CN104418447A - Process for treating waste liquid from catalytic cracking flue gas desulfurization - Google Patents
Process for treating waste liquid from catalytic cracking flue gas desulfurization Download PDFInfo
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- CN104418447A CN104418447A CN201310421183.XA CN201310421183A CN104418447A CN 104418447 A CN104418447 A CN 104418447A CN 201310421183 A CN201310421183 A CN 201310421183A CN 104418447 A CN104418447 A CN 104418447A
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- 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
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- 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
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- 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
- C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
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- 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
- C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
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- 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
- C02F1/66—Treatment of water, waste water, or sewage by neutralisation; pH adjustment
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- 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
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F11/00—Treatment of sludge; Devices therefor
- C02F11/12—Treatment of sludge; Devices therefor by de-watering, drying or thickening
- C02F11/121—Treatment of sludge; Devices therefor by de-watering, drying or thickening by mechanical de-watering
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- 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
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- Hydrology & Water Resources (AREA)
- Engineering & Computer Science (AREA)
- Environmental & Geological Engineering (AREA)
- Water Supply & Treatment (AREA)
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Separation Of Suspended Particles By Flocculating Agents (AREA)
- Treatment Of Water By Oxidation Or Reduction (AREA)
Abstract
The invention provides a process for treating waste liquids from catalytic cracking flue gas desulfurization. The process comprises the following steps: enabling a part of waste liquids from a quenching washing tower to enter a hydraulic cyclone separator so as to be subjected to solid-liquid separation, returning the thin liquids to the quenching washing tower so as to be recycled, enabling the thick liquids to enter a neutralization reactor so as to be subjected to neutralization reaction, enabling the neutralized waste liquids to enter a slurry pond so as to be mixed with a flocculating agent uniformly, and enabling the mixture to enter an expansion-drum type filter so as to be subjected to solid-liquid separation with a thick slurry and a supernatant being obtained; returning part of the supernatant to the quenching washing tower so as to be recycled, discharging the remaining supernatant into an oxidation tank, removing the pseudo-COD containing sulfite roots and bisulfite roots by oxidizing, and directly discharging the qualified sewage; enabling the thick slurry to enter a settling pond from the bottom of the expansion-drum type filter so as to be further settled, feeding the thick slurry subjected to settlement into a dewatering machine so as to be concentrated and dewatered, directly transporting the filter cakes obtained by dewatering the thick slurry, returning the filtrate from the dewatering of the thick slurry to the slurry pond, and mixing the filtrate with the waste liquids so as to be retreated. The process provided by the invention has the advantages of a stable and efficient treatment effect, strong shock resistance, low investment and small floor area occupation and convenience of operation.
Description
Technical field
The present invention relates to a kind for the treatment of process of waste liquid, relate in particular to a kind of catalytic cracking flue gas desulfuration waste liquid treatment process.
Background technology
Current catalytic cracking flue gas generally adopts wet desulfurizing process, and wet fuel gas desulfurizing technology comprises disposable absorption technique and renewable absorption technique two class.Renewable absorption technique is owing to can change the very high SO of purity into by the pollutent in flue gas
2reclaimed, and substantially do not produce secondary pollution and come into one's own, it comprises the washing of flue gas chilling, SO
2the operating units such as absorption and regeneration.The washing of flue gas chilling adopts fresh water to carry out dedusting cooling; system is in normal course of operation; need to control to protect the equipment such as pump, nozzle and pipeline to the suspended substance in circulation sour water, chlorion, soluble solid content; when These parameters exceeds standard, the recycle system needs outer row's partial acid to enter follow-up liquid waste treatment system.The principal pollutant contained in sour water have catalyst dust, sulfurous acid, sulfuric acid, sodium salt and heavy metal etc., if these pollutents process directly discharge not in time will certainly cause serious pollution to environment.Generally adopt at present and first sour water is added alkali and be neutralized to neutrality, then after filtration or subsider, after improving the solid content of waste liquid, then carry out solid-liquid separation with filtrate box, supernatant liquor discharge after oxidation tank oxidation of subsider.As CN101003412A describes a kind of flue gas desulfurization wastewater treatment system, it comprises: waste water Buffer Pool, neutralization/reaction/flocculation tanks, clarification/concentration basin, water tank compose in series through pipeline.CN101486517A discloses a kind for the treatment of process of desulfurization wastewater, it adopts inclined tube settling pond technology to process, wastewater emission or recycle up to standard after process, the scum silica frost that electric flocculation treatment device is discharged and the precipitating sludge that inclined tube settling pond is discharged enter sludge thickener and concentrate further.CN101993169A discloses a kind for the treatment of process of sintering flue gas desulfurization waste water, and waste water, by neutralization, flocculation, precipitation, is isolated filtrate, carried out biochemical treatment etc. to filtrate.Above-mentioned technique exists: the waste liquid residence time is long, and occupation area of equipment is large, and going out water suspension can not be up to standard, and sulfite oxidation is that vitriol is not thorough, and water outlet COD is too high, and device impact resistance is little; In addition, equipment checking maintenance difficulty, auxiliary facility investment is high, and schedule of operation is loaded down with trivial details, work under bad environment, and most for the treatment of process be intermittently affected, the shortcoming such as can not to run continuously.
The waste water treatment process of CN102815808A is as follows: waste water is entered slurry pool and mixes with flocculation agent, utilizing stirrer to stir makes waste water mix with flocculation agent, mixed waste water is drained in cripling pipe filter, coagulating is there is in cripling pipe filter lower end, by the finely ground particles flocculation in waste water, form large flocs unit, realize solid-liquid separation by membrane filtration again and obtain dense slag and supernatant liquor, and further this supernatant liquor is drained in oxidation tank, and the dense slag of back flushing, dense slag is made to enter follow-up strumbox, dense slag is carried out thickening in strumbox, concentrated mud cake outward transport, the water deviate from returns in slurry pool to mix with waste water and re-starts process, described supernatant liquor will containing inferior sulfate radical in oxidation tank, the false COD oxidation removal of bisulfite, qualified wastewater disposition.The waste water waste liquid that disposable sulfur removal technology produces for catalytic cracking unit adopts described in this patent, circulation fluid is the mixing solutions of S-WAT, sodium bisulfite and sodium sulfate, pH value 6.5 ~ 7, basic in neutral, do not need volume exogenously added alkali to neutralize, though this waste water treatment process ensure that the suspended substance in efflux wastewater is up to standard, its clear liquid sulfite salt concn is very high, oxygen-consumption is large, is oxidized not thorough; Dense Slag treatment adopts strumbox to leave standstill and filters, and equipment not only floor space is large, and is that interval is affected, manual handling waste residue, work under bad environment etc.
Summary of the invention
In order to problems such as the occupation area of equipment solving prior art existence are large, running cost is high, solid-liquid separation is thorough, mud cake water content is high, the invention provides a kind of catalytic cracking flue gas desulfuration waste liquid treatment process, adopt that this processing unit floor space is little, running cost is low, solid-liquid separation is thorough, clear liquid can directly discharge; Mud cake water content is low, can directly transport, good operational environment.
Catalytic cracking flue gas desulfuration waste liquid treatment process provided by the invention comprises the steps:
1) entering wet cyclone containing the part waste liquid of particulate matter, vitriol and sulphite and carry out concentration-type solid-liquid separation from chilling washing tower, returning the circulation of chilling washing tower through being separated the thin liquid produced through wet cyclone top, bottom wet cyclone, entering neutralization reactor through being separated the dope more containing particulate matter produced;
2) under the effect of alkali lye, there is neutralization reaction in the dope entering neutralization reactor, generate in neutral waste liquid, the waste liquid after neutralization enters slurry pool, under whipped state, add flocculation agent, waste liquid is mixed with flocculation agent, and mixed waste liquid is delivered in swollen drum strainer through submerged pump;
3) after entering the mixing of swollen drum strainer, waste liquid produces flocculation in swollen drum strainer, and small particulate matter flocculates into large flocs unit, then realizes solid-liquid separation by the membrane filtration of swollen drum strainer and obtain underflow and supernatant liquor; Supernatant liquor is discharged from cripling formula filter top, and part returns the reuse of chilling wash tower bottoms to reduce efflux wastewater amount, and remaining supernatant liquor is drained in oxidation tank; Underflow enters settling tank from cripling formula filter bottom;
4) supernatant liquor be drained in oxidation tank will contain the false COD oxidation removal of inferior sulfate radical, bisulfite in oxidation tank, and qualified sewage can be arranged directly outward; The underflow entering settling tank is in settling tank further after precipitation, and send into water extracter, in water extracter, carry out thickening, the filter cake after dehydration can directly transport, and the filtrate removed returns in slurry pool to mix with waste liquid and re-starts process.
The present invention has following advantages:
1, in catalytic cracking flue gas, catalyst powder particle concentration is high, enter in recycle acid water after being washed by chilling, after adopting wet cyclone, catalyst dust can be concentrated, on the basis not changing waste liquor treatment equipment size, greatly reduce the dust concentration in circulation sour water, reduce circulation sour water to the wearing and tearing of equipment, pipeline and pump, be conducive to the long-term operation of device.
2, adopt swollen drum strainer to carry out solid-liquid separation, filtering rate be fast, filtrate water conditioning, total suspended matter meets emission standard.
3, utilize serial or parallel connection oxidation tank to carry out fully oxidized to supernatant liquor, make sulfite oxidation be vitriol, remove the COD of sewage.
4, the mud in settling tank enters folded spiral shell formula water extracter and dewaters further, exports outer blowdown mud solid content about 40%, can directly transport, and equipment takes up an area little, safeguards simple, easy to operate.
5, whole set process floor space is little, solid-liquid separation thorough, and clear liquid can directly discharge; Mud cake can directly transport, good operational environment.
Accompanying drawing explanation
Fig. 1 is catalytic cracking flue gas desulfuration waste liquid treatment process schema of the present invention;
Fig. 2 is the fundamental diagram of wet cyclone;
Fig. 3 be swollen drum strainer in running order time fundamental diagram;
Fig. 4 be swollen drum strainer be in clear liquid deadweight recoil state time fundamental diagram.
In figure:
1-chilling washing tower, 2-recycle pump, 3-wet cyclone, 4-neutralization reactor, 5-alkali tank, the online pH analyser of 6-, 7-slurry pool, 8-flocculation agent feeder, 9-slurry pool stirrer, 10-submerged pump, 11-is swollen drum strainer, 12-transferpump, 13-oxidation tank, 14-air-distributor, 15-oxidation tank agitator, the online pH analyser of 16-, 17-effluent trough, 18-settling tank, 19-bleed valve, 20-folds spiral shell formula water extracter, 21-alkali tank pump, 22-underflow valve.
Embodiment
Below in conjunction with accompanying drawing, the invention will be further described, as shown in Figure 1, FCC flue gas enters chilling washing tower 1, and to carry out chilling saturated from the middle and lower part of chilling washing tower 1, formed containing particulate matter, the acid waste liquid of vitriol and sulphite, waste liquid is discharged at the bottom of tower, major part returns chilling washing tower 1 through recycle pump 2 circulation, remainder is sent into wet cyclone 3 and is carried out concentration-type solid-liquid separation, catalyst dust is separated from waste liquid, thin liquid through being separated generation returns chilling washing tower 1 through wet cyclone 3 top and circulates, bottom wet cyclone 3, neutralization reactor 4 is entered through being separated the dope more containing particulate matter produced.
The dope more containing particulate matter mixes with the alkali lye of coming through alkali tank pump 21 from alkali tank 5 in neutralization reactor 4, there is neutralization reaction, generate in neutral waste liquid, the alkali lye amount added is controlled by online pH analyser 6, waste liquid after neutralization enters slurry pool 7, flocculation agent feeder 8 injects flocculation agent to slurry pool 7, stirring through slurry pool stirrer 9 makes waste liquid mix with flocculation agent, mixed waste liquid is transported to swollen drum strainer 11 through submerged pump 10, and (swollen drum strainer is two, one open one standby, when one reach capacity need to carry out back flushing time, be switched to another, swollen drum strainer after back flushing is for subsequent use), after entering the mixing of swollen drum strainer 11, waste liquid produces flocculation in swollen drum strainer 11, and small particulate matter flocculates into large flocs unit, then realizes solid-liquid separation by the membrane filtration of swollen drum strainer 11 and obtain underflow and supernatant liquor.
Supernatant liquor is discharged from swollen drum strainer 11 top, part to return bottom chilling washing tower 1 reuse to reduce efflux wastewater amount, remaining supernatant liquor is transported in oxidation tank 13 by transferpump 12, establishes air-distributor 14, oxidation tank agitator 15 and on-line pH value analyser 16 in oxidation tank 13; Supernatant liquor enter in oxidation tank 13 with the non-purified compressed air injected bottom oxidation tank 13 and a small amount of alkali lye, fully contact under the effect of oxidation tank agitator 15, a large amount of aerations will contain the false COD oxidation removal of inferior sulfate radical, bisulfite in supernatant liquor, the COD of effective reduction discharge opeing, the injection rate of alkali lye is controlled by on-line pH value analyser 16, to ensure that water outlet is in neutral, supernatant liquor waste liquid total suspended matter (TSS) after treatment meets emission standard, can directly discharge through effluent trough 17.How much quantity of oxidation tank 13 can be arranged according to the concentration of waste liquid sulfite salt, can be one, two or more (in Fig. 1, oxidation tank is 1).When oxidation tank 13 is two or more, as 2 ~ 5, its mode of connection also can be able to be in parallel for series connection.
Underflow enters settling tank 18 and again precipitates bottom swollen drum strainer 11, when the block precipitation be flocculated bottom settling tank 18 gathers and reach a certain height at the bottom of pond, periodically folded spiral shell formula water extracter 20 is discharged to by the bleed valve 19 of bottom, in folded spiral shell formula water extracter 20, filter cake is further dehydrated mummification and reaches 35 ~ 40% to solid content, can directly transport, landfill, the filtrate removed returns after slurry pool 7 mixes with waste liquid and re-starts filtration.Certain water extracter also can adopt the water extracter of other patterns.
Described wet cyclone 3 can according to dust concentration manual regulation underflow valve 22 aperture in flue gas with the dust content in controlled circulation sour water; Folded spiral shell formula water extracter 20 instead of traditional filter cloth and centrifugal filter type, and occupation area of equipment is little, simple to operate, can according to sludge quantity flexible to be processed.
Wet cyclone 3 described in the present invention is the patented product (patent publication No.: CN102179126A) of technology maturation.It utilizes different media high speed rotating in cyclone pipe to produce centrifugal force difference, separated by catalyst dust from waste liquid.Cyclone pipe as wet cyclone core component forms primarily of parts such as separation cone, tail pipe and overflow ports.Material under certain pressure effect from quenched water import tangentially or the inside that enters swirler, involute urve direction carry out high speed rotating, because of the change of cross section of fluid channel after separation cone, make liquid stream speedup and form spiral fluidised form, reducing further because of cross section of fluid channel after fluid enters tail pipe, swirl velocity continues to increase, and defines a stable centrifuge field at separator interior.Aqueous phase is at cyclone pipe center convergence, and overflow from overflow port, solid phase is prolonged wall and moved to underflow opening, thus the enrichment realizing overflow port water clarification and catalyzer phase reclaims, principal defecation aqueous phase flows out from overflow port, and catalyzer is discharged from catalyst outlet, and the principle of work of wet cyclone 3 is shown in Fig. 2.
In the technical process shown in Fig. 1, wet cyclone 3 is selected mainly to consider its following performance characteristics:
(1) separation efficiency is high.
(2) easy care.
(3) pressure-losses is little.
(4) reliability is high, long service life.
(5) failure rate is low, movement-less part.
Swollen drum strainer 11 described in the present invention is patent equipment (patent publication No.: CN1613538A), is the product carrying out primary separation and unique design for the slip of different solid content.Be mainly solve in the past in tubular filter system filtration medium (filter bag) to recoil cleaning performance difference, the defect of easy fouling and clogging, and the supporting structure (cage) of the filtration medium (filter bag) in filtering system is newly designed, in strainer, the resting support of filtration medium filter bag is made up of the conical section of more piece rule or segmental arc, form overall undulatory cage, change into different geometries when making filtration medium (filter bag) be in different operating mode.When strainer is in running order (see Fig. 3), filtration slip and pressurized air enter strainer, filtering slip makes filter bag tighten along with pressure direction, be attached on cage and become corrugated, filter bag on corrugated cage body retains solid matter in filtrate (filter residue) at its outside surface, crosses cleaner liquid and returns to pulping tank; When strainer is in clear liquid deadweight recoil state (see Fig. 4), due to opening fast of end valve, the slurry of strainer lower end is begun to rehearse at a high speed, the filter bag external space forms backwash liquid in negative pressure and filter bag and causes pressure reduction, and by the clear liquid gravity of adverse current in filter bag, filter bag is in expansion state, be formed as more piece drum type outwardly, make the attached filter residue amassed in filter bag outside form bridge structure layer geometrical shape change fast and easily come off, the concentrate slip that finally recoils enters medial launder, pressurized air is discharged, and the underflow liquid after finally carrying delivers to the second-order separation.Moreover filter bag is in expansion state, the micropore of filtration medium also in expansion state, the also comparatively easy cleaning of the tamper in micropore.Again due to cage to open sky rate high, improve effective filtration area, filtering rate improved greatly.
In the technical process shown in Fig. 1, swollen drum strainer 11 is selected mainly to consider its following performance characteristics:
(1) the bag-shaped filter membrane of modification, does not harden, easy cleaning, and cross cleaner liquid water quality good, filter membrane material model washability is wide.
(2) cripling structure innovation, regenerate filtration media is effective, and filtrate strong adaptability, working efficiency is high.
(3) anti-corrosion, wear-resistant, anti-scaling measures is perfect, automatically switch according to the order of sequence, facility compact, reduced investment.
Folded spiral shell formula water extracter 20 described in the present invention belongs to prior art, is one group or several groups of filtering units being made up of auger axle, multiple fixing lamination and multiple travelling lamination.Each group filtering unit all divides concentrating part (THICKENING ZONE) and de-watering section (DEWATERING ZONE) two portions, sludge outlet from the mud inlet of concentrating part to de-watering section, the pitch of screw shaft diminishes gradually, and the gap between set collar and travelling ring also diminishes gradually.Sludge outlet place is provided with back pressure plate, with the pressure in adjusting screw chamber.The concentrated of mud and press dewatering are operated in a cylinder and complete by it, instead of traditional filter cloth and centrifugal filter type, break away from device for dehydrating sladge waste floor space in the past large, lower concentration and oily sludge cannot be processed, equipment running cost crosses a high difficult problem.
In the technical process shown in Fig. 1, folded spiral shell formula water extracter 20 is selected mainly to consider its following performance characteristics:
(1) applicable sludge concentration scope is wide.
(2) anti-oily sludge ability is strong, easily separated, do not block.
(3) clean environment firendly, without foul smell, noiselessness, without the need to high pressure washing, non-secondary pollution.
(4) body is little capable and vigorous, water saving, energy-conservation.
(5) daily maintenance easy maintenance, continuously-running, without the need to staff on duty.
The COD < 60mg/L of efflux wastewater after the art breading of the present invention shown in Fig. 1, total suspended matter concentration < 50mg/L, can directly discharge; Outer blowdown mud solid content about 40%, need not leave standstill dehydration more further and just can directly transport.
The experiment proved that, the catalytic cracking flue gas desulfuration waste liquid treatment process treatment effect stability and high efficiency of the present invention shown in Fig. 1, strong shock resistance, investment and floor space are little, easy and simple to handle.
Claims (4)
1. a catalytic cracking flue gas desulfuration waste liquid treatment process, is characterized in that comprising the steps:
1) entering wet cyclone containing the part waste liquid of particulate matter, vitriol and sulphite and carry out concentration-type solid-liquid separation from chilling washing tower, returning the circulation of chilling washing tower through being separated the thin liquid produced through wet cyclone top, bottom wet cyclone, entering neutralization reactor through being separated the dope more containing particulate matter produced;
2) under the effect of alkali lye, there is neutralization reaction in the dope entering neutralization reactor, generate in neutral waste liquid, the waste liquid after neutralization enters slurry pool, under whipped state, add flocculation agent, waste liquid is mixed with flocculation agent, and mixed waste liquid is delivered in swollen drum strainer through submerged pump;
3) after entering the mixing of swollen drum strainer, waste liquid produces flocculation in swollen drum strainer, and small particulate matter flocculates into large flocs unit, then realizes solid-liquid separation by the membrane filtration of swollen drum strainer and obtain underflow and supernatant liquor; Supernatant liquor is discharged from cripling formula filter top, and part returns the reuse of chilling wash tower bottoms to reduce efflux wastewater amount, and remaining supernatant liquor is drained in oxidation tank; Underflow enters settling tank from cripling formula filter bottom;
4) supernatant liquor be drained in oxidation tank will contain the false COD oxidation removal of inferior sulfate radical, bisulfite in oxidation tank, and qualified sewage can be arranged directly outward; The underflow entering settling tank is in settling tank further after precipitation, and send into water extracter, in water extracter, carry out thickening, the filter cake after dehydration can directly transport, and the filtrate removed returns in slurry pool to mix with waste liquid and re-starts process.
2. catalytic cracking flue gas desulfuration waste liquid treatment process according to claim 1, is characterized in that, described water extracter is folded spiral shell formula water extracter.
3. catalytic cracking flue gas desulfuration waste liquid treatment process according to claim 2, is characterized in that, the solid content of the filter cake after described dehydration reaches 35 ~ 40%.
4. catalytic cracking flue gas desulfuration waste liquid treatment process according to claim 1, is characterized in that, described oxidation tank is two or more, and its mode of connection is serial or parallel connection.
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106007148A (en) * | 2016-07-25 | 2016-10-12 | 中石化炼化工程（集团）股份有限公司 | Treatment method of catalytic cracking flue gas desulfurization wastewater |
| CN111018181A (en) * | 2019-12-20 | 2020-04-17 | 上海海事大学 | Magnesium-based ship tail gas desulfurization washing water treatment method |
| CN113060876A (en) * | 2021-03-26 | 2021-07-02 | 上海海事大学 | Air-flotation ultrafiltration treatment system and process for ship tail gas desulfurization washing wastewater |
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| JPH08192192A (en) * | 1995-01-12 | 1996-07-30 | Kansai Electric Power Co Inc:The | Method for treating flue gas desulfurization drain |
| CN101732968A (en) * | 2009-12-31 | 2010-06-16 | 华东理工大学 | Micro-cyclone de-solid method and device in catalytic cracking flue gas washing desulphurization process |
| CN102489136A (en) * | 2011-12-16 | 2012-06-13 | 国电环境保护研究院 | Flue gas desulfurizing waste water recovering process and device |
| CN102815808A (en) * | 2011-06-09 | 2012-12-12 | 中国石油化工股份有限公司 | Catalytic cracking fume desulfuration wastewater treatment process |
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2013
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Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH08192192A (en) * | 1995-01-12 | 1996-07-30 | Kansai Electric Power Co Inc:The | Method for treating flue gas desulfurization drain |
| CN101732968A (en) * | 2009-12-31 | 2010-06-16 | 华东理工大学 | Micro-cyclone de-solid method and device in catalytic cracking flue gas washing desulphurization process |
| CN102815808A (en) * | 2011-06-09 | 2012-12-12 | 中国石油化工股份有限公司 | Catalytic cracking fume desulfuration wastewater treatment process |
| CN102489136A (en) * | 2011-12-16 | 2012-06-13 | 国电环境保护研究院 | Flue gas desulfurizing waste water recovering process and device |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106007148A (en) * | 2016-07-25 | 2016-10-12 | 中石化炼化工程（集团）股份有限公司 | Treatment method of catalytic cracking flue gas desulfurization wastewater |
| CN111018181A (en) * | 2019-12-20 | 2020-04-17 | 上海海事大学 | Magnesium-based ship tail gas desulfurization washing water treatment method |
| CN113060876A (en) * | 2021-03-26 | 2021-07-02 | 上海海事大学 | Air-flotation ultrafiltration treatment system and process for ship tail gas desulfurization washing wastewater |
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Application publication date: 20150318 |