WO2023221647A1 - 一种控制氨法脱碳***氨逃逸的装置及方法 - Google Patents
一种控制氨法脱碳***氨逃逸的装置及方法 Download PDFInfo
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- WO2023221647A1 WO2023221647A1 PCT/CN2023/083695 CN2023083695W WO2023221647A1 WO 2023221647 A1 WO2023221647 A1 WO 2023221647A1 CN 2023083695 W CN2023083695 W CN 2023083695W WO 2023221647 A1 WO2023221647 A1 WO 2023221647A1
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- Prior art keywords
- ammonia
- liquid
- desulfurization
- washing
- gas
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- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 title claims abstract description 473
- 229910021529 ammonia Inorganic materials 0.000 title claims abstract description 236
- 238000000034 method Methods 0.000 title claims abstract description 121
- 238000005262 decarbonization Methods 0.000 title claims abstract description 69
- 238000005406 washing Methods 0.000 claims abstract description 170
- 238000006477 desulfuration reaction Methods 0.000 claims abstract description 127
- 230000023556 desulfurization Effects 0.000 claims abstract description 127
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 111
- 230000002378 acidificating effect Effects 0.000 claims abstract description 106
- BFNBIHQBYMNNAN-UHFFFAOYSA-N ammonium sulfate Chemical compound N.N.OS(O)(=O)=O BFNBIHQBYMNNAN-UHFFFAOYSA-N 0.000 claims abstract description 86
- 229910052921 ammonium sulfate Inorganic materials 0.000 claims abstract description 86
- 235000011130 ammonium sulphate Nutrition 0.000 claims abstract description 86
- 239000007788 liquid Substances 0.000 claims description 127
- 238000010521 absorption reaction Methods 0.000 claims description 42
- 238000005261 decarburization Methods 0.000 claims description 25
- 238000001816 cooling Methods 0.000 claims description 19
- 239000013618 particulate matter Substances 0.000 claims description 16
- 239000002253 acid Substances 0.000 claims description 12
- 239000000945 filler Substances 0.000 claims description 7
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 claims description 6
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 abstract description 20
- ATRRKUHOCOJYRX-UHFFFAOYSA-N Ammonium bicarbonate Chemical compound [NH4+].OC([O-])=O ATRRKUHOCOJYRX-UHFFFAOYSA-N 0.000 abstract description 10
- 239000001099 ammonium carbonate Substances 0.000 abstract description 10
- 229910002092 carbon dioxide Inorganic materials 0.000 abstract description 10
- 229910000013 Ammonium bicarbonate Inorganic materials 0.000 abstract description 8
- 235000012538 ammonium bicarbonate Nutrition 0.000 abstract description 8
- 239000003337 fertilizer Substances 0.000 abstract description 8
- 239000001569 carbon dioxide Substances 0.000 abstract description 5
- 239000003795 chemical substances by application Substances 0.000 abstract description 3
- 239000000126 substance Substances 0.000 abstract 2
- 239000007789 gas Substances 0.000 description 67
- 239000000243 solution Substances 0.000 description 32
- RAHZWNYVWXNFOC-UHFFFAOYSA-N Sulphur dioxide Chemical compound O=S=O RAHZWNYVWXNFOC-UHFFFAOYSA-N 0.000 description 12
- 230000000694 effects Effects 0.000 description 9
- 239000000110 cooling liquid Substances 0.000 description 7
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 6
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 6
- 229910052799 carbon Inorganic materials 0.000 description 6
- 239000003546 flue gas Substances 0.000 description 6
- 239000007921 spray Substances 0.000 description 6
- 239000003929 acidic solution Substances 0.000 description 5
- 239000000047 product Substances 0.000 description 5
- 230000000052 comparative effect Effects 0.000 description 4
- 238000005516 engineering process Methods 0.000 description 4
- QAOWNCQODCNURD-UHFFFAOYSA-L Sulfate Chemical compound [O-]S([O-])(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-L 0.000 description 3
- 239000002250 absorbent Substances 0.000 description 3
- 230000002745 absorbent Effects 0.000 description 3
- 150000001412 amines Chemical class 0.000 description 3
- 239000005431 greenhouse gas Substances 0.000 description 3
- XTQHKBHJIVJGKJ-UHFFFAOYSA-N sulfur monoxide Chemical class S=O XTQHKBHJIVJGKJ-UHFFFAOYSA-N 0.000 description 3
- 229910052815 sulfur oxide Inorganic materials 0.000 description 3
- 239000003570 air Substances 0.000 description 2
- 235000012501 ammonium carbonate Nutrition 0.000 description 2
- 230000009286 beneficial effect Effects 0.000 description 2
- 239000003245 coal Substances 0.000 description 2
- 230000007613 environmental effect Effects 0.000 description 2
- 238000012856 packing Methods 0.000 description 2
- AKEJUJNQAAGONA-UHFFFAOYSA-N sulfur trioxide Chemical compound O=S(=O)=O AKEJUJNQAAGONA-UHFFFAOYSA-N 0.000 description 2
- 238000010998 test method Methods 0.000 description 2
- LSNNMFCWUKXFEE-UHFFFAOYSA-N Sulfurous acid Chemical group OS(O)=O LSNNMFCWUKXFEE-UHFFFAOYSA-N 0.000 description 1
- 239000006096 absorbing agent Substances 0.000 description 1
- 239000012080 ambient air Substances 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 238000004177 carbon cycle Methods 0.000 description 1
- 239000003153 chemical reaction reagent Substances 0.000 description 1
- 150000001875 compounds Chemical class 0.000 description 1
- 239000012530 fluid Substances 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 239000000618 nitrogen fertilizer Substances 0.000 description 1
- 230000003647 oxidation Effects 0.000 description 1
- 238000007254 oxidation reaction Methods 0.000 description 1
- 230000001590 oxidative effect Effects 0.000 description 1
- 238000005554 pickling Methods 0.000 description 1
- 230000008635 plant growth Effects 0.000 description 1
- 238000012545 processing Methods 0.000 description 1
- 230000008929 regeneration Effects 0.000 description 1
- 238000011069 regeneration method Methods 0.000 description 1
- 238000011160 research Methods 0.000 description 1
- 239000002002 slurry Substances 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 238000002798 spectrophotometry method Methods 0.000 description 1
- 238000012360 testing method Methods 0.000 description 1
- 238000010792 warming Methods 0.000 description 1
- 239000002912 waste gas Substances 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
- 239000002351 wastewater Substances 0.000 description 1
Classifications
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- 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
- B01D53/77—Liquid phase processes
- B01D53/78—Liquid phase processes with gas-liquid contact
-
- 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
- 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
- B01D53/1425—Regeneration of liquid absorbents
-
- 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
- B01D53/1456—Removing acid components
- B01D53/1475—Removing carbon dioxide
-
- 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
- B01D53/1456—Removing acid components
- B01D53/1481—Removing sulfur dioxide or sulfur trioxide
-
- 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
- B01D53/1493—Selection of liquid materials for use as absorbents
-
- 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
- B01D53/185—Liquid distributors
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/46—Removing components of defined structure
- B01D53/48—Sulfur compounds
- B01D53/50—Sulfur oxides
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/46—Removing components of defined structure
- B01D53/48—Sulfur compounds
- B01D53/50—Sulfur oxides
- B01D53/501—Sulfur oxides by treating the gases with a solution or a suspension of an alkali or earth-alkali or ammonium compound
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/46—Removing components of defined structure
- B01D53/48—Sulfur compounds
- B01D53/50—Sulfur oxides
- B01D53/501—Sulfur oxides by treating the gases with a solution or a suspension of an alkali or earth-alkali or ammonium compound
- B01D53/502—Sulfur oxides by treating the gases with a solution or a suspension of an alkali or earth-alkali or ammonium compound characterised by a specific solution or suspension
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/46—Removing components of defined structure
- B01D53/54—Nitrogen compounds
- B01D53/58—Ammonia
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/46—Removing components of defined structure
- B01D53/62—Carbon oxides
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
- B01D53/75—Multi-step processes
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01C—AMMONIA; CYANOGEN; COMPOUNDS THEREOF
- C01C1/00—Ammonia; Compounds thereof
- C01C1/24—Sulfates of ammonium
- C01C1/242—Preparation from ammonia and sulfuric acid or sulfur trioxide
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01C—AMMONIA; CYANOGEN; COMPOUNDS THEREOF
- C01C1/00—Ammonia; Compounds thereof
- C01C1/26—Carbonates or bicarbonates of ammonium
-
- C—CHEMISTRY; METALLURGY
- C05—FERTILISERS; MANUFACTURE THEREOF
- C05C—NITROGENOUS FERTILISERS
- C05C3/00—Fertilisers containing other salts of ammonia or ammonia itself, e.g. gas liquor
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2251/00—Reactants
- B01D2251/20—Reductants
- B01D2251/206—Ammonium compounds
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2252/00—Absorbents, i.e. solvents and liquid materials for gas absorption
- B01D2252/10—Inorganic absorbents
- B01D2252/102—Ammonia
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2257/00—Components to be removed
- B01D2257/30—Sulfur compounds
- B01D2257/302—Sulfur oxides
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2257/00—Components to be removed
- B01D2257/40—Nitrogen compounds
- B01D2257/406—Ammonia
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2257/00—Components to be removed
- B01D2257/50—Carbon oxides
- B01D2257/504—Carbon dioxide
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P60/00—Technologies relating to agriculture, livestock or agroalimentary industries
- Y02P60/20—Reduction of greenhouse gas [GHG] emissions in agriculture, e.g. CO2
Definitions
- the invention belongs to the field of environmental protection technology, and specifically relates to a device and method for controlling ammonia escape in an ammonia desulfurization and decarbonization system.
- ammonium bicarbonate is a typical compound fertilizer that can provide nitrogen fertilizer and CO 2 to plants at the same time. It is especially suitable for the needs of modern agriculture and greenhouse plant growth in soilless cultivation. It truly realizes the resource utilization of CO 2 and realizes carbon cycle. Secondary pollution and CO2 environmental accidents that may be caused by carbon underground storage can be avoided.
- ammonia absorbs CO 2 more efficiently and ammonium bicarbonate is easier to regenerate, which can significantly reduce decarbonization costs.
- Ammonia decarbonization technology has always been the focus of research and is also the best way to solve greenhouse gases; however, ammonia is volatile, and decarbonization needs to be carried out under alkaline conditions, resulting in an increase in ammonia escape. If not solved, a large amount of ammonia will escape, which will not only increase the cost of decarbonization, but also cause secondary pollution.
- Patent CN113262625A proposes an integrated desulfurization and decarbonization device that uses desulfurization circulating liquid for washing to reduce part of the free ammonia in the process gas, and the washing liquid is returned to the desulfurization tower to be used as an absorbent for desulfurization.
- desulfurization circulating fluid For free ammonia in process gas, simply using desulfurization circulating fluid to clean it will still cause a large amount of ammonia to escape. After washing with desulfurization circulating solution and then washing with process water, a large amount of ammonia-containing solution will be produced.
- Returning to the desulfurization functional area to be used as a desulfurization absorbent will destroy the water balance of the desulfurization system and generate wastewater.
- Patent CN101600489B proposes a method of pickling ammonia using SO2 from flue gas, cooling the process gas with the help of a cooling liquid, and absorbing the sulfur dioxide of the process gas into the cooling liquid, thereby obtaining a cooling liquid containing sulfate .
- Ammonia is removed from the process gas that has been treated in the CO2 absorber.
- the main product generated after the cooling liquid absorbs sulfur dioxide is sulfite.
- sulfuric acid needs to be added to the cooling liquid to control the pH value of the cooling liquid, which greatly increases the difficulty of device control.
- this patent does not consider the material balance of desulfurization and decarbonization as an overall system, but only partially removes sulfur dioxide to obtain sulfate.
- the present invention has developed a device and method for controlling the escape of ammonia in an ammonia decarbonization system based on the operation experience of ammonia desulfurization and decarbonization.
- Ammonia is used as the desulfurization and decarburization agent.
- the gas first enters the desulfurization device for desulfurization.
- the final gas enters the decarbonization device to remove the carbon dioxide in the gas.
- the decarbonized gas contains free ammonia, and the acidic ammonium sulfate liquid and acidic water washing liquid used for ammonia desulfurization absorb the free ammonia in the gas.
- the invention effectively controls the escape of ammonia in the ammonia decarbonization system.
- the ammonia recovered by washing can also be used for desulfurization, thus saving ammonia consumption.
- the invention develops a device and method for controlling ammonia escape in an ammonia decarbonization system, using ammonia to remove sulfur oxides and CO 2 to generate ammonium sulfate fertilizer and ammonium bicarbonate fertilizer.
- the ammonia desulfurization and decarbonization device is equipped with an ammonia desulfurization functional area, an ammonia decarbonization functional area, and an ammonia escape control functional area.
- the ammonia desulfurization functional area includes a washing and cooling section, an absorption circulation section, a particulate matter control section, and an ammonia decarbonization functional area. It includes a cooling section and an absorption circulation section.
- the ammonia escape control functional area includes an acidic ammonium sulfate liquid washing system and an acidic water washing system.
- the absorption circulation section of the ammonia desulfurization functional area is connected to the acidic ammonium sulfate liquid washing system of the ammonia escape control functional area through pipelines.
- the particulate matter control section of the ammonia desulfurization functional area or the cooling section of the ammonia decarbonization functional area is connected to the ammonia escape area through pipelines. Control the connection of the acidic water washing system in the functional area.
- the ammonia decarburization absorption cycle section adopts multi-stage absorption, in which less or no ammonia is added in the last stage to reduce the escape of NH 3 after decarburization.
- Ammonia is used as the desulfurization and decarbonization agent.
- the gas first enters the desulfurization functional zone for desulfurization to generate ammonium sulfate fertilizer.
- the desulfurized gas enters the decarbonization functional zone to remove carbon dioxide in the gas and generate ammonium bicarbonate fertilizer for decarbonization.
- the final gas contains free ammonia, and the free ammonia in the absorbed gas is washed and absorbed with acidic ammonium sulfate liquid and acidic water washing liquid derived from ammonia desulfurization.
- the acidic ammonium sulfate liquid adopts the ammonia desulfurization functional zone to absorb the circulating section solution, the ammonium sulfate concentration is 10-38wt%, pH 4.5-6.5; the acidic water washing liquid adopts the ammonia desulfurization functional zone particulate matter control section solution or the ammonia decarbonization functional zone for cooling Section solution, ammonium sulfate concentration 0-5wt%, pH 3-7. After washing in the ammonia escape control functional area, the concentrations of acidic ammonium sulfate liquid and acidic water washing liquid remain basically unchanged.
- the pH of acidic ammonium sulfate liquid is 4.6-6.9, and the pH of acidic water washing liquid is 3.5-7.5.
- the temperature of the acidic ammonium sulfate liquid and acidic water washing liquid is 20-60°C, preferably 30-50°C.
- Acidic ammonium sulfate liquid and acidic water washing liquid scrubbers are provided with a liquid distributor and a gas-liquid contact component.
- the liquid distributor is preferably a trough distributor, and the gas-liquid contact component is preferably a filler.
- the acidic ammonium sulfate liquid and acidic water washing liquid of ammonia desulfurization Before using the acidic ammonium sulfate liquid and acidic water washing liquid of ammonia desulfurization to absorb free ammonia in the gas, it also includes washing with process water to absorb free ammonia.
- the process water is preferably desalted water or solution in the cooling section of the ammonia decarbonization functional area or drainage from the acidic water washing system in the ammonia escape control functional area.
- the acidic ammonium sulfate liquid washing of ammonia desulfurization is equipped with at least one layer of liquid distributor.
- the solution after gas-liquid contact washing is recovered and returned to the desulfurization system.
- the acidic water washing liquid of ammonia desulfurization is equipped with at least one layer of liquid distributor.
- the solution after gas-liquid contact washing is recovered and returned to the desulfurization system or decarbonization system.
- At least one layer of liquid distributor is installed for process water washing, and the ammonia-containing solution produced is returned to the desulfurization system or decarbonization system.
- each section is provided with at least one spray layer, and equipment/components that allow gas to pass are provided between sections.
- the particulate matter removal section it is divided into two parts. The first part of spray washing uses a high concentration solution containing ammonium sulfate for circulating washing, and the second part uses a dilute solution containing ammonium sulfate for circulating washing. There is a device/component between the two parts that allows the passage of gas.
- each section is provided with at least one spray layer, and equipment/components that allow gas to pass are provided between sections.
- a method for controlling the escape of ammonia in an ammonia decarbonization system which is characterized in that the gas after ammonia decarburization contains free ammonia, and the ammonia desulfurization is washed and absorbed with acidic ammonium sulfate liquid and acidic water washing liquid of ammonia desulfurization. Free ammonia in the gas after carbon.
- Embodiment 2 The method according to Embodiment 1, characterized in that, before using the acidic ammonium sulfate liquid and acidic water washing liquid desulfurized by the ammonia method to absorb free ammonia in the gas, it also includes washing with process water to absorb free ammonia, and the process
- the water is preferably desalted water, washing condensed water, or acidic water washing liquid drainage.
- Embodiment 3 The method according to Embodiment 1, characterized in that the ammonia-containing solution produced by washing the acidic ammonium sulfate liquid and acidic water washing liquid of ammonia desulfurization is returned to the desulfurization system or decarbonization system.
- Embodiment 4 The method according to Embodiment 1, characterized in that the acidic ammonium sulfate liquid washing for ammonia desulfurization is provided with at least one layer of liquid distributor, and the solution after gas-liquid contact washing is recovered and returned to the desulfurization system.
- Embodiment 5 The method according to Embodiment 1, characterized in that the acidic water wash of ammonia desulfurization is provided with at least one layer of liquid distributor, and the solution after gas-liquid contact washing is recovered and returned to the desulfurization system or decarbonization system.
- Embodiment 6 The method according to Embodiment 2, characterized in that the process water washing is provided with at least one layer of liquid distributor, The generated ammonia-containing solution is returned to the desulfurization system or decarbonization system.
- Embodiment 7 The method according to Embodiment 1, characterized in that, between the washing of the acidic ammonium sulfate liquid and the acidic water washing liquid used for ammonia desulfurization, equipment or components that only allow gas to pass are provided.
- Embodiment 8 The method according to Embodiment 2, characterized in that equipment or components that only allow gas to pass are provided between the acidic ammonium sulfate liquid desulfurized by ammonia and process water washing.
- ammonia decarburization absorption cycle section includes multi-stage absorption, in which less or no ammonia is added in the last stage to reduce the escape of NH 3 after decarburization.
- NH 3 content in the gas after being treated by the absorption circulation section of the ammonia decarburization functional zone is 200 to 2000 ppm; preferably 400 to 1500 ppm; more preferably 500 to 1000 ppm.
- liquid-to-gas ratio of the process water is usually 5-25, preferably 10-20, and more preferably 12-18.
- liquid-gas ratio of the acidic ammonium sulfate liquid is usually 1-20, preferably 1-10, and more preferably 2-6.
- liquid-to-gas ratio of the acidic water washing liquid is usually 1-15, preferably 1-8, and more preferably 2-5.
- gas-liquid contact parts are provided in the acidic ammonium sulfate liquid and acidic water washing liquid scrubbers, and the gas-liquid contact parts are preferably fillers.
- Embodiment 2 The method according to Embodiment 2, characterized in that acid is added to the process water, washing condensate water, and acidic washing liquid drainage to adjust the pH.
- the acid is sulfuric acid.
- a device for controlling ammonia escape in an ammonia desulfurization and decarbonization system which is characterized in that it includes an ammonia desulfurization functional area, Ammonia decarbonization functional area, ammonia escape control functional area,
- the ammonia desulfurization functional area includes a washing and cooling section, an absorption circulation section, and a particulate matter control section.
- the ammonia decarbonization functional area includes a cooling section and an absorption cycle section.
- the ammonia escape control functional area includes the ammonia escape control section, including the acidic ammonium sulfate liquid washing system and the acidic water washing system.
- the absorption circulation section of the ammonia desulfurization functional area is connected to the acidic ammonium sulfate washing system of the ammonia escape control functional area through pipelines.
- the particulate matter control section of the ammonia desulfurization functional area or the cooling section of the ammonia decarbonization functional area is connected to the ammonia escape control functional area through pipelines. Escape control functional area acid wash system connection.
- ammonia decarburization absorption cycle section includes multi-stage absorption, in which less or no ammonia is added in the last stage to reduce the escape of NH 3 after decarburization.
- the device according to embodiment 21, characterized in that the ammonia escape control functional area may also include a process water washing system.
- the process water washing system is connected to the process water pipe through a pipeline and is connected to the absorption circulation section of the ammonia desulfurization device or the ammonia desulfurization device. Carbon device absorption cycle section connection.
- Figure 1 shows Embodiment 1 of the present invention.
- process water is also used for washing to absorb free ammonia.
- FIG. 2 shows Embodiment 2 of the present invention, in which the acidic ammonium sulfate liquid and acidic water washing liquid used for ammonia desulfurization are used to wash free ammonia in the absorbed gas.
- Figure 3 shows a comparative example, using process water for washing to absorb free ammonia.
- Process gas 1 desulfurization functional area 2, desulfurization washing and cooling section 2-1, desulfurization absorption circulation section 2-2, desulfurization particulate matter control section 2-3, desulfurization circulation pump a 3, desulfurization circulation pump b 4, desulfurization circulation pump c 5 , Desulfurization circulation tank 6, oxidation air 7, desulfurization system and ammonia addition 8, ammonium sulfate discharge pump 9, desulfurization circulation pump d 10, desulfurization heat exchanger 11, tail gas after desulfurization 12, decarbonization absorption tower 13, decarbonization circulation pump 14. Ammonium bicarbonate discharge pump 15. Add ammonia to the decarburization system 16. Tail gas after decarburization 17. Ammonia washing tower 18.
- the gas after ammonia decarburization contains free ammonia.
- the present invention specifically uses acidic ammonium sulfate liquid and acidic water washing liquid for ammonia desulfurization to wash and absorb free ammonia in the gas after ammonia decarburization.
- the present invention also includes washing with process water to absorb free ammonia before using the acidic ammonium sulfate liquid and acidic water washing liquid desulfurized by ammonia method to absorb free ammonia.
- the process water is preferably desalted water and washing condensed water.
- the flow rate of the acidic ammonium sulfate liquid, acidic water washing liquid or process water used for washing and absorption can be appropriately adjusted as needed.
- the liquid-gas ratio of the process water is usually 5-25, preferably 10-20. More preferably, 12-18 is used; the liquid-to-gas ratio of the acidic ammonium sulfate liquid is usually 1-20, preferably 1-10, and more preferably 2-6; the liquid-to-gas ratio of the acidic water washing liquid is usually 1-20, preferably 1-15, and more Preferably 2-10.
- V process gas flow after ammonia decarburization (working conditions, that is, gas flow under operating conditions (temperature, pressure, etc.)), m 3 /h.
- the treatment carried out according to the method of the present invention mainly removes free ammonia contained in the gas after decarburization by the ammonia method, and has little effect on the SO 2 content and CO 2 content.
- the pH of the acidic ammonium sulfate liquid is 4.5-6.5, and the ammonium sulfate concentration is 10-38wt%, preferably 12-35wt%, more preferably 15-30wt%, most preferably 17-28wt%;
- the pH of the acidic water wash liquid is 3-7, and the ammonium sulfate concentration is 0-5wt%, preferably 0-3wt%, more preferably 0-1wt%, most preferably 0-0.6wt%.
- the temperature of the acidic ammonium sulfate liquid and the acidic water washing liquid is 20-60°C, preferably 30-50°C.
- the NH 3 content in the gas after being treated by the decarbonization absorption tower is 200 to 2000 ppm; preferably 400 to 1500 ppm; more preferably 500 to 1000 ppm.
- the SO 2 content in the gas after being treated by the decarbonization absorption tower is 0 to 20 mg/Nm 3 ; preferably 0 to 15 mg/Nm 3 ; more preferably 0 to 10 mg/Nm 3 .
- the CO 2 content in the gas after being treated by the decarbonization absorption tower is 0-20v%; preferably 1-10v%; more preferably 2-7v%.
- the NH 3 content in the gas after being treated by the method of the present invention is 0 to 30 ppm; preferably 0 to 20 ppm; more preferably 0 to 10 ppm.
- the method for controlling the escape of ammonia in an ammonia-based decarbonization system protected by the present invention is preferably carried out in a device for controlling the escape of ammonia from an ammonia-based desulfurization and decarbonization system as defined by the present invention.
- the method and device of the present invention achieve beneficial economic effects in addition to technical effects, especially reducing ammonia escape and particularly significantly reducing ammonia consumption.
- the ammonia consumption loss can be reduced by 96%-99%, preferably 97%-99%. %, specifically as shown in the following examples.
- the testing method for the SO 2 content in the gas in the present invention is HJ 629-2011 Fixed pollution source waste gas. Determination of sulfur dioxide. Non-dispersive infrared absorption method;
- the test method for CO2 content is HJ 870-2017 Determination of carbon dioxide in exhaust gas from fixed pollution sources, non-dispersive infrared absorption method;
- test method for NH 3 content is HJ 533-2009 Determination of Ammonia in Ambient Air and Exhaust Gas Nessler's Reagent Spectrophotometry.
- the present invention specifically provides Examples 1 and 2 and comparative examples to further illustrate the technical solution of the present invention and its beneficial effects.
- the process gas 1 containing sulfur oxides and CO2 enters the desulfurization functional zone 2, and sequentially passes through the desulfurization washing and cooling section 2-1, the desulfurization absorption cycle section 2-2, and the desulfurization particulate matter control section 2-3.
- the cooling section 2-1 uses the desulfurization circulation pump-a 3 to perform a spray cycle. While the tail gas is cooled, the ammonium sulfate solution is concentrated. The concentrated and precipitated solid ammonium sulfate slurry is sent to the ammonium sulfate discharge pump 9 to produce ammonium sulfate 26.
- desulfurization circulation pump-b 4 Use desulfurization circulation pump-b 4, desulfurization circulation pump-c 5, and desulfurization circulation tank 6 to perform absorption spray circulation to absorb sulfur oxides (sulfur dioxide and sulfur trioxide) in the exhaust gas.
- the desulfurization circulation pump-c 5 sends out part of the ammonium sulfate solution 20 and is cooled to 35°C by the cooler 32 and then goes to the ammonium sulfate washing section 18-2 of the ammonia tower.
- the washed solution 21 returns to the desulfurization circulation tank 6.
- the desulfurization circulation pump-d 10 is used to perform the washing spray cycle, and the desulfurization heat exchanger 11 is used to control the washing temperature and the temperature of the desulfurized tail gas 12.
- the particulate matter control section 2-3 of the ammonia desulfurization functional area realizes the cooling function of ammonia decarbonization.
- the acidic solution 23 condensed from the flue gas is cooled to 35°C by the cooler 33 and then used as the acid water washing section 18-3 of the ammonia washing tower to replenish water.
- the washed solution 24 is returned to the desulfurization circulation tank 6.
- To desulfurize After the ammonia added to the system 8 is measured, it goes to the desulfurization circulation tank 6 to add ammonia.
- the oxidizing air 7 goes to the desulfurization circulation tank 6 to oxidize the solution.
- the tail gas 12 enters the decarbonization absorption tower 13, uses the decarbonization circulation pump 14 for absorption circulation, and uses the ammonium carbonate discharge pump 15 to deliver the finished product ammonium carbonate 27.
- the decarbonization absorption tower 13 adds ammonia after metering.
- the tail gas 17 enters the ammonia washing tower 18, passes through the process water washing section 18-1, the ammonium sulfate washing section 18-2, and the acid liquid washing section 18-3 in sequence, and uses ammonia washing in the ammonia washing tower process water washing section 18-1.
- the circulating pump-a 19 performs process water washing.
- the ammonia washing tower process water washing section 18-1 is equipped with a trough distributor 31-1 and a filler 30-1. The process water is replenished through the external process water pipe 28, and the washed ammonia-containing solution 29 Go to decarburization tower 13.
- the ammonium sulfate washing section 18-2 of the ammonia washing tower is equipped with a trough distributor 31-2 and a filler 30 -2, the washed solution (that is, returned to the desulfurization liquid) 21 returns to the desulfurization circulation tank 6.
- the acidic solution condensed from the flue gas (i.e., the desulfurization particulate matter control section solution) 23 sent out by the desulfurization circulating pump-d 10 is used as water replenishment for the acidic water washing section 18-3 of the ammonia washing tower.
- the acidic water washing section 18-3 of the ammonia washing tower is equipped with a trough type distributor 31-3 and filler 30-3, the washed solution (that is, returned to the acidic solution) 24 returns to the desulfurization circulation tank 6. After washing, 25% of the clean flue gas is discharged.
- the acidic ammonium sulfate liquid 20 has a flow rate of 350m 3 /h, pH 6.4, and an ammonium sulfate concentration of 18 wt%.
- the acidic ammonium sulfate liquid returned after entering the ammonia washing tower for washing has a pH of 6.9, and the ammonium sulfate concentration remains basically unchanged.
- the flow rate of the acidic washing liquid 23 is adjusted according to the pH value of the washing liquid in the acid washing section 18-3 of the ammonia washing tower.
- the pH is 3.8 and the ammonium sulfate concentration is 2wt%.
- the acidic washing liquid returned after entering the ammonia washing tower for washing has a pH of 4.2 and the ammonium sulfate concentration remains basically unchanged.
- the ammonia washing circulation pump b 22 has a circulation capacity of 500m 3 /h to ensure the ammonia washing effect.
- the flow rate of process water 28 is adjusted according to the pH value of the washing liquid in the process water washing section 18-1 of the ammonia washing tower.
- the circulation volume of the ammonia washing circulation pump a 19 is 1200m 3 /h to ensure the ammonia washing effect.
- the pH of the demineralized water is 6.9, and the pH of the solution returned after entering the ammonia washing tower is 7.9.
- Desulfurization and decarburization use 99.6% liquid ammonia as the absorbent.
- the parameters of process gas 1 are shown in the table below:
- the amount of ammonia escaped is 4.98t/year, and the ammonia consumption loss is about 20,000 yuan/year.
- the amount of ammonia escaped is 8.96t/year, and the ammonia consumption loss is about 36,000 yuan/year.
- the amount of ammonia escaped is 248t/year, and the ammonia consumption loss is about 992,000 yuan/year.
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Abstract
Description
Claims (25)
- 一种控制氨法脱碳***氨逃逸的方法,其特征在于,氨法脱碳后的气体中含有游离氨,用氨法脱硫的酸性硫酸铵液和酸性水洗液洗涤吸收该氨法脱碳后的气体中的游离氨。
- 如权利要求1所述的方法,其特征在于,在用氨法脱硫的酸性硫酸铵液和酸性水洗液吸收气体中的游离氨前,还包括用工艺水进行洗涤,吸收游离氨,工艺水优选脱盐水、洗涤冷凝水、酸性水洗液排水。
- 如权利要求1所述的方法,其特征在于,氨法脱硫的酸性硫酸铵液和酸性水洗液洗涤产生的含氨溶液返回脱硫***或脱碳***。
- 如权利要求1所述的方法,其特征在于,氨法脱硫的酸性硫酸铵液洗涤至少设置1层液体分布器,气液接触洗涤后的溶液回收,返回脱硫***。
- 如权利要求1所述的方法,其特征在于,氨法脱硫的酸性水洗液洗涤至少设置1层液体分布器,气液接触洗涤后的溶液回收,返回脱硫***或脱碳***。
- 如权利要求2所述的方法,其特征在于,工艺水洗涤至少设置1层液体分布器,产生的含氨溶液返回脱硫***或脱碳***。
- 如权利要求1所述的方法,其特征在于,用氨法脱硫的酸性硫酸铵液和酸性水洗液洗涤之间,设有仅允许气体通过的设备或部件。
- 如权利要求2所述的方法,其特征在于,用氨法脱硫的酸性硫酸铵液和工艺水洗涤之间,设有仅允许气体通过的设备或部件。
- 如权利要求1所述的方法,其特征在于,氨法脱碳吸收循环段包括多级吸收,其中最后一级少加氨或不加氨,以减少脱碳后的NH3逃逸。
- 如权利要求1所述的方法,其特征在于,经氨法脱碳功能区吸收循环段处理后气体中NH3含量为200至2000ppm;优选400至1500ppm;更优选500至1000ppm。
- 如权利要求1所述的方法,其特征在于,在经过氨逃逸控制功能区处理之后气体中NH3含量为0至30ppm;优选0至20ppm;更优选0至10ppm。
- 如权利要求1所述的方法,其特征在于,酸性硫酸铵液pH 4.5-6.5,硫酸铵浓度10-38wt%;酸性水洗液pH 3-7,硫酸铵浓度0-5wt%。
- 如权利要求1所述的方法,其特征在于,酸性硫酸铵液、酸性水洗液温度20-60℃,优选30-50℃。
- 如权利要求1所述的方法,其特征在于,酸性硫酸铵液、酸性水洗液洗涤前通过冷却器冷却降温后再洗涤。
- 如权利要求2所述的方法,其特征在于,工艺水的液气比通常采用5-25,优选10-20,更优选12-18。
- 如权利要求1所述的方法,其特征在于,酸性硫酸铵液的液气比通常采用1-20,优选1-10,更优选2-6。
- 如权利要求1所述的方法,其特征在于,酸性水洗液的液气比通常采用1-15,优选1-8,更优选2-5。
- 如权利要求1所述的方法,其特征在于,酸性硫酸铵液、酸性水洗液洗涤器中设置气液接触部件,气液接触部件优选填料。
- 如权利要求2所述的方法,其特征在于,工艺水、洗涤冷凝水、酸性水洗液排水的pH不大于8。
- 如权利要求2所述的方法,其特征在于,工艺水、洗涤冷凝水、酸性水洗液排水加入酸调节pH,优选该酸是硫酸。
- 一种控制氨法脱硫脱碳***氨逃逸的装置,其特征在于,包括氨法脱硫功能区、氨法脱碳功能区、氨逃逸控制功能区,其中,氨法脱硫功能区包括洗涤降温段、吸收循环段、颗粒物控制段,氨法脱碳功能区包括冷却降温段、吸收循环段,氨逃逸控制功能区包括氨逃逸控制段包括酸性硫酸铵液洗涤***、酸性水洗***,氨法脱硫功能区的吸收循环段和通过管道与氨逃逸控制功能区酸性硫酸铵液洗涤***连接,氨法脱硫功能区的颗粒物控制段或氨法脱碳功能区的冷却降温段通过管道与氨逃逸控制功能区酸性水洗***连接。
- 如权利要求21所述的装置,其特征在于,氨法脱碳吸收循环段包括多级吸收,其中最后一级少加氨或不加氨,以减少脱碳后的NH3逃逸。
- 如权利要求21所述的装置,其特征在于,氨逃逸控制功能区还可包括工艺水洗***,工艺水洗***通过管道与工艺水管连接,并与氨法脱硫装置吸收循环段或氨法脱碳装置吸收循环段连接。
- 如权利要求21所述的装置,其特征在于,氨法脱硫功能区、氨法脱碳功能区各段,可以组合成一个塔中或多个塔中,段与段之间设有允许气体通过的设备/部件。
- 如权利要求21所述的装置,其特征在于,氨法脱硫功能区颗粒物控制段可部分或全部实现氨法脱碳功能区冷却降温段功能。
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CA3210444A CA3210444A1 (en) | 2022-05-19 | 2023-03-24 | Device and method for controlling ammonia escape in ammonia-based decarbonization system |
MX2023010155A MX2023010155A (es) | 2022-05-19 | 2023-03-24 | Dispositivo y metodo para controlar el escape de amoniaco en un sistema de descarbonizacion a base de amoniaco. |
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Citations (6)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
CN101600489A (zh) | 2007-01-31 | 2009-12-09 | 阿尔斯托姆科技有限公司 | 使用来自烟气的so2对氨进行酸洗 |
US20150352486A1 (en) * | 2013-04-24 | 2015-12-10 | Jiangsu New Century Jiangnan Environmental Protection Co., Ltd | Flue gas-treating method and apparatus for treating acidic tail gas by using ammonia process |
CN211274164U (zh) * | 2019-07-17 | 2020-08-18 | 实联化工(江苏)有限公司 | 一种碱行业干铵工段含氨尾气处理装置 |
CN111957191A (zh) * | 2020-09-18 | 2020-11-20 | 镇海石化工程股份有限公司 | 一种防止氨逃逸的氨法脱硫装置及其生产方法 |
CN113262625A (zh) | 2021-05-11 | 2021-08-17 | 江苏新世纪江南环保股份有限公司 | 一种氨法脱硫脱碳一体化装置及方法 |
CN114917743A (zh) * | 2022-05-19 | 2022-08-19 | 江苏新世纪江南环保股份有限公司 | 一种控制氨法脱碳***氨逃逸的装置及方法 |
Family Cites Families (6)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
CN101703878A (zh) * | 2009-11-11 | 2010-05-12 | 王建敏 | 排烟处理装置和方法 |
US8858905B2 (en) * | 2011-02-16 | 2014-10-14 | Anhui Huaihua Co. Ltd. | System and process for trapping sulfur dioxide and carbon dioxide by ammonia absorption at atmospheric pressure |
CN102908890A (zh) * | 2012-11-15 | 2013-02-06 | 王正中 | 烟气氨法脱硫脱硝中防止氨逃逸装置 |
CN110201508A (zh) * | 2019-05-09 | 2019-09-06 | 山东明晟化工工程有限公司 | 一种氨逃逸和氨法脱硫气溶胶联合处理方法 |
CN112569752A (zh) * | 2020-12-16 | 2021-03-30 | 昆岳互联环境技术(江苏)有限公司 | 一种高效节能型氨法脱硫超低排放装置及方法 |
CN114146549A (zh) * | 2021-11-29 | 2022-03-08 | 中国科学院过程工程研究所 | 一种烟气氨法脱硫脱硝脱碳的***装置及方法 |
-
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Patent Citations (7)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
CN101600489A (zh) | 2007-01-31 | 2009-12-09 | 阿尔斯托姆科技有限公司 | 使用来自烟气的so2对氨进行酸洗 |
US20150352486A1 (en) * | 2013-04-24 | 2015-12-10 | Jiangsu New Century Jiangnan Environmental Protection Co., Ltd | Flue gas-treating method and apparatus for treating acidic tail gas by using ammonia process |
CN211274164U (zh) * | 2019-07-17 | 2020-08-18 | 实联化工(江苏)有限公司 | 一种碱行业干铵工段含氨尾气处理装置 |
CN111957191A (zh) * | 2020-09-18 | 2020-11-20 | 镇海石化工程股份有限公司 | 一种防止氨逃逸的氨法脱硫装置及其生产方法 |
CN113262625A (zh) | 2021-05-11 | 2021-08-17 | 江苏新世纪江南环保股份有限公司 | 一种氨法脱硫脱碳一体化装置及方法 |
US20220362706A1 (en) * | 2021-05-11 | 2022-11-17 | Jiangnan Environmental Protection Group Inc. | Integrated ammonia-based desulfurization and decarbonization apparatus and method |
CN114917743A (zh) * | 2022-05-19 | 2022-08-19 | 江苏新世纪江南环保股份有限公司 | 一种控制氨法脱碳***氨逃逸的装置及方法 |
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