature of the flue gas is further reduced, and more arsenic elements in the flue gas enter the sulfuric acid solution in the form of As2O3 crystals and fall into the acid liquor pool along with the sulfuric acid solution.
5. When there are more As2O3 crystals in the acidizing fluid pond, As2O3 crystal can condense together and subside to the acidizing fluid bottom of the pool along with gravity, when more large granule As2O3 crystal appears in the acidizing fluid bottom of the pool, the arsenic filter mouth of tower body can be opened, later under the drive of hydraulic pump, the acidizing fluid and the As2O3 crystal of acidizing fluid bottom of the pool all can be carried out sedimentation separation in the input swash plate sedimentation separator, when sedimentation separation, the As2O3 crystal can subside to the settling zone bottom along the filter slope.
6. When more As2O3 crystals are gathered at the bottom of the settling zone, the arsenic removal port is opened, then the As2O3 crystals at the bottom of the settling zone are conveyed into a plate-and-frame filter press to be subjected to filter pressing under the driving of a hydraulic pump, and the sulfuric acid solution subjected to filter pressing enters a settling pond from a secondary liquid inlet to be subjected to secondary settling separation.
7. The sulfuric acid solution entering the clarification zone through the inclined filter plate is input into the liquid heat exchanger for heat exchange treatment, the temperature of the sulfuric acid solution after heat exchange treatment is 30-50 ℃, and the sulfuric acid solution enters the acid solution pool again from the acid solution return port under the driving of the hydraulic pump, so that the circulating spraying of the flue gas is formed.
8. The flue gas after the acid washing treatment leaves the acid liquor spray tower from the exhaust port at the top of the tower and is input into a demister for demisting treatment, the flue gas after the demisting treatment is continuously sent into a plastic burning plate dust remover for dedusting treatment, and waste materials obtained in the demisting treatment process and the dedusting treatment process are all sent into a waste material collecting pool for centralized collection;
9. and finally, inputting the flue gas subjected to dust removal treatment into a water spray tower for water washing treatment, wherein the arsenic content of the flue gas subjected to water washing treatment is less than 0.1mg/m3, the flue gas reaches the emission standard, and the flue gas can be directly discharged.
The invention has the following beneficial effects:
1. greatly reduces the flow of treating the flue gas by a vulcanization method and reduces the operation cost.
2. This is through using low-temperature water adiabatic evaporation cooling for the formation of flue gas quench process in order to avoid glass arsenic has reduced the aqueous vapor content in the flue gas under the same condition, has improved the dew point temperature of flue gas greatly, reduces the moisturizing volume to the system simultaneously, has avoided entire system's water yield expansion.
3. After the invention is used for treating the flue gas, the arsenic concentration of the flue gas can be lower than 0.1mg/m 3.
Drawings
FIG. 1 is a schematic diagram of the system of the present invention.
Fig. 2 is a schematic structural diagram of the acid liquor spray tower of the present invention.
FIG. 3 is a schematic structural diagram of the inclined plate sedimentation separator of the present invention.
The system comprises a factory 1, an insulating evaporator 2, an acid liquor spray tower 3, a rotary dust collector 4, a demister 5, a plate-and-frame filter press 6, an inclined plate sedimentation separator 7, a liquid heat exchanger 8, a sintered plate dust collector 9, a water spray tower 10, a waste collection tank 11, a carbon steel flue 12, a tower body 13, an acid washing pipeline 14, a reverse spray nozzle 15, an acid liquor tank 16, a first spray layer 17, a second spray layer 18, a tower top exhaust port 19, an arsenic filtering port 20, a first-stage acid liquor port 21, an acid liquor reflux port 22, a third-stage acid liquor port 23, a second-stage acid liquor port 24, a sedimentation tank 25, an inclined filter plate 26, a sedimentation zone 27, a clarification zone 28, an arsenic removal port 29, a filtrate inlet 30, a second-stage liquid inlet 31, a filtrate outlet 32 and an atomization nozzle 33.
Detailed Description
The technical scheme of the invention is further specifically described by the following embodiments and the accompanying drawings.
Example (b): further explained according to attached drawings 1, 2 and 3, the nonferrous smelting flue gas heat-insulation evaporation cooling acid washing arsenic-removal purification system and the method thereof comprise a factory 1, a heat-insulation evaporator 2, an acid liquor spray tower 3, a rotary dust collector 4, a demister 5, a plate-and-frame filter press 6, an inclined plate sedimentation separator 7, a liquid heat exchanger 8, a plastic burning plate dust collector 9, a water spray tower 10 and a waste collection pool 11, wherein a carbon steel flue 12 is arranged between the exhaust end of the factory 1 and the air inlet end of the heat-insulation evaporator 2, the air outlet end of the heat-insulation evaporator 2 is connected with the air inlet end of the rotary dust collector 4 through a pipeline, the waste end of the rotary dust collector 4 is connected with the air inlet end of the waste collection pool 11 through a pipeline, the air outlet end of the rotary dust collector 4 is connected with the air inlet end of the acid liquor spray tower 3 through an air pressure pump and a pipeline, the air outlet end of the acid liquor spray tower 3 is connected with the air inlet end of the demister 5 through an air pressure pump and a pipeline, the gas outlet end of the demister 5 is connected with a gas inlet end pipeline of a plastic-fired plate dust remover 9, the waste end of the demister 5 and the waste end of the plastic-fired plate dust remover 9 are respectively connected with a feed end pipeline of a waste collecting pool 11, the gas outlet end of the plastic-fired plate dust remover 9 is connected with a gas inlet end of a water spray tower 10 through a pneumatic pump and a pipeline, the liquid outlet end of an acid liquor spray tower 3 is connected with the liquid inlet end of an inclined plate sedimentation separator 7 through a hydraulic pump and a pipeline, the liquid outlet end of the inclined plate sedimentation separator 7 is connected with the liquid inlet end pipeline of a liquid heat exchanger 8, the liquid outlet end of the liquid heat exchanger 8 is connected with the liquid inlet end of the acid liquor spray tower 3 through a hydraulic pump and a pipeline, the waste end of the inclined plate sedimentation separator 7 is connected with the liquid inlet end of a plate frame filter press 6 through a hydraulic pump and a pipeline, the liquid outlet end of the plate frame filter press 6 is connected with the liquid inlet end pipeline of the inclined plate sedimentation separator 7, and the waste end of the plate-and-frame filter press 6 is connected with the feed end of the waste collecting tank 11 through a pipeline.
The acidizing fluid spray column 3 include the tower body 13, tower body 13 left side be equipped with pickling pipeline 14, pickling pipeline 14 in be equipped with contrary shower nozzle 15, tower body 13 in the bottom be equipped with sour liquid pond 16, the acidizing fluid in the sour liquid pond 16 is the sulphuric acid solution of concentration 50-60%, sour liquid pond 16 top be equipped with spray layer 17 No. one, spray layer 17 top be equipped with spray layer 18 No. two, spray layer 18 top and be equipped with top of the tower gas vent 19 No. two.
The acid liquor pool 16 is filled with 50-60% sulphuric acid solution, the left end of the bottom of the tower body 13 is provided with an arsenic filtering port 20, the tower body 13 above the arsenic filtering port 20 is provided with a primary acid liquor port 21, the right end of the tower body 13 is provided with an acid liquid return opening 22, a third-stage acid liquid opening 23 is arranged above the acid liquid return opening 22, a second-stage acid liquid port 24 is arranged above the third-stage acid liquid port 23, the arsenic filtering port 20 is connected with the inclined plate sedimentation separator 7 through a hydraulic pump and a pipeline, the primary acid liquid port 21 is connected with the liquid injection end of the reverse spray nozzle 15 through a hydraulic pump and a pipeline, the third-stage acid liquid port 23 is connected with the liquid injection end of the second spray layer 18 through a hydraulic pump and a pipeline, the second-stage acid liquid port 24 is connected with the liquid injection end of the first spraying layer 17 through a hydraulic pump and a pipeline, and the acid liquid return port 22 is connected with the liquid heat exchanger 8 through a hydraulic pump and a pipeline.
The inclined plate sedimentation separator 7 comprises a sedimentation tank 25 as a main body, an inclined filter plate 26 is arranged in the sedimentation tank 25, the inclination of the inclined filter plate 26 is 45-60 degrees, the inclined filter plate 26 is provided with a plurality of filter holes which are uniformly distributed and have the diameter of 1mm, the left side of the inclined filter plate 26 is a sedimentation area 27, the right side of the inclined filter plate 26 is a clarification area 28, the bottom of the sedimentation area 27 is provided with an arsenic removal port 29, the left side of the sedimentation area 27 is provided with a filtrate inlet 30, the filtrate inlet 30 is provided with a secondary liquid inlet 31 below, the right side of the clarification area 28 is provided with a filtrate outlet 32, the arsenic removal port 20 and the filtrate inlet 30 are connected through a hydraulic pump and a pipeline, the arsenic removal port 29 and the liquid inlet end of the plate and frame filter press 6 are connected through a hydraulic pump and a pipeline, the secondary liquid inlet 31 and the liquid outlet end of the plate and frame filter press 6 are connected through a hydraulic pump and a pipeline, the filtrate outlet 32 is connected with the liquid heat exchanger 8 through a hydraulic pump and a pipeline.
The purification method comprises the following steps:
1. firstly, flue gas discharged from a factory 1 is input into the heat-insulating evaporator 2 through the carbon steel flue 12 for preliminary cooling, and during preliminary cooling, the atomizing spray nozzle 33 in the heat-insulating evaporator 2 can spray atomized cooling water to carry out heat-insulating evaporation heat exchange on the flue gas by spraying the atomized cooling water, so that the temperature of the flue gas is reduced from 300 ℃ to about 90 ℃, and arsenic contained in the flue gas is changed into solid arsenic oxide from gaseous state.
2. The flue gas passing through the heat insulation evaporator 2 is input into a rotary dust collector 4, solid dust particles in the flue gas are separated from the gas flow and collected on the wall of the device by means of centrifugal force in the rotating process of the rotary dust collector 4, the solid dust particles fall into a waste material collecting pool 11 under the action of gravity, and the content of the solid particles in the flue gas is less than 1500mg/Nm3 after the flue gas is treated by the rotary dust collector 4.
3. After being treated by the rotary dust remover 4, the flue gas is input into the acid liquor spray tower 3 for acid washing treatment, during the acid washing treatment, the flue gas is input into the acid washing pipeline 14 firstly, the reverse spray nozzle 15 performs primary acid washing on the flue gas in the acid washing pipeline 14, the flue gas after the primary acid washing is continuously introduced into the tower body 13, the temperature of the flue gas is 65-70 ℃, the primary spray layer 17 in the tower body 13 performs secondary acid washing on the flue gas, the flue gas after the secondary acid washing rises in the tower body 13, the secondary spray layer 18 performs tertiary acid washing on the flue gas after the secondary acid washing, the flue gas after the tertiary acid washing is discharged from the exhaust port 19 at the top of the tower, and the temperature of the flue gas is 50-55 ℃.
4. When the primary pickling is carried out, the temperature of the flue gas is reduced, and at the moment, part of arsenic element in the flue gas enters the sulfuric acid solution in the form of As2O3 crystals and flows into the acid liquor pool 16 along the pickling pipeline 14 along with the sulfuric acid solution; after the second-stage pickling and the third-stage pickling, respectively, the temperature of the flue gas is further lowered, and more arsenic in the flue gas enters the sulfuric acid solution in the form of As2O3 crystals and falls into the acid liquid pool 16 along with the sulfuric acid solution.
5. When a large amount of As2O3 crystals exist in the acid liquor pool 16, the As2O3 crystals can be coagulated and settle to the bottom of the acid liquor pool 16 along with gravity, when a large amount of large-particle As2O3 crystals appear at the bottom of the acid liquor pool 16, the arsenic filtering port 20 of the tower body 13 can be opened, then under the drive of the hydraulic pump, acid liquor and As2O3 crystals at the bottom of the acid liquor pool 16 can be input into the inclined plate sedimentation separator 7 for sedimentation separation, and during sedimentation separation, the As2O3 crystals can settle to the bottom of the sedimentation zone 27 along the inclined filtering plate 26.
6. When more As2O3 crystals are collected at the bottom of the settling zone 27, the arsenic removal port 29 is opened, then the As2O3 crystals at the bottom of the settling zone 27 are conveyed to the plate-and-frame filter press 6 under the drive of the hydraulic pump for filter pressing treatment, and the sulfuric acid solution after filter pressing treatment enters the settling tank 25 from the secondary liquid inlet 31 for secondary settling separation.
7. The sulfuric acid solution entering the clarification zone 28 through the inclined filter plate 26 is input into the liquid heat exchanger 8 for heat exchange treatment, the temperature of the sulfuric acid solution after heat exchange treatment is 30-50 ℃, and the sulfuric acid solution enters the acid solution tank 16 again from the acid solution return port 22 under the driving of the hydraulic pump, so that circulating spraying on the flue gas is formed.
8. The flue gas after the pickling process can leave the acid liquor spray tower 3 from the exhaust port 19 on the top of the tower and is input into the demister 5 for demisting treatment, the flue gas after the demisting treatment is continuously sent into the sintering plate dust remover 9 for dedusting treatment, and the waste materials obtained in the demisting treatment process and the dedusting treatment process can be sent into the waste material collecting tank 11 for centralized collection.
9. And finally, inputting the flue gas subjected to dust removal treatment into a water spray tower 10 for water washing treatment, wherein the arsenic content of the flue gas subjected to water washing treatment is less than 0.1mg/m3, the flue gas reaches the emission standard, and the flue gas can be directly discharged.
The above description is only an embodiment of the present invention, but the structural features of the present invention are not limited thereto, and any changes or modifications within the scope of the present invention by those skilled in the art are covered by the present invention.
Claims (5)
1. The utility model provides a non-ferrous smelting flue gas adiabatic evaporation cooling acid washing removes arsenic clean system, includes mill (1), adiabatic evaporimeter (2), acidizing fluid spray column (3), rotary dust collector (4), defroster (5), plate and frame filter press (6), inclined plate sedimentation separator (7), liquid heat exchanger (8), mould and burn board dust remover (9), water spray column (10) and waste material collecting tank (11), characterized by, the exhaust end of mill (1) and adiabatic evaporimeter (2) inlet end within a definite time be equipped with carbon steel flue (12), the end of giving vent to anger of adiabatic evaporimeter (2) and the inlet end pipe connection of rotary dust collector (4), the waste material end of rotary dust collector (4) and the feed end pipe connection of waste material collecting tank (11), the end of giving vent to anger of rotary dust collector (4) and the inlet end of acidizing fluid spray column (3) be connected through pneumatic pump and pipeline, the acid liquor spraying tower is characterized in that the exhaust end of the acid liquor spraying tower (3) is connected with the air inlet end of the demister (5) through a pneumatic pump and a pipeline, the air outlet end of the demister (5) is connected with the air inlet end of the plastic-burning plate dust remover (9) through a pipeline, the waste end of the demister (5) and the waste end of the plastic-burning plate dust remover (9) are respectively connected with the feed end of the waste collecting pool (11) through a pipeline, the air outlet end of the plastic-burning plate dust remover (9) is connected with the air inlet end of the water spraying tower (10) through a pneumatic pump and a pipeline, the liquid outlet end of the acid liquor spraying tower (3) is connected with the liquid inlet end of the inclined plate sedimentation separator (7) through a hydraulic pump and a pipeline, the liquid outlet end of the inclined plate sedimentation separator (7) is connected with the liquid inlet end of the liquid heat exchanger (8) through a pipeline, the liquid outlet end of the liquid heat exchanger (8) is connected with the liquid inlet end of the acid liquor spraying tower (3) through a hydraulic pump and a pipeline, the waste material end of swash plate sedimentation separator (7) and the inlet end of plate and frame filter press (6) be connected through hydraulic pump and pipeline, the play liquid end of plate and frame filter press (6) be connected with the inlet end pipe connection of swash plate sedimentation separator (7), the waste material end of plate and frame filter press (6) be connected with the feed end pipe connection of waste material collecting pond (11).
2. The non-ferrous smelting flue gas adiabatic evaporative cooling acid washing arsenic removal purification system as claimed in claim 1, wherein the acid liquor spray tower (3) comprises a tower body (13), an acid washing pipeline (14) is arranged on the left side of the tower body (13), a reverse spray head (15) is arranged in the acid washing pipeline (14), an acid liquor pool (16) is arranged at the bottom in the tower body (13), acid liquor in the acid liquor pool (16) is sulfuric acid solution with the concentration of 50-60%, a spray layer (17) is arranged above the acid liquor pool (16), a spray layer (18) is arranged above the spray layer (17), and a tower top exhaust port (19) is arranged above the spray layer (18).
3. The non-ferrous smelting flue gas adiabatic evaporative cooling acid washing arsenic-removing purification system as claimed in claim 2, wherein the acid liquor pool (16) is internally provided with a sulfuric acid solution with a concentration of 50-60%, the left end of the bottom of the tower body (13) is provided with an arsenic filtering port (20), the tower body (13) above the arsenic filtering port (20) is provided with a first-stage acid liquor port (21), the right end of the tower body (13) is provided with an acid liquor return port (22), the acid liquor return port (22) is provided with a third-stage acid liquor port (23), the third-stage acid liquor port (23) is provided with a second-stage acid liquor port (24), the arsenic filtering port (20) and the inclined plate sedimentation separator (7) are connected through a hydraulic pump and a pipeline, the first-stage acid liquor port (21) is connected with the liquid injection end of the reverse spray nozzle (15) through a hydraulic pump and a pipeline, and the third-stage acid liquor port (23) and the liquid injection end of the second spray layer (18) are connected through a hydraulic pump and a pipeline The secondary acid liquid port (24) is connected with the liquid injection end of the first spraying layer (17) through a hydraulic pump and a pipeline, and the acid liquid return port (22) is connected with the liquid heat exchanger (8) through the hydraulic pump and the pipeline.
4. The non-ferrous smelting flue gas adiabatic evaporative cooling acid washing arsenic-removing purification system as claimed in claim 1, wherein the inclined plate sedimentation separator (7) comprises a sedimentation tank (25) as a main body, an inclined filter plate (26) is arranged in the sedimentation tank (25), the inclination of the inclined filter plate (26) is 45-60 degrees, a plurality of filter holes which are uniformly distributed and have a diameter of 1mm are formed in the inclined filter plate (26), a sedimentation zone (27) is formed in the left side of the inclined filter plate (26), a clarification zone (28) is formed in the right side of the inclined filter plate (26), an arsenic-removing opening (29) is formed in the bottom of the sedimentation zone (27), a filtrate inlet (30) is formed in the left side of the sedimentation zone (27), a secondary liquid inlet (31) is formed below the filtrate inlet (30), a filtrate outlet (32) is formed in the right side of the clarification zone (28), the arsenic filtering port (20) is connected with the filtrate inlet (30) through a hydraulic pump and a pipeline, the arsenic removing port (29) is connected with the liquid inlet end of the plate-and-frame filter press (6) through a hydraulic pump and a pipeline, the secondary liquid inlet (31) is connected with the liquid outlet end of the plate-and-frame filter press (6) through a hydraulic pump and a pipeline, and the filtrate outlet (32) is connected with the liquid heat exchanger (8) through a hydraulic pump and a pipeline.
5. The purification method of the non-ferrous smelting flue gas adiabatic evaporation cooling acid washing arsenic removal purification system, which is suitable for the non-ferrous smelting flue gas adiabatic evaporation cooling acid washing arsenic removal purification system, is characterized in that,
firstly, flue gas emitted from a factory (1) is input into an adiabatic evaporator (2) through a carbon steel flue (12) for preliminary cooling, during preliminary cooling, an atomizing nozzle (33) in the adiabatic evaporator (2) can spray atomized cooling water, the flue gas is subjected to adiabatic evaporation heat exchange by spraying the atomized cooling water, the temperature of the flue gas is reduced from 300 ℃ to about 90 ℃, and arsenic element contained in the flue gas is changed into solid arsenic oxide from a gaseous state in the process;
inputting the flue gas passing through the heat insulation evaporator (2) into a rotary dust collector (4), separating solid dust particles in the flue gas from gas flow by means of centrifugal force in the rotating process of the rotary dust collector (4) and collecting the solid dust particles on the wall of the device, enabling the solid dust particles to fall into a waste material collecting pool (11) under the action of gravity, and enabling the content of the solid particles in the flue gas to be less than 1500mg/Nm3 after the flue gas is treated by the rotary dust collector (4);
after being treated by a rotary dust remover (4), flue gas is input into an acid liquor spray tower (3) for acid washing treatment, during acid washing treatment, the flue gas is input into an acid washing pipeline (14) firstly, a reverse spray nozzle (15) can carry out primary acid washing on the flue gas in the acid washing pipeline (14), the flue gas after primary acid washing is continuously introduced into a tower body (13), the temperature of the flue gas is 65-70 ℃, a first spray layer (17) in the tower body (13) can carry out secondary acid washing on the flue gas, the flue gas after secondary acid washing is raised in the tower body (13), a second spray layer (18) can carry out tertiary acid washing on the flue gas after secondary acid washing, the flue gas after tertiary acid washing is discharged from a tower top exhaust port (19), and the temperature of the flue gas is 50-55 ℃;
when primary pickling is carried out, the temperature of the flue gas is reduced, and at the moment, part of arsenic element in the flue gas enters a sulfuric acid solution in the form of As2O3 crystals and flows into an acid liquor pool (16) along a pickling pipeline (14) along with the sulfuric acid solution; after the secondary pickling and the tertiary pickling are respectively carried out, the temperature of the flue gas is further reduced, more arsenic elements in the flue gas enter a sulfuric acid solution in the form of As2O3 crystals and fall into an acid liquor pool (16) along with the sulfuric acid solution;
when more As2O3 crystals exist in the acid liquid pool (16), the As2O3 crystals can be coagulated and settle to the bottom of the acid liquid pool (16) along with gravity, when more large-particle As2O3 crystals appear at the bottom of the acid liquid pool (16), an arsenic filtering port (20) of the tower body (13) can be opened, then acid liquid at the bottom of the acid liquid pool (16) and the As2O3 crystals can be input into an inclined plate settling separator (7) for settling separation under the driving of a hydraulic pump, and during the settling separation, the As2O3 crystals can settle to the bottom of a settling zone (27) along an inclined filter plate (26);
when more As2O3 crystals are collected at the bottom of the settling zone (27), opening the arsenic removal port (29), then inputting the As2O3 crystals at the bottom of the settling zone (27) into a plate-and-frame filter press (6) under the drive of a hydraulic pump for filter pressing treatment, and enabling the sulfuric acid solution after filter pressing treatment to enter a settling pond (25) from a secondary liquid inlet (31) for secondary settling separation;
the sulfuric acid solution entering the clarification zone (28) through the inclined filter plate (26) is input into the liquid heat exchanger (8) for heat exchange treatment, the temperature of the sulfuric acid solution after heat exchange treatment is 30-50 ℃, and the sulfuric acid solution enters the acid solution tank (16) again from the acid solution return port (22) under the driving of the hydraulic pump, so that the circulating spraying of the flue gas is formed;
the flue gas after the acid washing treatment leaves the acid liquor spray tower (3) from the exhaust port (19) at the top of the tower and is input into a demister (5) for demisting treatment, the flue gas after the demisting treatment is continuously sent into a sintering plate dust remover (9) for dedusting treatment, and waste materials obtained in the demisting treatment process and the dedusting treatment process are all sent into a waste material collecting tank (11) for centralized collection;
and finally, inputting the flue gas subjected to dust removal treatment into a water spray tower (10) for water washing treatment, wherein the arsenic content of the flue gas subjected to water washing treatment is less than 0.1mg/m3, the flue gas reaches the emission standard, and the flue gas can be directly discharged.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202110511728.0A CN113230831A (en) | 2021-05-11 | 2021-05-11 | System and method for washing, arsenic removal and purification of nonferrous smelting flue gas through adiabatic evaporation and cooling |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202110511728.0A CN113230831A (en) | 2021-05-11 | 2021-05-11 | System and method for washing, arsenic removal and purification of nonferrous smelting flue gas through adiabatic evaporation and cooling |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN113230831A true CN113230831A (en) | 2021-08-10 |
Family
ID=77133395
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202110511728.0A Pending CN113230831A (en) | 2021-05-11 | 2021-05-11 | System and method for washing, arsenic removal and purification of nonferrous smelting flue gas through adiabatic evaporation and cooling |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN113230831A (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113893627A (en) * | 2021-10-15 | 2022-01-07 | 航天环境工程有限公司 | Dust treatment system and method in slag dumping and dragging process of steel slag hot-stewing pool |
Citations (15)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4138231A (en) * | 1976-04-09 | 1979-02-06 | Boliden Aktiebolag | Method of wet-cleaning gases containing sulfur dioxide, halogens and arsenic from pyrometallurgical treatment of sulphidic materials |
| JP2003305331A (en) * | 2002-04-12 | 2003-10-28 | Cottrell Kogyo Kk | Recovery method and recovery apparatus for specific component in exhaust gas |
| CN102225312A (en) * | 2011-05-18 | 2011-10-26 | 江苏正通宏泰股份有限公司 | Process for enhancing dual alkali desulfurization |
| CN102228787A (en) * | 2011-05-17 | 2011-11-02 | 江苏正通宏泰股份有限公司 | Novel semi-dry flue gas desulphurization technology |
| CN104324597A (en) * | 2014-11-04 | 2015-02-04 | 上海蓝科石化工程技术有限公司 | Combined flue gas cleaning system and flue gas cleaning method thereof |
| CN104548823A (en) * | 2014-12-24 | 2015-04-29 | 中国恩菲工程技术有限公司 | Method and system for treating arsenic-containing metallurgical off-gas |
| CN105561768A (en) * | 2016-02-23 | 2016-05-11 | 江苏澄天环保科技有限公司 | Method for recycling arsenic from nonferrous smelting flue gas |
| US20160152474A1 (en) * | 2013-06-04 | 2016-06-02 | Sichuan Ko Chang Technology Co., Ltd | Apparatus for preparing phosphoric acid from fume exiting the kiln in a kiln phosphoric acid process |
| CN207361978U (en) * | 2017-08-25 | 2018-05-15 | 金川集团股份有限公司 | A kind of device of acid waste water evaporation emission reduction |
| CN108339361A (en) * | 2018-04-11 | 2018-07-31 | 昆明理工大学 | A kind of processing method and processing device for burning arsenical fume |
| CN109534301A (en) * | 2019-01-03 | 2019-03-29 | 众德环保科技有限公司 | A kind of oxygen-enriched acid-making process of sulfur-containing smoke gas double-absorption |
| CN110280125A (en) * | 2019-06-27 | 2019-09-27 | 上海交通大学 | One kind containing arsenic and SO3Flue gas during smelting dry cleaning method |
| CN111408262A (en) * | 2020-04-29 | 2020-07-14 | 江苏琥珀环境技术有限公司 | Device and method for dedusting and purifying tail gas of glass melting furnace |
| CN111473353A (en) * | 2020-04-14 | 2020-07-31 | 长沙有色冶金设计研究院有限公司 | Quenching arsenic removal technology for smelting flue gas |
| CN211847454U (en) * | 2019-12-24 | 2020-11-03 | 湖南中集环境投资有限公司 | Arsenic-containing waste residue landfill and waste mine leachate wastewater treatment combined pool |
-
2021
- 2021-05-11 CN CN202110511728.0A patent/CN113230831A/en active Pending
Patent Citations (15)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4138231A (en) * | 1976-04-09 | 1979-02-06 | Boliden Aktiebolag | Method of wet-cleaning gases containing sulfur dioxide, halogens and arsenic from pyrometallurgical treatment of sulphidic materials |
| JP2003305331A (en) * | 2002-04-12 | 2003-10-28 | Cottrell Kogyo Kk | Recovery method and recovery apparatus for specific component in exhaust gas |
| CN102228787A (en) * | 2011-05-17 | 2011-11-02 | 江苏正通宏泰股份有限公司 | Novel semi-dry flue gas desulphurization technology |
| CN102225312A (en) * | 2011-05-18 | 2011-10-26 | 江苏正通宏泰股份有限公司 | Process for enhancing dual alkali desulfurization |
| US20160152474A1 (en) * | 2013-06-04 | 2016-06-02 | Sichuan Ko Chang Technology Co., Ltd | Apparatus for preparing phosphoric acid from fume exiting the kiln in a kiln phosphoric acid process |
| CN104324597A (en) * | 2014-11-04 | 2015-02-04 | 上海蓝科石化工程技术有限公司 | Combined flue gas cleaning system and flue gas cleaning method thereof |
| CN104548823A (en) * | 2014-12-24 | 2015-04-29 | 中国恩菲工程技术有限公司 | Method and system for treating arsenic-containing metallurgical off-gas |
| CN105561768A (en) * | 2016-02-23 | 2016-05-11 | 江苏澄天环保科技有限公司 | Method for recycling arsenic from nonferrous smelting flue gas |
| CN207361978U (en) * | 2017-08-25 | 2018-05-15 | 金川集团股份有限公司 | A kind of device of acid waste water evaporation emission reduction |
| CN108339361A (en) * | 2018-04-11 | 2018-07-31 | 昆明理工大学 | A kind of processing method and processing device for burning arsenical fume |
| CN109534301A (en) * | 2019-01-03 | 2019-03-29 | 众德环保科技有限公司 | A kind of oxygen-enriched acid-making process of sulfur-containing smoke gas double-absorption |
| CN110280125A (en) * | 2019-06-27 | 2019-09-27 | 上海交通大学 | One kind containing arsenic and SO3Flue gas during smelting dry cleaning method |
| CN211847454U (en) * | 2019-12-24 | 2020-11-03 | 湖南中集环境投资有限公司 | Arsenic-containing waste residue landfill and waste mine leachate wastewater treatment combined pool |
| CN111473353A (en) * | 2020-04-14 | 2020-07-31 | 长沙有色冶金设计研究院有限公司 | Quenching arsenic removal technology for smelting flue gas |
| CN111408262A (en) * | 2020-04-29 | 2020-07-14 | 江苏琥珀环境技术有限公司 | Device and method for dedusting and purifying tail gas of glass melting furnace |
Non-Patent Citations (1)
| Title |
|---|
| 赵玉明: "《环境工程工艺设计教程》", 30 September 2013, 中国环境出版社 * |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113893627A (en) * | 2021-10-15 | 2022-01-07 | 航天环境工程有限公司 | Dust treatment system and method in slag dumping and dragging process of steel slag hot-stewing pool |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN106435197B (en) | A kind of SCR denitration dead catalyst valuable metal alkaline extraction retracting device and technique | |
| CN101597070B (en) | Purifying device of ammonium sulphate solution produced by flue gas desulfurization by ammonia process in the sintering, palletizing and kiln processes and method thereof | |
| CN105695733B (en) | Zinc hydrometallurgy process | |
| CN1994531A (en) | Process for purifying arsenic-containing mineral burned fume | |
| CN106268179A (en) | The energy saving technique of a kind of synthetical recovery sulfuric acid purification spent acid and system | |
| CN109264674A (en) | A kind of technique and system using flue gas during smelting extracting sulfuric acid | |
| CN113230831A (en) | System and method for washing, arsenic removal and purification of nonferrous smelting flue gas through adiabatic evaporation and cooling | |
| CN202880923U (en) | Titanium tetrachloride wet-process dust collecting and leaching device | |
| CN206138987U (en) | Carry in copper tailings desorption flue gas device of SO2 and resourceization | |
| CN105727727A (en) | Treating method for vanadium slag roasting tail gas | |
| CN208893910U (en) | A kind of dry regenerative system of hydrogen chloride gas | |
| CN215842387U (en) | Non-ferrous smelting flue gas adiabatic evaporation cooling acid washing arsenic removal clean system | |
| CN202161911U (en) | Flue gas treatment equipment | |
| CN205076806U (en) | Novel gas purification device | |
| CN108793089B (en) | Process for producing refined sulfuric acid in sulfuric acid plant | |
| CN218155574U (en) | Acidizing calcination flue gas processing system | |
| CN102294168B (en) | Method for processing flue gas | |
| CN212102960U (en) | Valuable metal recovery system in dirty acid | |
| CN212769875U (en) | Purification system of gas distribution acid making process | |
| CN112370951A (en) | Method and system for removing arsenic from smelting flue gas by wet method | |
| CN1177756C (en) | Process for preparing sulfuric acid | |
| CN1266033C (en) | Recovery and use for dilute acid in boiling furnace mixing-burning sulphur production installation | |
| CN211112234U (en) | Acid recovery device for reverse ion exchange | |
| CN113620256A (en) | Acid making method in antimony smelting process of oxygen-enriched side-blown column smelting | |
| CN102284236B (en) | Equipment for treating gas fume |
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 | ||
| RJ01 | Rejection of invention patent application after publication |
Application publication date: 20210810 |