CN104045210A - Method for treating and recycling sewage of integrated oil-ethylene refining device - Google Patents
Method for treating and recycling sewage of integrated oil-ethylene refining device Download PDFInfo
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Abstract
The invention relates to a method for treating and recycling sewage of an integrated oil-ethylene refining device. The method for treating and recycling the sewage of the integrated oil-ethylene refining device comprises the following steps: (1) sequentially carrying out wet oxidation and SBR (sequencing batch reactor) treatment on oil refining caustic sludge waste water; (2) mixing ethylene caustic sludge waste water with circulating cooling water, sewage and waste water obtained through treatment in the step (1) after the wet oxidation treatment is carried out, sequentially treating the mixed sewage by virtue of a biological aerated filter and an advanced oxidation and biological aerated filter, mixing the treated mixed sewage with acid-alkali wastewater, and discharging; and (3) mixing with waste water with salt content less than or equal to 500mg/L, sequentially treating the mixed waste water by virtue of an oil removal tank, an air floatation tank, a biochemical tank and a biological aerated filter, sterilizing and filtering, and then recycling the treated waste water in a recirculating cooling water system. The method for treating and recycling the sewage of the integrated oil-ethylene refining device has the advantages that reuse rate of the sewage can be greatly increased, investment and running cost are low, and operation management is simple.
Description
Technical field
The present invention relates to the processing reuse method of oil refining-Ethylene Complex unit sewage.
Background technology
China is the country of a shortage of water resources, approximately 2200 cubic metres of water resources ownership per capitas, 1/4th of Jin You world mean number.Meanwhile, due to the growth of China's population, what water requirement had approached water resources can exploitation amount.
Petrochemical complex is one of five large high water consumption industries of China, and ethylene production water consumption is wherein particularly outstanding, and the production equipment of 1,000,000 tons of ethene of a set of annual output need be fetched water approximately 1,850 ten thousand tons/year, and sewer is approximately 1,200 ten thousand tons/year simultaneously.Huge water loss has not only restricted China's Ethylene Development, and is the serious waste to water resources.By reuse after the sewage disposal of ethylene industry, not only can solve the problem of environmental pollution of externally discharged waste water, and can significantly reduce water intaking, be saving water resource, the inevitable requirement that realizes Sustainable development.
The kind of ethylene plant's sewage is many, complicated component, and all kinds of sewage in the main Shi Jiang of existing treatment process ethylene plant mixes, then unified processing.At present, most ethylene plants still adopts " old three covers " the art breading combined sewage by oil removal, air supporting and biochemical composition, due to the impact of high-concentration sewage to biochemical system, use the sewage of " old three covers " art breading still can not stably reach national grade one discharge standard, more can not carry out reuse.Individual other enterprise carries out advanced treatment to sewage, can realize the part reuse of sewage, but its reusing sewage rate is also undesirable, and reusing sewage investment is large, running cost is high, without economic benefit.Some oil refining enterprise take the measure of " shunting of removing contamination, dirty dividing and ruling ", and high-concentration and low-concentration waste water is processed respectively, and overall process effect is better, but reusing sewage rate is still lower.It is to avoid the impact of high-concentration sewage to biochemical system that oil refining enterprise takes the main purpose of " shunting of removing contamination, dirty dividing and ruling ", makes the sewage after processing can stably reach national emission standard, is not the reuse for sewage.
In sum, guarantee externally discharged waste water can stably reaching standard, do not increase again under the prerequisite of excessive cost simultaneously, the reclamation rate that further improves sewage is an urgent demand of ethene enterprise.
Summary of the invention
The invention provides the processing reclaiming system of a kind of ethylene plant sewage and process reuse method, adopting this system and method, can increase substantially the reclamation rate of ethylene plant's sewage, and investment and running cost is lower, operational administrative is easy, technology is reliable.
The processing reclaiming system of ethylene plant's sewage, by the first sewage treatment unit and the second sewage treatment unit and reusing sewage unit, formed, the first sewage treatment unit comprises wet oxidation reaction device, the first BAF, advanced oxidation reactor and the second BAF in order, and the second sewage treatment unit comprises oil trap, air flotation pool, biochemistry pool and BAF in order; Wherein, the water outlet pipeline of the second sewage treatment unit and the inhalent siphon line of reusing sewage unit are connected, and water outlet pipeline and the recirculating cooling water system of reusing sewage unit are connected, and the inhalent siphon line of recirculated cooling water sewer pipeline and the first BAF is connected.
In preferred situation, recirculated cooling water sewer pipeline is also connected with the inhalent siphon line of the second sewage treatment unit.
A processing reuse method for ethylene plant's sewage, comprising:
(1) alkaline sewage, after wet oxidation is processed, mixes with recirculated cooling water sewer, the COD≤2000mg/L of combined sewage, and combined sewage after BAF, advanced oxidation and BAF are processed, mixes with acidic and alkaline waste water successively, discharge;
(2) waste water of salts contg≤500mg/L is mixed, after oil removal, air supporting, biochemistry, BAF are processed, carry out sterilization and filtration treatment successively, be then back to recirculating cooling water system.
In preferred situation, alkaline sewage, after wet oxidation is processed, mixes with part recirculated cooling water sewer; After the waste water of salts contg≤500mg/L mixes with another part recirculated cooling water sewer, then process.
In preferred situation, in step (1), alkaline sewage, after wet oxidation is processed, mixes with recirculated cooling water sewer, and the COD that makes combined sewage is 1500～2000mg/L.
Described wet oxidation (wet Oxida tion, abbreviation WO) belongs to prior art, and its common reaction conditions is: 120～350 ℃ of temperature, pressure 0.5～22MPa, residence time 15min～120min.
Described BAF (Biological Aerated Fil ter, abbreviation BAF) belong to prior art, the present invention can adopt conventional BAF, and the preferred inorganic filtrate of filtrate, as clay, haydite, volcanics, zeolite, fly ash grain etc.
Described oil trap, air flotation pool and biochemistry pool belong to routine techniques.Ethylene plant for having " old three covers " technique, can be used the technology and equipment of " old three overlap ".
Described reusing sewage unit is for carrying out sterilization and filtration treatment to sewage.
Described advanced oxidation refers in oxidising process, can produce hydroxyl radical free radical.According to the difference of oxygenant used, need to regulate the pH value of waste water.While adopting ozone to make oxygenant, the pH value of waste water is 7～12, preferably 8～11.While adopting potassium permanganate, chlorine to make oxygenant, the pH value of waste water is 1～7, preferably 2～6.While adopting hydrogen peroxide, dioxide peroxide or clorox to make oxygenant, the pH value of waste water is 1～7, is preferably 2～6.Described advanced oxidation comprises catalyzed oxidation, while being oxygenant as employing hydrogen peroxide, dioxide peroxide or clorox, also needs to add catalyzer, and described catalyzer can be selected from transition metal ion Fe
2+, Mn
2+, Ni
2+, Co
2+, Cd
2+, Cu
2+, Ag
+, Cr
3+and Zn
2+in one or more, also can be selected from metal oxide MnO
2, TO
2and Al
2o
3in one or more.
Advanced oxidation treating processes of the present invention is preferably under agitation carried out, and can adopt churned mechanically method, also can adopt in aeration agitation or beat the method that pump around circuit stirs.The time of oxidizing reaction can be 10～120 minutes, preferably 30～60 minutes.
Described advanced oxidation reactor refers to and can to sewage, carry out the reactor of advanced oxidation processing, and it belongs to prior art.The present invention preferably adopts reaction tank, more preferably adopts the reaction tank with whipping device.Described whipping device refers to the equipment that can produce mixing effect, device as anti-raw in mechanical stirring, aeration or recycle pump etc.
In the present invention, also can adopt the effect of one or more householder methods raising oxidizing reactions in photochemical catalysis, electrocatalysis, ultrasonically catalyzing, magnetic force catalysis, as: adopt the modes such as light+hydrogen peroxide, light+ozone, electricity+hydrogen peroxide to process waste water.
The present invention also provides a kind of processing reuse method of oil refining-Ethylene Complex unit sewage, comprising:
(1) oil refining alkaline sewage carries out wet oxidation successively, SBR processes;
(2) ethene alkaline sewage is after wet oxidation is processed, waste water after processing with recirculated cooling water sewer and step (1) mixes, make the COD≤2000mg/L of combined sewage, combined sewage is successively after BAF, advanced oxidation and BAF are processed, mix discharge with acidic and alkaline waste water;
(3) waste water of salts contg≤500mg/L is mixed, after oil removal, air supporting, biochemistry, BAF are processed, carry out sterilization and filtration treatment successively, be then back to recirculating cooling water system.
In preferred situation, ethene alkaline sewage, after wet oxidation is processed, mixes with the recirculated cooling water sewer of part and the waste water after step (1) processing; After the waste water of salts contg≤500mg/L mixes with another part recirculated cooling water sewer, then process.
In preferred situation, in step (2), ethene alkaline sewage is after wet oxidation is processed, and the waste water after processing with recirculated cooling water sewer and step (1) mixes, and the COD that makes combined sewage is 1500～2000mg/L.
The present invention also provides the processing reuse method of another kind of oil refining-Ethylene Complex unit sewage, comprising:
(1) will refine oil alkaline sewage mixes with ethene alkaline sewage, after wet oxidation is processed, mix with recirculated cooling water sewer again, make the COD≤2000mg/L of combined sewage, combined sewage is successively after BAF, advanced oxidation and BAF are processed, mix discharge with acidic and alkaline waste water;
(2) waste water of salts contg≤500mg/L is mixed, after oil removal, air supporting, biochemistry, BAF are processed, carry out sterilization and filtration treatment successively, be then back to recirculating cooling water system.
In preferred situation, the alkaline sewage of refining oil mixes with ethene alkaline sewage, after wet oxidation is processed, mixes with the recirculated cooling water sewer of part; After the waste water of salts contg≤500mg/L mixes with another part recirculated cooling water sewer, then process.
In preferred situation, in step (1), the alkaline sewage of refining oil mixes with ethene alkaline sewage, after wet oxidation is processed, then mixes with recirculated cooling water sewer, and the COD that makes combined sewage is 1500～2000mg/L.
SBR belongs to prior art, is again continuous batch of formula bio-reactor, activated sludge reactor intermittently, has the feature of plug-flow, anaerobic-aerobic operation, brief water inlet concurrently, is a kind of simple and easy, low consumption and sewage-treating reactor fast.
Described oil refining-Ethylene Complex unit refers to that oil refining apparatus and ethylene unit share a set of general facilities, as common recycle water system and steam system etc.
In prior art, after all ethene sewage is mixed, unified processing.Bring thus two main problems, the one, the impact of high-concentration sewage to biochemical system, causes the effluent quality of biochemical system unstable, even likely causes the sewage can not qualified discharge; The 2nd, combined sewage, after ethylene plant " old three cover " art breading, can not carry out reuse, although can realize the part reuse of sewage by increasing advanced treatment facility, reusing sewage rate is still undesirable and cost is too high.Contriver investigates and has analyzed water supply, water, sewage and the Sewage treatment systems of existing ethene enterprise all sidedly, by lot of experiments, has proposed above-mentioned technical solution.In the sewage of ethylene production, alkaline sewage and acidic and alkaline waste water account for 5% of sewage total amount, but saltiness accounts for the more than 50% of sewage total salinity, and wherein the COD of acidic and alkaline waste water is very low, and the COD of alkaline sewage is very high.The present invention separates the alkaline sewage of high COD concentration and high saliferous, by the combination of oxidation style and biochemical process, processes separately, finally realizes stably reaching standard discharge.In ethylene production, the circulating cooling water yield accounts for 96% of ethylene production total water amount, and water withdrawal accounts for 70% of the total water withdrawal of ethylene production, and recirculated cooling water is lower to the requirement of reuse water quality.Other sewage of ethylene production (not comprising recirculated cooling water sewer), salts contg is lower, although indivedual sewage COD concentration is higher, but after these sewage mix, average COD is not high, can pass through the treatment process of ethylene plant's routine, and increase BAF treatment process one, meet the reuse requirement of recirculated cooling water.The present invention mixes other sewage of ethylene production with recirculated cooling water sewer, after the conventional sewage treatment process in ethylene plant (" old three covers " technique) and BAF processing, be back to recirculated cooling water sewer, thereby significantly improved the reclamation rate of ethylene plant's sewage.
Compare with existing ethene sewage reuse techuique, the present invention has the following advantages:
1. the reusing sewage rate of prior art is generally no more than 70%, and reusing sewage rate of the present invention can reach more than 70%, the highlyest can reach 95% left and right.In addition, the present invention can also avoid the impact of high-concentration sewage to biochemical system, realizes the stably reaching standard discharge of sewage.
2. prior art need to could realize reusing sewage by complicated desalinating process, and technical process is long, technical difficulty is large, and reliability is poor.The inventive method does not need sewage to carry out desalting treatment, thereby has greatly shortened sewage recycling process flow process, make technology more simply, more reliable.
3. prior art need to be carried out the reuse that advanced treatment could realize sewage to a large amount of combined sewages, and technical difficulty is large, technical process is long, working cost is high, unreasonable economically.The present invention carries out sub-prime processing to sewage, has significantly reduced difficult sewage quantity, avoided complicated desalting treatment simultaneously, shortened technical process, so working cost is lower, more reasonable economically.
4. large, the technical process length of the difficulty of prior art, complicated operation, floor space are large, and the difficulty of therefore implementing is larger.The present invention, owing to taking sewage sub-prime to process, has significantly reduced difficult sewage quantity, has avoided desalting treatment, only needs newly-built a small amount of facility (can utilize existing " old three covers " technique), therefore implements to be more prone to.
Accompanying drawing explanation
Fig. 1 is the Sewage treatment systems schematic diagram of comparative example 1.
Fig. 2 is the Sewage treatment systems schematic diagram of embodiment 1.
Fig. 3 is the Sewage treatment systems schematic diagram of comparative example 2.
Fig. 4 is the Sewage treatment systems schematic diagram of embodiment 2.
Fig. 5 is the Sewage treatment systems schematic diagram of comparative example 3.
Fig. 6 is the Sewage treatment systems schematic diagram of embodiment 3.
Fig. 7 is the Sewage treatment systems schematic diagram of embodiment 4.
Embodiment
Below in conjunction with accompanying drawing, describe the present invention in detail.
As shown in Figure 2, one embodiment of the present invention are: in ethylene plant's sewage, the hyposaline waste water of all saltiness≤500mg/L mixes with part recirculated cooling water sewer, entering successively oil trap, air flotation pool, biochemistry pool, BAF processes, sewage after processing enters reusing sewage unit to carry out, after sterilization, filtration, entering circulating water cooling system; Ethylene plant's alkaline sewage is after wet oxidation is processed, mix with another part recirculated cooling water sewer, through BAF, catalyzed oxidation (advanced oxidation a kind of) and BAF, process successively, the sewage after processing mixes with acidic and alkaline waste water afterwards and discharges.
As shown in Figure 6, another two kinds of embodiments of the present invention are: in ethylene plant's sewage, the hyposaline waste water of all saltiness≤500mg/L enters successively oil trap, air flotation pool, biochemistry pool, BAF and processes, sewage after processing enters reusing sewage unit to carry out, after sterilization, filtration, entering circulating water cooling system; Ethylene plant's alkaline sewage, after wet oxidation is processed, mixes with recirculated cooling water sewer, processes successively through BAF, catalyzed oxidation (advanced oxidation a kind of) and BAF, and the sewage after processing mixes with acidic and alkaline waste water afterwards and discharges.
Further illustrate by the following examples the present invention.
Comparative example 1
The large-scale ethylene producing device of certain throughput 1,000,000 t/a, the surface water of use saliferous 150mg/L, water intaking 1,850 ten thousand m
3/ a, wherein recirculating cooling water system water intaking 1,400 ten thousand m
3/ a.Total sewer 1,200 ten thousand m
3/ a, wherein alkaline sewage 120,000 m of saliferous 22000mg/L, COD20000-50000mg/L
3/ a, acidic and alkaline waste water 300,000 m of saliferous 48000mg/L
3/ a, recirculating cooling water system sewer 2,200,000 m of saliferous 1250mg/L
3/ a, the waste water that other saliferous are less than 500mg/L amounts to 9,380,000 m
3/ a.
As shown in Figure 1, all waste water is mixed, carry out oil removal-air supporting-biochemical treatment, water outlet saltiness is 2040mg/L, COD < 100mg/L, saltiness and COD amount, can not direct reuses all over recirculated water reuse index request (saltiness≤1200mg/L, COD≤60mg/L).
Embodiment 1
The situation of ethylene producing device and various sewage is identical with comparative example 1.
As shown in Figure 2, alkaline sewage, acidic and alkaline waste water and part recirculated cooling water sewer are cut out from Waste Water Treatment; 120000 m
3the alkaline sewage of/a is after wet oxidation is processed, with 800,000 m
3the recirculated cooling water sewer of/a mixes, mixed COD < 1000mg/L, combined sewage adopts " BAF+ catalyzed oxidation+BAF " art breading, water outlet again with 300,000 m
3discharge after the acidic and alkaline waste water of/a mixes, the COD < 60mg/L of sewage effluent, water quality reaches National Environmental first discharge standard; Wherein, after BAF processes for the first time, the B/C < 0.3 of sewage, COD < 200mg/L.
Saliferous is less than to 9,380,000 m of 500mg/L
3/ a waste water and 1,400,000 m
3/ a recirculating cooling water system sewer mixes, after the Sewage treatment systems in comparative example 1 is processed, adopt again BAF art breading, water outlet saltiness < 1200mg/L, COD < 60mg/L, after sterilization, filtering, fully recovering circulating water system, reusing sewage rate is 89.8%.
Comparative example 2
The large-scale petroleum chemical joint venture of certain oil-refining capacity 1,000 ten thousand t/a, ethylene production capacity 800,000 t/a, the surface water of use saliferous 250mg/L, water intaking 2,150 ten thousand m
3/ a, wherein recirculating cooling water system water intaking 1,450 ten thousand m
3/ a.Total sewer 1,250 ten thousand m
3/ a, wherein oil refining alkaline sewage 1.4 ten thousand m of saliferous 300000mg/L, COD150000-200000mg/L
3/ a, ethene alkaline sewage 8.6 ten thousand m of saliferous 45000mg/L, COD30000-70000mg/L
3acidic and alkaline waste water 430,000 m of/a, saliferous 46000mg/L
3/ a, recirculating cooling water system sewer 3,500,000 m of saliferous 1800mg/L
3/ a, other saliferous are less than waste water 8,470,000 m of 500mg/L
3/ a.
As shown in Figure 3, all waste water is mixed, carry out oil removal-air supporting-biochemical treatment, water outlet saliferous is 2770mg/L, COD < 100mg/L, saltiness and COD amount, can not direct reuses all over recirculated water reuse index request (saltiness≤1200mg/L, COD≤60mg/L).
Embodiment 2
The situation of production equipment and various sewage is identical with comparative example 2.
As shown in Figure 4, oil refining alkaline sewage, ethene alkaline sewage, acidic and alkaline waste water and part recirculated cooling water sewer are cut out to 1.4 ten thousand m that will process through " wet oxidation+SBR " from Waste Water Treatment
3/ a oil refining alkaline sewage, 8.6 ten thousand m that process through wet oxidation
31,500,000 m of/a ethene alkaline sewage and saliferous 1800mg/L
3/ a recirculating cooling water system sewer merges, and adopts " BAF+ catalyzed oxidation+BAF " technique to process, water outlet again with 430,000 m
3discharge after/a acidic and alkaline waste water merges, the COD < 60mg/L of sewage effluent, water quality reaches National Environmental first discharge standard; Wherein, after BAF processes for the first time, the B/C of sewage is 0.1-0.3, COD < 200mg/L.
Saliferous is less than to 8,470,000 m of 500mg/L
3/ a waste water and 2,000,000 m
3the blowdown of/a recirculating cooling water system mixes, after the Sewage treatment systems in comparative example 2 is processed, adopt again BAF art breading, water outlet saltiness < 1200mg/L, COD < 60mg/L, after sterilization, filtering, fully recovering circulating water system, reusing sewage rate is 83.8%.
Comparative example 3
The ethylene producing device of certain throughput 300,000 t/a, the surface water of use saliferous 450mg/L, water intaking 6,800,000 m
3/ a, wherein recirculating cooling water system water intaking 4,800,000 m
3/ a.Total sewer 3,500,000 m
3/ a, wherein alkaline sewage 4.5 ten thousand m of saliferous 30000mg/L, COD40000-80000mg/L
3acidic and alkaline waste water 110,000 m of/a, saliferous 50000mg/L
3/ a, recirculating cooling water system sewer 800,000 m of saliferous 3200mg/L
3/ a, the waste water that other saliferous are less than 500mg/L amounts to 254.5 ten thousand m
3/ a.
As shown in Figure 5, all waste water is mixed, carry out oil removal-air supporting-biochemical treatment, water outlet saltiness is 3050mg/L, COD < 100mg/L, saltiness and COD amount, can not direct reuses all over recirculated water reuse index request (saltiness≤1200mg/L, COD≤60mg/L).
Embodiment 3
The situation of ethylene producing device and various sewage is identical with comparative example 3.
As shown in Figure 6, alkaline sewage, acidic and alkaline waste water and part recirculated cooling water sewer are cut out from Waste Water Treatment; 4.5 ten thousand m
3/ a alkaline sewage is after wet oxidation is processed, with 800,000 m
3/ a recirculating cooling water system sewer mixes, mixed COD < 2000mg/L, combined sewage adopts " BAF+ catalyzed oxidation+BAF " art breading, water outlet again with 110,000 m
3discharge after/a acidic and alkaline waste water mixes, the COD < 60mg/L of sewage effluent, water quality reaches National Environmental first discharge standard; Wherein, after BAF processes for the first time, the B/C of sewage is 0.1-0.4, COD < 200mg/L.
Saliferous is less than 254.5 ten thousand m of 500mg/L
3/ a waste water, after the Sewage treatment systems of comparative example 3 is processed, then adopts BAF art breading, water outlet saltiness < 1200mg/L, COD < 60mg/L, after sterilization, filtering, fully recovering circulating water system, reusing sewage rate is 72.7%.
Embodiment 4
The situation of production equipment and various sewage is identical with comparative example 2.
As shown in Figure 7, oil refining alkaline sewage, ethene alkaline sewage, acidic and alkaline waste water and part recirculated cooling water sewer are cut out to 1.4 ten thousand m from Waste Water Treatment
3/ a oil refining alkaline sewage and 8.6 ten thousand m
3/ a ethene alkaline sewage mixes, after wet oxidation is processed, with 500,000 m of saliferous 1800mg/L
3/ a recirculating cooling water system sewer merges, and adopts " BAF+ catalyzed oxidation+BAF " technique to process, water outlet again with 430,000 m
3discharge after/a acidic and alkaline waste water merges, the COD < 60mg/L of sewage effluent, water quality reaches National Environmental first discharge standard; Wherein, after BAF processes for the first time, the B/C < 0.4 of sewage, COD < 200mg/L.
Saliferous is less than to 8,470,000 m of 500mg/L
3/ a waste water and 2,000,000 m
3the blowdown of/a recirculating cooling water system mixes, after the Sewage treatment systems in comparative example 2 is processed, adopt again BAF art breading, water outlet saltiness < 1200mg/L, COD < 60mg/L, after sterilization, filtering, fully recovering circulating water system, reusing sewage rate is 83.8%.
Claims (12)
1. a processing reuse method for oil refining-Ethylene Complex unit sewage, comprising:
(1) oil refining alkaline sewage carries out wet oxidation successively, SBR processes;
(2) ethene alkaline sewage is after wet oxidation is processed, waste water after processing with recirculated cooling water sewer and step (1) mixes, make the COD≤2000mg/L of combined sewage, combined sewage is successively after the first BAF, advanced oxidation and the second BAF are processed, mix discharge with acidic and alkaline waste water;
(3) waste water of salts contg≤500mg/L is mixed, after oil removal, air supporting, biochemistry, the 3rd BAF are processed, carry out sterilization and filtration treatment successively, be then back to recirculating cooling water system.
2. in accordance with the method for claim 1, it is characterized in that, ethene alkaline sewage, after wet oxidation is processed, mixes with the recirculated cooling water sewer of part and the waste water after step (1) processing; After the waste water of salts contg≤500mg/L mixes with another part recirculated cooling water sewer, then process.
3. in accordance with the method for claim 1, it is characterized in that, in step (2), ethene alkaline sewage is after wet oxidation is processed, waste water after processing with recirculated cooling water sewer and step (1) mixes, and the COD that makes combined sewage is 1500～2000mg/L.
4. in accordance with the method for claim 1, it is characterized in that, when sewage is carried out to advanced oxidation processing, adopting ozone to make oxygenant and regulate the pH value of waste water is 7～12.
5. in accordance with the method for claim 1, it is characterized in that, when sewage is carried out to advanced oxidation processing, adopting potassium permanganate or chlorine to make oxygenant and regulate the pH value of waste water is 1～7.
6. in accordance with the method for claim 1, it is characterized in that, when sewage is carried out to advanced oxidation processing, adopt hydrogen peroxide, dioxide peroxide or clorox to make oxygenant, regulate the pH value of waste water to be 1～7 and to add catalyzer, described catalyzer is selected from transition metal ion Fe
2+, Mn
2+, Ni
2+, Co
2+, Cd
2+, Cu
2+, Ag
+, Cr
3+and Zn
2+in one or more, or be selected from metal oxide MnO
2, TiO
2and Al
2o
3in one or more.
7. a processing reuse method for oil refining-Ethylene Complex unit sewage, comprising:
(1) will refine oil alkaline sewage mixes with ethene alkaline sewage, after wet oxidation is processed, mix with recirculated cooling water sewer again, make the COD≤2000mg/L of combined sewage, combined sewage is successively after the first BAF, advanced oxidation and the second BAF are processed, mix discharge with acidic and alkaline waste water;
(2) waste water of salts contg≤500mg/L is mixed, after oil removal, air supporting, biochemistry, the 3rd BAF are processed, carry out sterilization and filtration treatment successively, be then back to recirculating cooling water system.
8. in accordance with the method for claim 7, it is characterized in that, the alkaline sewage of refining oil mixes with ethene alkaline sewage, after wet oxidation is processed, mixes with the recirculated cooling water sewer of part; After the waste water of salts contg≤500mg/L mixes with another part recirculated cooling water sewer, then process.
9. in accordance with the method for claim 7, it is characterized in that, in step (1), the alkaline sewage of refining oil mixes with ethene alkaline sewage, after wet oxidation is processed, then mix with recirculated cooling water sewer, the COD that makes combined sewage is 1500～2000mg/L.
10. in accordance with the method for claim 7, it is characterized in that, when sewage is carried out to advanced oxidation processing, adopting ozone to make oxygenant and regulate the pH value of waste water is 7～12.
11. in accordance with the method for claim 7, it is characterized in that, when sewage is carried out to advanced oxidation processing, adopting potassium permanganate or chlorine to make oxygenant and regulate the pH value of waste water is 1～7.
12. in accordance with the method for claim 7, it is characterized in that, when sewage is carried out to advanced oxidation processing, adopt hydrogen peroxide, dioxide peroxide or clorox to make oxygenant, regulate the pH value of waste water to be 1～7 and to add catalyzer, described catalyzer is selected from transition metal ion Fe
2+, Mn
2+, Ni
2+, Co
2+, Cd
2+, Cu
2+, Ag
+, Cr
3+and Zn
2+in one or more, or be selected from metal oxide MnO
2, TiO
2and Al
2o
3in one or more.
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104478020A (en) * | 2014-12-09 | 2015-04-01 | 王宝辉 | High-efficiency gel and emulsion breaking, desulfurizing and sterilizing agent for oilfield fracturing flow-back fluid |
| CN112850944A (en) * | 2020-12-23 | 2021-05-28 | 苏州清然环保科技有限公司 | Method for treating waste alkali residue and waste water of ethylene |
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| CN112850944A (en) * | 2020-12-23 | 2021-05-28 | 苏州清然环保科技有限公司 | Method for treating waste alkali residue and waste water of ethylene |
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