CN105439370B - A kind of process of combination BAF processing refinery sewage - Google Patents
A kind of process of combination BAF processing refinery sewage Download PDFInfo
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- CN105439370B CN105439370B CN201410385565.6A CN201410385565A CN105439370B CN 105439370 B CN105439370 B CN 105439370B CN 201410385565 A CN201410385565 A CN 201410385565A CN 105439370 B CN105439370 B CN 105439370B
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- 239000010865 sewage Substances 0.000 title claims abstract description 98
- 238000000034 method Methods 0.000 title claims abstract description 58
- 230000008569 process Effects 0.000 title claims abstract description 43
- 238000012545 processing Methods 0.000 title claims abstract description 38
- 239000010802 sludge Substances 0.000 claims abstract description 76
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 70
- 230000003197 catalytic effect Effects 0.000 claims abstract description 36
- 238000006385 ozonation reaction Methods 0.000 claims abstract description 30
- 238000011282 treatment Methods 0.000 claims abstract description 15
- CBENFWSGALASAD-UHFFFAOYSA-N Ozone Chemical compound [O-][O+]=O CBENFWSGALASAD-UHFFFAOYSA-N 0.000 claims description 28
- 239000003921 oil Substances 0.000 claims description 27
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 claims description 24
- 238000007254 oxidation reaction Methods 0.000 claims description 21
- 238000001914 filtration Methods 0.000 claims description 19
- 230000003647 oxidation Effects 0.000 claims description 17
- 239000003054 catalyst Substances 0.000 claims description 16
- 238000011001 backwashing Methods 0.000 claims description 14
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- 230000000694 effects Effects 0.000 claims description 11
- 239000003344 environmental pollutant Substances 0.000 claims description 10
- TWNQGVIAIRXVLR-UHFFFAOYSA-N oxo(oxoalumanyloxy)alumane Chemical compound O=[Al]O[Al]=O TWNQGVIAIRXVLR-UHFFFAOYSA-N 0.000 claims description 10
- 231100000719 pollutant Toxicity 0.000 claims description 10
- 238000005273 aeration Methods 0.000 claims description 9
- RHZUVFJBSILHOK-UHFFFAOYSA-N anthracen-1-ylmethanolate Chemical compound C1=CC=C2C=C3C(C[O-])=CC=CC3=CC2=C1 RHZUVFJBSILHOK-UHFFFAOYSA-N 0.000 claims description 9
- 239000003830 anthracite Substances 0.000 claims description 9
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- 230000015556 catabolic process Effects 0.000 claims description 8
- 238000006731 degradation reaction Methods 0.000 claims description 8
- HNPSIPDUKPIQMN-UHFFFAOYSA-N dioxosilane;oxo(oxoalumanyloxy)alumane Chemical compound O=[Si]=O.O=[Al]O[Al]=O HNPSIPDUKPIQMN-UHFFFAOYSA-N 0.000 claims description 8
- 239000003380 propellant Substances 0.000 claims description 8
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- 239000001301 oxygen Substances 0.000 claims description 7
- 229910052760 oxygen Inorganic materials 0.000 claims description 7
- 230000006641 stabilisation Effects 0.000 claims description 7
- 238000011105 stabilization Methods 0.000 claims description 7
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 6
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 claims description 6
- 238000011068 loading method Methods 0.000 claims description 6
- 230000014759 maintenance of location Effects 0.000 claims description 6
- 229910052684 Cerium Inorganic materials 0.000 claims description 5
- RYGMFSIKBFXOCR-UHFFFAOYSA-N Copper Chemical compound [Cu] RYGMFSIKBFXOCR-UHFFFAOYSA-N 0.000 claims description 5
- 229910002651 NO3 Inorganic materials 0.000 claims description 5
- NHNBFGGVMKEFGY-UHFFFAOYSA-N Nitrate Chemical compound [O-][N+]([O-])=O NHNBFGGVMKEFGY-UHFFFAOYSA-N 0.000 claims description 5
- 229910052802 copper Inorganic materials 0.000 claims description 5
- 239000010949 copper Substances 0.000 claims description 5
- ATRRKUHOCOJYRX-UHFFFAOYSA-N Ammonium bicarbonate Chemical compound [NH4+].OC([O-])=O ATRRKUHOCOJYRX-UHFFFAOYSA-N 0.000 claims description 4
- XSQUKJJJFZCRTK-UHFFFAOYSA-N Urea Chemical compound NC(N)=O XSQUKJJJFZCRTK-UHFFFAOYSA-N 0.000 claims description 4
- 239000001099 ammonium carbonate Substances 0.000 claims description 4
- 235000012501 ammonium carbonate Nutrition 0.000 claims description 4
- 239000004202 carbamide Substances 0.000 claims description 4
- 229910052799 carbon Inorganic materials 0.000 claims description 4
- 239000012876 carrier material Substances 0.000 claims description 4
- 230000008859 change Effects 0.000 claims description 4
- 238000009833 condensation Methods 0.000 claims description 4
- 230000005494 condensation Effects 0.000 claims description 4
- 238000001035 drying Methods 0.000 claims description 4
- 238000005188 flotation Methods 0.000 claims description 4
- 230000009471 action Effects 0.000 claims description 3
- GWXLDORMOJMVQZ-UHFFFAOYSA-N cerium Chemical compound [Ce] GWXLDORMOJMVQZ-UHFFFAOYSA-N 0.000 claims description 3
- 239000003795 chemical substances by application Substances 0.000 claims description 3
- 229910017052 cobalt Inorganic materials 0.000 claims description 3
- 239000010941 cobalt Substances 0.000 claims description 3
- GUTLYIVDDKVIGB-UHFFFAOYSA-N cobalt atom Chemical compound [Co] GUTLYIVDDKVIGB-UHFFFAOYSA-N 0.000 claims description 3
- 238000011109 contamination Methods 0.000 claims description 3
- 238000011010 flushing procedure Methods 0.000 claims description 3
- 239000007789 gas Substances 0.000 claims description 3
- 239000004519 grease Substances 0.000 claims description 3
- JEGUKCSWCFPDGT-UHFFFAOYSA-N h2o hydrate Chemical group O.O JEGUKCSWCFPDGT-UHFFFAOYSA-N 0.000 claims description 3
- 229910052742 iron Inorganic materials 0.000 claims description 3
- WPBNNNQJVZRUHP-UHFFFAOYSA-L manganese(2+);methyl n-[[2-(methoxycarbonylcarbamothioylamino)phenyl]carbamothioyl]carbamate;n-[2-(sulfidocarbothioylamino)ethyl]carbamodithioate Chemical compound [Mn+2].[S-]C(=S)NCCNC([S-])=S.COC(=O)NC(=S)NC1=CC=CC=C1NC(=S)NC(=O)OC WPBNNNQJVZRUHP-UHFFFAOYSA-L 0.000 claims description 3
- 238000004519 manufacturing process Methods 0.000 claims description 3
- 239000002808 molecular sieve Substances 0.000 claims description 3
- 239000002957 persistent organic pollutant Substances 0.000 claims description 3
- 230000035484 reaction time Effects 0.000 claims description 3
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- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 claims description 3
- 229910052723 transition metal Inorganic materials 0.000 claims description 3
- 230000032696 parturition Effects 0.000 claims 1
- 230000008901 benefit Effects 0.000 abstract description 3
- 239000008235 industrial water Substances 0.000 abstract description 2
- 238000004062 sedimentation Methods 0.000 description 5
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- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 description 2
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- 239000002253 acid Substances 0.000 description 2
- 150000007513 acids Chemical class 0.000 description 2
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- 241000894006 Bacteria Species 0.000 description 1
- MYMOFIZGZYHOMD-UHFFFAOYSA-N Dioxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 description 1
- 241000196324 Embryophyta Species 0.000 description 1
- PWHULOQIROXLJO-UHFFFAOYSA-N Manganese Chemical compound [Mn] PWHULOQIROXLJO-UHFFFAOYSA-N 0.000 description 1
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Landscapes
- Treatment Of Water By Oxidation Or Reduction (AREA)
- Water Treatment By Sorption (AREA)
Abstract
The present invention relates to Treatment of Industrial Water technical field, specifically a kind of process of combination BAF processing refinery sewage, concretely comprise the following steps：Step 1, homogeneous is adjusted；Step 2, oil removal air supporting；Step 3, interior circulation BAF；Step 4, Sludge Bed is adsorbed；Step 5, A/O+ settling systems；Step 6, catalytic ozonation；Step 7, up flow type BAF；The sewage of final process reaches discharge standard and discharged.The process of combination BAF processing refinery sewage of the present invention, the characteristic of BAF devices is taken full advantage of, can both avoid activated sludge tank from being impacted from water quality, increases the processing depth of sewage again, available in sewage inferior, the particularly processing of heavy crude refinery sewage.
Description
Technical field
It is specifically a kind of to combine BAF processing refinery sewage the present invention relates to Treatment of Industrial Water technical field
Process.The refinery sewage is high COD, heavy oil (heavy crude) the refinery sewage (oil refining sewerage) of high salt.
Background technology
Due to the shortage of petroleum resources, domestic increasing oil plant needs to produce and process heavy crude.Refine heavy
Waste component caused by crude oil is complicated, and water quality is unstable, and sewage treatment plant is often subject to water quality impact, causes sewage disposal
System is abnormal, and water quality treatment is not up to standard.
Due to difficult raw containing a large amount of aphthenic acids etc. in sewage (referred to as heavy oil refinery sewage) caused by heavy crude refining
Change the organic pollution of degraded, COD may be up to 2000~3000mg/L, and the processing of traditional biochemical process is difficult to up to standard.Meanwhile adopt
When handling heavy oil refinery sewage inferior with conventional refinery sewage technique " oil removal+two-stage air supporting+aeration and biological pond+second pond ",
" oil removal+two-stage air supporting " materialization section is difficult to meet water-oil separating condition, materialization section water outlet pollutant burden superelevation, causes to biochemistry
The impact of section, causes microorganism mortality, biochemical section water outlet severe overweight.
Chinese patent (201010200264.3) discloses a kind of method that advanced treating is carried out to not permitted discharge, will not
Enter catalytic ozonation tower after sewage water filtration up to standard, water outlet enters interior circulation after 0.5~4h is buffered in oxidation buffer pond
Biofilter.The larger molecular organicses of difficult degradation in sewage can be more prone to be oxidized into easy biology by catalytic ozonation tower
The small-molecule substance of degraded, or even carbon dioxide and water are directly degraded to, improve Biodegradability of Wastewater.Eliminated in buffer pool remaining
Ozone, the organic matter in sewage is further removed in inner circulating aerating biological filtering tank.
It is advanced that Chinese patent (200810092565.1) discloses a kind of increase Fenton after the biochemical treatment of routine
Oxidation and BAF handling process, will be difficult to be handled by routine biochemistry by Fenton oxidation and BAF further biochemistry in sewage
Organic matter removal, country-level standard of drainage can be reached, and the dosage by increasing advanced oxidation pond can reach reuse
Water water standard.
Chinese patent (200910018509.8) discloses a kind of high calcium high salt process for treating industrial waste water, pretreatment system
It is hydrolysis acidification anaerobic biological treatment afterwards, then sewage passes into the suitable salt bacterium pure oxygen aeration biological treatment system of domestication
System, enters back into catalytic oxidation embrane method biological treatment system, and the system shock formula adds 5~10mg/L nitrifier, by precipitation
Enter BAF filter tanks after pond, BAF ponds add 8~15mg/L alcohols or carboxylic acids co-substrate.Handle salinity 3.0%, calcium content
500~8000mg/L, COD1250mg/L, ammonia nitrogen 41.3mg/L waste water, effluent quality can reach COD ＜ 60mg/L, ammonia nitrogen ＜
5mg/L。
Chinese patent (201210447495.3) discloses a kind of combination treatment method of oil refining sewerage containing aphthenic acids.Passing
In " oil removing+A/O " technique of system, A/O ponds front end increase BAF pretreating process, A/O increases device for catalyzing and oxidating ozone afterwards,
Increase sewage handles depth.
Chinese patent (201110418658.0), which discloses one kind, includes one-level anaerobic hydrolysis-acidification tank, circulating activity dirt
Level Four biochemical treatment system processing inferior heavy oil refinery sewage disposal including mud method pond, secondary anaerobic hydrolysis acidification time and BAF
System, water quality can reach national and local discharge standard after processing.
BAF devices combine the feature of contact-oxidation pool and filtering ponds, have been widely used in the processing of refinery sewage.
How heavy crude refinery sewage makes full use of BAF devices, and the advanced treating for carrying out sewage requires study, be perfect.
The content of the invention
For defect present in prior art, combine BAF it is an object of the invention to provide one kind and handle
The process of refinery sewage, the characteristic of BAF devices is taken full advantage of, can both avoid activated sludge tank from being impacted from water quality, again
Increase the processing depth of sewage, available in sewage inferior, the particularly processing of heavy crude refinery sewage.
To achieve the above objectives, the present invention adopts the technical scheme that：
A kind of process of combination BAF processing refinery sewage, it is characterised in that：Set before A/O systems
Interior circulation BAF and Sludge Bed, are provided with catalytic ozonation system and up flow type BAF after A/O systems,
Second pond is provided between A/O systems and catalytic ozonation system,
Retentions and counter-flushing process of the interior circulation BAF by filtrate, backwash is increased in the case where water quality is severe
Frequency, follow-up A/O systems are protected not impacted by water quality；
The returned sludge that the Sludge Bed receives second pond carries out suction-operated to sewage, removes partial contamination thing, passes through
Discharge excess sludge takes away pollutant；
The pollutant oxidation removal of A/O system bio-refractories is improved sewage by the catalytic ozonation system
Biodegradability；
The up flow type BAF removes oil removal by the filtration of filtrate, and by biochemical action degraded by smelly
Oxygen catalysis oxidation improves the sewage of biodegradability, and final process water outlet can be with qualified discharge.
On the basis of above-mentioned technical proposal, concretely comprise the following steps：
Step 1, homogeneous is adjusted：Refinery sewage enters regulation tank and carries out homogeneous regulation, and the residence time is at least 24h, described
Adjust tank and contain the preliminary oil removing of tank progress in tank；
Step 2, oil removal air supporting：Adjust tank water outlet and enter inclined plate grease+cavitation/molten gas two-stage air supporting pretreatment oil removing；
Step 3, interior circulation BAF：Refinery sewage after oil removal air-flotation process enters interior circulation BAF, the interior circulation BAF
Run using up flow type, filler is any one in haydite, zeolite, anthracite, medical stone, fibrous nodules and aluminum oxide；
Step 4, Sludge Bed is adsorbed：Interior circulation BAF productions water enters Sludge Bed, and the Sludge Bed utilizes second pond returned sludge
Suction-operated absorption effluent in organic matter, the organic matter adsorption effect for especially being difficult to greatly degrade to molecular weight is more preferable；
Step 5, A/O+ settling systems：Sludge Bed water outlet enters A/O systems, and A/O systems carry out biochemical treatment, A/ to sewage
The water outlet of O systems enters second pond；
Step 6, catalytic ozonation：Secondary clarifier effluent enters catalytic ozonation system, the catalytic ozonation system
System comprises at least：Ozone generation system, catalyst oxidation reactor and stabilization pond；
Step 7, up flow type BAF：The water outlet of stabilization pond into up flow type BAF, the up flow type BAF filler for haydite,
Any one in zeolite, anthracite, medical stone, fibrous nodules and aluminum oxide；The sewage of final process reaches discharge standard progress
Discharge.
On the basis of above-mentioned technical proposal, in step 3, filtering velocity control is 2~5m/h, gas-water ratio 3:1~5:1, inside follow
Ring ratio is 100%~150%, and it is 36~72h to control backwashing period according to condition of water quality, and backwash is drained into regulation tank.
On the basis of above-mentioned technical proposal, in step 4, the hydraulic detention time of Sludge Bed is 0.5~1.5h, and sludge is dense
It is the 10%~20% of water water to spend for 10~15g/L, sludge reflux amount, sets sludge condensation bucket discharge system remaining dirty
Mud.
On the basis of above-mentioned technical proposal, in A/O+ settling systems described in step 5,
COD volumetric loading ratio is 0.5~1.2kg COD/m3D, the A/O residence time are 12~16/40~56h, interior
Reflux ratio is 200%~300%, and return sludge ratio is 80%~100%, and sludge concentration is 3~5g/L, Aerobic Pond aeration intensity
For 7~10m3/m2·h；
In sewage majority of organic pollutants, degradable COD in A/O systems by biochemical degradation.
On the basis of above-mentioned technical proposal, in step 6, ozone generation system is supplied using source of oxygen, and ozone concentration is
70~80mg/L；
Selected in catalyst oxidation reactor by modified haydite, aluminum oxide, molecular sieve, column-shaped active carbon or seed activity
Charcoal is the catalyst of carrier, and is loaded with the above transition of one or both of 3.0%~5.0% copper, iron, manganese, cerium or cobalt
Metallic element；
Ozone dosage is 20~50mg/L, and the reaction time is 25~50min.
On the basis of above-mentioned technical proposal, in step 7, filtering velocity control is 3~5m/h, gas-water ratio 3:1~5:1, according to
It is 48~96h that condition of water quality, which controls backwashing period,.
On the basis of above-mentioned technical proposal, in step 6, the method for modifying of ozone catalytic agent carrier is：
By carrier material and be dissolved in the water concentration be 10%~30% ammonia propellant in 120~140 DEG C and 2 air
Pressure 1~2h of processing, then drying process is stand-by；
The ammonia propellant is ammonia, ammonium carbonate or urea.
The process of combination BAF processing refinery sewage of the present invention, takes full advantage of BAF devices
Characteristic, can both avoid activated sludge tank from being impacted from water quality, and increase the processing depth of sewage again, it is special available for sewage inferior
Be not heavy crude refinery sewage processing in.
The process of combination BAF processing refinery sewage of the present invention, is a kind of depth of refinery sewage
Processing method is spent, circulation BAF and Sludge Bed are as pretreatment work in the increase of the A/O front ends of traditional " oil removing+A/O " technique
Skill, increase catalytic ozonation and up flow type BAF systems in A/O rear ends as advanced treatment process, the water quality that is particularly suitable for use in ripple
The advanced treating of dynamic, difficult refinery sewage.
Brief description of the drawings
The present invention has drawings described below：
The process chart of Fig. 1 present invention.
Embodiment
The present invention is described in further detail below in conjunction with accompanying drawing.
As shown in figure 1, the process of combination BAF processing refinery sewage of the present invention, in A/O systems
Interior circulation BAF and Sludge Bed are provided with before system, catalytic ozonation system and up flow type BAF are provided with after A/O systems,
Second pond (sedimentation basin) is provided between A/O systems and catalytic ozonation system,
Retentions and counter-flushing process of the interior circulation BAF by filtrate, backwash is increased in the case where water quality is severe
Frequency, follow-up A/O systems are protected not impacted by water quality；
The returned sludge that the Sludge Bed receives second pond carries out suction-operated to sewage, removes partial contamination thing, passes through
Discharge excess sludge takes away pollutant；
The pollutant oxidation removal of A/O system bio-refractories is improved sewage by the catalytic ozonation system
Biodegradability；
The up flow type BAF removes oil removal by the filtration of filtrate, and by biochemical action degraded by smelly
Oxygen catalysis oxidation improves the sewage of biodegradability, and final process water outlet can be with qualified discharge.
On the basis of above-mentioned technical proposal, concretely comprise the following steps：
Step 1, homogeneous is adjusted：Refinery sewage enters regulation tank and carries out homogeneous regulation, and the residence time is at least 24h, described
Adjust tank and contain the preliminary oil removing of tank progress in tank；
Step 2, oil removal air supporting：Adjust tank water outlet and enter inclined plate grease+cavitation/molten gas two-stage air supporting pretreatment oil removing；
Step 3, interior circulation BAF：Refinery sewage after oil removal air-flotation process enters interior circulation BAF, the interior circulation BAF
Run using up flow type, filler is any one in haydite, zeolite, anthracite, medical stone, fibrous nodules and aluminum oxide；
Filtering velocity control is 2~5m/h, gas-water ratio 3:1~5:1, nitrate recirculation ratio is 100%~150%, according to condition of water quality
It is 36~72h to control backwashing period, and backwash is drained into regulation tank；
Interior circulation BAF realizes hydraulic hoisting while central lift pipe is aerated, and sewage circulates downwards by filtrate, filler
Retain the suspended solid in sewage and biological membranous layer is formed on surface, the organic matter in absorption effluent carries out biochemical degradation；Operation
Backwash is carried out after certain time, the suspension of retention and biological membranous layer backwash are fallen, carrier is regained cutoff performance, backwash
It is drained into regulation tank；Therefore circulation BAF can not only realize the retention of suspension but also can carry out biochemical removal COD, BOD in；
Sewage quality difference can be provided more by circulating BAF backwash frequencies in increase by filtrate retention and backwash for follow-up system
Stable condition of water quality, follow-up system is set to be impacted from water quality；
Step 4, Sludge Bed is adsorbed：Interior circulation BAF productions water enters Sludge Bed, and the Sludge Bed utilizes second pond (sedimentation basin)
Organic matter in the suction-operated absorption effluent of returned sludge, especially it is difficult to the organic matter adsorption effect degraded greatly to molecular weight
More preferably；
The hydraulic detention time of Sludge Bed is 0.5~1.5h, and sludge concentration is 10~15g/L, and sludge reflux amount is water
The 10%~20% of water, sludge condensation bucket discharge system excess sludge is set；
Step 5, A/O+ settling systems：Sludge Bed water outlet enters A/O systems, and A/O systems carry out biochemical treatment, A/ to sewage
The water outlet of O systems enters second pond；
In the A/O+ settling systems：
COD volumetric loading ratio is 0.5~1.2kg COD/m3D, the A/O residence time are 12~16/40~56h, interior
Reflux ratio is 200%~300%, and return sludge ratio is 80%~100%, and sludge concentration is 3~5g/L, Aerobic Pond aeration intensity
For 7~10m3/m2·h；
In sewage majority of organic pollutants, degradable COD in A/O systems by biochemical degradation；
Step 6, catalytic ozonation：Secondary clarifier effluent enters catalytic ozonation system, the catalytic ozonation system
System comprises at least：Ozone generation system, catalyst oxidation reactor and stabilization pond；
Ozone generation system is supplied using source of oxygen, and ozone concentration is 70~80mg/L；
Selected in catalyst oxidation reactor by modified haydite, aluminum oxide, molecular sieve, column-shaped active carbon or seed activity
Charcoal is the catalyst (ozone catalyst) of carrier, and one kind for being loaded with 3.0%~5.0% copper, iron, manganese, cerium or cobalt or
Two or more transition metals；
Ozone dosage is 20~50mg/L, and the reaction time is 25~50min；
Catalyst (ozone catalyst) with absorption property can be in absorption effluent organic matter, aoxidized in active metal
Degraded in the presence of thing and ozone, remove the COD for being difficult to degrade after A/O biochemistry；Catalytic ozonation can also improve dirt
The biodegradability of water, sewage realize advanced treating by subsequent biochemical；
Step 7, up flow type BAF：The water outlet of stabilization pond into up flow type BAF, the up flow type BAF filler for haydite,
Any one in zeolite, anthracite, medical stone, fibrous nodules and aluminum oxide；
Filtering velocity control is 3~5m/h, gas-water ratio 3:1~5:1, it is 48~96h to control backwashing period according to condition of water quality；
Up flow type BAF effect be by by catalytic ozonation improve biodegradability the further biochemical degradation of sewage its
In BOD, and the suspension for removing sewage is acted on by filtrate, the sewage of final process reaches discharge standard and discharged.
On the basis of above-mentioned technical proposal, in step 6, the method for modifying of ozone catalytic agent carrier is：By carrier material
1~2h is handled under 120~140 DEG C and 2 atmospheric pressure with ammonia propellants such as the ammonia that is dissolved in the water, ammonium carbonate or urea, then
Drying process is stand-by.
Such as：Carrier material and the concentration that is dissolved in the water are existed for the ammonia propellant of 10%~30% (mass percent)
1~2h is handled under 120~140 DEG C and 2 atmospheric pressure, then drying process is stand-by；
The ammonia propellant is ammonia, ammonium carbonate or urea.
The process of combination BAF processing refinery sewage of the present invention, specific work process are as follows：
1st, pre-process：Refinery sewage (following referred to as sewage) is promoted to regulation tank by elevator pump, through overregulating tank
Preliminary oil removing and average regulation, sewage enter the further oil removing of oil removal air flotation cell；
2nd, the sewage by pretreatment enters interior circulation BAF processing units through feed pump, and sewage carries out cyclic aeration filtering,
Operation a period of time carries out combined water and air backwash, and backwashing water comes from second pond (sedimentation basin) water outlet, and backwash is drained into
Adjust tank；
3rd, interior circulation BAF water outlets enter Sludge Bed, remaining using the pollutant in the sludge absorption sewage of sedimentation basin backflow
Sludge is discharged by Sludge Bed sludge condensation；
4th, sewage enters back into A/O processing units and carries out biochemical treatment, removes the most pollutant in sewage, second pond
(sedimentation basin) sludge part is back to Sludge Bed, is partly refluxed to A ponds；
5th, the pollutant after A/O cell processings in sewage also containing part difficult for biological degradation, by ozone catalytic oxygen
Change degraded to remove, or reduce contaminant molecule amount by catalytic ozonation and improve its biodegradable, ozone catalytic oxygen
Sewage passes through in stabilization pond draining-off sewage the ozone remained after change, avoids producing inhibitory action to subsequent biochemical；
6th, enter up flow type BAF by the sewage of catalytic ozonation, carry out the BOD in biochemical degradation removal sewage again
And COD, up flow type BAF backwashing water clear pond from outer, backwash is drained into the Sludge Bed in flow；
The final qualified discharge of sewage by above-mentioned serial flow processing.
It is embodiment below.
Embodiment 1：
Certain sewage from oil refinery is handled according to above-mentioned flow, main processing units process conditions are as follows：
Interior circulation BAF fillers are anthracite, filtering velocity 3m/h, gas-water ratio 3:1, nitrate recirculation ratio 150%, backwashing period 48h；
The Sludge Bed residence time is 1.0h, sludge concentration 10g/L in Sludge Bed, sludge reflux amount 20%；
The COD volumetric loadings in A/O ponds are 0.8kg COD/m3D, residence time 12/48h, internal reflux ratio 300% are dirty
Mud reflux ratio 80%, sludge concentration 4g/L, aeration intensity 8m3/m2·h；
The catalyst that catalytic ozonation system uses loads 3.0% Ce elements for modified ceramsite carrier, and ozone adds
Measure as 40mg/L, oxidization time 30min；
Up flow type BAF uses ceramics filling, filtering velocity 5m/h, gas-water ratio 4:1, backwashing period 72h.Each unit processing
Effect is shown in Table 1：
The technique each unit of table 1. handles effluent quality table
Embodiment 2：
Certain refinery factory saline sewage is handled according to above-mentioned flow, main processing units process conditions are as follows：
Interior circulation BAF fillers are medical stone, filtering velocity 2m/h, gas-water ratio 3:1, nitrate recirculation ratio 150%, backwashing period 36h；
The Sludge Bed residence time is 1.5h, sludge concentration 13g/L in Sludge Bed, sludge reflux amount 20%；
The COD volumetric loadings in A/O ponds are 1.2kg COD/m3D, residence time 16/56h, internal reflux ratio 300% are dirty
Mud reflux ratio 80%, sludge concentration 5g/L, aeration intensity 10m3/m2·h；
The catalyst that catalytic ozonation system uses for modified column-shaped active carbon carrier loaded 3.0% copper and 2.0%
Ce elements, ozone dosage 50mg/L, oxidization time 30min；
Up flow type BAF uses zeolite filler, filtering velocity 5m/h, gas-water ratio 5:1, backwashing period 48h.Each unit processing
Effect is shown in Table 2：
The technique each unit of table 2. handles effluent quality table
Embodiment 3：
Certain refinery factory saline sewage is handled according to above-mentioned flow, main processing units process conditions are as follows：
Interior circulation BAF fillers are fibrous nodules, filtering velocity 5m/h, gas-water ratio 3:1, nitrate recirculation ratio 150%, backwashing period 48h；
The Sludge Bed residence time is 1.5h, sludge concentration 10g/L in Sludge Bed, sludge reflux amount 10%；
The COD volumetric loadings in A/O ponds are 1.0kg COD/m3D, residence time 14/48h, internal reflux ratio 300% are dirty
Mud reflux ratio 90%, sludge concentration 5g/L, aeration intensity 10m3/m2·h；
The catalyst that catalytic ozonation system uses loads 3.0% manganese and 3.0% copper for modified aluminium oxide supports
Element, ozone dosage 40mg/L, oxidization time 50min；
Up flow type BAF uses anthracite filler, filtering velocity 3m/h, gas-water ratio 5:1, backwashing period 72h.At each unit
Reason effect is shown in Table 3：
The technique each unit of table 3. handles effluent quality table
The process of combination BAF processing refinery sewage of the present invention, sets between pretreatment and A/O
Interior circulation BAF and Sludge Bed have been put, has increased sewage disinfection treatment effect, avoids A/O from being impacted by water quality；It is provided with after A/O
Catalytic ozonation and up flow type BAF techniques, improve the processing depth of sewage.BAF fillers are haydite, zeolite, anthracite, wheat meal
Any one in stone, fibrous nodules and aluminum oxide.The catalyst of device for catalyzing and oxidating ozone uses the carrier by pretreatment, and
Active transition metals oxide is loaded, the Vehicle element method is to be pre-processed using ammonia propellant.
The content not being described in detail in this specification belongs to prior art known to professional and technical personnel in the field.
Claims (7)
- A kind of 1. process of combination BAF processing refinery sewage, it is characterised in that：It is provided with before A/O systems Interior circulation BAF and Sludge Bed, catalytic ozonation system and up flow type BAF are provided with after A/O systems,Second pond is provided between A/O systems and catalytic ozonation system,Retentions and counter-flushing process of the interior circulation BAF by filtrate, backwash frequency is increased in the case where water quality is severe, Follow-up A/O systems are protected not impacted by water quality；The returned sludge that the Sludge Bed receives second pond carries out suction-operated to sewage, removes partial contamination thing, passes through discharge Excess sludge takes away pollutant；The pollutant oxidation removal of A/O system bio-refractories is improved giving birth to for sewage by the catalytic ozonation system The property changed；The up flow type BAF removes oil removal by the filtration of filtrate, and is degraded by biochemical action and urged by ozone Change the sewage that oxidation improves biodegradability, final process water outlet can be with qualified discharge；Concretely comprise the following steps：Step 1, homogeneous is adjusted：Refinery sewage enters regulation tank and carries out homogeneous regulation, and the residence time is at least 24h, the regulation Tank contains tank in tank and carries out preliminary oil removing；Step 2, oil removal air supporting：Adjust tank water outlet and enter inclined plate grease+cavitation/molten gas two-stage air supporting pretreatment oil removing；Step 3, interior circulation BAF：Refinery sewage after oil removal air-flotation process enters interior circulation BAF, and the interior circulation BAF is used Up flow type is run, and filler is any one in haydite, zeolite, anthracite, medical stone, fibrous nodules and aluminum oxide；Step 4, Sludge Bed is adsorbed：Interior circulation BAF productions water enters Sludge Bed, and the Sludge Bed utilizes the suction of second pond returned sludge Organic matter in attached effect absorption effluent；Step 5, A/O+ settling systems：Sludge Bed water outlet enters A/O systems, and A/O systems carry out biochemical treatment, A/O systems to sewage System water outlet enters second pond；Step 6, catalytic ozonation：Secondary clarifier effluent enters catalytic ozonation system, and the catalytic ozonation system is extremely Include less：Ozone generation system, catalyst oxidation reactor and stabilization pond；Step 7, up flow type BAF：The water outlet of stabilization pond into up flow type BAF, the up flow type BAF filler for haydite, zeolite, Any one in anthracite, medical stone, fibrous nodules and aluminum oxide；The sewage of final process reaches discharge standard and discharged.
- 2. as claimed in claim 1 with reference to the process of BAF processing refinery sewage, it is characterised in that：Step In 3, filtering velocity control is 2~5m/h, gas-water ratio 3:1~5:1, nitrate recirculation ratio is 100%~150%, is controlled according to condition of water quality Backwashing period is 36~72h, and backwash is drained into regulation tank.
- 3. as claimed in claim 1 with reference to the process of BAF processing refinery sewage, it is characterised in that：Step In 4, the hydraulic detention time of Sludge Bed is 0.5~1.5h, and sludge concentration is 10~15g/L, and sludge reflux amount is water water 10%~20%, set sludge condensation bucket discharge system excess sludge.
- 4. as claimed in claim 1 with reference to the process of BAF processing refinery sewage, it is characterised in that：Step In the 5 A/O+ settling systems,It is 12~16/40~56h 0.5~1.2kg COD/m3d, A/O residence times that COD volumetric loading ratio, which is, interior backflow Than for 200%~300%, return sludge ratio is 80%~100%, sludge concentration be 3~5g/L, and Aerobic Pond aeration intensity is 7 ~10m3/m2h；In sewage majority of organic pollutants, degradable COD in A/O systems by biochemical degradation.
- 5. as claimed in claim 1 with reference to the process of BAF processing refinery sewage, it is characterised in that：Step In 6, ozone generation system is supplied using source of oxygen, and ozone concentration is 70~80mg/L；Selected in catalyst oxidation reactor and be by modified haydite, aluminum oxide, molecular sieve, column-shaped active carbon or granular activated carbon The catalyst of carrier, and it is loaded with one or both of 3.0%~5.0% copper, iron, manganese, cerium or cobalt above transition metal Element；Ozone dosage is 20~50mg/L, and the reaction time is 25~50min.
- 6. as claimed in claim 1 with reference to the process of BAF processing refinery sewage, it is characterised in that：Step In 7, filtering velocity control is 3~5m/h, gas-water ratio 3:1~5:1, it is 48~96h to control backwashing period according to condition of water quality.
- 7. as claimed in claim 1 with reference to the process of BAF processing refinery sewage, it is characterised in that：Step In 6, the method for modifying of ozone catalytic agent carrier is：By carrier material and be dissolved in the water concentration be 10%~30% ammonia propellant under 120~140 DEG C and 2 atmospheric pressure 1~2h is handled, then drying process is stand-by；The ammonia propellant is ammonia, ammonium carbonate or urea.
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| CN106430845A (en) * | 2016-11-21 | 2017-02-22 | 中机国际工程设计研究院有限责任公司 | Kitchen garbage wastewater treatment apparatus |
| CN109534620B (en) * | 2019-01-03 | 2021-01-29 | 清华大学 | Ozone catalytic oxidation and aeration biological activated carbon filter tank sewage advanced treatment device |
| CN110330187A (en) * | 2019-07-24 | 2019-10-15 | 杰瑞环境工程技术有限公司 | A kind of greasy filth pyrolysis waste water treatment system |
| CN113511775A (en) * | 2020-04-10 | 2021-10-19 | 中国石油化工股份有限公司 | Finished oil depot sewage treatment system and finished oil depot sewage treatment method |
| CN112811727A (en) * | 2020-12-31 | 2021-05-18 | 北京邦源环保科技股份有限公司 | Comprehensive sewage treatment process |
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| CN1579968A (en) * | 2004-05-19 | 2005-02-16 | 天津大学 | Integrated treating process of waste water extracted from gas well for reaching effluent standard |
| CN201809255U (en) * | 2010-08-13 | 2011-04-27 | 北京神州瑞霖环保科技有限公司 | Oil shale waste water treatment system |
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| CN1579968A (en) * | 2004-05-19 | 2005-02-16 | 天津大学 | Integrated treating process of waste water extracted from gas well for reaching effluent standard |
| CN201809255U (en) * | 2010-08-13 | 2011-04-27 | 北京神州瑞霖环保科技有限公司 | Oil shale waste water treatment system |
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