CN109297037B - Environment-friendly recycling system for chlorine-containing organic waste gas - Google Patents
Environment-friendly recycling system for chlorine-containing organic waste gas Download PDFInfo
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- CN109297037B CN109297037B CN201811278560.8A CN201811278560A CN109297037B CN 109297037 B CN109297037 B CN 109297037B CN 201811278560 A CN201811278560 A CN 201811278560A CN 109297037 B CN109297037 B CN 109297037B
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- 239000000460 chlorine Substances 0.000 title claims abstract description 52
- ZAMOUSCENKQFHK-UHFFFAOYSA-N Chlorine atom Chemical compound [Cl] ZAMOUSCENKQFHK-UHFFFAOYSA-N 0.000 title claims abstract description 45
- 229910052801 chlorine Inorganic materials 0.000 title claims abstract description 45
- 239000007789 gas Substances 0.000 title claims abstract description 33
- 239000010815 organic waste Substances 0.000 title claims abstract description 27
- 238000004064 recycling Methods 0.000 title claims abstract description 21
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims abstract description 76
- 239000003546 flue gas Substances 0.000 claims abstract description 76
- 238000010791 quenching Methods 0.000 claims abstract description 67
- 238000010521 absorption reaction Methods 0.000 claims abstract description 63
- 230000000171 quenching effect Effects 0.000 claims abstract description 57
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims abstract description 51
- 229910002804 graphite Inorganic materials 0.000 claims abstract description 49
- 239000010439 graphite Substances 0.000 claims abstract description 49
- 239000000779 smoke Substances 0.000 claims abstract description 32
- 239000002918 waste heat Substances 0.000 claims abstract description 28
- 238000003303 reheating Methods 0.000 claims abstract description 17
- 239000003513 alkali Substances 0.000 claims abstract description 13
- 239000000945 filler Substances 0.000 claims abstract description 13
- 239000002253 acid Substances 0.000 claims description 38
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 claims description 30
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 29
- 238000011049 filling Methods 0.000 claims description 16
- 238000012856 packing Methods 0.000 claims description 16
- 229910021529 ammonia Inorganic materials 0.000 claims description 13
- 239000000446 fuel Substances 0.000 claims description 10
- 230000007797 corrosion Effects 0.000 claims description 8
- 238000005260 corrosion Methods 0.000 claims description 8
- 238000002485 combustion reaction Methods 0.000 claims description 7
- 239000003054 catalyst Substances 0.000 claims description 6
- 230000007613 environmental effect Effects 0.000 claims description 6
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 claims description 4
- 239000007921 spray Substances 0.000 claims description 4
- 238000000926 separation method Methods 0.000 claims description 3
- 241000208125 Nicotiana Species 0.000 claims description 2
- 235000002637 Nicotiana tabacum Nutrition 0.000 claims description 2
- 238000009434 installation Methods 0.000 claims description 2
- 238000009413 insulation Methods 0.000 claims description 2
- 238000002347 injection Methods 0.000 claims 2
- 239000007924 injection Substances 0.000 claims 2
- 238000000889 atomisation Methods 0.000 claims 1
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 abstract description 78
- 239000002912 waste gas Substances 0.000 abstract description 16
- 239000000126 substance Substances 0.000 abstract description 9
- 238000011084 recovery Methods 0.000 abstract description 4
- 238000004519 manufacturing process Methods 0.000 abstract description 3
- 239000000575 pesticide Substances 0.000 abstract description 3
- 238000006243 chemical reaction Methods 0.000 abstract description 2
- 238000012423 maintenance Methods 0.000 abstract description 2
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 abstract 1
- 239000001257 hydrogen Substances 0.000 abstract 1
- 229910052739 hydrogen Inorganic materials 0.000 abstract 1
- 238000006386 neutralization reaction Methods 0.000 abstract 1
- IXCSERBJSXMMFS-UHFFFAOYSA-N hydrogen chloride Substances Cl.Cl IXCSERBJSXMMFS-UHFFFAOYSA-N 0.000 description 62
- 229910000041 hydrogen chloride Inorganic materials 0.000 description 62
- 238000000034 method Methods 0.000 description 17
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 13
- 239000007788 liquid Substances 0.000 description 12
- 230000008569 process Effects 0.000 description 8
- 238000001179 sorption measurement Methods 0.000 description 8
- 238000005507 spraying Methods 0.000 description 7
- 238000005406 washing Methods 0.000 description 7
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 6
- 239000003344 environmental pollutant Substances 0.000 description 6
- 230000003647 oxidation Effects 0.000 description 6
- 238000007254 oxidation reaction Methods 0.000 description 6
- 231100000719 pollutant Toxicity 0.000 description 6
- 239000000243 solution Substances 0.000 description 6
- HGUFODBRKLSHSI-UHFFFAOYSA-N 2,3,7,8-tetrachloro-dibenzo-p-dioxin Chemical compound O1C2=CC(Cl)=C(Cl)C=C2OC2=C1C=C(Cl)C(Cl)=C2 HGUFODBRKLSHSI-UHFFFAOYSA-N 0.000 description 5
- 239000000498 cooling water Substances 0.000 description 5
- 239000000969 carrier Substances 0.000 description 4
- 239000000463 material Substances 0.000 description 4
- 230000007935 neutral effect Effects 0.000 description 4
- 239000002699 waste material Substances 0.000 description 4
- VEXZGXHMUGYJMC-UHFFFAOYSA-M Chloride anion Chemical compound [Cl-] VEXZGXHMUGYJMC-UHFFFAOYSA-M 0.000 description 3
- 239000012267 brine Substances 0.000 description 3
- 238000010438 heat treatment Methods 0.000 description 3
- 229910052757 nitrogen Inorganic materials 0.000 description 3
- HPALAKNZSZLMCH-UHFFFAOYSA-M sodium;chloride;hydrate Chemical compound O.[Na+].[Cl-] HPALAKNZSZLMCH-UHFFFAOYSA-M 0.000 description 3
- 241000196324 Embryophyta Species 0.000 description 2
- FAPWRFPIFSIZLT-UHFFFAOYSA-M Sodium chloride Chemical compound [Na+].[Cl-] FAPWRFPIFSIZLT-UHFFFAOYSA-M 0.000 description 2
- RAHZWNYVWXNFOC-UHFFFAOYSA-N Sulphur dioxide Chemical compound O=S=O RAHZWNYVWXNFOC-UHFFFAOYSA-N 0.000 description 2
- 238000009825 accumulation Methods 0.000 description 2
- 230000009471 action Effects 0.000 description 2
- 230000003197 catalytic effect Effects 0.000 description 2
- 150000001805 chlorine compounds Chemical class 0.000 description 2
- 230000007547 defect Effects 0.000 description 2
- 238000011161 development Methods 0.000 description 2
- 238000004043 dyeing Methods 0.000 description 2
- 238000002156 mixing Methods 0.000 description 2
- 230000003472 neutralizing effect Effects 0.000 description 2
- 239000005416 organic matter Substances 0.000 description 2
- 238000006864 oxidative decomposition reaction Methods 0.000 description 2
- 238000007639 printing Methods 0.000 description 2
- 230000009467 reduction Effects 0.000 description 2
- 229920006395 saturated elastomer Polymers 0.000 description 2
- 239000013589 supplement Substances 0.000 description 2
- 238000005979 thermal decomposition reaction Methods 0.000 description 2
- 230000001988 toxicity Effects 0.000 description 2
- 231100000419 toxicity Toxicity 0.000 description 2
- 206010003497 Asphyxia Diseases 0.000 description 1
- KZBUYRJDOAKODT-UHFFFAOYSA-N Chlorine Chemical compound ClCl KZBUYRJDOAKODT-UHFFFAOYSA-N 0.000 description 1
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 description 1
- 239000006096 absorbing agent Substances 0.000 description 1
- 230000004913 activation Effects 0.000 description 1
- 239000000956 alloy Substances 0.000 description 1
- 229910045601 alloy Inorganic materials 0.000 description 1
- 230000004075 alteration Effects 0.000 description 1
- 238000004458 analytical method Methods 0.000 description 1
- 150000004945 aromatic hydrocarbons Chemical class 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 238000013475 authorization Methods 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000006065 biodegradation reaction Methods 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 238000004364 calculation method Methods 0.000 description 1
- 238000005266 casting Methods 0.000 description 1
- 238000010276 construction Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 210000001508 eye Anatomy 0.000 description 1
- 239000013505 freshwater Substances 0.000 description 1
- 239000002920 hazardous waste Substances 0.000 description 1
- 230000036541 health Effects 0.000 description 1
- 230000007794 irritation Effects 0.000 description 1
- 230000007774 longterm Effects 0.000 description 1
- 238000005259 measurement Methods 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 210000004400 mucous membrane Anatomy 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- -1 polytetrafluoroethylene Polymers 0.000 description 1
- 229920001343 polytetrafluoroethylene Polymers 0.000 description 1
- 239000004810 polytetrafluoroethylene Substances 0.000 description 1
- 239000000047 product Substances 0.000 description 1
- 230000002035 prolonged effect Effects 0.000 description 1
- 230000001737 promoting effect Effects 0.000 description 1
- 210000002345 respiratory system Anatomy 0.000 description 1
- 150000003839 salts Chemical class 0.000 description 1
- 239000003566 sealing material Substances 0.000 description 1
- 239000010865 sewage Substances 0.000 description 1
- 230000035939 shock Effects 0.000 description 1
- 229910002027 silica gel Inorganic materials 0.000 description 1
- 239000000741 silica gel Substances 0.000 description 1
- 210000003491 skin Anatomy 0.000 description 1
- 239000011780 sodium chloride Substances 0.000 description 1
- 239000007779 soft material Substances 0.000 description 1
- 238000002336 sorption--desorption measurement Methods 0.000 description 1
- 238000003860 storage Methods 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
- 231100000331 toxic Toxicity 0.000 description 1
- 230000002588 toxic effect Effects 0.000 description 1
- 238000004056 waste incineration Methods 0.000 description 1
Classifications
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
- F23G7/00—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals
- F23G7/06—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals of waste gases or noxious gases, e.g. exhaust gases
-
- 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
-
- 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
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/38—Removing components of undefined structure
- B01D53/40—Acidic components
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
- B01D53/75—Multi-step processes
-
- 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
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
- B01D53/86—Catalytic processes
- B01D53/8621—Removing nitrogen compounds
- B01D53/8625—Nitrogen oxides
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F22—STEAM GENERATION
- F22B—METHODS OF STEAM GENERATION; STEAM BOILERS
- F22B1/00—Methods of steam generation characterised by form of heating method
- F22B1/02—Methods of steam generation characterised by form of heating method by exploitation of the heat content of hot heat carriers
- F22B1/18—Methods of steam generation characterised by form of heating method by exploitation of the heat content of hot heat carriers the heat carrier being a hot gas, e.g. waste gas such as exhaust gas of internal-combustion engines
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES
- F23J15/00—Arrangements of devices for treating smoke or fumes
- F23J15/02—Arrangements of devices for treating smoke or fumes of purifiers, e.g. for removing noxious material
- F23J15/04—Arrangements of devices for treating smoke or fumes of purifiers, e.g. for removing noxious material using washing fluids
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES
- F23J15/00—Arrangements of devices for treating smoke or fumes
- F23J15/06—Arrangements of devices for treating smoke or fumes of coolers
-
- 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
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E20/00—Combustion technologies with mitigation potential
- Y02E20/30—Technologies for a more efficient combustion or heat usage
Landscapes
- Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- Environmental & Geological Engineering (AREA)
- Analytical Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- General Chemical & Material Sciences (AREA)
- Health & Medical Sciences (AREA)
- Biomedical Technology (AREA)
- General Engineering & Computer Science (AREA)
- Mechanical Engineering (AREA)
- Combustion & Propulsion (AREA)
- Life Sciences & Earth Sciences (AREA)
- Sustainable Development (AREA)
- Sustainable Energy (AREA)
- Physics & Mathematics (AREA)
- Thermal Sciences (AREA)
- Treating Waste Gases (AREA)
Abstract
The invention discloses an environment-friendly recycling system for chlorine-containing organic waste gas, which realizes the environment-friendly and energy-saving requirements of 'three-conversion' through high-temperature incineration, waste heat recovery, HCl absorption, alkali liquor neutralization and SCR denitration. The integrated structure mainly comprises an adiabatic incinerator, a horizontal smoke tube waste heat boiler, a graphite quenching tower, a graphite HCl absorption tower, a deacidification filler tower, a smoke reheating device, an SCR denitration device and a chimney. Chlorine-containing organic matters in the waste gas are decomposed at high temperature, chlorine element and hydrogen element are combined to generate HCl gas, heat is recovered through a waste heat boiler, and the HCl gas is absorbed through a quenching tower and an absorption tower to generate hydrochloric acid with the concentration of about 20%. And the flue gas is discharged into the atmosphere through a chimney after passing through a deacidification tower and SCR denitration. The invention has the characteristics of simple manufacturing process, convenient maintenance, safe and stable operation and high resource recycling rate, and is suitable for popularization and use in treating clean chlorine-containing organic waste gas in the industries of chemical industry, pesticide and the like.
Description
Technical Field
The invention relates to the energy-saving and environment-friendly industry, in particular to a unit system for carrying out innocent treatment and recycling on clean chlorine-containing organic waste gas generated in the production process of the industries such as chemical industry, pesticide industry, printing and dyeing industry and the like.
Background
In recent years, with the rapid development of economy, in the production process of chemical industry, pesticide industry, printing and dyeing industry and the like, a few waste gases containing chlorine elements are often generated, wherein the existence forms of the chlorine elements mainly comprise chlorine gas, hydrogen chloride and organic matters containing the chlorine elements. Most of the chlorine-containing organic matters are macromolecular structures, wherein chlorinated aromatic hydrocarbon has toxicity, stable chemical property and difficult biodegradation, and can stay in the environment for a long time; chlorine has toxicity, is twice as harmful to plants as sulfur dioxide, and can form hydrochloric acid smog when contacted with humid air; the hydrogen chloride has asphyxia smell, has strong irritation to upper respiratory tract, and has corrosion to eyes, skin and mucous membrane. Therefore, the waste gas cannot be directly discharged into the nature, otherwise, the environment is polluted, the ecological environment is damaged, and the human health is damaged. Therefore, a reasonable and effective technology for treating chlorine-containing organic waste gas is found, so that the pollution of the part of waste gas to the environment is reduced, and the method has important significance for promoting sustainable development of the environment and industries. At present, domestic treatment methods for chlorine-containing organic waste gas mainly comprise an adsorption-analysis method, a catalytic oxidation method, a thermal decomposition method, a high-temperature incineration method and the like.
The main adsorption carriers of the adsorption-desorption method are activated carbon and silica gel, so that chlorides in the waste gas are adsorbed at a lower temperature, and the waste gas can be desorbed at a high temperature. However, in the adsorption process, physical adsorption and chemical adsorption exist, and adsorption carriers react with chlorine-containing organic matters in the chemical adsorption, so that the adsorption carriers are consumables, and in practical application, new adsorption carriers are required to be continuously added to ensure the removal rate of the chlorides in the exhaust gas.
The catalytic oxidation method is to reduce the reaction activation energy in the presence of catalyst, so that the chlorine-containing organic matter can be oxidatively decomposed into CO at a lower temperature 2 、H 2 O, HCl and a small amount of Cl 2 The operation temperature of the method is generally 100-300 ℃, but dioxin substances can be generated in the temperature range, and the dioxin substances have extremely toxic effects and have great influence on the environment and human bodies.
The thermal decomposition method adopts thermal storage oxidation to carry out oxidative decomposition on chlorine-containing waste gas, the oxidation temperature can reach more than 800 ℃, and the generation of dioxin can be avoided. However, because HCl generated by heat accumulation and oxidation of chlorine-containing waste gas generates serious chloride ion corrosion to a pipeline and a heat accumulation and oxidation switching valve, the switching valve is generally sealed by soft materials such as polytetrafluoroethylene and the like which resist the chloride ion corrosion, but the sealing material cannot be used under the working condition of 1200 ℃ or more, and when the smoke exhaust temperature is higher, the stable operation of the device cannot be ensured; the switching valve seal can also be an alloy hard seal with the capability of resisting chloride ion corrosion, but the cost of the valve is 3-5 times of that of a common valve, and the construction cost of the device is greatly increased.
Patent No. CN 103736378B proposes a chlorine-containing absorption system comprising: the device comprises a pre-washing tower, a primary tower, a secondary tower, an alkali adding pump connected with the secondary tower, a control device and a liquid alkali adding pump, wherein when the control device detects that the pH value of the primary tower absorption liquid is lower than the standard value, the primary tower absorption liquid is automatically discharged to the pre-washing tower, and the secondary tower absorption liquid is automatically discharged to the primary tower; when the control device detects that the pH value of the washing liquid in the pre-washing tower is lower than the standard value, the washing liquid is automatically discharged, and the absorption liquid of the first-stage tower is automatically discharged into the pre-washing tower. The device is simple in structure and convenient to connect, and meanwhile, chlorine-containing flue gas can be fully neutralized, however, on one hand, a large amount of alkali liquor is required to be prepared by the device, and most of flue gas heat is wasted. On the other hand, the utilization rate of the flue gas is extremely low, and NO in the flue gas is not excluded X And other pollutants are discharged beyond standard, so that the requirements of pollution control and resource utilization are difficult to meet.
Special purpose for authorization number CN 101634453AThe process includes feeding chlorine-containing waste liquid/waste gas into incinerator, burning auxiliary fuel to raise the temperature in incinerator and to oxidize and decompose chlorine-containing organic matter to produce CO 2 、H 2 O, HCl and a small amount of Cl 2 . The high-temperature flue gas after incineration directly enters a quenching tower and is rapidly cooled to 90 ℃ under the action of sprayed cooling water, so that the generation of dioxin substances is avoided. Then the flue gas enters a deacidification tower and alkali liquor is used for neutralizing HCl and Cl in the flue gas 2 And the flue gas after alkaline washing reaches the emission standard and is discharged into the atmosphere through a chimney. The patent process device mainly comprises an incinerator, a quenching tower, a deacidification tower, a chimney and the like, wherein the quenching tower is used for quenching the flue gas by using circulating acid liquor, and the flue gas is discharged after the acid liquor reaches a certain concentration. The patent can completely oxidize and decompose the chlorine-containing organic waste gas, and the pollutant emission meets the national standard. However, this patent process has several drawbacks: (1) Since the standard prescribes that the burning temperature of the chlorine-containing organic matters must be higher than 1200 ℃, the flue gas with such high temperature is directly quenched, not only is huge heat wasted, but also the material requirement on the quenching tower is high, the quenching tower material must have good thermal shock resistance, and the consumption of cooling water is huge after being quenched from 1200 ℃ to 90 ℃. (2) During high-temperature incineration, nitrogen element in the organic matters can generate NO X Thermal NO at 1200 DEG C X May also be generated, which does not take into account NO X Under the condition of increasingly strict environmental protection requirements, the patent smoke emits NO X The concentration is difficult to reach the standard. (3) The patent process flow only arranges a primary quenching tower to absorb HCl in flue gas, the absorption efficiency is poorer and worse along with the increasing concentration of circulating acid liquid, more HCl escapes to a deacidification tower, more alkali liquid is required to be consumed, more neutral salt water is generated, and the subsequent water treatment burden is increased.
Disclosure of Invention
The purpose of the invention is that: aiming at the defects of the prior art, the clean chlorine-containing organic waste gas recycling unit system has the advantages of high hazardous waste incineration rate, high waste heat recovery efficiency, high HCl recovery efficiency, simple process and convenient maintenance.
In order to achieve the above object, the following technical scheme is implemented:
the utility model provides a chlorine-containing organic waste gas environmental protection type resource utilization system, contains adiabatic incinerator, horizontal tobacco pipe exhaust-heat boiler, graphite quench tower, HCl absorption tower, deacidification filler tower, flue gas reheater, SCR denitrification facility, chimney, its characterized in that: the upper part of the heat-insulating incinerator is provided with a combined burner, a waste burner is arranged in the combined burner, auxiliary fuel is directly conveyed to the combined burner, a horizontal smoke tube waste heat boiler is arranged behind the heat-insulating incinerator, and the horizontal boiler is selected for enabling high-temperature flue gas to pass through a heating surface in a tube so as to ensure that the high-temperature flue gas containing HCl does not leak to an outer guard plate of the boiler. A steam drum is arranged above the horizontal smoke tube waste heat boiler, the horizontal smoke tube waste heat boiler and the steam drum form a natural circulation loop, the steam drum is connected with a steam separation cylinder, and softened water injected from the outside sequentially passes through a thermal deaerator and a boiler water supply pump and then enters the steam drum; arranging a graphite quenching tower behind the horizontal smoke tube waste heat boiler, wherein the graphite quenching tower is sequentially connected with a quenching tower circulating pump and a graphite heat exchanger, and acid liquor at the lower part of the graphite quenching tower sequentially passes through the quenching tower circulating pump, the graphite heat exchanger at the lower part of the graphite quenching tower and an atomizing spray gun at the upper part of the quenching tower to return to the lower part of the graphite quenching tower to form a circulating loop, and an acid discharge valve is arranged at the lower part of the graphite quenching tower; a first-stage HCl absorption tower is arranged behind the graphite quenching tower, a desalted water nozzle is arranged at the top end of the HCl absorption tower, a layer of bubble cap is arranged at the lower part of the desalted water nozzle, a packing layer is arranged in the middle of the HCl absorption tower, so that smoke and circulating acid liquor are fully contacted in the packing layer, the installation position of the HCl absorption tower is higher than that of the graphite quenching tower, the acid liquor at the lower part of the HCl absorption tower is pumped to the acid liquor nozzle at the upper part of the HCl absorption tower through the circulating pump of the absorption tower to be sprayed, and the acid liquor falls into the lower part of the absorption tower after passing through the packing layer from top to bottom in the HCl absorption tower to form a closed circulating loop; when the acid liquor is discharged from the quenching tower, the HCl absorption tower supplements the acid liquor into the graphite quenching tower, and meanwhile, the desalted water is supplemented from a desalted water nozzle at the upper part of the HCl absorption tower. Arranging a deacidification filler tower behind the HCl absorption tower, wherein an alkali liquor nozzle is arranged at the upper end of the deacidification filler tower, a demister is further arranged at the top of the deacidification filler tower 5 to remove larger water drops carried in the flue gas, and three filler layers are arranged below the deacidification filler tower from top to bottom, wherein the filler is in the form of pall rings to ensure that alkali liquor and the flue gas are fully contacted; the temperature of the flue gas from the deacidification tower is 60 ℃, a flue gas reheating device is arranged behind the deacidification filling tower in order to reach the proper temperature of the denitration catalyst, the left side of the flue gas reheating device is connected with a flue gas reheating burner, and auxiliary fuel and combustion air are conveyed into the flue gas reheating burner through a pipeline to heat the flue gas; two rows of ammonia nozzles are arranged in a flue behind the flue gas reheating device, an ammonia spraying grid is arranged in the flue behind the ammonia nozzles to promote mixing of ammonia and flue gas, and an SCR denitration device is arranged behind the ammonia spraying grid; and a chimney is arranged behind the SCR denitration device, and a draught fan is arranged on a flue between the SCR denitration device and the chimney.
Preferably, the furnace wall of the heat-insulating incinerator is formed by pouring high-alumina refractory castable with HCl corrosion resistance, so that the service life of the heat-insulating incinerator can be effectively prolonged.
Preferably, the split cylinder is provided with two steam outlet pipelines, one of which is connected with the thermal deaerator, and the other of which is connected with external steam equipment.
The outstanding characteristics of the invention are concentrated on the following technical measures:
(1) The horizontal smoke tube waste heat boiler is arranged behind the adiabatic incinerator, the temperature of the smoke can be reduced to 550 ℃ through thermal calculation and a reasonably designed boiler heating surface, most of heat in the recovered smoke is used for generating steam for plant area self-use or being integrated into a steam pipe network, and secondary pollution caused by dioxin pollutants is effectively avoided. The waste heat boiler adopts a horizontal smoke tube waste heat boiler, so that high-temperature smoke gas is led to pass through the heating surface tube, and the high-temperature smoke gas containing HCl is ensured to be difficult to leak to an outer guard plate of the boiler, so that the boiler is prevented from being corroded by hydrochloric acid. Meanwhile, the arrangement of the waste heat boiler reduces the temperature of the flue gas entering the quenching tower, and the flue gas at 550 ℃ enters the quenching tower, so that the requirement on the wall material of the quenching tower is reduced, and a large amount of cooling water is saved.
(2) A primary HCl absorption tower is arranged behind the quenching tower to further absorb HCl in the flue gas, and an HCl absorption system is optimized. After passing through the quenching tower, the HCl content in the flue gas is reduced greatly, so that a packing layer is arranged in the HCl absorption tower, so that the flue gas and the circulating acid liquor are fully contacted in the packing layer, and the absorption efficiency of HCl is ensured. Because the amount of HCl absorbed by the quenching tower is more than that absorbed by the absorption tower, the circulating acid liquor of the quenching tower can reach the discharge concentration faster than that of the circulating acid liquor of the absorption tower, and when the concentration of the circulating acid liquor of the quenching tower reaches the discharge value and is discharged, the circulating acid liquor of the HCl absorption tower is supplemented to the quenching tower, and fresh water is supplemented to the absorption tower. In short, the HCl absorption system produces acid in the quenching tower and supplements water in the absorption tower, so that the purposes of absorbing high-concentration HCl smoke by high-concentration acid liquor and absorbing low-concentration HCl smoke by low-concentration acid liquor are truly realized, and the HCl absorption efficiency is improved to more than 99%. The heat of the circulating acid liquor is taken away by the circulating cooling water in the graphite heat exchanger, so that the temperature stability of the circulating acid liquor sprayed into the quenching tower is ensured.
(3) A first-stage deacidification tower is arranged behind the HCl absorption tower, and NaOH solution is adopted to neutralize residual HCl and free Cl in the flue gas 2 A NaCl solution was formed. And (3) circulating and spraying the NaOH solution, when the concentration of the circulating alkali liquor is reduced to a set value, opening a valve to discharge the nearly neutral brine to a sewage treatment plant, and then continuously deacidifying the newly-entered NaOH solution.
(4) Most of the organic matters contain nitrogen element, and the nitrogen element is oxidized into NO at high temperature X And in an incinerator at 1200 ℃, thermal NO X The invention is provided with an SCR denitration device for removing NO in the flue gas X The pollutant concentration in the flue gas can completely reach the national emission standard.
The invention has the beneficial effects that: the invention provides an environment-friendly recycling system for chlorine-containing organic waste gas, which overcomes the defects of the traditional chlorine-containing organic waste gas treatment system and ensures that a clean chlorine-containing organic waste gas recycling unit system is simpler, more complete and more reliable. Specifically, the invention relates to an environment-friendly recycling system for chlorine-containing organic waste gas: firstly, the incineration temperature of the incinerator is not lower than 1200 ℃, so that the environmental protection effect of thoroughly incinerating organic components is completely achieved; secondly, the incinerator adopts high-alumina refractory castable, is resistant to corrosion by HCl, and ensures long-term and stable operation of the incinerator. Thirdly, arranging a horizontal smoke tube waste heat boiler to meet the heat energy recovery requirement of chlorine-containing high-temperature smoke; fourth, set up two-stage HCl absorbing device, first level is the quench tower, and the second level is the HCl absorbing tower, makes HCl absorption efficiency improve to more than 99%, and by-product 20% concentration hydrochloric acid has reached the HCl resource utilization purpose. Fifth, the whole system of the invention has no expansion joint, and the thermal expansion is absorbed by the pipe elbow, thereby effectively reducing the leakage point of the system and preventing corrosion of equipment after HCl leakage. Sixth, the system of the invention can be popularized and used in the clean chlorine-containing organic waste liquid resource utilization unit system under specific conditions. In a word, the invention can recycle heat energy to generate steam or hot water while treating waste gas, and can recycle HCl gas in the flue gas to generate hydrochloric acid with the concentration of about 20%, thereby achieving the environmental protection purposes of saving energy, reducing waste emission and recycling.
Drawings
FIG. 1 is a schematic view of the overall structure of the present invention;
fig. 2 is a system flow diagram of the present resource utilization system.
As shown in the figure: 1. the device comprises an adiabatic incinerator, 2 parts of a horizontal smoke tube waste heat boiler, 3 parts of a graphite quenching tower, 4 parts of an HCl absorption tower, 5 parts of a deacidification filler tower, 6 parts of a flue gas reheater, 7 parts of an SCR denitration device, 8 parts of a chimney, 9 parts of a thermal deaerator, 10 parts of a steam drum, 11 parts of a steam drum, 12 parts of a graphite heat exchanger, 13 parts of a waste gas booster fan, 14 parts of a combustion fan, 15 parts of a boiler water supply pump, 16 parts of a quench tower circulating pump, 17 parts of an absorption tower circulating pump, 18 parts of a deacidification tower circulating pump, 19 parts of an induced draft fan, 20 parts of a high-level water tank, 21 parts of a combined burner, 22 parts of a waste gas burner, 23 parts of a bubble cap, 24 parts of an absorption tower filler layer, 25 parts of a demister, 26 parts of a deacidification tower filler layer, 27 parts of a low-temperature denitration catalyst, 28 parts of a flue gas reheater burner, 29 parts of an ammonia-spraying grid, 30 parts of an acid discharge valve.
Detailed Description
The following description of the embodiments of the present invention will be made clearly and fully with reference to the accompanying drawings, in which it is evident that the embodiments described are only some, but not all, of the preferred embodiments of the present invention. All other embodiments, which can be made by those skilled in the art based on the embodiments of the invention without making any inventive effort, are intended to be within the scope of the invention.
The environment-friendly recycling system of the chlorine-containing organic waste gas shown in the figure 1 is a flue gas running process and main equipment from left to right; the process equipment mainly comprises the following steps: the device comprises a heat insulation incinerator 1, a horizontal smoke tube waste heat boiler 2, a graphite quenching tower 3, an HCl absorption tower 4, a deacidification filler tower 5, a smoke reheating device 6, an SCR denitration device 7 and a chimney 8. An environment-friendly recycling system for chlorine-containing organic waste gas is characterized in that a combined burner 21 is arranged at the upper part of the adiabatic incinerator 1, a waste gas burner 22 is arranged in the combined burner 21, and auxiliary fuel is directly conveyed to the combined burner 21. The heat-insulating incinerator 1 is provided with a horizontal smoke tube waste heat boiler 2 which is well sealed at high temperature, a steam drum 10 is arranged above the horizontal smoke tube waste heat boiler 2, the horizontal smoke tube waste heat boiler 2 and the steam drum 10 form a natural circulation loop, the steam drum 10 is connected with a steam separation cylinder 11, and the added softened water sequentially passes through a thermal deaerator 9 and a boiler water supply pump 15 and then enters the steam drum 10; a graphite quenching tower 3 is arranged behind the horizontal smoke tube waste heat boiler 2, the graphite quenching tower 3 is sequentially connected with a quenching tower circulating pump 16 and a graphite heat exchanger 12, the graphite heat exchanger 12 is arranged at the lower part of the graphite quenching tower 3, and the upper half part of the graphite quenching tower 3 is sleeved with a circle of jacket; a primary HCl absorption tower 4 is arranged behind the graphite quenching tower 3, a desalted water nozzle is arranged at the top end of the HCl absorption tower 4, a layer of bubble cap 23 is arranged at the lower part of the desalted water nozzle, and a packing layer 24 is arranged at the middle part of the HCl absorption tower 4; a deacidification filling tower 5 is arranged behind the HCl absorption tower 4, an alkali liquor nozzle is arranged at the top end of the deacidification filling tower 5, a demister is arranged below the nozzle, and three filling layers are arranged below the demister from top to bottom; a flue gas reheating device 6 is arranged behind the deacidification packing tower 5, the left side of the flue gas reheating device 6 is connected with a flue gas reheating burner 28, and auxiliary fuel and combustion air are conveyed into the flue gas reheating burner 28 through a pipeline; an ammonia gas nozzle is arranged in a flue behind the flue gas reheating device 6, an ammonia spraying grid 29 is arranged in the flue behind the ammonia gas nozzle, an SCR denitration device 7 is arranged behind the ammonia spraying grid 29, and a low-temperature denitration catalyst 27 is arranged in the SCR denitration device 7; a chimney 8 is arranged behind the SCR denitration device 7, and a draught fan 19 is arranged between the SCR denitration device 7 and the chimney 8.
FIG. 2 is a schematic view of the working flow of the present invention, and in conjunction with the flow, an environment-friendly recycling system for chlorine-containing organic waste gas is further described, wherein a combined burner 21 is arranged at the upper part of the adiabatic incinerator 1, auxiliary fuel is delivered to the combined burner 21, combustion air is delivered to the combined burner 21 by a combustion-supporting fan 14, clean chlorine-containing organic waste gas is delivered to a waste gas burner 22 by a booster fan 13, the auxiliary fuel is continuously combusted in the air, so that the temperature in the incinerator is not lower than 1200 ℃, and the chlorine-containing organic matters in the waste gas react with oxygen to generate oxidative decomposition to generate CO 2 、H 2 O、NO X HCl and small amounts of free Cl 2 . The adiabatic incinerator 1 is formed by casting a high alumina refractory castable material on the fire side furnace wall, and does not react with HCl in flue gas.
The high-temperature flue gas enters a horizontal smoke tube waste heat boiler 2 from an outlet of the adiabatic incinerator 1, and exchanges heat with boiler water in the waste heat boiler. And in the other direction, the softened water enters a thermal deaerator 9, the temperature is raised to 104 ℃ after deaeration by low-pressure steam, the softened water is conveyed to a steam drum 10 by a boiler water supply pump, and the steam drum 10 and a waste heat boiler body form a circulation loop to exchange heat with high-temperature flue gas to generate saturated steam. Saturated steam enters a branch cylinder 11, two steam outlet pipelines are arranged on the branch cylinder 11, one steam outlet pipeline is connected with the thermal deaerator 9, and the other steam outlet pipeline is connected with external steam equipment.
The temperature of the flue gas after the flue gas comes out of the horizontal flue pipe waste heat boiler 2 is 550 ℃, then the flue gas enters the graphite quenching tower 3, the flue gas contacts with the sprayed circulating acid liquor in the graphite quenching tower 3 for heat exchange, and the temperature of the flue gas is reduced from 550 ℃ to 60 ℃ and the HCl is absorbed in a very short time. And after the circulating acid liquor is cooled by the quench tower circulating pump 16 and the graphite heat exchanger 12 in sequence, the heat of the circulating acid liquor is sprayed into the graphite quench tower 3 again for circulation, and the heat of the circulating acid liquor is absorbed and taken away by the circulating cooling water in the graphite heat exchanger 12.
The flue gas exiting the graphite quench tower 3 was at 60 c and then entered the HCl absorber tower 4. The packing layer 24 is arranged in the HCl absorption tower 4, acid liquor at the lower part of the HCl absorption tower 4 is sent to the upper part of the packing layer 24 by the absorption tower circulating pump 17 and sprayed, and flue gas moves in the packing layer 24 in opposite directions with the circulating acid liquor, so that the flue gas is fully contacted and HCl in the flue gas is further absorbed. After the timing measurement value of the circulating acid liquor in the graphite quench tower 3 reaches 20% concentration, the circulating acid liquor at the bottom of the quench tower is discharged from an acid discharge valve 30 to the outside of the boundary region for treatment, then the acid liquor at the lower part of the HCl absorption tower 4 is supplemented to the lower part of the graphite quench tower 3, meanwhile, fresh desalted water is supplemented to a bubble cap 23 at the upper part of the HCl absorption tower 4, and the desalted water falls into a packing layer 24 after being uniformly distributed by the bubble cap 23.
The flue gas enters the deacidification filling tower 5 after coming out of the HCl absorption tower 4, naOH solution at the bottom of the deacidification filling tower 5 is conveyed to the upper part of the deacidification filling tower filling layer 26 by the deacidification tower circulating pump 17 to be sprayed, three layers of deacidification filling tower filling layers 26 are arranged in the deacidification filling tower 5, the flue gas is ensured to be fully contacted with circulating alkali liquor, and HCl and Cl in the flue gas are ensured to be fully contacted 2 And (5) neutralizing. After circulation for a period of time, the alkali liquor gradually becomes neutral brine, the absorption efficiency is greatly reduced, at the moment, the bottom valve of the deacidification filling tower 5 is opened to discharge the neutral brine, and new NaOH solution is added again to continue circulation. The flue gas from the deacidification packing tower 5 carries a lot of moisture, and a layer of demister 25 is arranged at the top of the deacidification packing tower 5 and is used for removing larger liquid drops carried in the flue gas.
The flue gas enters a flue gas reheater 6 after coming out of the deacidification packing tower 5, and auxiliary fuel and combustion air are conveyed into a flue gas reheater burner 28 for combustion through pipelines, so that the temperature of the flue gas is heated from 60 ℃ to 220 ℃.
The flue gas coming out of the flue gas reheater 6 is led into the SCR denitration device 7 through a pipeline, an ammonia nozzle is arranged in a flue in front of the SCR denitration device 7, and an ammonia spraying grid 29 is arranged behind the ammonia nozzle for fully mixing the flue gas and the ammonia. The mixed flue gas enters an SCR denitration device 7 and is subjected to low-temperature denitration catalyst27, NO in the flue gas is removed by the action of the catalyst X Reduction to N 2 And H 2 O。
HCl and Cl in flue gas discharged from SCR denitration device 7 2 、NO X The concentration of the atmospheric pollutants meets the national standard, and finally the pollutants are led out by a draught fan 19 and then sent into a chimney 8 to be discharged into the atmosphere.
The invention not only carries out harmless, reduction and waste recycling treatment on the chlorine-containing organic waste gas, but also recovers the heat energy generated by incineration of the waste gas, and the recovered hydrochloric acid with 20 percent concentration can be used as an industrial product, thereby realizing the requirements of environmental protection, energy saving and resource utilization of the chlorine-containing organic waste gas, saving energy and protecting the atmosphere environment.
Although embodiments of the present invention have been shown and described, it will be understood by those skilled in the art that various changes, modifications, substitutions and alterations can be made therein without departing from the principles and spirit of the invention, the scope of which is defined in the appended claims and their equivalents.
Claims (6)
1. The utility model provides a chlorine-containing organic waste gas environmental protection type resource utilization system, contains adiabatic incinerator (1), horizontal tobacco pipe exhaust-heat boiler (2), graphite quench tower (3), HCl absorption tower (4), deacidification filler tower (5), flue gas reheater (6), SCR denitrification facility (7), chimney (8), its characterized in that: a horizontal smoke tube waste heat boiler (2) is arranged behind the heat insulation incinerator (1), a horizontal smoke tube waste heat boiler (2) which is well sealed at a high temperature is selected, and a steam drum (10) is connected above the horizontal smoke tube waste heat boiler (2);
a graphite quenching tower (3) is arranged behind the horizontal smoke tube waste heat boiler (2), the graphite quenching tower (3) is sequentially connected with a quenching tower circulating pump (16) and a graphite heat exchanger (12), the graphite heat exchanger (12) is arranged at the lower part of the graphite quenching tower (3), and a circle of jacket is sleeved outside the inner wall of the upper part of the graphite quenching tower (3); a primary HCl absorption tower (4) is arranged behind the graphite quenching tower (3), a desalted water nozzle is arranged on the inner wall of the top end of the HCl absorption tower (4), a layer of bubble cap (23) is arranged on the lower part of the desalted water nozzle, and a packing layer is arranged in the middle of the HCl absorption tower (4); a deacidification filling tower (5) is arranged behind the HCl absorption tower (4), an alkali liquor nozzle is arranged at the top end of the deacidification filling tower (5), a demister is further arranged below the nozzle, and three filling layers are arranged below the demister from top to bottom; a flue gas reheating device (6) is arranged behind the deacidification filling tower (5), the left side of the flue gas reheating device (6) is connected with a flue gas reheating burner (28), and auxiliary fuel and combustion air are conveyed into the flue gas reheating burner (28) through a pipeline; two rows of ammonia gas spray holes are arranged in a flue behind the flue gas reheating device (6), an ammonia injection grid (29) is arranged in the flue behind the ammonia gas spray holes, an SCR denitration device (7) is arranged behind the ammonia injection grid (29), and a proper amount of low-temperature denitration catalyst is arranged in the SCR denitration device (7); a chimney (8) is arranged behind the SCR denitration device (7), and a draught fan (19) is arranged on a flue between the two devices; the acid liquor at the lower part of the graphite quenching tower (3) sequentially passes through a quenching tower circulating pump (16), a graphite heat exchanger (12) and an atomization spray gun at the upper part of the quenching tower, and returns to the lower part of the graphite quenching tower (3) to form a circulating loop; the graphite heat exchanger (12) is arranged at the lower part of the graphite quenching tower (3); an acid discharge valve is arranged at the lower part of the graphite quenching tower (3);
the installation position of the HCl absorption tower (4) is higher than that of the graphite quenching tower (3), acid liquor at the lower part of the HCl absorption tower (4) is sent to an acid liquor nozzle at the upper part of the HCl absorption tower (4) through an absorption tower circulating pump (17) to be sprayed, and the acid liquor falls into the lower part of the absorption tower from top to bottom through a packing layer (24) in the HCl absorption tower (4) to form a closed circulating loop;
an acid discharge pipeline is connected between the HCl absorption tower (4) and the graphite quenching tower (3), and a desalted water nozzle is arranged at the upper part of the HCl absorption tower (4).
2. The environment-friendly recycling system for chlorine-containing organic waste gas according to claim 1, which is characterized in that: the upper part of the heat-insulating incinerator (1) is provided with a combined burner (21), an exhaust gas burner (22) is arranged in the combined burner (21), and auxiliary fuel is directly conveyed to the combined burner (21).
3. The environment-friendly recycling system for chlorine-containing organic waste gas according to claim 1, which is characterized in that: the furnace wall of the heat-insulating incinerator (1) is formed by pouring high-alumina refractory castable with HCl corrosion resistance.
4. The environment-friendly recycling system for chlorine-containing organic waste gas according to claim 1, which is characterized in that: the horizontal smoke tube waste heat boiler (2) and the steam drum (10) form a natural circulation loop, a steam separation cylinder (11) is connected to the outer side of the steam drum (10), and softened water injected from the outside of the system sequentially passes through the thermal deaerator (9) and the boiler water supply pump (15) and then enters the steam drum (10).
5. The environment-friendly recycling system for chlorine-containing organic waste gas according to claim 4, wherein the recycling system is characterized in that: two steam outlet pipelines are arranged on the steam dividing cylinder (11), one of the steam outlet pipelines is connected with the thermal deaerator (9), and the other steam outlet pipeline is connected with external steam equipment.
6. The environment-friendly recycling system for chlorine-containing organic waste gas according to claim 4, wherein the recycling system is characterized in that: the thermal deaerator (9) can deoxidize softened water by low-pressure steam.
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| CN111947167A (en) * | 2019-05-16 | 2020-11-17 | 黄锐 | Combined treatment system and process method for nitrogen-containing waste gas and waste liquid of ethylene glycol device |
| CN110732547A (en) * | 2019-11-14 | 2020-01-31 | 中冶南方都市环保工程技术股份有限公司 | Resource utilization method and system for waste incineration fly ash |
| CN111219722A (en) * | 2020-03-02 | 2020-06-02 | 广西金源生物化工实业有限公司 | A pressurization burner for low pressure waste gas |
| CN112628772B (en) * | 2020-10-19 | 2022-08-05 | 湖北兴瑞硅材料有限公司 | Process for burning waste gas generated in production of methyl chlorosilane |
| CN113041837A (en) * | 2021-03-08 | 2021-06-29 | 聊城氟尔新材料科技有限公司 | Process for denitration of flue gas generated after incineration of fluorine-containing waste liquid of fluorine material |
| CN113058404A (en) * | 2021-04-27 | 2021-07-02 | 天津辰创环境工程科技有限责任公司 | System and method for treating waste gas/liquid with high phosphorus content, chlorine content and sulfur content |
| CN113483348A (en) * | 2021-05-28 | 2021-10-08 | 光大绿色环保管理（深圳）有限公司 | Hazardous waste incineration flue gas treatment device and method |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1632379A (en) * | 2004-12-24 | 2005-06-29 | 哈尔滨工业大学 | Double temperature double bed gasification, oxidization and fluidized bed incinerator for disposing high concentration organic effluent liquor |
| CN101634453A (en) * | 2009-08-31 | 2010-01-27 | 北京航天动力研究所 | Quenching process and quenching device of incineration smoke of waste liquid and waste gas containing chlorine |
| CN103133067A (en) * | 2013-03-15 | 2013-06-05 | 南京凯盛开能环保能源有限公司 | Steel-mill residual blast-furnace gas and residual saturated steam comprehensive utilization power generation system |
| CN203784966U (en) * | 2014-04-08 | 2014-08-20 | 大连科林能源工程技术开发有限公司 | High concentration saliferous organic waste liquid recovery chemical intermediate and waste heat using boiler system |
| CN107120657A (en) * | 2017-06-11 | 2017-09-01 | 无锡绿麦环保科技有限公司 | Solid waste incineration system and its technique |
-
2018
- 2018-10-30 CN CN201811278560.8A patent/CN109297037B/en active Active
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1632379A (en) * | 2004-12-24 | 2005-06-29 | 哈尔滨工业大学 | Double temperature double bed gasification, oxidization and fluidized bed incinerator for disposing high concentration organic effluent liquor |
| CN101634453A (en) * | 2009-08-31 | 2010-01-27 | 北京航天动力研究所 | Quenching process and quenching device of incineration smoke of waste liquid and waste gas containing chlorine |
| CN103133067A (en) * | 2013-03-15 | 2013-06-05 | 南京凯盛开能环保能源有限公司 | Steel-mill residual blast-furnace gas and residual saturated steam comprehensive utilization power generation system |
| CN203784966U (en) * | 2014-04-08 | 2014-08-20 | 大连科林能源工程技术开发有限公司 | High concentration saliferous organic waste liquid recovery chemical intermediate and waste heat using boiler system |
| CN107120657A (en) * | 2017-06-11 | 2017-09-01 | 无锡绿麦环保科技有限公司 | Solid waste incineration system and its technique |
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