CN105399265A - Oil-containing waste water processing and recycling method - Google Patents
Oil-containing waste water processing and recycling method Download PDFInfo
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- CN105399265A CN105399265A CN201410385576.4A CN201410385576A CN105399265A CN 105399265 A CN105399265 A CN 105399265A CN 201410385576 A CN201410385576 A CN 201410385576A CN 105399265 A CN105399265 A CN 105399265A
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
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- Y02A20/124—Water desalination
- Y02A20/131—Reverse-osmosis
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Abstract
The invention relates to an oil-containing waste water processing and recycling method. Oil-containing waste water is processed through a process adopting rotational flow extraction and separation, an internal-circulation biological aerated filtering pool, traditional biochemical treatment, multi-medium filtering, ozone oxidation/a buffer pool, secondary biochemical treatment, and a reverse osmosis system. The Oil-containing waste water comes from an oil-refining enterprise, and specifically is draining of normal/reduced-pressure electro-desalting through an asphalt producing device, draining of electro-desalting through an integrated device, and mixed draining of an alkaline-residue processing apparatus from a sulphur workshop. According to the oil-containing waste water processing and recycling method, light oil is adopted for extracting and separating oil in the oil-containing waste water to remove most of the oil in the waste water, and residual oil and organic matters in the waste water is filtered through the internal-circulation biological aerated filtering pool to stabilize the water quality for later processing and ensure normal stable operation of conventional biochemical treatment. The process of oxidation, secondary biochemical treatment, and desalting is added after the traditional biochemical treatment, so that the oil-containing waste water is finally reused rather than drained.
Description
Technical field
The present invention relates to trade effluent comprehensive treating process field, is a kind for the treatment of for reuse method of oily(waste)water specifically.
Background technology
Petrochemical complex, as the industry of high energy consumption, high pollution, will discharge a large amount of trade effluents every year.The difference of oil refining process and product, causes each enterprise draining water quantity reduction to there is bigger difference, but all comprises a large amount of poisonous and hazardous organic pollutant in waste discharge.Along with crude oil heaviness and high-sulfurized, add more auxiliary agent in oil refining process, in waste water, hard-degraded substance increases, and wastewater biodegradability is deteriorated.
Oily(waste)water of the present invention refers to oil refining enterprise's oily(waste)water, refer to specifically: asphalt production device Atmospheric vacuum electric desalting draining, machinery electric desalting draining and its Future about Alkaline Residue Treatment Unit mixing draining of sulphur workshop, owing to usually containing a large amount of oil (the present invention refers to petroleum-type in the whole text) and high COD in this strand of waste water, its pollution load accounts for more than 60% of total load between whole enterprise cesspoolage truck, and because the variation water quality of this strand of waste water is large, enterprise is often to this burst of waste water individual curing, and the oil of high-content usually causes extreme shock to the operation in sewage farm in this strand of waste water, affect the steady running of whole oil-contained waste water treatment system.
Carry out investigation to oil refining enterprise's discharge process for treating oil-containing waste water to find, all adopt traditional technology process for oily(waste)water at present, main technique comprises: oil removal+flotation+biochemistry, and many discharges after wastewater treatment, this causes the waste greatly of water resources undoubtedly.In the process adopting traditional technology process, because oil-contg fluctuation is comparatively large in oily(waste)water, often cause Waste Water Treatment in paralyzed state, and the restore cycle of impacting rear system is each time also very long, have a strong impact on the normal production of enterprise, say nothing of the reuse after oiliness sewage treatment.
Summary of the invention
For the defect existed in prior art, the object of the present invention is to provide a kind for the treatment of for reuse method of oily(waste)water, solve high amounts of oil in waste water and, to the impact of Waste Water Treatment, achieve the reuse after oily(waste)water advanced treatment simultaneously.
For reaching above object, the technical scheme that the present invention takes is:
A treatment for reuse method for oily(waste)water, is characterized in that: adopt " eddy flow extracting and separating+inner circulating aerating biological filtering tank+conventional biochemical+multi-medium filtering+ozone oxidation/Buffer Pool+secondary biochemistry+reverse osmosis system " technique to process oily(waste)water.
On the basis of technique scheme, described oily(waste)water is oil refining enterprise's oily(waste)water.
On the basis of technique scheme, described oil refining enterprise oily(waste)water refers to asphalt production device Atmospheric vacuum electric desalting draining, machinery electric desalting draining and its Future about Alkaline Residue Treatment Unit mixing draining of sulphur workshop.
On the basis of technique scheme, specifically comprise the following steps:
Step 1, eddy flow extracting and separating: oily(waste)water enters eddy flow extraction separator through pump pressurization, injects the light oil of the handled oily waste water water yield 0.5 ~ 5% simultaneously by mass percentage in eddy flow extraction separator,
Light oil and the oily(waste)water with density difference produce Taylor vortex flow along with the rotor high-speed in separator rotates mixing, realize the separation of oil, water,
The water ratio of isolated oil phase is less than 0.5%, and total dissolved solid concentration is less than 20mg/L, directly can be recycled into electric desalting outlet,
Isolate oil concentration in aqueous phase and be less than 100mg/L;
Step 2, inner circulating aerating biological filtering tank: in the aqueous phase that eddy flow extracting and separating obtains and inner circulating aerating biological filtering tank, sewage sucks recirculation reactor in the lump through back window, and in this mixing oxygenation, then from the outflow suitable for reading of aeration riser tube, flow into bottom pond through return line again, enter biochemical areas and carry out bio-oxidation, filtration, biological adsorption;
Due to retaining of biomembranous growth and packing layer, after running certain hour, back flushing need be carried out to packing layer, make it Recovery processing efficiency again;
Step 3, conventional biochemical: inner circulating aerating biological filtering tank water outlet directly enters conventional biochemical process, this biochemical treatment comprises anoxic+aerobic+settling tank, and in inner circulating aerating biological filtering tank water outlet, most of biodegradable organic is removed through conventional biochemical process;
Step 4, multi-medium filtering: multi-medium filtering can remove the suspended substance in settling tank water outlet further, avoids reducing substances residual in settling tank water outlet to the consumption of ozone, increases running cost, and after this step process, multi-medium filtering product water turbidity is less than 1NTU;
Step 5, ozone oxidation system: multi-medium filtering produces water and enters ozone oxidation reaction tower, through oxidizing reaction after a while, the biodegradability that multi-medium filtering produces water is improved, and oxidation water outlet enters Buffer Pool makes residue ozone in water fully be degraded;
Step 6, secondary is biochemical: Buffer Pool water outlet enters secondary biochemical treatment, comprising: A+O+MBR, and here, the small organic molecule after chain rupture continues to be degraded;
Step 7, reverse osmosis system: MBR water outlet enters reverse osmosis desalination after being introduced into cartridge filter again, reverse osmosis system produces water direct reuse to desalted water station.
On the basis of technique scheme, the water quality characteristic of described oily(waste)water is: petroleum-type 200 ~ 150000mg/L, COD500 ~ 10000mg/L, specific conductivity 1000 ~ 5000 μ S/cm.
On the basis of technique scheme, the light oil injecting eddy flow extraction separator is reformate, petroleum naphtha, petroleum naphtha or kerosene.
On the basis of technique scheme, the optimum light oil injecting the handled oily waste water water yield 1% by mass percentage in eddy flow extraction separator.
On the basis of technique scheme, the rotor speed of eddy flow extraction separator is 200 ~ 2500rpm.
On the basis of technique scheme, inner circulating aerating biological filtering tank is isolated aeration, and wherein aeration riser tube aeration rate is 0.1 ~ 0.2Nm/min, and operation aeration rate is 0.08 ~ 0.1Nm/min.
On the basis of technique scheme, inner circulating aerating biological filtering tank filtering velocity is 10 ~ 30m/h.
On the basis of technique scheme, the circular flow of inner circulating aerating biological filtering tank: flooding quantity=2 ~ 8.
On the basis of technique scheme, in the aeration tank of inner circulating aerating biological filtering tank, load the organic-biological filtrate of lightweight, high cavity rate, high-ratio surface,
The design parameter of organic-biological filtrate is: particle diameter: 8 ~ 10mm, and specific surface area is 2.5 ~ 3.8 × 104cm
2/ g, porosity: 58 ~ 65%, tap density≤0.85t/m
3.
On the basis of technique scheme, the inner circulating aerating biological filtering tank residence time is 8 ~ 36h, and the BAF backwash cycle is 12 ~ 72h, backwash air quantity 3 ~ 5Nm/min, backwash time 1 ~ 12h, and backwash flow is 3 ~ 5 times of flooding quantity.
On the basis of technique scheme, in step 3, the anoxic process residence time 12 ~ 48h, dissolved oxygen 0.2 ~ 0.5mg/L, the aerobic process residence time 12 ~ 24h, dissolved oxygen 2 ~ 5mg/L, settling tank upflow velocity is 1 ~ 3m/h.
On the basis of technique scheme, in step 4, more medium filter filtering accuracy is 150 microns, loads crushed stone, quartz sand, hard coal successively from bottom to top in strainer, backwash cycle 30min, backwash time 10 ~ 30min.
On the basis of technique scheme, in step 5, ozone oxidation adopts reverse flow to run, and ozone concn is at 50mg/L ~ 100mg/L, and ozone oxidation time controling is at 1 ~ 15min.
On the basis of technique scheme, in step 5, reacting pipe and the device inwall of all flow of ozone warps all use PVDF material.
On the basis of technique scheme, in step 5, ozone oxidation water outlet is 0.5 ~ 1h in the Buffer Pool residence time.
On the basis of technique scheme, in step 6, the A pond residence time is 8 ~ 10h, the O pond residence time is 1 ~ 5h, and membrane cisterna working time is 20 ~ 40min.
On the basis of technique scheme, in step 6, MBR membrane material is PTFE or PVDF, membrane pore size 0.2 ~ 0.4 micron.
On the basis of technique scheme, in MBR membrane cisterna, sludge concentration is 8000 ~ 20000mg/L.
On the basis of technique scheme, cartridge filter filtering accuracy is 5 microns, and strainer adopts PE material filter core.
On the basis of technique scheme, reverse osmosis adopts polyamide composite film.
On the basis of technique scheme, reverse osmosis operating pressure is 8 ~ 16bar, and ratio of desalinization is greater than 95%, Water Sproading rate more than 75%.
The treatment for reuse method of oily(waste)water of the present invention, adopt light oil to carry out extracting and separating to the oil in oily(waste)water and remove most of oil in waste water, pass through oil and the organic matter's residual in inner circulating aerating biological filtering tank removed by filtration waste water again with stable back-end processing water quality, guarantee that the normal table of conventional biochemical process runs, after traditional biochemical treatment, add reuse instead of discharge that oxidation+secondary biochemistry+desalinating process achieves final oily(waste)water.
The treatment for reuse method of oily(waste)water of the present invention, has following beneficial effect:
1, high for oily(waste)water oil-contg and the large water quality characteristics that fluctuates, by adding light oil in waste water, eddy flow extraction and separation technology is adopted to realize effectively being separated of oily waste water oil-in-water and water, oil after separation directly can be recycled into electric desalting outlet, realize the secondary recovery of oil, the impact of oil to whole oil-contained waste water treatment system can be avoided through this step process;
2, inner circulating aerating biological filtering tank improves treatment effect and the shock resistance of oil-contained waste water treatment system with the feature of the operation scheme of its uniqueness (isolated aeration) and large discharge backwash, and water outlet can directly enter conventional biochemical treatment system; Inner circulating aerating biological filtering tank realizes waste water in the abundant circulation of inside, biological filter and then make Organic Pollutants in Wastewater obtain depth degradation, improves the water quality of oily(waste)water further, stablizes biochemical influent quality;
3, traditional biochemical processing process removes the organic pollutant of most of bio-degradable in oily(waste)water of the present invention; The conventional biochemical treatment process process remained in waste water larger molecular organics not can be carried out chain rupture (high-concentrated ozone of employing and pollutent contact with the oxidation of ozone short period of time the chain rupture realizing larger molecular organics in oily(waste)water) through ozone oxidation by conventional biochemical process water outlet, and oxidation water outlet flows through Buffer Pool and residue ozone in waste water is fully degraded;
4, enter secondary biochemical treatment system through the small organic molecule of oxidative degradation to be removed further, produce water through reverse osmosis desalination can direct reuse to desalted water station; Secondary biochemistry adopts A/O/MBR, makes waste water small molecular organism under higher sludge concentration by efficient degradation; Through reverse osmosis desalination process, the product water of more than 75% can direct reuse.
Accompanying drawing explanation
The present invention has following accompanying drawing:
Fig. 1 present invention process schematic flow sheet.
Embodiment
Below in conjunction with accompanying drawing, the present invention is described in further detail.
As shown in Figure 1, the treatment for reuse method of oily(waste)water of the present invention, for being used by oily(waste)water to greatest extent, " eddy flow extracting and separating+inner circulating aerating biological filtering tank+conventional biochemical+multi-medium filtering+ozone oxidation/Buffer Pool+secondary biochemistry+reverse osmosis system " technique is adopted to process oily(waste)water.
On the basis of technique scheme, specifically comprise the following steps:
Step 1, eddy flow extracting and separating: oily(waste)water enters eddy flow extraction separator through pump pressurization, injects the light oil of the handled oily waste water water yield 0.5 ~ 5% simultaneously by mass percentage in eddy flow extraction separator,
Light oil and the oily(waste)water with density difference produce Taylor vortex flow along with the rotor high-speed in separator rotates mixing, realize the separation of oil, water,
The water ratio of isolated oil phase is less than 0.5% (mass percent), and total dissolved solid concentration is less than 20mg/L, directly can be recycled into electric desalting outlet,
Isolate oil concentration in aqueous phase and be less than 100mg/L;
Step 2, inner circulating aerating biological filtering tank: in the aqueous phase that eddy flow extracting and separating obtains and inner circulating aerating biological filtering tank, sewage sucks recirculation reactor in the lump through back window, and in this mixing oxygenation, then from the outflow suitable for reading of aeration riser tube, flow into bottom pond through return line again, enter biochemical areas (biologic packing material bed) and carry out bio-oxidation, filtration, biological adsorption;
When strengthening aeration, the bubbles volume of generation increases, and the water that mixing is floated is also along with increasing, and quantity of circulating water increases, then the number of times circulated is more, and the microorganism adsorption in filled and the chance of degraded increase greatly, and the organic pollutant removal rate of last water outlet is just large;
When being increased to certain cycle index, not obvious to the clearance change of organic pollutant;
Due to retaining of biomembranous growth and packing layer, after running certain hour, back flushing need be carried out to packing layer, make it Recovery processing efficiency again;
Step 3, conventional biochemical: inner circulating aerating biological filtering tank water outlet directly enters conventional biochemical process, this biochemical treatment comprises anoxic+aerobic+settling tank, and in inner circulating aerating biological filtering tank water outlet, most of biodegradable organic is removed through conventional biochemical process;
Step 4, multi-medium filtering: multi-medium filtering can remove the suspended substance in settling tank water outlet further, avoids reducing substances residual in settling tank water outlet to the consumption of ozone, increases running cost, and after this step process, multi-medium filtering product water turbidity is less than 1NTU;
Step 5, ozone oxidation system: multi-medium filtering produces water and enters ozone oxidation reaction tower, through oxidizing reaction after a while, the biodegradability that multi-medium filtering produces water is improved, and oxidation water outlet enters Buffer Pool makes residue ozone in water fully be degraded;
Step 6, secondary is biochemical: Buffer Pool water outlet enters secondary biochemical treatment, comprising: A+O+MBR (anoxic+aerobic+membrane bioreactor), and here, the small organic molecule after chain rupture continues to be degraded;
Step 7, reverse osmosis system: MBR water outlet enters reverse osmosis desalination after being introduced into cartridge filter again, reverse osmosis system produces water direct reuse to desalted water station.
Described oily(waste)water is by above-mentioned steps process, and Water Sproading rate is greater than 75%.
On the basis of technique scheme, the water quality characteristic of described oily(waste)water is: petroleum-type 200 ~ 150000mg/L, COD500 ~ 10000mg/L, specific conductivity 1000 ~ 5000 μ S/cm.
On the basis of technique scheme, in step 1, the light oil injecting eddy flow extraction separator is reformate, petroleum naphtha, petroleum naphtha or kerosene, and optimum is kerosene.
On the basis of technique scheme, in step 1, the optimum light oil injecting the handled oily waste water water yield 1% by mass percentage in eddy flow extraction separator.
On the basis of technique scheme, in step 1, the rotor speed of eddy flow extraction separator is 200 ~ 2500rpm, and optimum is 960rpm.
On the basis of technique scheme, in step 2, inner circulating aerating biological filtering tank is isolated aeration, and wherein aeration riser tube aeration rate is 0.1 ~ 0.2Nm/min, and operation aeration rate is 0.08 ~ 0.1Nm/min.
On the basis of technique scheme, in step 2, inner circulating aerating biological filtering tank filtering velocity is 10 ~ 30m/h, and optimum is 25m/h.
On the basis of technique scheme, in step 2, the circular flow of inner circulating aerating biological filtering tank: flooding quantity=2 ~ 8, optimum is 5.5.
On the basis of technique scheme, in step 2, in the aeration tank of inner circulating aerating biological filtering tank, load the organic-biological filtrate of lightweight, high cavity rate, high-ratio surface,
The design parameter of organic-biological filtrate is: particle diameter: 8 ~ 10mm, and specific surface area is 2.5 ~ 3.8 × 104cm
2/ g, porosity: 58 ~ 65%, tap density≤0.85t/m
3.
On the basis of technique scheme, in step 2, the inner circulating aerating biological filtering tank residence time is 8 ~ 36h, optimum is 12h, and the BAF backwash cycle is 12 ~ 72h, and optimum is 48h, backwash air quantity 3 ~ 5Nm/min, backwash time 1 ~ 12h, optimum is 1 ~ 2h, and backwash flow is 3 ~ 5 times of flooding quantity.
On the basis of technique scheme, in step 3, the anoxic process residence time 12 ~ 48h, dissolved oxygen 0.2 ~ 0.5mg/L, the aerobic process residence time 12 ~ 24h, dissolved oxygen 2 ~ 5mg/L, settling tank upflow velocity is 1 ~ 3m/h.
On the basis of technique scheme, in step 4, more medium filter filtering accuracy is 150 microns, loads crushed stone, quartz sand, hard coal successively from bottom to top in strainer, backwash cycle 30min, backwash time 10 ~ 30min.
On the basis of technique scheme, in step 5, ozone oxidation adopts reverse flow to run, and ozone concn is at 50mg/L ~ 100mg/L, and ozone oxidation time controling is at 1 ~ 15min.
On the basis of technique scheme, in step 5, reacting pipe and the device inwall of all flow of ozone warps all use PVDF material.
On the basis of technique scheme, in step 5, ozone oxidation water outlet is 0.5 ~ 1h in the Buffer Pool residence time.
On the basis of technique scheme, in step 6, the A pond residence time is 8 ~ 10h, the O pond residence time is 1 ~ 5h, and membrane cisterna working time is 20 ~ 40min, and optimum is 30min.
On the basis of technique scheme, in step 6, MBR membrane material is PTFE (tetrafluoroethylene) or PVDF (polyvinylidene difluoride (PVDF)), membrane pore size 0.2 ~ 0.4 micron.
On the basis of technique scheme, in step 6, in MBR membrane cisterna, sludge concentration is 8000 ~ 20000mg/L.
On the basis of technique scheme, in step 7, cartridge filter filtering accuracy is 5 microns, and strainer adopts PE material filter core.
On the basis of technique scheme, in step 7, reverse osmosis adopts polyamide composite film.
On the basis of technique scheme, in step 7, reverse osmosis operating pressure is 8 ~ 16bar, and ratio of desalinization is greater than 95%, Water Sproading rate more than 75%.
Below, by reference to the accompanying drawings and specific embodiment, invention is further described.
Embodiment 1,2,3
Certain Petrochemical Enterprises oily(waste)water, water quality situation is in table 1
Table 1 oily(waste)water water quality
Adopt method of the present invention:
(1) oily(waste)water enters eddy flow extraction separator through pump pressurization, injects the light oil of the handled oily waste water water yield 0.5 ~ 5% by mass percentage in eddy flow extraction separator simultaneously,
Be separated through eddy flow extraction separator high speed rotating, realize the high efficiency separation of oil, water, be separated oil concentration in the aqueous phase obtained and be less than 100mg/L;
(2) aqueous phase obtained through eddy flow extracting and separating filters through inner circulating aerating biological filtering tank, and in waste water, most of oil and the organic matter's is removed further;
(3) inner circulating aerating biological filtering tank water outlet directly enters conventional biochemical process, and this biochemical treatment comprises anoxic+aerobic+settling tank, and in waste water, most of biodegradable organic pollutant is degraded through conventional biochemical process;
(4) multi-medium filtering can remove the suspended substance in waste water further, avoids reducing substances wherein to the consumption of ozone, increases running cost, and after this step process, multi-medium filtering product water turbidity is less than 1NTU;
(5) ozone oxidation/Buffer Pool: multi-medium filtering produces water and enters ozone oxidation reaction tower, and through oxidizing reaction after a while, high oily wastewater biodegradability is improved, oxidation water outlet flows through Buffer Pool makes residue ozone fully be degraded;
(6) secondary is biochemical: Buffer Pool water outlet enters secondary biochemical treatment, comprising: anoxic+aerobic+MBR, and here, the small organic molecule after chain rupture continues to be degraded;
(7) reverse osmosis: secondary bio-chemical effluent enters reverse osmosis desalination, produces water direct reuse to desalted water station.
In embodiment, each processing unit operational condition and treatment effect are as shown in table 2, table 3:
The each embodiment operational condition of table 2
Each cell processing effect in table 3 embodiment
The content be not described in detail in this specification sheets belongs to the known prior art of professional and technical personnel in the field.
Claims (24)
1. a treatment for reuse method for oily(waste)water, is characterized in that: adopt " eddy flow extracting and separating+inner circulating aerating biological filtering tank+conventional biochemical+multi-medium filtering+ozone oxidation/Buffer Pool+secondary biochemistry+reverse osmosis system " technique to process oily(waste)water.
2. the treatment for reuse method of oily(waste)water as claimed in claim 1, is characterized in that: described oily(waste)water is oil refining enterprise's oily(waste)water.
3. the treatment for reuse method of oily(waste)water as claimed in claim 2, is characterized in that: described oil refining enterprise oily(waste)water refers to asphalt production device Atmospheric vacuum electric desalting draining, machinery electric desalting draining and its Future about Alkaline Residue Treatment Unit mixing draining of sulphur workshop.
4. the treatment for reuse method of oily(waste)water as claimed in claim 1, is characterized in that, specifically comprise the following steps:
Step 1, eddy flow extracting and separating: oily(waste)water enters eddy flow extraction separator through pump pressurization, injects the light oil of the handled oily waste water water yield 0.5 ~ 5% simultaneously by mass percentage in eddy flow extraction separator,
Light oil and the oily(waste)water with density difference produce Taylor vortex flow along with the rotor high-speed in separator rotates mixing, realize the separation of oil, water,
The water ratio of isolated oil phase is less than 0.5%, and total dissolved solid concentration is less than 20mg/L, directly can be recycled into electric desalting outlet,
Isolate oil concentration in aqueous phase and be less than 100mg/L;
Step 2, inner circulating aerating biological filtering tank: in the aqueous phase that eddy flow extracting and separating obtains and inner circulating aerating biological filtering tank, sewage sucks recirculation reactor in the lump through back window, and in this mixing oxygenation, then from the outflow suitable for reading of aeration riser tube, flow into bottom pond through return line again, enter biochemical areas and carry out bio-oxidation, filtration, biological adsorption;
Due to retaining of biomembranous growth and packing layer, after running certain hour, back flushing need be carried out to packing layer, make it Recovery processing efficiency again;
Step 3, conventional biochemical: inner circulating aerating biological filtering tank water outlet directly enters conventional biochemical process, this biochemical treatment comprises anoxic+aerobic+settling tank, and in inner circulating aerating biological filtering tank water outlet, most of biodegradable organic is removed through conventional biochemical process;
Step 4, multi-medium filtering: multi-medium filtering can remove the suspended substance in settling tank water outlet further, avoids reducing substances residual in settling tank water outlet to the consumption of ozone, increases running cost, and after this step process, multi-medium filtering product water turbidity is less than 1NTU;
Step 5, ozone oxidation system: multi-medium filtering produces water and enters ozone oxidation reaction tower, through oxidizing reaction after a while, the biodegradability that multi-medium filtering produces water is improved, and oxidation water outlet enters Buffer Pool makes residue ozone in water fully be degraded;
Step 6, secondary is biochemical: Buffer Pool water outlet enters secondary biochemical treatment, comprising: A+O+MBR, and here, the small organic molecule after chain rupture continues to be degraded;
Step 7, reverse osmosis system: MBR water outlet enters reverse osmosis desalination after being introduced into cartridge filter again, reverse osmosis system produces water direct reuse to desalted water station.
5. the treatment for reuse method of oily(waste)water as claimed in claim 4, is characterized in that: the water quality characteristic of described oily(waste)water is: petroleum-type 200 ~ 150000mg/L, COD500 ~ 10000mg/L, specific conductivity 1000 ~ 5000 μ S/cm.
6. the treatment for reuse method of oily(waste)water as claimed in claim 4, is characterized in that: the light oil injecting eddy flow extraction separator is reformate, petroleum naphtha, petroleum naphtha or kerosene.
7. the treatment for reuse method of oily(waste)water as claimed in claim 4, is characterized in that: the optimum light oil injecting the handled oily waste water water yield 1% by mass percentage in eddy flow extraction separator.
8. the treatment for reuse method of oily(waste)water as claimed in claim 4, is characterized in that: the rotor speed of eddy flow extraction separator is 200 ~ 2500rpm.
9. the treatment for reuse method of oily(waste)water as claimed in claim 4, it is characterized in that: inner circulating aerating biological filtering tank is isolated aeration, wherein aeration riser tube aeration rate is 0.1 ~ 0.2Nm/min, and operation aeration rate is 0.08 ~ 0.1Nm/min.
10. the treatment for reuse method of oily(waste)water as claimed in claim 4, is characterized in that: inner circulating aerating biological filtering tank filtering velocity is 10 ~ 30m/h.
The treatment for reuse method of 11. oily(waste)waters as claimed in claim 4, is characterized in that: the circular flow of inner circulating aerating biological filtering tank: flooding quantity=2 ~ 8.
The treatment for reuse method of 12. oily(waste)waters as claimed in claim 4, is characterized in that: the organic-biological filtrate loading lightweight, high cavity rate, high-ratio surface in the aeration tank of inner circulating aerating biological filtering tank,
The design parameter of organic-biological filtrate is: particle diameter: 8 ~ 10mm, and specific surface area is 2.5 ~ 3.8 × 104cm
2/ g, porosity: 58 ~ 65%, tap density≤0.85t/m
3.
The treatment for reuse method of 13. oily(waste)waters as claimed in claim 4, it is characterized in that: the inner circulating aerating biological filtering tank residence time is 8 ~ 36h, the BAF backwash cycle is 12 ~ 72h, backwash air quantity 3 ~ 5Nm/min, backwash time 1 ~ 12h, backwash flow is 3 ~ 5 times of flooding quantity.
The treatment for reuse method of 14. oily(waste)waters as claimed in claim 4, is characterized in that: in step 3, the anoxic process residence time 12 ~ 48h, dissolved oxygen 0.2 ~ 0.5mg/L, the aerobic process residence time 12 ~ 24h, dissolved oxygen 2 ~ 5mg/L, settling tank upflow velocity is 1 ~ 3m/h.
The treatment for reuse method of 15. oily(waste)waters as claimed in claim 4, it is characterized in that: in step 4, more medium filter filtering accuracy is 150 microns, loads crushed stone, quartz sand, hard coal successively from bottom to top in strainer, backwash cycle 30min, backwash time 10 ~ 30min.
The treatment for reuse method of 16. oily(waste)waters as claimed in claim 4, is characterized in that: in step 5, and ozone oxidation adopts reverse flow to run, and ozone concn is at 50mg/L ~ 100mg/L, and ozone oxidation time controling is at 1 ~ 15min.
The treatment for reuse method of 17. oily(waste)waters as claimed in claim 4, is characterized in that: in step 5, reacting pipe and the device inwall of all flow of ozone warps all use PVDF material.
The treatment for reuse method of 18. oily(waste)waters as claimed in claim 4, it is characterized in that: in step 5, ozone oxidation water outlet is 0.5 ~ 1h in the Buffer Pool residence time.
The treatment for reuse method of 19. oily(waste)waters as claimed in claim 4, is characterized in that: in step 6, the A pond residence time is 8 ~ 10h, the O pond residence time is 1 ~ 5h, and membrane cisterna working time is 20 ~ 40min.
The treatment for reuse method of 20. oily(waste)waters as claimed in claim 4, it is characterized in that: in step 6, MBR membrane material is PTFE or PVDF, membrane pore size 0.2 ~ 0.4 micron.
The treatment for reuse method of 21. oily(waste)waters as claimed in claim 4, is characterized in that: in MBR membrane cisterna, sludge concentration is 8000 ~ 20000mg/L.
The treatment for reuse method of 22. oily(waste)waters as claimed in claim 4, is characterized in that: cartridge filter filtering accuracy is 5 microns, and strainer adopts PE material filter core.
The treatment for reuse method of 23. oily(waste)waters as claimed in claim 4, is characterized in that: reverse osmosis adopts polyamide composite film.
The treatment for reuse method of 24. oily(waste)waters as claimed in claim 4, is characterized in that: reverse osmosis operating pressure is 8 ~ 16bar, and ratio of desalinization is greater than 95%, Water Sproading rate more than 75%.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201410385576.4A CN105399265B (en) | 2014-08-07 | 2014-08-07 | A kind for the treatment of for reuse method of oily waste water |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201410385576.4A CN105399265B (en) | 2014-08-07 | 2014-08-07 | A kind for the treatment of for reuse method of oily waste water |
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| Publication Number | Publication Date |
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Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105753255A (en) * | 2016-04-07 | 2016-07-13 | 桑德集团有限公司 | Advanced treatment recycling system for industrial park wastewater |
| CN109081531A (en) * | 2018-10-23 | 2018-12-25 | 广东欧沃环境科技有限公司 | A kind of oiliness sewage treatment device |
| CN111170494A (en) * | 2018-11-12 | 2020-05-19 | 中国石油天然气股份有限公司 | Treatment device for circulating water discharged sewage |
| CN112744982A (en) * | 2020-12-25 | 2021-05-04 | 西华师范大学 | Water treatment system based on reverse osmosis technology and treatment method thereof |
| CN115196812A (en) * | 2021-04-08 | 2022-10-18 | 富钰精密组件（昆山）有限公司 | Wastewater treatment system and wastewater treatment method |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101708919A (en) * | 2009-11-16 | 2010-05-19 | 北京大学深圳研究生院 | Method for treating leachate in refuse landfill site |
| CN102515442A (en) * | 2011-12-29 | 2012-06-27 | 蓝星环境工程有限公司 | Treatment method for recycling complex waste water in coal chemical industry |
| CN102690016A (en) * | 2011-03-24 | 2012-09-26 | 中国石油化工股份有限公司 | Treatment recycle method of sewage from oil refinery |
| US20130313191A1 (en) * | 2009-05-14 | 2013-11-28 | Omni Water Solutions, Inc. | Water treatment systems and methods |
| CN203474604U (en) * | 2013-09-27 | 2014-03-12 | 厦门绿邦膜技术有限公司 | Waste water advanced treatment and recycling system for paper-making reconstituted tobacco |
-
2014
- 2014-08-07 CN CN201410385576.4A patent/CN105399265B/en active Active
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US20130313191A1 (en) * | 2009-05-14 | 2013-11-28 | Omni Water Solutions, Inc. | Water treatment systems and methods |
| CN101708919A (en) * | 2009-11-16 | 2010-05-19 | 北京大学深圳研究生院 | Method for treating leachate in refuse landfill site |
| CN102690016A (en) * | 2011-03-24 | 2012-09-26 | 中国石油化工股份有限公司 | Treatment recycle method of sewage from oil refinery |
| CN102515442A (en) * | 2011-12-29 | 2012-06-27 | 蓝星环境工程有限公司 | Treatment method for recycling complex waste water in coal chemical industry |
| CN203474604U (en) * | 2013-09-27 | 2014-03-12 | 厦门绿邦膜技术有限公司 | Waste water advanced treatment and recycling system for paper-making reconstituted tobacco |
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105753255A (en) * | 2016-04-07 | 2016-07-13 | 桑德集团有限公司 | Advanced treatment recycling system for industrial park wastewater |
| CN109081531A (en) * | 2018-10-23 | 2018-12-25 | 广东欧沃环境科技有限公司 | A kind of oiliness sewage treatment device |
| CN111170494A (en) * | 2018-11-12 | 2020-05-19 | 中国石油天然气股份有限公司 | Treatment device for circulating water discharged sewage |
| CN112744982A (en) * | 2020-12-25 | 2021-05-04 | 西华师范大学 | Water treatment system based on reverse osmosis technology and treatment method thereof |
| CN115196812A (en) * | 2021-04-08 | 2022-10-18 | 富钰精密组件（昆山）有限公司 | Wastewater treatment system and wastewater treatment method |
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