CN114772830A - Treatment method and system for ammonia desulphurization waste liquid - Google Patents
Treatment method and system for ammonia desulphurization waste liquid Download PDFInfo
- Publication number
- CN114772830A CN114772830A CN202210473764.7A CN202210473764A CN114772830A CN 114772830 A CN114772830 A CN 114772830A CN 202210473764 A CN202210473764 A CN 202210473764A CN 114772830 A CN114772830 A CN 114772830A
- Authority
- CN
- China
- Prior art keywords
- waste liquid
- water
- tail gas
- pipe
- collecting channel
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Pending
Links
- 239000007788 liquid Substances 0.000 title claims abstract description 93
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 title claims abstract description 71
- 239000002699 waste material Substances 0.000 title claims abstract description 67
- 238000000034 method Methods 0.000 title claims abstract description 37
- 229910021529 ammonia Inorganic materials 0.000 title claims abstract description 29
- 238000009833 condensation Methods 0.000 claims abstract description 99
- 230000005494 condensation Effects 0.000 claims abstract description 99
- 238000006477 desulfuration reaction Methods 0.000 claims abstract description 77
- 230000023556 desulfurization Effects 0.000 claims abstract description 77
- SOIFLUNRINLCBN-UHFFFAOYSA-N ammonium thiocyanate Chemical compound [NH4+].[S-]C#N SOIFLUNRINLCBN-UHFFFAOYSA-N 0.000 claims abstract description 36
- 238000007254 oxidation reaction Methods 0.000 claims abstract description 30
- 230000003647 oxidation Effects 0.000 claims abstract description 29
- BFNBIHQBYMNNAN-UHFFFAOYSA-N ammonium sulfate Chemical compound N.N.OS(O)(=O)=O BFNBIHQBYMNNAN-UHFFFAOYSA-N 0.000 claims abstract description 26
- 229910052921 ammonium sulfate Inorganic materials 0.000 claims abstract description 26
- 235000011130 ammonium sulphate Nutrition 0.000 claims abstract description 26
- VHUUQVKOLVNVRT-UHFFFAOYSA-N Ammonium hydroxide Chemical compound [NH4+].[OH-] VHUUQVKOLVNVRT-UHFFFAOYSA-N 0.000 claims abstract description 21
- 235000011114 ammonium hydroxide Nutrition 0.000 claims abstract description 21
- 238000000926 separation method Methods 0.000 claims abstract description 18
- 238000007738 vacuum evaporation Methods 0.000 claims abstract description 18
- XYXNTHIYBIDHGM-UHFFFAOYSA-N ammonium thiosulfate Chemical compound [NH4+].[NH4+].[O-]S([O-])(=O)=S XYXNTHIYBIDHGM-UHFFFAOYSA-N 0.000 claims abstract description 17
- 239000013078 crystal Substances 0.000 claims abstract description 16
- 230000003197 catalytic effect Effects 0.000 claims abstract description 13
- 238000005406 washing Methods 0.000 claims abstract description 13
- 238000002425 crystallisation Methods 0.000 claims abstract description 12
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 claims abstract description 10
- 230000008025 crystallization Effects 0.000 claims abstract description 10
- 229910052717 sulfur Inorganic materials 0.000 claims abstract description 9
- 239000011593 sulfur Substances 0.000 claims abstract description 9
- 239000000706 filtrate Substances 0.000 claims abstract description 7
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 127
- 238000011084 recovery Methods 0.000 claims description 35
- 239000000945 filler Substances 0.000 claims description 20
- 238000005507 spraying Methods 0.000 claims description 20
- 239000007921 spray Substances 0.000 claims description 18
- 230000008569 process Effects 0.000 claims description 12
- 230000004087 circulation Effects 0.000 claims description 11
- 230000007246 mechanism Effects 0.000 claims description 11
- 230000000149 penetrating effect Effects 0.000 claims description 6
- 239000003054 catalyst Substances 0.000 claims description 5
- 238000000605 extraction Methods 0.000 claims description 5
- 238000004891 communication Methods 0.000 claims description 4
- 230000002829 reductive effect Effects 0.000 claims description 3
- 238000004042 decolorization Methods 0.000 claims description 2
- 238000001291 vacuum drying Methods 0.000 claims description 2
- 238000004064 recycling Methods 0.000 claims 2
- 238000007599 discharging Methods 0.000 claims 1
- 238000012545 processing Methods 0.000 abstract description 10
- 238000001035 drying Methods 0.000 abstract description 5
- 230000008859 change Effects 0.000 abstract description 2
- 239000007789 gas Substances 0.000 description 93
- 239000000047 product Substances 0.000 description 14
- 230000000694 effects Effects 0.000 description 13
- 150000003839 salts Chemical group 0.000 description 11
- 239000000126 substance Substances 0.000 description 11
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical group [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 6
- 230000008901 benefit Effects 0.000 description 6
- 239000000571 coke Substances 0.000 description 6
- 238000004939 coking Methods 0.000 description 6
- 239000003245 coal Substances 0.000 description 5
- 238000012856 packing Methods 0.000 description 5
- 238000001704 evaporation Methods 0.000 description 4
- 238000001816 cooling Methods 0.000 description 3
- 238000003912 environmental pollution Methods 0.000 description 3
- 230000008020 evaporation Effects 0.000 description 3
- 238000004519 manufacturing process Methods 0.000 description 3
- 239000003960 organic solvent Substances 0.000 description 3
- 239000002351 wastewater Substances 0.000 description 3
- GWEVSGVZZGPLCZ-UHFFFAOYSA-N Titan oxide Chemical group O=[Ti]=O GWEVSGVZZGPLCZ-UHFFFAOYSA-N 0.000 description 2
- 239000003513 alkali Substances 0.000 description 2
- 230000009286 beneficial effect Effects 0.000 description 2
- 230000002354 daily effect Effects 0.000 description 2
- 238000007255 decyanation reaction Methods 0.000 description 2
- 238000004134 energy conservation Methods 0.000 description 2
- 239000000284 extract Substances 0.000 description 2
- 230000002147 killing effect Effects 0.000 description 2
- 238000002156 mixing Methods 0.000 description 2
- 238000004806 packaging method and process Methods 0.000 description 2
- 230000009467 reduction Effects 0.000 description 2
- 238000011160 research Methods 0.000 description 2
- 238000001179 sorption measurement Methods 0.000 description 2
- 239000004575 stone Substances 0.000 description 2
- 239000005864 Sulphur Substances 0.000 description 1
- 238000004458 analytical method Methods 0.000 description 1
- 239000003034 coal gas Substances 0.000 description 1
- MPMSMUBQXQALQI-UHFFFAOYSA-N cobalt phthalocyanine Chemical compound [Co+2].C12=CC=CC=C2C(N=C2[N-]C(C3=CC=CC=C32)=N2)=NC1=NC([C]1C=CC=CC1=1)=NC=1N=C1[C]3C=CC=CC3=C2[N-]1 MPMSMUBQXQALQI-UHFFFAOYSA-N 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000004821 distillation Methods 0.000 description 1
- 238000000909 electrodialysis Methods 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 230000003203 everyday effect Effects 0.000 description 1
- 239000002360 explosive Substances 0.000 description 1
- 238000001640 fractional crystallisation Methods 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 238000009776 industrial production Methods 0.000 description 1
- 150000002500 ions Chemical class 0.000 description 1
- 230000000670 limiting effect Effects 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000036961 partial effect Effects 0.000 description 1
- 239000002245 particle Substances 0.000 description 1
- 239000012466 permeate Substances 0.000 description 1
- 238000011112 process operation Methods 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 230000000717 retained effect Effects 0.000 description 1
- 238000007086 side reaction Methods 0.000 description 1
- 239000002904 solvent Substances 0.000 description 1
- 238000000638 solvent extraction Methods 0.000 description 1
- 238000003860 storage Methods 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
- 239000004408 titanium dioxide Substances 0.000 description 1
- 239000002912 waste gas Substances 0.000 description 1
Images
Classifications
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F9/00—Multistage treatment of water, waste water or sewage
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D5/00—Condensation of vapours; Recovering volatile solvents by condensation
- B01D5/0033—Other features
- B01D5/0036—Multiple-effect condensation; Fractional condensation
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D5/00—Condensation of vapours; Recovering volatile solvents by condensation
- B01D5/0078—Condensation of vapours; Recovering volatile solvents by condensation characterised by auxiliary systems or arrangements
- B01D5/009—Collecting, removing and/or treatment of the condensate
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D5/00—Condensation of vapours; Recovering volatile solvents by condensation
- B01D5/0078—Condensation of vapours; Recovering volatile solvents by condensation characterised by auxiliary systems or arrangements
- B01D5/0093—Removing and treatment of non condensable 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
- B01D53/002—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 condensation
-
- 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
- B01D53/02—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 adsorption, e.g. preparative gas chromatography
- B01D53/04—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 adsorption, e.g. preparative gas chromatography with stationary adsorbents
-
- 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
- B01D2257/00—Components to be removed
- B01D2257/40—Nitrogen compounds
- B01D2257/406—Ammonia
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/02—Treatment of water, waste water, or sewage by heating
- C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/28—Treatment of water, waste water, or sewage by sorption
- C02F1/283—Treatment of water, waste water, or sewage by sorption using coal, charred products, or inorganic mixtures containing them
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/38—Treatment of water, waste water, or sewage by centrifugal separation
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/72—Treatment of water, waste water, or sewage by oxidation
- C02F1/725—Treatment of water, waste water, or sewage by oxidation by catalytic oxidation
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/72—Treatment of water, waste water, or sewage by oxidation
- C02F1/74—Treatment of water, waste water, or sewage by oxidation with air
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2103/00—Nature of the water, waste water, sewage or sludge to be treated
- C02F2103/18—Nature of the water, waste water, sewage or sludge to be treated from the purification of gaseous effluents
Landscapes
- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Engineering & Computer Science (AREA)
- Analytical Chemistry (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Life Sciences & Earth Sciences (AREA)
- Hydrology & Water Resources (AREA)
- Environmental & Geological Engineering (AREA)
- Water Supply & Treatment (AREA)
- Organic Chemistry (AREA)
- Treating Waste Gases (AREA)
Abstract
The invention discloses a method and a system for treating ammonia desulphurization waste liquid, which belong to the field of desulphurization waste liquid treatment, and comprise the following steps: s1: carry out catalytic oxidation with the desulfurization waste liquid, change the ammonium thiosulfate in the desulfurization waste liquid into ammonium sulfate, carry out condensation washing processing, S2 through tail gas treatment system to oxidation kettle exhaust tail gas: and (3) decolorizing the desulfurization waste liquid after catalytic oxidation, carrying out solid-liquid separation to separate out sulfur, and S3: and (3) carrying out vacuum evaporation on the desulfurization waste liquid, and drying to obtain ammonium sulfate, wherein S4: and (4) allowing the filtrate subjected to solid-liquid separation in the step S3 to enter a crystallization kettle to obtain ammonium thiocyanate crystal liquid, performing solid-liquid separation on the ammonium thiocyanate crystal liquid, and drying the separated ammonium thiocyanate crystals to obtain the ammonium thiocyanate. The method and the system for treating the ammonia desulphurization waste liquid treat the tail gas generated by catalytic oxidation, namely recycle ammonia water and ensure that the treated tail gas reaches the standard and is discharged.
Description
Technical Field
The invention belongs to the field of desulfurization waste liquid treatment, and particularly relates to a method and a system for treating ammonia desulfurization waste liquid.
Background
The desulfurization process with ammonia is generally applied to the desulfurization of coke oven gas in the coking industry in recent years. The process adopts ammonia carried in coal gas as an alkali source, adopts phthalocyanine cobalt (PDS) compounds as main components as a desulfurization and decyanation catalyst, has the advantages of low desulfurization operation cost, low investment, simple process operation, high desulfurization and decyanation efficiency, does not need an additional alkali source, is a desulfurization process commonly adopted in the coking industry at present, and achieves better effect by adopting the method for desulfurization by more than two hundred enterprises in China according to incomplete statistics.
However, the desulfurization process generates and accumulates secondary salts such as ammonium thiocyanate, ammonium thiosulfate, ammonium sulfate, etc. due to side reactions. When the content of the secondary salt in the desulfurization solution exceeds 250g/L, the desulfurization effect is affected, the energy consumption is increased, the desulfurization efficiency is reduced, and the desulfurization efficiency is poorer as the content of the secondary salt is higher. In order to ensure the desulfurization efficiency, a part of the desulfurization solution has to be discharged and a part of new desulfurization solution is supplemented to reduce the content of secondary salts in the desulfurization system. A coke oven gas desulfurization system for producing 100 million tons of coke annually needs to discharge more than 50m3 of desulfurization solution every day, so that the content of secondary salt in the desulfurization solution is basically ensured to be not more than 250 g/L. At present, most coking plants in China adopt a coal blending incineration method to treat desulfurization waste liquid, namely desulfurization waste liquid is blended with coal and sent into a coke oven, but the method has the problems that the calorific value of the coal is reduced, a large amount of harmful gas is generated after incineration, coke oven equipment is corroded, and meanwhile, the operation environment is extremely poor in the coal conveying process due to the fact that ammonia and other substances in the waste water have large odor. In addition, the desulfurization wastewater cannot be completely retained in the coal blending process, nearly half of the desulfurization wastewater can permeate to the ground surface, so that the ground and underground pollution is caused, and serious secondary pollution is generated.
From another aspect, these substances are also high value-added chemical products. Therefore, products with high added values are recovered from the discharged desulfurization solution, so that the secondary salt in the desulfurization system can be balanced, the desulfurization efficiency is ensured, the environmental pollution can be eliminated, certain economic benefit can be generated, and the method is a feasible method for treating the discharged desulfurization solution.
At present, some research works are carried out at home and abroad for treating the desulfurization waste liquid. The recovery of ammonium thiocyanate from a desulfurization waste liquid is considered extremely difficult in japanese patent because ammonium thiosulfate and ammonium thiocyanate are both very soluble in water with little difference in solubility, and separation by difference in solubility is impossible, so that japanese patent proposes an electrodialysis method, which can produce ammonium thiocyanate, but cannot achieve industrial production due to complicated treatment process, high equipment cost, and large power consumption.
At present, a few domestic coking plants adopt a gradient crystallization salt extraction method, ammonia evaporation is carried out on desulfurization waste liquid, and fractional crystallization salt extraction is carried out by heating and concentrating according to different solubilities, so that three salts of ammonium thiocyanate, ammonium thiosulfate and ammonium sulfate can be extracted. But because the solubility difference between ammonium thiosulfate and ammonium thiocyanate is very small, the purity of salt extraction is very low, and the content is 50-70%. High investment and complex operation. In particular, the proposed ammonium thiosulfate has a large amount and low purity, is not commercially consumed, and is essentially useless waste, so that the method still does not solve the pollution problem, and is not feasible.
Another method is solvent extraction, which extracts ammonium sulfate, ammonium thiosulfate and ammonium thiocyanate by extracting the desulfurization waste liquid with an organic chemical solvent, and primarily separates them to obtain the purity of 90-95%. The method has obvious defects that firstly, organic solvent is used for extraction, the cost is high, the pollution caused in the distillation process of the extracted solution is serious because the extracted solution contains the organic solvent, and the waste gas emission cannot reach the standard and still needs to be subjected to secondary treatment; secondly, the organic solvent is flammable and explosive, government control is very strict, and transportation and storage have huge hidden dangers; thirdly, the purity of the extracted chemical raw materials is not high and can not reach the lowest national standard, and the market sale price is low.
According to the characteristics of the desulfurization waste liquid of a coke-oven plant, the key problems of recovery and treatment of the desulfurization waste liquid can be easily seen by integrating the research results at home and abroad, firstly, the solubility of ammonium thiocyanate and ammonium thiosulfate is similar, and the ammonium thiocyanate and the ammonium thiosulfate are difficult to separate, and the purity of the separated secondary salt is low, so that the requirement of the market can not be met; secondly, a large amount of ammonium thiosulfate is extracted from the desulfurization waste liquid without market demand.
And the existing desulfurization waste liquid treatment can generate tail gas, and direct ash influences the environment.
Disclosure of Invention
The invention aims to provide a method and a system for treating ammonia desulphurization waste liquid, which completely convert ammonium thiosulfate in the desulphurization waste liquid into ammonium sulfate by a catalytic oxidation method, and extract high-quality ammonium thiocyanate and ammonium sulfate by an evaporation crystallization method, thereby completely solving two key problems in the treatment of the coke oven gas desulphurization waste liquid, and treating the tail gas generated by catalytic oxidation, namely recovering ammonia water and enabling the treated tail gas to reach the standard for emission.
In order to achieve the purpose, the invention adopts the following technical scheme:
the invention provides a method for treating ammonia desulphurization waste liquid, which comprises the following steps: s1: send into the reation kettle with the desulfurization waste liquid, carry out catalytic oxidation under the circumstances of adding catalyst and air, change the ammonium thiosulfate in the desulfurization waste liquid into ammonium sulfate, carry out condensation washing processing through tail gas treatment system to reation kettle exhaust tail gas, will press from both sides the tail gas condensation that has the ammonia and become the aqueous ammonia, return desulfurization system, tail gas after the condensation is washed and is absorbed the discharge up to standard, S2: carrying out decolorization treatment on the desulfurization waste liquid after catalytic oxidation, carrying out solid-liquid separation on the decolorized desulfurization waste liquid, and separating out sulfur, wherein S3: carry out vacuum evaporation to the desulfurization waste liquid of isolating sulphur, the cooling is appeared the ammonium sulfate crystallization, carries out solid-liquid separation under the constant temperature state, and the ammonium sulfate crystallization drying that will separate obtains the ammonium sulfate, and the steam of vacuum evaporation process is recycled to tail gas processing system as the washing water after condensing into water, S4: and (4) enabling the filtrate subjected to solid-liquid separation in the step S3 to enter a crystallization kettle to obtain an ammonium thiocyanate crystal liquid, carrying out solid-liquid separation on the ammonium thiocyanate crystal liquid, returning the separated filtrate to the step S3 to continue vacuum evaporation, and drying the separated ammonium thiocyanate crystals to obtain the ammonium thiocyanate.
The invention also provides an ammonia desulphurization waste liquid treatment system for realizing the ammonia desulphurization waste liquid treatment method, which comprises an oxidation kettle, a decoloration tower, a first centrifugal separator, a vacuum evaporation kettle, a second centrifugal separator, a crystallization kettle and a third centrifugal separator which are sequentially connected, wherein a tail gas discharge port of the oxidation kettle is connected with the tail gas treatment system, a steam outlet of the oxidation kettle is connected with a condenser, a condensed water outlet of the condenser is connected with the tail gas treatment system, and a liquid outlet of the third centrifugal separator is connected with the vacuum evaporation kettle through a first return pipe.
Preferably, the tail gas treatment system comprises a treatment tower, a recovery tower, a first gas pipe, a second gas pipe, a gas pump, a first condensation body, a connecting pipe, a second condensation body and a spraying mechanism, wherein the first condensation body is fixed below the inside of the treatment tower, a first water collecting channel penetrating through the left side wall and the right side wall of the first condensation body is arranged inside the first condensation body, the first water collecting channel is communicated with the recovery tower, a first cavity for containing the condensation body is formed in the upper wall of the first condensation body, a plurality of first gas holes for gas to pass through are formed in the first condensation body, the first gas holes are not communicated with the first water collecting channel and the first cavity, the second condensation body is fixed below the inside of the treatment tower, is positioned above the first condensation body and is communicated with the first condensation body through the connecting pipe, a second water collecting channel penetrating through the left side wall of the second condensation body is formed inside the second condensation body, the second water collecting channel is communicated with the recovery tower, the communicating position is located above the communicating position of the first water collecting channel and the recovery tower, a second cavity used for containing condensate is formed in the upper wall of the second condensate body, a plurality of second air holes used for gas to pass through are formed in the second condensate body, the second air holes and the second water collecting channel are not communicated, the top of the recovery tower is fixedly provided with an air extracting pump, the air extracting pump is communicated with a first air pipe, the air inlet end of the first air pipe extends to the upper portion inside the recovery tower, the air outlet end of the first air pipe is fixedly communicated with the bottom of the treatment tower, one end of the second air pipe is communicated with a tail gas discharge port of the oxidation kettle, the other end of the second air pipe penetrates through the bottom walls of the recovery tower and the first condensate body to be communicated with the first water collecting channel, the spraying end of the spraying mechanism extends to the upper portion inside the treatment tower, and is located above the second condensate body.
Preferably, the first water collecting channel and the second water collecting channel are both in a spherical segment shape, the spherical center of the first water collecting channel is positioned below the first water collecting channel, and the spherical center of the second water collecting channel is positioned above the second water collecting channel.
Preferably, the first air hole is filled with a first filler, and the second air hole is filled with a second filler.
Preferably, the space between the first condensate body, the second condensate body and the treatment tower is filled with a third packing.
Preferably, first cavity and second cavity all communicate with two circulating line, and two circulations all are equipped with the circulating pump with circulation tank intercommunication on every circulating line.
Preferably, the recovery tower comprises a first collecting part, a second collecting part and a liquid outlet pipe, the first collecting part is sleeved outside the treatment tower and is communicated with the first water collecting channel, the second collecting part is communicated with the first collecting part and is communicated with the second water collecting channel, and the liquid outlet pipe is arranged at the lower part of the side wall of the second collecting part.
Preferably, the mechanism that sprays includes spray tank, retrieval and utilization pipe, water pump, water pipe and shower head, and spray tank's top is fixed with the water pump, is connected with the water pipe on the water pump, and the bottom of water pipe extends to the inside below of spray tank, and the treatment column is passed to the left end of water pipe, and extends to the fixed intercommunication in inside top of treatment column has a plurality of shower heads, and the fixed intercommunication in upper portion of spray tank right side wall has the retrieval and utilization pipe with the comdenstion water export intercommunication of condenser.
Preferably, the connection point of the connection pipe and the first condensation body is located at the center of the first condensation body, and the connection point of the connection pipe and the second condensation body is located at the center of the second condensation body.
The beneficial effects of the invention are as follows:
1. the tail gas generated by catalytic oxidation is subjected to condensation washing treatment through the arrangement of a tail gas treatment system, so that ammonia water is recovered, and the treated tail gas can reach the standard and be discharged; the whole treatment method adopts closed cycle, all three products are recovered, and no three wastes are discharged.
2. The ammonium thiosulfate which has the solubility similar to that of the ammonium thiocyanate and is difficult to separate is converted into the ammonium sulfate which has the solubility different from that of the ammonium thiocyanate, so that the subsequent separation is convenient. The extracted product comprises ammonium sulfate, ammonium thiocyanate and sulfur, the quality of the product reaches the first-class standard, and the product has good market demand. A large amount of chemical products are extracted from the desulfurization waste liquid, so that the purposes of energy conservation and emission reduction are achieved, the resource is recycled, higher economic benefit is brought to enterprises, waste is changed into valuable, and the aim of killing two birds with one stone is fulfilled.
3. The process is simple, novel, reliable, advanced and practical, solves the problem of environmental pollution of the desulfurization waste liquid of coking enterprises, and saves water.
4. Through the arrangement of the tail gas treatment system and the connection with the condenser, the tail gas treatment system can realize the condensation and washing of the tail gas, and the tail gas treatment effect is good; and the condensed water of the condenser is recycled, so that resources are saved.
5. The arrangement of the first condensing body and the second condensing body is adopted, so that double condensation is performed, and the recovery rate of ammonia water is ensured; the effect of slowing is also achieved, the problem that the spraying is incomplete due to the fact that the tail gas enters the upper part of the treatment tower at a high speed is solved, and the spraying and washing treatment effect is improved; and the second condensation body and the first condensation body that distribute from top to bottom and set up can effectively separate the aqueous ammonia after the condensation and the tail gas after the condensation, and the aqueous ammonia of being convenient for is retrieved, takes out from the processing with tail gas.
6. The arrangement of the first water collecting channel and the second water collecting channel in the spherical segment shape improves the contact area with tail gas, so that the condensation effect is better, and the condensation efficiency is improved. And the centre of sphere of first passageway of catchmenting is located the below of first passageway of catchmenting, and the centre of sphere of second passageway of catchmenting is located the top of second passageway of catchmenting, and this not only makes the aqueous ammonia after first passageway of catchmenting and the condensation of second passageway of catchmenting better discharge, also makes the tail gas after the condensation of second passageway of catchmenting better discharge, improves condensation treatment effect and efficiency.
7. The tail gas treatment effect is further improved through the arrangement of the first filler, the second filler and the third filler, and the tail gas is further slowed.
Drawings
FIG. 1 is a system block diagram of the present invention.
FIG. 2 is a schematic view of the structure of the tail gas treatment system of the present invention.
FIG. 3 is a schematic view of a treatment tower according to the present invention, partially in section.
FIG. 4 is a schematic cross-sectional view of the first condenser, the connecting pipe, and the second condenser according to the present invention.
Fig. 5 is a schematic sectional view along the line a-a in fig. 4.
Fig. 6 is a schematic top view of the first condensate, the circulation pipe, the circulation tank, and the circulation pump according to the present invention.
FIG. 7 is a schematic top view of a recovery column according to the present invention.
Fig. 8 is a schematic front view of the water pipe and the shower head of the present invention.
The symbols in the drawings are: 100-oxidation kettle, 200-decoloration tower, 300-first centrifugal separator, 400-vacuum evaporation kettle, 500-second centrifugal separator, 600-crystallization kettle, 700-third centrifugal separator, 800-first return pipe, 900-tail gas treatment system, 1000-condenser, 1-treatment tower, 2-first gas pipe, 3-second gas pipe, 4-recovery tower, 41-first collection part, 42-second collection part, 43-liquid outlet pipe, 5-air pump, 6-first condensate, 7-connecting pipe, 8-second condensate, 9-spraying mechanism, 91-spraying water tank, 92-recovery pipe, 93-water pump, 94-water pipe, 95-spraying head, 10-first water collecting channel, 11-first cavity, 12-a first air hole, 13-a second water collecting channel, 14-a second cavity, 15-a second air hole, 16-a first filler, 17-a second filler, 18-a third filler, 19-a circulating pipeline, 20-a circulating water tank and 21-a circulating pump.
Detailed Description
The invention will now be further described with reference to the drawings and the detailed description.
Those not described in detail in this specification are within the skill of the art. In the description of the present invention, it is to be understood that the terms "center", "upper", "lower", "front", "rear", "left", "right", "vertical", "horizontal", "top", "bottom", "inner", "outer", "clockwise", "counterclockwise", and the like, indicate orientations or positional relationships based on those shown in the drawings, and are used only for convenience in describing the present invention and for simplicity in description, and do not indicate or imply that the device or element being referred to must have a particular orientation, be constructed in a particular orientation, and be operated, and thus, should not be construed as limiting the present invention. Furthermore, the terms "first," "second," "third," and the like are used solely to distinguish one from another and are not to be construed as indicating or implying relative importance.
The treatment method of the ammonia desulfurization waste liquid provided in the embodiment comprises the following steps:
s1: the desulfurization waste liquid containing ammonium thiosulfate and ammonium thiocyanate is sent into an oxidation kettle 100, catalytic oxidation is carried out under the condition that a catalyst and air are added, and the ammonium thiosulfate in the desulfurization waste liquid is converted into ammonium sulfate. Wherein the catalyst is titanium dioxide particles. The solubility of ammonium thiocyanate and ammonium sulfate are different greatly, and the ammonium thiocyanate and the ammonium sulfate can be separated easily. The tail gas discharged from the oxidation kettle 100 is condensed and washed by the tail gas treatment system 900, the tail gas with ammonia gas is condensed into ammonia water, the ammonia water returns to the desulfurization system, and the condensed tail gas is washed and absorbed and then is discharged after reaching the standard.
S2: the desulfurization waste liquid after catalytic oxidation is decolorized by a decolorizing tower 200, decolorized filler is activated carbon, and the decolorized desulfurization waste liquid is subjected to solid-liquid separation by a first centrifugal separator 300 to separate sulfur (the purity is more than or equal to 97%).
S3: and (3) performing vacuum evaporation on the desulfurization waste liquid from which the sulfur is separated through a vacuum evaporation kettle 400, cooling to separate out ammonium sulfate crystals after evaporation to a certain degree, performing solid-liquid separation through a second centrifugal separator 500 under a constant temperature state, drying the separated ammonium sulfate crystals to obtain ammonium sulfate (the purity is more than or equal to 98.5%), and packaging to obtain a finished product. The steam from the vacuum evaporation process is condensed into water by the condenser 1000 and then recycled to the tail gas treatment system 900 as wash water.
S4: and (3) enabling the filtrate subjected to solid-liquid separation in the step S3 to enter a crystallization kettle 600, evaporating, cooling and crystallizing to obtain ammonium thiocyanate crystal liquid, performing solid-liquid separation on the ammonium thiocyanate crystal liquid by using a third centrifugal separator 700, returning the separated filtrate to the step S3 to continue vacuum evaporation, drying the separated ammonium thiocyanate crystal to obtain ammonium thiocyanate (the purity is more than or equal to 99%), and packaging for sale.
The invention converts the ammonium thiosulfate which has the solubility similar to that of the ammonium thiocyanate and is difficult to separate into the ammonium sulfate which has the solubility different from that of the ammonium thiocyanate, thereby facilitating the subsequent separation. The extracted product comprises ammonium sulfate, ammonium thiocyanate and sulfur, the quality of the product reaches the first-class standard, and the product has good market demand. A large amount of chemical products are extracted from the desulfurization waste liquid, so that the purposes of energy conservation and emission reduction are achieved, the resource is recycled, higher economic benefit is brought to enterprises, waste is changed into valuable, and the aim of killing two birds with one stone is fulfilled. The process is simple, novel, reliable, advanced and practical, solves the problem of environmental pollution of the desulfurization waste liquid of coking enterprises, and saves water. The whole treatment method adopts closed cycle, three products are all recovered, and three wastes are not discharged. And the tail gas that produces catalytic oxidation carries out condensation washing through setting up of tail gas processing system 900 and handles, not only retrieves the aqueous ammonia, and the tail gas after handling can reach emission standard moreover.
And (3) economic benefit analysis:
treating desulfurized waste liquid by 100m in daily3The daily production of ammonium thiocyanate is 10 tons, the production of ammonium sulfate is 15 tons, and the production of sulfur is about 3.5 tons.
The operation cost is as follows:
the product value is as follows:
profit per day: 67750 ion 23000 (44750 yuan).
Therefore, the desulfurization waste liquid treatment method has great economic benefit.
As shown in fig. 1 to 8, the present invention further provides an ammonia desulfurization waste liquid treatment system for implementing the above-mentioned method for treating ammonia desulfurization waste liquid, which includes an oxidation kettle 100, a decoloring tower 200, a first centrifugal separator 300, a vacuum evaporation kettle 400, a second centrifugal separator 500, a crystallization kettle 600, and a third centrifugal separator 700 connected in sequence, wherein a tail gas discharge port of the oxidation kettle 100 is connected to the tail gas treatment system 900, a steam outlet of the tail gas treatment system is connected to a condenser 1000, a condensed water outlet of the condenser 1000 is connected to the tail gas treatment system 900, and a liquid outlet of the third centrifugal separator 700 is connected to the vacuum evaporation kettle 400 through a first return pipe 800. Thus, by arranging the tail gas treatment system 900 and connecting the tail gas treatment system 900 with the condenser 1000, the tail gas treatment system 900 can realize condensation washing of the tail gas, and the tail gas treatment effect is good; and the condensed water of the condenser 1000 is recycled, so that resources are saved.
Wherein, the tail gas processing system 900 comprises a processing tower 1, a recovery tower 4, a first gas pipe 2, a second gas pipe 3, an air pump 5, a first condensation body 6, a connecting pipe 7, a second condensation body 8 and a spraying mechanism 9, the first condensation body 6 is fixed below the inside of the processing tower 1, the inside of the first condensation body 6 is provided with a first water collecting channel 10 penetrating through the left and right side walls of the first condensation body 6, the first water collecting channel 10 is communicated with the recovery tower 4, the upper wall of the first condensation body 6 is internally provided with a first cavity 11 for containing the condensation body, the first condensation body 6 is provided with a plurality of first gas holes 12 for gas to pass through, the first gas holes 12 are not communicated with the first water collecting channel 10 and the first cavity 11, the second condensation body 8 is fixed below the inside of the processing tower 1 and is positioned above the first condensation body 6 and is communicated with the first condensation body 6 through the connecting pipe 7, a second water collecting channel 13 penetrating through the left side wall of the second condensation body 8 is arranged in the second condensation body 8, the second water collecting channel 13 is communicated with the recovery tower 4, the communication position is positioned above the communication position of the first water collecting channel 10 and the recovery tower 4, a second cavity 14 for containing condensate is arranged in the upper wall of the second condensation body 8, a plurality of second air holes 15 for gas to pass through are arranged on the second condensation body 8, the second air holes 15 are not communicated with the second water collecting channel 13 and the second cavity 14, an air extracting pump 5 is fixed at the top of the recovery tower 4, a first air pipe 2 is communicated on the air extracting pump 5, the air inlet end of the first air pipe 2 extends to the upper part in the recovery tower 4, the air outlet end of the first air pipe 2 is fixed at the bottom of the treatment tower 1, one end of the second air pipe 3 is communicated with tail gas of the oxidation kettle 100, the other end of the second air pipe 3 penetrates through the bottom walls of the recovery tower 4 and the first condensation body 6 and is communicated with the first water collecting channel 10, the spraying end of the spraying mechanism 9 extends to the upper part of the inside of the treatment tower 1 and is positioned above the second condensation body 8.
The first condensation body 6 and the second condensation body 8 can keep low temperature through the condensed water in the first cavity 11 and the second cavity 14, and the tail gas is condensed. The tail gas discharged from the oxidation reactor 100 enters the first water collecting channel 10 through the second pipe, and the upper wall of the first water collecting channel 10 meets the condensation to form water, and the water falls into the recovery tower 4. The tail gas condensed by the first condensing body 6 enters the second water collecting channel 13 through the connecting pipe 7, the upper wall of the second water collecting channel 13 is condensed into water when meeting cold, the condensed water in the second water collecting channel 13 enters the first water collecting channel 10 through the second pipe, and finally drops into the recovery tower 4 through the first water collecting channel 10. The tail gas after the double condensation treatment by the first condensation body 6 and the second condensation body 8 enters the recovery tower 4 through the left opening of the second water collecting channel 13. The tail gas in the recovery tower 4 is pumped to the lower part in the treatment tower 1 through the first gas pipe 2 by the air pump 5, the tail gas rises to the upper part in the treatment tower 1 through the first gas hole 12 and the second gas hole 15, and the tail gas is sprayed and washed by the spraying mechanism 9 and then is discharged after reaching the standard. The arrangement of the first condensing body 6 and the second condensing body 8 is adopted, so that double condensation is not performed, the condensation is more thorough, and the recovery rate of ammonia water is ensured; the device also has the function of slowing, avoids the problem of incomplete spraying caused by high speed of tail gas entering the upper part in the treatment tower 1, and improves the spraying and washing treatment effect; and the second condensation body 8 and the first condensation body 6 which are distributed and arranged from top to bottom can effectively separate the ammonia water after condensation from the tail gas after condensation, so that the ammonia water can be conveniently recovered, and the tail gas can be extracted and treated.
Wherein, first water collecting channel 10 and second water collecting channel 13 all are the segment form, and the setting of first water collecting channel 10 and second water collecting channel 13 that are the segment form improves the area of contact with tail gas for the condensation effect is better, improves condensation efficiency. And the centre of sphere of first water collecting channel 10 is located the below of first water collecting channel 10, and the centre of sphere of second water collecting channel 13 is located the top of second water collecting channel 13, and this not only makes the aqueous ammonia after first water collecting channel 10 and the condensation of second water collecting channel 13 better discharge, also makes the tail gas after the condensation of second water collecting channel 13 better discharge, improves condensation treatment effect and efficiency.
Wherein, first cavity 11 and second cavity 14 all communicate with two circulating line 19, and two circulations all are equipped with circulating pump 21 with circulation tank 20 intercommunication on every circulating line 19. The circulation keeps the condensate in the first cavity 11 and the second cavity 14 at a low temperature, ensuring that the condensation is performed efficiently.
Wherein, recovery tower 4 includes first collection portion 41, second collection portion 42 and drain pipe 43, and first collection portion 41 cover is located the processing tower 1 outside, and with first water channel 10 intercommunication that catchments, second collection portion 42 and first collection portion 41 intercommunication, and with second water channel 13 intercommunication that catchments, the lower part of second collection portion 42 lateral wall is provided with drain pipe 43. Retrieve the aqueous ammonia through first collection portion 41 for the aqueous ammonia is located second collection portion 42 lower part, retrieves the tail gas after the condensation through second collection portion 42, makes the tail gas after the condensation be located the upper portion of second collection portion 42, effectively separates, and the aqueous ammonia of being convenient for is retrieved and tail gas is taken out and is left.
Wherein, spray mechanism includes spray water tank 91, retrieval and utilization pipe 92, water pump 93, water pipe 94, and shower head 95, spray water tank 91's top is fixed with water pump 93, be connected with water pipe 94 on the water pump 93, the bottom of water pipe 94 extends to the inside below of spray water tank 91, the left end of water pipe 94 passes treatment tower 1, and extend to the fixed intercommunication in the top of 1 inside of treatment tower and have a plurality of shower heads 95, the fixed intercommunication in the upper portion of spray water tank 91 right side wall has the retrieval and utilization pipe 92 with the comdenstion water export intercommunication of condenser 1000. The water is pumped out from the spray water tank 91 by the water pump 93 and sprayed out through the spray head 95 to perform spray washing treatment on the exhaust gas. And partial water of the spray water tank 91 can be recycled by water condensed by the condenser 1000, so that water resources are saved.
The connection position of the connection pipe 7 and the first condensation body 6 is located at the center of the first condensation body 6, and the connection position of the connection pipe 7 and the second condensation body 8 is located at the center of the second condensation body 8. The connecting pipe 7 in the right center position is more beneficial to the flow of the tail gas and the collection of the ammonia water.
The above examples are only intended to illustrate the technical solution of the present invention, but not to limit it; although the present invention has been described in detail with reference to the foregoing embodiments, it will be understood by those of ordinary skill in the art; the technical solutions described in the foregoing embodiments may still be modified, or some technical features may be equivalently replaced; and such modifications or substitutions do not depart from the spirit and scope of the corresponding technical solutions of the embodiments of the present invention.
Claims (10)
1. The method for treating the ammonia desulphurization waste liquid is characterized by comprising the following steps:
s1: sending the desulfurization waste liquid into an oxidation kettle, carrying out catalytic oxidation under the condition of adding a catalyst and air, converting ammonium thiosulfate in the desulfurization waste liquid into ammonium sulfate, carrying out condensation washing treatment on tail gas discharged from the oxidation kettle through a tail gas treatment system, condensing the tail gas with ammonia gas into ammonia water, returning the ammonia water to the desulfurization system, washing and absorbing the condensed tail gas, and then discharging the tail gas up to the standard;
s2: carrying out decolorization treatment on the desulfurization waste liquid after catalytic oxidation, and carrying out solid-liquid separation on the decolorized desulfurization waste liquid to separate out sulfur;
s3: vacuum evaporation is carried out on the desulfurization waste liquid from which sulfur is separated, the temperature is reduced to separate out ammonium sulfate crystals, solid-liquid separation is carried out under the constant temperature state, the separated ammonium sulfate crystals are dried to obtain ammonium sulfate, and steam in the vacuum evaporation process is condensed into water and then recycled to a tail gas treatment system to be used as washing water;
s4: and (4) enabling the filtrate subjected to solid-liquid separation in the step S3 to enter a crystallization kettle to obtain an ammonium thiocyanate crystal liquid, carrying out solid-liquid separation on the ammonium thiocyanate crystal liquid, returning the separated filtrate to the step S3 to continue vacuum evaporation, and drying the separated ammonium thiocyanate crystals to obtain the ammonium thiocyanate.
2. An ammonia desulfurization waste liquid treatment system for realizing the method for treating ammonia desulfurization waste liquid according to claim 1, characterized in that:
comprises an oxidation kettle, a decoloration tower, a first centrifugal separator, a vacuum evaporation kettle, a second centrifugal separator, a crystallization kettle and a third centrifugal separator which are connected in sequence;
the tail gas discharge port of the oxidation kettle is connected with a tail gas treatment system;
the steam outlet is connected with a condenser, and a condensed water outlet of the condenser is connected with the tail gas treatment system;
and a liquid outlet of the third centrifugal separator is connected with the vacuum evaporation kettle through a first return pipe.
3. The ammonia desulfurization waste liquid treatment system according to claim 2, characterized in that:
the tail gas treatment system comprises a treatment tower, a recovery tower, a first gas pipe, a second gas pipe, a gas extraction pump, a first condensing body, a connecting pipe, a second condensing body and a spraying mechanism;
the first condensation body is fixed below the inside of the treatment tower, a first water collecting channel penetrating through the left side wall and the right side wall of the first condensation body is formed in the first condensation body, the first water collecting channel is communicated with the recovery tower, a first cavity for containing condensate is formed in the upper wall of the first condensation body, a plurality of first air holes for gas to pass through are formed in the first condensation body, and the first air holes are not communicated with the first water collecting channel and the first cavity;
the second condensation body is fixed below the interior of the treatment tower, positioned above the first condensation body and communicated with the first condensation body through a connecting pipe;
a second water collecting channel penetrating through the left side wall of the second condensation body is formed in the second condensation body, the second water collecting channel is communicated with the recovery tower, the communication position of the second water collecting channel is located above the communication position of the first water collecting channel and the recovery tower, a second cavity for containing condensate is formed in the upper wall of the second condensation body, a plurality of second air holes for gas to pass through are formed in the second condensation body, and the second air holes are not communicated with the second water collecting channel and the second cavity;
an air suction pump is fixed at the top of the recovery tower, a first air pipe is communicated with the air suction pump, the air inlet end of the first air pipe extends to the upper part of the interior of the recovery tower, and the air outlet end of the first air pipe is fixedly communicated with the bottom of the treatment tower;
one end of the second air pipe is communicated with a tail gas discharge port of the oxidation kettle, and the other end of the second air pipe penetrates through the recovery tower and the bottom wall of the first condensation body to be communicated with the first water collecting channel;
and the spraying end of the spraying mechanism extends to the upper part inside the treatment tower and is positioned above the second condensation body.
4. The ammonia desulfurization waste liquid treatment system according to claim 3, characterized in that:
the first water collecting channel and the second water collecting channel are both in a spherical segment shape, the spherical center of the first water collecting channel is located below the first water collecting channel, and the spherical center of the second water collecting channel is located above the second water collecting channel.
5. The ammonia desulfurization waste liquid treatment system according to claim 3, characterized in that:
the first air hole is filled with a first filler, and the second air hole is filled with a second filler.
6. The ammonia desulfurization waste liquid treatment system according to claim 3, characterized in that:
and a third filler is filled in the space among the first condensation body, the second condensation body and the treatment tower.
7. The ammonia desulfurization waste liquid treatment system according to claim 3, characterized in that:
first cavity and second cavity all communicate has two circulating line, and two circulations all are equipped with the circulating pump with circulation tank intercommunication on every circulating line.
8. The ammonia desulfurization waste liquid treatment system according to claim 3, characterized in that:
the recovery tower comprises a first collecting part, a second collecting part and a liquid outlet pipe;
the first collecting part is sleeved outside the treatment tower and is communicated with the first water collecting channel;
the second collecting part is communicated with the first collecting part and the second water collecting channel;
and a liquid outlet pipe is arranged at the lower part of the side wall of the second collecting part.
9. The ammonia desulfurization waste liquid treatment system according to claim 3, characterized in that:
the spraying mechanism comprises a spraying water tank, a recycling pipe, a water pump, a water pipe and a spraying head;
a water pump is fixed at the top of the spray water tank, a water pipe is connected to the water pump, the bottom end of the water pipe extends to the lower part inside the spray water tank, the left end of the water pipe penetrates through the treatment tower, and a plurality of spray headers are fixedly communicated with the upper part extending to the inside of the treatment tower;
and the upper part of the right side wall of the spray water tank is fixedly communicated with a recycling pipe communicated with a condensate water outlet of the condenser.
10. The ammonia desulfurization waste liquid treatment system according to claim 3, characterized in that:
the connection position of the connecting pipe and the first condensation body is positioned at the right center of the first condensation body;
the connecting position of the connecting pipe and the second condensation body is located at the positive center of the second condensation body.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202210473764.7A CN114772830A (en) | 2022-04-29 | 2022-04-29 | Treatment method and system for ammonia desulphurization waste liquid |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202210473764.7A CN114772830A (en) | 2022-04-29 | 2022-04-29 | Treatment method and system for ammonia desulphurization waste liquid |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN114772830A true CN114772830A (en) | 2022-07-22 |
Family
ID=82435890
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202210473764.7A Pending CN114772830A (en) | 2022-04-29 | 2022-04-29 | Treatment method and system for ammonia desulphurization waste liquid |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN114772830A (en) |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN201441879U (en) * | 2009-07-09 | 2010-04-28 | 聊城市鲁西化工工程设计有限责任公司 | Melamine tail gas recovery tower |
| CN204454584U (en) * | 2014-12-29 | 2015-07-08 | 赵引德 | Desulfurization waste liquor puies forward salt system |
| CN104941355A (en) * | 2014-03-30 | 2015-09-30 | 天津东大化工集团有限公司 | Comprehensive recovery tower for tail gas in sodium benzoate production process |
| CN207102255U (en) * | 2017-08-23 | 2018-03-16 | 湖北三才堂化工科技有限公司 | A kind of dichloromethane device for recovering tail gas |
-
2022
- 2022-04-29 CN CN202210473764.7A patent/CN114772830A/en active Pending
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN201441879U (en) * | 2009-07-09 | 2010-04-28 | 聊城市鲁西化工工程设计有限责任公司 | Melamine tail gas recovery tower |
| CN104941355A (en) * | 2014-03-30 | 2015-09-30 | 天津东大化工集团有限公司 | Comprehensive recovery tower for tail gas in sodium benzoate production process |
| CN204454584U (en) * | 2014-12-29 | 2015-07-08 | 赵引德 | Desulfurization waste liquor puies forward salt system |
| CN207102255U (en) * | 2017-08-23 | 2018-03-16 | 湖北三才堂化工科技有限公司 | A kind of dichloromethane device for recovering tail gas |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN110833754B (en) | Device for absorbing ethylene oxide waste gas and method for treating ethylene oxide waste gas | |
| CN101654305B (en) | Process for changing phenolic nitrate effluent into useful material by extracting, evaporating, crystallizing and coupling | |
| CN103058442B (en) | Method for processing secondary salt in desulphurization waste liquid | |
| CN105036438B (en) | A kind of sodium alkali desulfurization waste liquid method for innocent treatment | |
| CN206553478U (en) | Coal oven dithio-gas purifier | |
| CN110921953B (en) | Resource treatment process and device for coking desulfurization waste liquid | |
| CN108083538A (en) | The recycling processing method and its device of coking desulfurization salt bearing liquid wastes | |
| CN210736624U (en) | Production system for recycling taurine mother liquor completely | |
| CN104492106B (en) | A kind of coking desulfurization sulfur foam and the drying means of desulfurization waste liquor | |
| CN112125319A (en) | Process for recovering all components of desulfurization waste liquid | |
| CN202038998U (en) | Production system for recycling carbolic oil through acidolysis separation of phenol sodium salt and co-producing sodium sulfite | |
| CN104232133B (en) | Potassium, the method and device of sodium ions content in a kind of reduction coal tar | |
| CN114772830A (en) | Treatment method and system for ammonia desulphurization waste liquid | |
| CN210559766U (en) | Wet vanadium recovery wastewater resource utilization system | |
| CN107739314A (en) | A kind of decoloration of glycin mother liquid method | |
| CN102381943B (en) | System and technology for producing coked crude phenol | |
| CN103708993A (en) | Alkali washing and dehydrating process for crude cracked gas in vinylidene fluoride production | |
| CN206751389U (en) | A kind of chlorine recovery system during pyridine compounds and their continuous chlorination | |
| CN112979516B (en) | Energy-saving methyl mercaptan synthesis device | |
| CN103732562B (en) | Preparation has the method for the organic fertilizer of high nutrient density, and for performing the arrangement of described method | |
| CN202265523U (en) | Production system for coking crude phenol | |
| CN110980766B (en) | Conversion process and device for salt in desulfurization waste liquid | |
| CN108217690A (en) | A kind of technique that secondary salt is extracted from desulfurization waste liquor | |
| US10960391B2 (en) | Method and system of elemental sulfur recycling and catalyst regenerating for sulfur-deposited catalyst | |
| CN214437829U (en) | Energy-saving environment-friendly ammonia desulphurization zero-emission system of sulfur recovery device |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination |