CN104628221A - Method for treating acid-containing heavy crude oil refining saline sewage - Google Patents
Method for treating acid-containing heavy crude oil refining saline sewage Download PDFInfo
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Abstract
The invention discloses a method for treating acid-containing heavy crude oil refining saline sewage. The method comprises the following treatment on the saline sewage: gravity settling oil removal treatment, inclined plate settling oil removal treatment, two-stage air floatation treatment, bio-aeration treatment, anaerobic hydrolysis acidification treatment, nitrification-denitrification treatment and catalytic ozonization treatment. The water body treated by adopting the method can meet the requirements that COD cr is less than or equal to 60mg/L, petroleum is less than or equal to 5mg/L, ammonia nitrogen is less than or equal to 10mg/L and the total nitrogen is less than or equal to 40mg/L.
Description
Technical field
The invention belongs to Refinery Wastewater Treatment Technology field, relate to the technology of heavy crude refinery sewage process up to standard, particularly relate to a kind for the treatment of process containing sour heavy crude refinery saline sewage.
Background technology
Typically refer to acid number containing sour heavy crude and be greater than 2.0mgKOH/g, relative density is greater than 0.931g/cm simultaneously
3crude oil.Containing sour heavy crude except have low API °, high specific gravity, high carbon residue, the mink cell focus such as high gum asphaltic content denominator except, generally also there is the features such as high-sulfur nitrogen, high saliferous, high acid value.Because global conventional oil reserves reduce day by day, in domestic imported crude oil, the high ratio containing sour heavy crude is more and more higher.In domestic newly-built Petrochemical Enterprises, also carry out work flow design containing sour heavy crude as main raw material mainly with height.
Can be divided into time processing device and secondary processing device containing sour heavy crude processing unit (plant), whole point source sewage of discharge are divided into oily(waste)water series and saline sewage series according to its pollutent characteristic.Oily(waste)water is mainly from secondary processing device, and pollution level is comparatively light, can produce pure water reuse boiler after materialization-biochemistry-advanced treatment.And saline sewage due to saltiness higher, be not suitable for utilizing reverse osmosis membrane explained hereafter pure water, be generally through process after qualified discharge.Petroleum tank dehydration is mainly originated from containing sour heavy crude refinery saline sewage, and the electrodesalting and electrodehydrating process of time processing device.Saline sewage macroscopically has high COD(> 4000mg/L), the polluting property of high oil-containing (> 1000mg/L), high ammonia nitrogen (> 200mg/L), high conductivity (> 4000 μ s/cm), microcosmic composition has organic acid, ester class, alcohols, polluting property that heterocycles isopolarity pollutant load is high.Therefore, saline sewage shows stronger emulsifying property, and more weak biodegradability.Require (CODcr≤60mg/L, petroleum-type≤5mg/L, ammonia nitrogen≤10mg/L, total nitrogen≤40mg/L) along with a lot of province starts the first discharge standard performed in Guangdong Province's provincial standard " water pollutions emission limit " (DB44/26-2001) (the second period), stricter processing requirements up to standard is proposed to saline sewage.
A kind of method that extremely-viscous crude sewage carries out advanced treatment is disclosed in ZL 200910081479.5, the whole point source saline sewages utilizing " sedimentation oil removing pot-inclined plate grease device-two-stage air-floating apparatus-one-stage hydrolysis souring tank-cyclic activated sludge process (CAST) pond-secondary hydrolysis acidification pool-BAF-coagulation basin-Lan Meila inclined-plate clarifying basin " technical process to produce processing super-viscous oil, oily(waste)water carry out concentrated process up to standard, effluent index meets petroleum-type≤10mg/L, CODcr≤100mg/L, the requirement of ammonia nitrogen≤15mg/L.Super-viscous oil is also the high one containing sour heavy crude, although above-mentioned patented technology has carried out process to a certain degree for height containing sour heavy crude saline sewage, but its method still exists the defect of sewage difficulty up to standard, the effluent index of this patented method is still not enough to the requirement (CODcr≤60mg/L, petroleum-type≤5mg/L, ammonia nitrogen≤10mg/L, total nitrogen≤40mg/L) of the first discharge standard met completely in Guangdong Province's provincial standard " water pollutions emission limit " (DB44/26-2001) (the second period).
Summary of the invention
The object of the invention is the above-mentioned defect in order to overcome prior art, reduce the CODcr value of the rear water body of process, petroleum content, ammonia-nitrogen content and total nitrogen content, provide a kind of and process the treatment process containing sour heavy crude refinery saline sewage that rear water body can meet CODcr≤60mg/L, petroleum-type≤5mg/L, ammonia nitrogen≤10mg/L, total nitrogen≤40mg/L require.
The present inventor surprisingly finds under study for action, containing sour heavy crude refinery saline sewage successively through gravity settling oil removal treatment, sloping plate deposition oil removal treatment, two-stage air-flotation process, bio-aeration process, anaerobic hydrolysis-acidification process, nitrification-denitrification denitrogenation processing and catalytic ozonation process, significantly can reduce the CODcr value of the rear water body of process, petroleum content, ammonia-nitrogen content and total nitrogen content, enable the water body after process meet the requirement of CODcr≤60mg/L, petroleum-type≤5mg/L, ammonia nitrogen≤10mg/L, total nitrogen≤40mg/L.
Therefore, to achieve these goals, the invention provides a kind for the treatment of process containing sour heavy crude refinery saline sewage, described method comprises and being handled as follows successively by described saline sewage: gravity settling oil removal treatment, sloping plate deposition oil removal treatment, two-stage air-flotation process, bio-aeration process, anaerobic hydrolysis-acidification process, nitrification-denitrification denitrogenation processing and catalytic ozonation process.
Treatment process containing sour heavy crude refinery saline sewage of the present invention, significantly can reduce the CODcr value of the rear water body of process, petroleum content, ammonia-nitrogen content and total nitrogen content, make the high high organic loading difficult degradation saline sewage containing producing in sour heavy crude refinery process can meet the requirement of CODcr≤60mg/L, petroleum-type≤5mg/L, ammonia nitrogen≤10mg/L, total nitrogen≤40mg/L after treatment, thus solve the high sewage difficult problem up to standard caused containing sour heavy crude of refinery's processing.
Other features and advantages of the present invention are described in detail in embodiment part subsequently.
Accompanying drawing explanation
Fig. 1 is the structural representation containing sour heavy crude refinery saline sewage treatment facility of the present invention.
Description of reference numerals
1 homogeneous regulating tank; 2 swash plate oil eliminators; 3 one-level cavitation air flotation equipment; 4 secondary air-dissolving air-float equipment; 5 inner circulating aerating biological filtering tanks; 6 anaerobic hydrolysis-acidification tanks; 7 one-level A ponds; 8 one-level O ponds; 9 medium sediment pools; 10 secondary A ponds; 11 secondary O ponds; 12 MBR ponds; 13 catalytic ozonation towers.
Embodiment
Below in conjunction with Fig. 1, the specific embodiment of the present invention is described in detail.Should be understood that, embodiment described herein, only for instruction and explanation of the present invention, is not limited to the present invention.
The invention provides a kind for the treatment of process containing sour heavy crude refinery saline sewage, the method comprises and being handled as follows successively by saline sewage: gravity settling oil removal treatment, sloping plate deposition oil removal treatment, two-stage air-flotation process, bio-aeration process, anaerobic hydrolysis-acidification process, nitrification-denitrification denitrogenation processing and catalytic ozonation process.
In the inventive method, namely gravity settling oil removal treatment refers to by by sedimentation after water mixing, removes the petroleum-type floating on surface, removes the non-dissolved pollutants such as the suspended substance (SS) falling to bottom.Method for gravity settling oil removal treatment does not have particular requirement, can adopt the various methods that this area is conventional, if can by carrying out containing each point source saline sewage of sour heavy crude refinery mixing, sedimentation.In order to effectively remove the non-dissolved pollutant such as petroleum-type, SS in saline sewage, under preferable case, gravity settling oil removal treatment is carried out in homogeneous regulating tank.The method carrying out processing in homogeneous regulating tank can be: will concentrate input homogeneous regulating tank containing each point source saline sewage of sour heavy crude refinery, regularly, the point source saline sewage of irregularly discharge regulates in-tank mixing at homogeneous and realizes homogeneous, then gravity settling more than 24 hours, oil slick, macrobead SS are separated with water body, reclaim the oil slick floating up to homogeneous regulating tank top, remove the macrobead SS be settled down to bottom homogeneous regulating tank, and water body is inputted in next treatment unit.
In the inventive method, namely sloping plate deposition oil removal treatment refers to and utilizes the coalescent effect of swash plate and shallow pond sedimentation theory, by coalescent for the dispersed oil in water body formation comparatively larger oil droplet, by coalescent for small-particle SS formation larger particles SS, thus realizes water body and oil and being separated of SS.Method for sloping plate deposition oil removal treatment does not have particular requirement, can adopt the various methods that this area is conventional.In order to effectively remove the non-dissolved pollutant such as petroleum-type, SS in water body further, under preferable case, sloping plate deposition oil removal treatment is carried out in swash plate oil eliminator.The method carrying out processing in swash plate oil eliminator can be: in swash plate oil eliminator, utilize the coalescent effect of swash plate and shallow pond sedimentation theory, by coalescent for the dispersed oil in the water body in swash plate oil eliminator formation comparatively larger oil droplet, by coalescent for small-particle SS formation larger particles SS, macrobead SS, oil droplet are separated with water body, reclaim the oil droplet floating up to swash plate oil eliminator top, remove the SS be settled down to bottom swash plate oil eliminator, and water body is inputted in next treatment unit.
It will be understood by those skilled in the art that in the present invention, oil slick refers to that particle diameter is greater than the oil droplet floating on water surface of 80 μm; Dispersed oil refers to that particle diameter is less than the small oil droplet of 10 μm, is scattered in water with suspended state, more unstable; Oil in water emulsion refers to the existence due to tensio-active agent, and oil is in milk sap in water, and easily form O/W type emulsified particle, particle diameter is less than 1 μm, more stable in water, not easily bubbles through the water column.
In the inventive method, air-flotation process namely refer to utilize bubble that oil is brought to water surface with SS thus realize oily with SS with being separated of water body.Method for two-stage air-flotation process does not have particular requirement, the various methods that this area is conventional can be adopted, in order to effectively remove the non-dissolved pollutant such as petroleum-type, SS in water body, under preferable case, two-stage air-flotation process carries out respectively in one-level cavitation air flotation equipment and secondary air-dissolving air-float equipment.Particularly, be input in one-level cavitation air flotation equipment after first the water body after sloping plate deposition oil removal treatment being mixed with coagulating agent, coagulant aids to process; Input in secondary air-dissolving air-float equipment after again the water body after one-level cavitation air flotation device processes being mixed with coagulating agent, coagulant aids and process.
In the inventive method, the method that the method carrying out processing in one-level cavitation air flotation equipment and secondary air-dissolving air-float equipment can be commonly used for this area, can be such as: in one-level cavitation air flotation equipment, impeller high-speed rotation is utilized to form vacuum zone in water, ullage air is by aerator input water, microbubble produces thereupon and rises, and is separated at the top that (colloidal attitude) suspended substance and the oil in water emulsion of breakdown of emulsion take one-level cavitation air flotation equipment to.In secondary air-dissolving air-float equipment, the bubble of saturated dissolved gas is little, and it adheres to the effective of SS and oil droplet; Assist sedimentation in conjunction with swash plate, oil in water emulsion and the non-dissolved pollutants such as SS float up to secondary air-dissolving air-float equipment top to carry out the degree of depth and is separated simultaneously.
Wherein, the concrete kind for the coagulating agent added in one-level cavitation air flotation equipment and secondary air-dissolving air-float equipment, coagulant aids does not have particular requirement, can adopt coagulating agent, coagulant aids that this area is conventional respectively.In order to more effectively remove the non-dissolved pollutant such as petroleum-type, SS in water body, under preferable case, coagulating agent is at least one in aluminium iron polychloride, polymerize aluminum chloride, poly-ferric chloride, is more preferably aluminium iron polychloride; Coagulant aids is polyacrylamide.One-level cavitation air flotation equipment can be identical with the kind of the coagulating agent added in secondary air-dissolving air-float equipment, coagulant aids, also can be different, but conveniently operate, under preferable case, one-level cavitation air flotation equipment is identical with the kind of the coagulating agent added in secondary air-dissolving air-float equipment, coagulant aids.
Wherein, under preferable case, in one-level cavitation air flotation equipment, the dosage of coagulating agent is 100 ~ 150 grams of/ton of staying waters, and the dosage of coagulant aids is 3 ~ 5 grams of/ton of staying waters; In secondary air-dissolving air-float equipment, the dosage of coagulating agent is 50 ~ 100 grams of/ton of staying waters, and the dosage of coagulant aids is 0.5 ~ 1.0 gram of/ton of staying water.
In the inventive method, gravity settling oil removal treatment, sloping plate deposition oil removal treatment, two-stage air-flotation process are materializing strategy, under preferable case, above-mentioned materializing strategy adopts homogeneous regulating tank, swash plate oil eliminator, one-level cavitation air flotation equipment and secondary air-dissolving air-float equipment to carry out materializing strategy respectively, after above-mentioned materializing strategy, containing in sour heavy crude refinery saline sewage the non-dissolved pollutant such as petroleum-type, SS remove more thorough, corresponding organic pollution load is also minimized, for biochemical system cloud gray model improves water quality guarantee.
In the inventive method, in order to depth degradation biochemical oxygen demand (BOD) (BOD), significantly reduce organic pollution load, under preferable case, bio-aeration process is carried out in inner circulating aerating biological filtering tank.Water body after secondary air-dissolving air-float device processes carries out biochemical pre-treatment in inner circulating aerating biological filtering tank, inner circulating aerating biological filtering tank preferably adopts systemic circulation ratio and excess aeration, for strengthening the mass transfer between pollutent-oxygen-microorganism, possess the characteristic of complete mix flow, high organic pollution load can be born; Meanwhile, pond is built with filtrate, and filter material surface can form high-density microbial film, can form sludge filtering layer between filtrate gap, make BOD degrade and suspended substance adsorption filtration effect stronger.
Wherein, under preferable case, in inner circulating aerating biological filtering tank, the condition of bio-aeration process comprises: the recycle ratio of inner circulating aerating biological filtering tank is 20 ~ 30:1, and hydraulic detention time is 10 ~ 15 hours, and in pond, dissolved oxygen concentration is 3 ~ 5mg/L; In pond fill diameter be the haydite of 8 ~ 12mm as biofilter material medium, packing height accounts for 60 ~ 70% of pond height.
In the inventive method, in order to the macromole Persistent organic pollutants in the water body after inner circulating aerating biological filtering tank process are converted into the easy degradable organic pollutant of small molecules more up hill and dale, improve the biodegradability of water body, under preferable case, anaerobic hydrolysis-acidification process is carried out in anaerobic hydrolysis-acidification tank.For by the anaerobically fermenting Process flowchart in anaerobic hydrolysis-acidification tank hydrolysis, souring stage, the condition optimization of anaerobic hydrolysis-acidification process comprises: the dissolved oxygen concentration in anaerobic hydrolysis-acidification tank is 0.2 ~ 0.5mg/L, hydraulic detention time is 24 ~ 48 hours, redox potential is-100 ~-300mV, and sludge concentration is 6000 ~ 10000mg/L.
It will be understood by those skilled in the art that water body is after bio-aeration process, organic pollution load declines, and biodegradability also has and significantly declines simultaneously; But after anaerobic hydrolysis-acidification process, the biological degradability of water quality can return.Therefore, water body, after " inner circulating aerating biological filtering tank-anaerobic hydrolysis-acidification tank " biochemical pretreatment unit process, synchronously can realize organic pollution load decline, the improved regulating and controlling water quality target of biodegradability.
In the inventive method, in order to effectively control chemical oxygen demand (COD) (COD), ammonia nitrogen, total nitrogen index, under preferable case, nitrification-denitrification denitrogenation processing is carried out successively in one-level A/O/ medium sediment pool and secondary A/O/MBR pond.It will be understood by those skilled in the art that one-level A/O/ medium sediment pool refers to the one-level anoxic pond (one-level A pond) of sequential communication, one-level Aerobic Pond (one-level O pond) and medium sediment pool.Secondary A/O/MBR pond refers to the secondary anoxic pond (secondary A pond) of sequential communication, secondary Aerobic Pond (secondary O pond) and membrane bioreactor (MBR pond).
Process in water body input one-level A/O/ medium sediment pool after the process of anaerobic hydrolysis-acidification tank, A/O technique meets complete nitrification-denitrification denitrogenation mechanism.In one-level A pond, the nitrate nitrogen in one-level O pond backflow nitrification liquid is by denitrification, and in water inlet, COD is utilized by denitrifying bacteria and partly removes, and acidication occurs simultaneously and improves biodegradability; In one-level O pond, ammonia nitrogen is by nitrated one-tenth nitrate nitrogen, and COD is degraded by aerobic biochemical.
Wherein, in order to significantly reduce COD, significantly remove the inorganic pollutant such as ammonia nitrogen, total nitrogen simultaneously.Under preferable case, in one-level A/O/ medium sediment pool, the condition of nitrification-denitrification denitrogenation processing comprises: the dissolved oxygen concentration in one-level A pond is 0.2 ~ 0.5mg/L, and hydraulic detention time is 5 ~ 10 hours, redox potential is-100 ~-300mV, and sludge concentration is 5000 ~ 7000mg/L; The dissolved oxygen concentration in one-level O pond is 2.0 ~ 2.5mg/L, and hydraulic detention time is 10 ~ 20 hours, and sludge concentration is 4000 ~ 5000mg/L; The nitrification liquid volume ratio refluxed to one-level A pond in one-level O pond is 3 ~ 4:1; The sludge volume ratio that medium sediment pool refluxes to one-level O pond is 0.5 ~ 1:1.Wherein, medium sediment pool hydraulic surface loading can be 0.61m
3/ m
2/ h.
Process in the water body input secondary A/O/MBR pond after the process of one-level A/O/ medium sediment pool, in secondary A pond, nitrate nitrogen is reduced total nitrogen content by denitrification, synchronously reduces COD; In secondary O pond, ammonia nitrogen is by nitrated generation nitrate nitrogen, and COD is degraded by aerobic biochemical; In MBR pond, the hydraulic detention time sufficiently long of Persistent organic pollutants, be also beneficial to the retaining of Autotrophic nitrification bacterium, Growth and reproduction, ammonia nitrogen continues nitrated generation nitrate nitrogen in MBR pond, and COD is by sustaining degradation.
Wherein, the pollutents such as COD, ammonia nitrogen, total nitrogen are removed in order to the degree of depth, under preferable case, in secondary A/O/MBR pond, the condition of nitrification-denitrification denitrogenation processing comprises: the dissolved oxygen concentration in secondary A pond is 0.2 ~ 0.5mg/L, hydraulic detention time is 5 ~ 10 hours, and redox potential is-100 ~-200mV, and sludge concentration is 3000 ~ 5000mg/L; The dissolved oxygen concentration in secondary O pond is 2.0 ~ 2.5mg/L, and hydraulic detention time is 10 ~ 20 hours, and sludge concentration is 3000 ~ 5000mg/L; The dissolved oxygen concentration in MBR pond is 3 ~ 5mg/L, and hydraulic detention time is 4 ~ 6 hours, and sludge concentration is 6000 ~ 8000mg/L; The nitrification liquid volume ratio refluxed to secondary A pond in secondary O pond is 2 ~ 4:1; The sludge volume ratio refluxed to secondary O pond in MBR pond is 0.5 ~ 1:1.
Water body, after nitrification-denitrification denitrogenation processing, under preferable case, after " one-level A/O/ medium sediment pool-secondary A/O/MBR pond " main biochemical cell processing, the degree of depth can remove the pollutents such as COD, ammonia nitrogen, total nitrogen.
In the inventive method, catalytic ozonation process is preferably undertaken by the synergy of ozone/heterogeneous catalyst in catalytic ozonation tower.
Wherein, in order to make COD and difficult degradation type organic pollutant degrade until mineralising further, ensure the CODcr≤60mg/L of the water body after process simultaneously.Under preferable case, the condition of catalytic ozonation process comprises: in catalytic ozonation tower, and the dosage of ozone is 60 ~ 90 grams of/ton of staying waters, and controlling catalytic ozonation tower hydraulic detention time is 20 ~ 30min; Fill heterogeneous catalyst in catalytic ozonation tower, the packing height of heterogeneous catalyst is 50 ~ 70% of tower body height.
In the present invention, particular requirement be there is no to the concrete kind of heterogeneous catalyst, the various ozone catalytic oxidation catalysts that can reduce water body CODcr value that this area can be adopted to commonly use.In order to reduce CODcr value further, amorphous alumina preferably mixes in butt weight 100:1 ~ 30 ratio with hydroxyl oxidize iron powder by described heterogeneous catalyst; Through the finished catalyst that rolling granulation, maintenance, oven dry, each step of roasting are made; The preparation method of described heterogeneous catalyst comprises the following steps:
A amorphous alumina mixes with hydroxyl oxidize iron powder by ();
B step (a) gained mixture is put into rotation tablets press by (), spray into binding agent and carry out rolling granulation, binding agent selects one in water, silicon sol, Alumina gel or its mixture, spray into solution or colloidal form atomization, the amount that binding agent sprays into is 2 ~ 50% of amorphous alumina total mass; The diameter controlling granulation is 1 ~ 8mm;
The maintenance under the water vapor condition of 100 ~ 110 DEG C of c particulate matter that step (b) obtains by (), curing time 3 ~ 24 hours;
D catalyzer that step (c) obtains by () is dried; Bake out temperature is 50 ~ 180 DEG C, and time of drying is 2 ~ 10 hours, then roasting; The maturing temperature of catalyzer is 400 ~ 600 DEG C, and roasting time is 2 ~ 8 hours; Obtain finished catalyst,
Described amorphous alumina is obtained through high temperature fast dewatering by industrial aluminium hydroxide, and its specific surface area is 150 ~ 350m
2/ g, total pore volume 0.20 ~ 0.45mL/g, mean particle size 1 ~ 80 μm;
Described hydrous iron oxide chemical formula is α-FeO (OH), and its specific surface area is greater than 80m
2/ g, total pore volume is greater than 0.2mL/g, and acicular particles length is 0.2 ~ 1mm.
In the inventive method, as shown in Figure 1, the equipment containing sour heavy crude refinery saline sewage treatment process for realizing the present invention preferably includes the technique unit of order setting: homogeneous regulating tank 1, swash plate oil eliminator 2, one-level cavitation air flotation equipment 3, secondary air-dissolving air-float equipment 4, inner circulating aerating biological filtering tank 5, anaerobic hydrolysis-acidification tank 6, one-level A pond 7, one-level O pond 8, medium sediment pool 9, secondary A pond 10, secondary O pond 11, MBR pond 12 and catalytic ozonation tower 13.Under preferable case, by sewer line sequential communication between described technique unit.
The inventive method is applicable to high containing sour heavy crude both at home and abroad, as Da Liya, new Wenchang, Bath Lip river, crude oil such as the new Xijiang River, Peng Lai etc.
Embodiment
The present invention is further illustrated for following embodiment, but therefore do not limit the present invention.
The treatment facility containing sour heavy crude refinery saline sewage in the present invention comprises the technique unit that order is arranged: homogeneous regulating tank 1, swash plate oil eliminator 2, one-level cavitation air flotation equipment 3, secondary air-dissolving air-float equipment 4, inner circulating aerating biological filtering tank 5, anaerobic hydrolysis-acidification tank 6, one-level A pond 7, one-level O pond 8, medium sediment pool 9, secondary A pond 10, secondary O pond 11, MBR pond 12 and catalytic ozonation tower 13, by sewer line sequential communication between described technique unit.Each technique unit that the present invention uses, as being not particularly limited, is various instruments, device or equipment that this area is conventional.
Homogeneous regulating tank: ∮ 14m × 17.82m.
Swash plate oil eliminator: 9m × 6m × 6.3m, the residence time is 66min.
One-level cavitation air flotation equipment: purchased from McWong Environmental & Energy Group (Shanghai), model is CAF-150E.
Secondary air-dissolving air-float equipment: dissolved-air pressure is 0.6MPa, and the residence time is 12.4min, purchased from Liaoning Huafu-Ai De Mo Environmental Protection Equipment Co., Ltd, model is ADAF-150.
Inner circulating aerating biological filtering tank: 96m × 15m × 5m, the residence time is 15h.
Anaerobic hydrolysis-acidification tank: ∮ 20m × 17.82m.
Between one-level A pond: 17.75m × 17m × 6m × 2.
Between one-level O pond: 22.3m × 10.9m × 6m × 4.
Medium sediment pool: ∮ 25m × 4.2m.
Secondary A pond: between 12.5m × 7.5m × 6m × 4.
Secondary O pond: between 12.5m × 7.5m × 6m × 4.
Between MBR pond: 12m × 7.7m × 5.1m × 2.
Catalytic ozonation tower: ∮ 3m × 8.5m.
Aluminium iron polychloride to be radically reformed water purification equipment company limited purchased from Shenzhen; Polymerize aluminum chloride to be radically reformed water purification equipment company limited purchased from Shenzhen; Poly-ferric chloride is purchased from Zhong Run fine chemicals company limited of Wuhan City; Polyacrylamide is purchased from CNOOC Tianjin Chemical Research & Design Institute, and model is TS-424.
In sewage, the measuring method of petroleum content: GB/T 16488-1996.
The measuring method of CODcr: GB11914-89.
The measuring method of ss suspended solid content: GB11901-89.
BOD
5measuring method: GB7488-87.
The measuring method of COD: GB11914-89.
The measuring method of total nitrogen content: HJ636-2012.
The measuring method of ammonia-nitrogen content: GB7478-87.
Preparation embodiment
Prepare heterogeneous catalyst according to the method for embodiment 1 in Chinese patent application ZL 201010287230.2, concrete grammar is: get 110gFeOOH powder (commercial goods; Specific Surface Area Measurement 125m
2/ g) and 5kg amorphous alumina (commercial goods, Specific Surface Area Measurement 260m
2/ g) mix, use water to stop to during particle diameter 3mm for binding agent carries out rolling granulation, maintenance 20hr at 101 DEG C, 110 DEG C of dry 4hr, 450 DEG C of roasting 3hr, obtain heterogeneous catalyst.
Embodiment 1
The present embodiment is for illustration of the treatment process containing sour heavy crude refinery saline sewage of the present invention.
To concentrate in input homogeneous regulating tank 1 containing each point source saline sewage of sour heavy crude Peng Lai 19-3 crude oil refinery, regularly, the point source saline sewage of irregularly discharge mixes and realizes homogeneous in homogeneous regulating tank 1, and the petroleum content after saline sewage mixing homogeneous is 732mg/L, CODcr is 4615mg/L, BOD
5/ COD is 0.4, ss suspended solid content is 1233mg/L, ammonia-nitrogen content is 78mg/L, total nitrogen content is 120mg/L; By the saline sewage gravity settling after homogeneous 36 hours, make oil slick, macrobead SS is separated with water body, reclaim the oil slick floating up to homogeneous regulating tank 1 top, remove the macrobead SS be settled down to bottom homogeneous regulating tank 1; Process in the water body input swash plate oil eliminator 2 in homogeneous regulating tank 1, reclaim the oil droplet floating up to swash plate oil eliminator 2 top, remove the SS be settled down to bottom swash plate oil eliminator 2; Input in one-level cavitation air flotation equipment 3 after water body in swash plate oil eliminator 2 is mixed with aluminium iron polychloride, polyacrylamide and process, the dosage of aluminium iron polychloride is 120 grams of/ton of staying waters, the dosage of polyacrylamide is 4 grams of/ton of staying waters, removes oil in water emulsion and the colloidal attitude suspended substance at one-level cavitation air flotation equipment 3 top; Input in secondary air-dissolving air-float equipment 4 after water body in one-level cavitation air flotation equipment 3 is mixed with aluminium iron polychloride, polyacrylamide and process, the dosage of aluminium iron polychloride is 80 grams of/ton of staying waters, the dosage of polyacrylamide is 0.8 gram of/ton of staying water, removes oil in water emulsion and the suspended substance at secondary air-dissolving air-float equipment 4 top.Water body after the process of secondary air-dissolving air-float equipment 4, petroleum content is 5.3mg/L, CODcr is 2554mg/L, BOD
5/ COD is 0.469, ss suspended solid content is 8mg/L, ammonia-nitrogen content is 78mg/L, total nitrogen content is 120mg/L.
By the water body input inner circulating aerating biological filtering tank 5(filter tank in secondary air-dissolving air-float equipment 4 built with filtrate, filter material surface forms high-density microbial film, filtrate forms sludge filtering layer between gap) in carry out pre-treatment, the recycle ratio of inner circulating aerating biological filtering tank 5 is 30:1, hydraulic detention time is 14 hours, and in pond, dissolved oxygen concentration is 3.4mg/L; In pond fill diameter be the haydite of 8mm as biofilter material medium, biofilter material haydite Filled Dielectrics pond height is 70%.Water body after inner circulating aerating biological filtering tank 5 processes, petroleum content is 2.15mg/L, CODcr is 1159mg/L, BOD
5/ COD is 0.169, ammonia-nitrogen content is 73mg/L, total nitrogen content is 112mg/L.
Process in the water body input anaerobic hydrolysis-acidification tank 6 after inner circulating aerating biological filtering tank 5 processes, in anaerobic hydrolysis-acidification tank 6, dissolved oxygen concentration is 0.3mg/L, and hydraulic detention time is 40 hours, and redox potential is-250mV; Sludge concentration is 6700mg/L.Water body after anaerobic hydrolysis-acidification tank 6 processes, petroleum content is 0.45mg/L, CODcr is 1040mg/L, BOD
5/ COD is 0.254, ammonia-nitrogen content is 83mg/L, total nitrogen content is 110.7mg/L.
Process in the water body input one-level A/O/ medium sediment pool after anaerobic hydrolysis-acidification tank 6 processes, the dissolved oxygen concentration in one-level A pond 7 is 0.5mg/L, and hydraulic detention time is 9 hours, and redox potential is-130mV, and sludge concentration is 5230mg/L; The dissolved oxygen concentration in one-level O pond 8 is 2.5mg/L, and hydraulic detention time is 18 hours, and sludge concentration is 4500mg/L; The nitrification liquid volume ratio refluxed to one-level A pond 7 in one-level O pond 8 is 3:1; Medium sediment pool 9 hydraulic surface loading is 0.61m
3/ m
2/ h, the sludge volume that medium sediment pool 9 refluxes to one-level O pond 8 is than being 1:1.Water body after the process of one-level A/O/ medium sediment pool, petroleum content is 0.36mg/L, CODcr is 130.2mg/L, BOD
5/ COD is 0.11, total nitrogen content is 37.13mg/L, and ammonia-nitrogen content is 18.32mg/L.
Process in the water body input secondary A/O/MBR pond after the process of one-level A/O/ medium sediment pool, the dissolved oxygen concentration in secondary A pond 10 is 0.5mg/L, and hydraulic detention time is 8 hours, and redox potential is-120mV, and sludge concentration is 4100mg/L; The dissolved oxygen concentration in secondary O pond 11 is 2.0mg/L, and hydraulic detention time is 16 hours, and sludge concentration is 3600mg/L; The dissolved oxygen concentration in MBR pond 12 is 3.5mg/L, and hydraulic detention time is 6 hours, and sludge concentration is 7500mg/L; The nitrification liquid volume ratio refluxed to secondary A pond 10 in secondary O pond 11 is the sludge volume ratio refluxed to secondary O pond 11 in 2:1, MBR pond 12 is 1:1.Water body after the process of secondary A/O/MBR pond, petroleum content is 0.1mg/L, CODcr is 60.2mg/L, BOD
5/ COD is 0.13, total nitrogen content is 12.76mg/L, and ammonia-nitrogen content is 1.82mg/L.
Process in the water body input catalytic ozonation tower 13 after the process of secondary A/O/MBR pond, in catalytic ozonation tower 13, ozone dosage is 90 grams of/ton of staying waters, and catalytic ozonation tower 13 hydraulic detention time is 22min; The heterogeneous catalyst that preparation embodiment obtains is filled to 60% of tower body height.Water body after catalytic ozonation tower 13 processes, petroleum content is 0.05mg/L, CODcr is 48.6mg/L, BOD
5/ COD is 0, total nitrogen content is 12.76mg/L, and ammonia-nitrogen content is 0.08mg/L.
Embodiment 2
The present embodiment is for illustration of the treatment process containing sour heavy crude refinery saline sewage of the present invention.
To concentrate in input homogeneous regulating tank 1 containing each point source saline sewage of sour heavy crude Bath Lip river crude oil refinery, regularly, the point source saline sewage of irregularly discharge mixes and realizes homogeneous in homogeneous regulating tank 1, and the petroleum content after saline sewage mixing homogeneous is 943mg/L, CODcr is 5005mg/L, BOD
5/ COD is 0.42, ss suspended solid content is 1564mg/L, ammonia-nitrogen content is 78mg/L, total nitrogen content is 117mg/L; By the saline sewage gravity settling after homogeneous 36 hours, make oil slick, macrobead SS is separated with water body, reclaim the oil slick floating up to homogeneous regulating tank 1 top, remove the macrobead SS be settled down to bottom homogeneous regulating tank 1; Process in the water body input swash plate oil eliminator 2 in homogeneous regulating tank 1, reclaim the oil droplet floating up to swash plate oil eliminator 2 top, remove the SS be settled down to bottom swash plate oil eliminator 2; Input in one-level cavitation air flotation equipment 3 after water body in swash plate oil eliminator 2 is mixed with polymerize aluminum chloride, polyacrylamide and process, the dosage of polymerize aluminum chloride is 100 grams of/ton of staying waters, the dosage of polyacrylamide is 3 grams of/ton of staying waters, removes oil in water emulsion and the colloidal attitude suspended substance at one-level cavitation air flotation equipment 3 top; Input in secondary air-dissolving air-float equipment 4 after water body in one-level cavitation air flotation equipment 3 is mixed with polymerize aluminum chloride, polyacrylamide and process, the dosage of polymerize aluminum chloride is 100 grams of/ton of staying waters, the dosage of polyacrylamide is 1.0 grams of/ton of staying waters, removes oil in water emulsion and the suspended substance at secondary air-dissolving air-float equipment 4 top.Water body after the process of secondary air-dissolving air-float equipment 4, petroleum content is 3.65mg/L, CODcr is 2596mg/L, BOD
5/ COD is 0.38, ss suspended solid content is 6mg/L, ammonia-nitrogen content is 78mg/L, total nitrogen content is 117mg/L.
By the water body input inner circulating aerating biological filtering tank 5(filter tank in secondary air-dissolving air-float equipment 4 built with filtrate, filter material surface forms high-density microbial film, filtrate forms sludge filtering layer between gap) in carry out pre-treatment, the recycle ratio of inner circulating aerating biological filtering tank 5 is 20:1, hydraulic detention time is 15 hours, and in pond, dissolved oxygen concentration is 5.0mg/L; In pond fill diameter be the haydite of 10mm as biofilter material medium, biofilter material haydite Filled Dielectrics pond height is 60%.Water body after inner circulating aerating biological filtering tank 5 processes, petroleum content is 1.79mg/L, CODcr is 1102mg/L, BOD
5/ COD is 0.18, ammonia-nitrogen content is 83mg/L, total nitrogen content is 122mg/L.
Process in the water body input anaerobic hydrolysis-acidification tank 6 after inner circulating aerating biological filtering tank 5 processes, in anaerobic hydrolysis-acidification tank 6, dissolved oxygen concentration is 0.2mg/L, and hydraulic detention time is 48 hours, and redox potential is-300mV; Sludge concentration is 6000mg/L.Water body after anaerobic hydrolysis-acidification tank 6 processes, petroleum content is 1.33mg/L, CODcr is 728mg/L, BOD
5/ COD is 0.23, ammonia-nitrogen content is 75mg/L, total nitrogen content is 115mg/L.
Process in the water body input one-level A/O/ medium sediment pool after anaerobic hydrolysis-acidification tank 6 processes, the dissolved oxygen concentration in one-level A pond 7 is 0.3mg/L, and hydraulic detention time is 10 hours, and redox potential is-100mV, and sludge concentration is 5000mg/L; The dissolved oxygen concentration in one-level O pond 8 is 2.2mg/L, and hydraulic detention time is 20 hours, and sludge concentration is 5000mg/L; The nitrification liquid volume ratio refluxed to one-level A pond 7 in one-level O pond 8 is 3.5:1; Medium sediment pool 9 hydraulic surface loading is 0.61m
3/ m
2/ h, the sludge volume that medium sediment pool 9 refluxes to one-level O pond 8 is than being 0.8:1.Water body after the process of one-level A/O/ medium sediment pool, petroleum content is 0.68mg/L, CODcr is 128mg/L, BOD
5/ COD is 0.13, total nitrogen content is 37mg/L, and ammonia-nitrogen content is 9.5mg/L.
Process in the water body input secondary A/O/MBR pond after the process of one-level A/O/ medium sediment pool, the dissolved oxygen concentration in secondary A pond 10 is 0.3mg/L, and hydraulic detention time is 10 hours, and redox potential is-200mV, and sludge concentration is 5000mg/L; The dissolved oxygen concentration in secondary O pond 11 is 2.5mg/L, and hydraulic detention time is 20 hours, and sludge concentration is 3000mg/L; The dissolved oxygen concentration in MBR pond 12 is 3.0mg/L, and hydraulic detention time is 5 hours, and sludge concentration is 6000mg/L; The nitrification liquid volume ratio refluxed to secondary A pond 10 in secondary O pond 11 is the sludge volume ratio refluxed to secondary O pond 11 in 3:1, MBR pond 12 is 0.8:1.Water body after the process of secondary A/O/MBR pond, petroleum content is 0.08mg/L, CODcr is 63mg/L, BOD
5/ COD is 0.05, total nitrogen content is 18mg/L, and ammonia-nitrogen content is 0.9mg/L.
Process in the water body input catalytic ozonation tower 13 after the process of secondary A/O/MBR pond, in catalytic ozonation tower 13, ozone dosage is 80 grams of/ton of staying waters, and catalytic ozonation tower 13 hydraulic detention time is 20min; The heterogeneous catalyst that preparation embodiment obtains is filled to 70% of tower body height.Water body after catalytic ozonation tower 13 processes, petroleum content is 0mg/L, CODcr is 40.6mg/L, BOD
5/ COD is 0, total nitrogen content is 18mg/L, and ammonia-nitrogen content is 0.1mg/L.
Embodiment 3
The present embodiment is for illustration of the treatment process containing sour heavy crude refinery saline sewage of the present invention.
To concentrate in input homogeneous regulating tank 1 containing each point source saline sewage of sour heavy crude new Xijiang River crude oil refinery, regularly, the point source saline sewage of irregularly discharge mixes and realizes homogeneous in homogeneous regulating tank 1, and the petroleum content after saline sewage mixing homogeneous is 689mg/L, CODcr is 4003mg/L, BOD
5/ COD is 0.38, ss suspended solid content is 1024mg/L, ammonia-nitrogen content is 81mg/L, total nitrogen content is 129mg/L; By the saline sewage gravity settling after homogeneous 36 hours, make oil slick, macrobead SS is separated with water body, reclaim the oil slick floating up to homogeneous regulating tank 1 top, remove the macrobead SS be settled down to bottom homogeneous regulating tank 1; Process in the water body input swash plate oil eliminator 2 in homogeneous regulating tank 1, reclaim the oil droplet floating up to swash plate oil eliminator 2 top, remove the SS be settled down to bottom swash plate oil eliminator 2; Input in one-level cavitation air flotation equipment 3 after water body in swash plate oil eliminator 2 is mixed with poly-ferric chloride, polyacrylamide and process, the dosage of poly-ferric chloride is 150 grams of/ton of staying waters, the dosage of polyacrylamide is 5 grams of/ton of staying waters, removes oil in water emulsion and the colloidal attitude suspended substance at one-level cavitation air flotation equipment 3 top; Input in secondary air-dissolving air-float equipment 4 after water body in one-level cavitation air flotation equipment 3 is mixed with poly-ferric chloride, polyacrylamide and process, the dosage of poly-ferric chloride is 50 grams of/ton of staying waters, the dosage of polyacrylamide is 0.5 gram of/ton of staying water, removes oil in water emulsion and the suspended substance at secondary air-dissolving air-float equipment 4 top.Water body after the process of secondary air-dissolving air-float equipment 4, petroleum content is 6.31mg/L, CODcr is 2703mg/L, BOD
5/ COD is 0.39, ss suspended solid content is 7mg/L, ammonia-nitrogen content is 81mg/L, total nitrogen content is 130mg/L.
By the water body input inner circulating aerating biological filtering tank 5(filter tank in secondary air-dissolving air-float equipment 4 built with filtrate, filter material surface forms high-density microbial film, filtrate forms sludge filtering layer between gap) in carry out pre-treatment, the recycle ratio of inner circulating aerating biological filtering tank 5 is 25:1, hydraulic detention time is 10 hours, and in pond, dissolved oxygen concentration is 3.0mg/L; In pond fill diameter be the haydite of 12mm as biofilter material medium, biofilter material haydite Filled Dielectrics pond height is 65%.Water body after inner circulating aerating biological filtering tank 5 processes, petroleum content is 2.56mg/L, CODcr is 1119mg/L, BOD
5/ COD is 0.16, ammonia-nitrogen content is 85mg/L, total nitrogen content is 129mg/L.
Process in the water body input anaerobic hydrolysis-acidification tank 6 after inner circulating aerating biological filtering tank 5 processes, in anaerobic hydrolysis-acidification tank 6, dissolved oxygen concentration is 0.5mg/L, and hydraulic detention time is 24 hours, and redox potential is-100mV; Sludge concentration is 10000mg/L.Water body after anaerobic hydrolysis-acidification tank 6 processes, petroleum content is 1.35mg/L, CODcr is 758mg/L, BOD
5/ COD is 0.216, ammonia-nitrogen content is 85mg/L, total nitrogen content is 129mg/L.
Process in the water body input one-level A/O/ medium sediment pool after anaerobic hydrolysis-acidification tank 6 processes, the dissolved oxygen concentration in one-level A pond 7 is 0.2mg/L, and hydraulic detention time is 5 hours, and redox potential is-300mV, and sludge concentration is 7000mg/L; The dissolved oxygen concentration in one-level O pond 8 is 2.0mg/L, and hydraulic detention time is 10 hours, and sludge concentration is 4000mg/L; The nitrification liquid volume ratio refluxed to one-level A pond 7 in one-level O pond 8 is 4:1; Medium sediment pool 9 hydraulic surface loading is 0.61m
3/ m
2/ h, the sludge volume that medium sediment pool 9 refluxes to one-level O pond 8 is than being 0.5:1.Water body after the process of one-level A/O/ medium sediment pool, petroleum content is 0.97mg/L, CODcr is 147mg/L, BOD
5/ COD is 0.105, total nitrogen content is 47mg/L, and ammonia-nitrogen content is 10.8mg/L.
Process in the water body input secondary A/O/MBR pond after the process of one-level A/O/ medium sediment pool, the dissolved oxygen concentration in secondary A pond 10 is 0.2mg/L, and hydraulic detention time is 5 hours, and redox potential is-100mV, and sludge concentration is 3000mg/L; The dissolved oxygen concentration in secondary O pond 11 is 2.2mg/L, and hydraulic detention time is 10 hours, and sludge concentration is 5000mg/L; The dissolved oxygen concentration in MBR pond 12 is 5.0mg/L, and hydraulic detention time is 4 hours, and sludge concentration is 8000mg/L; The nitrification liquid volume ratio refluxed to secondary A pond 10 in secondary O pond 11 is the sludge volume ratio refluxed to secondary O pond 11 in 4:1, MBR pond 12 is 0.5:1.Water body after the process of secondary A/O/MBR pond, petroleum content is 0.01mg/L, CODcr is 66mg/L, BOD
5/ COD is 0.03, total nitrogen content is 17mg/L, and ammonia-nitrogen content is 0.3mg/L.
Process in the water body input catalytic ozonation tower 13 after the process of secondary A/O/MBR pond, in catalytic ozonation tower 13, ozone dosage is 60 grams of/ton of staying waters, and catalytic ozonation tower 13 hydraulic detention time is 30min; The heterogeneous catalyst that preparation embodiment 1 obtains is filled to 50% of tower body height.Water body after catalytic ozonation tower 13 processes, petroleum content is 0mg/L, CODcr is 45mg/L, BOD
5/ COD is 0, total nitrogen content is 17mg/L, and ammonia-nitrogen content is 0.1mg/L.
Comparative example 1
According to the method in ZL 200910081479.5 to processing containing sour heavy crude Peng Lai 19-3 crude oil refinery saline sewage in embodiment 1, the method is specific as follows: will carry out preliminary oil removing containing sour heavy crude Peng Lai 19-3 crude oil refinery saline sewage input grille well, flat flow settling bowl in embodiment 1, then pumping plant water collecting basin is entered, by one-level lift pump, the water body in pumping plant water collecting basin is pumped into regulating tank, when flooding quantity, water quality are normal, water body enters sedimentation oil removing pot and processes, and this tank arranges constant high water outlet liquid level 16m;
Water body after the process of sedimentation oil removing pot processes from flowing in inclined plate grease device, and the water body gravity flow after inclined plate grease enters the (dosing in two-stage air flotation processing device: XN-FH1 flocculation agent host 0.15m of two-stage air flotation processing device
3/ h, XN-FH2 flocculation agent auxiliary agent 0.18m
3/ h); Wherein, the water body after the process of inclined plate grease device, petroleum content is 95mg/L; Water body after the process of one-level air-floating apparatus, petroleum content is 55mg/L; Water body after the process of secondary air-floatation device, petroleum content is 18mg/L.
By the water body input one-stage hydrolysis souring tank after the process of secondary air-floatation device, processing parameter: dissolved oxygen is 0.2mg/L; By the water body input CAST reaction tank after the process of one-stage hydrolysis souring tank, processing parameter: return sludge ratio 20%, dissolved oxygen: bioselection section 0.2mg/L, main reaction section 3mg/L; By the water body input secondary hydrolysis acidification pool after the process of CAST reaction tank, pond built with anaerobic activated sludge, processing parameter: dissolved oxygen is 0.2mg/L; By after the process of secondary hydrolysis acidification pool water body input BAF, pond built with filtrate and aerobic biologic membrane, processing parameter: dissolved oxygen: 3mg/L; By the water body input coagulation basin (dosing in coagulation basin: XN-FH2 flocculation agent auxiliary agent 0.03m after BAF process
3/ h), processing parameter: outlet ss suspended solid is 115mg/L; By the water body input Lan Meila inclined-plate clarifying basin after coagulation basin process, processing parameter: outlet ss suspended solid is 94mg/L; Finally by the water body Input Monitor Connector pond after the process of Lan Meila inclined-plate clarifying basin, processing parameter: outlet CODcr is 90mg/L.
Water body after monitoring pool process, petroleum content is 6.25mg/L, CODcr is 90mg/L, BOD
5/ COD is 0.11, total nitrogen content is 43.8mg/L, and ammonia-nitrogen content is 12.2mg/L.
Compared with comparative example 1 from embodiment 1-3, the inventive method is used to process containing sour heavy crude refinery saline sewage, obviously can reduce the CODcr value of the rear water body of process, petroleum content, ammonia-nitrogen content and total nitrogen content, after enabling process, water body meets CODcr≤60mg/L, petroleum-type≤5mg/L, ammonia nitrogen≤10mg/L, total nitrogen≤40mg/L requirement.
More than describe the preferred embodiment of the present invention in detail; but the present invention is not limited to the detail in above-mentioned embodiment, within the scope of technical conceive of the present invention; can carry out multiple simple variant to technical scheme of the present invention, these simple variant all belong to protection scope of the present invention.
It should be noted that in addition, each concrete technical characteristic described in above-mentioned embodiment, in reconcilable situation, can be combined by any suitable mode, in order to avoid unnecessary repetition, the present invention illustrates no longer separately to various possible array mode.
In addition, also can carry out arbitrary combination between various different embodiment of the present invention, as long as it is without prejudice to thought of the present invention, it should be considered as content disclosed in this invention equally.
Claims (15)
1. the treatment process containing sour heavy crude refinery saline sewage, it is characterized in that, described method comprises and being handled as follows successively by described saline sewage: gravity settling oil removal treatment, sloping plate deposition oil removal treatment, two-stage air-flotation process, bio-aeration process, anaerobic hydrolysis-acidification process, nitrification-denitrification denitrogenation processing and catalytic ozonation process.
2. method according to claim 1, wherein, described gravity settling oil removal treatment is carried out in homogeneous regulating tank.
3. method according to claim 1, wherein, described sloping plate deposition oil removal treatment is carried out in swash plate oil eliminator.
4. method according to claim 1, wherein, described two-stage air-flotation process carries out respectively in one-level cavitation air flotation equipment and secondary air-dissolving air-float equipment.
5. method according to claim 4, wherein, described two-stage air-flotation process inputs in one-level cavitation air flotation equipment after first being mixed with coagulating agent, coagulant aids by the water body after sloping plate deposition oil removal treatment to process; Input in secondary air-dissolving air-float equipment after again the water body after one-level cavitation air flotation device processes being mixed with coagulating agent, coagulant aids and process.
6. method according to claim 5, wherein, described coagulating agent is at least one in aluminium iron polychloride, polymerize aluminum chloride, poly-ferric chloride, and described coagulant aids is polyacrylamide.
7. method according to claim 6, wherein, in one-level cavitation air flotation equipment, the dosage of described coagulating agent is 100 ~ 150 grams of/ton of staying waters, and the dosage of described coagulant aids is 3 ~ 5 grams of/ton of staying waters; In secondary air-dissolving air-float equipment, the dosage of described coagulating agent is 50 ~ 100 grams of/ton of staying waters, and the dosage of described coagulant aids is 0.5 ~ 1.0 gram of/ton of staying water.
8. method according to claim 1, wherein, described bio-aeration process is carried out in inner circulating aerating biological filtering tank.
9. method according to claim 8, wherein, the condition of described bio-aeration process comprises: the recycle ratio of inner circulating aerating biological filtering tank is 20 ~ 30:1, and hydraulic detention time is 10 ~ 15 hours, and in pond, dissolved oxygen concentration is 3 ~ 5mg/L; In pond fill diameter be the haydite of 8 ~ 12mm as biofilter material medium, packing height accounts for 60 ~ 70% of pond height.
10. method according to claim 1, wherein, described anaerobic hydrolysis-acidification process is carried out in anaerobic hydrolysis-acidification tank.
11. methods according to claim 10, wherein, the condition of described anaerobic hydrolysis-acidification process comprises: the dissolved oxygen concentration in anaerobic hydrolysis-acidification tank is 0.2 ~ 0.5mg/L, hydraulic detention time is 24 ~ 48 hours, redox potential is-100 ~-300mV, and sludge concentration is 6000 ~ 10000mg/L.
12. methods according to claim 1, wherein, described nitrification-denitrification denitrogenation processing is carried out successively in one-level A/O/ medium sediment pool and secondary A/O/MBR pond.
13. methods according to claim 12, wherein, in one-level A/O/ medium sediment pool, the condition of process comprises: the dissolved oxygen concentration in one-level A pond is 0.2 ~ 0.5mg/L, hydraulic detention time is 5 ~ 10 hours, and redox potential is-100 ~-300mV, and sludge concentration is 5000 ~ 7000mg/L; The dissolved oxygen concentration in one-level O pond is 2.0 ~ 2.5mg/L, and hydraulic detention time is 10 ~ 20 hours, and sludge concentration is 4000 ~ 5000mg/L; The nitrification liquid volume ratio refluxed to one-level A pond in one-level O pond is 3 ~ 4:1; The sludge volume ratio that medium sediment pool refluxes to one-level O pond is 0.5 ~ 1:1;
In secondary A/O/MBR pond, the condition of process comprises: the dissolved oxygen concentration in secondary A pond is 0.2 ~ 0.5mg/L, and hydraulic detention time is 5 ~ 10 hours, and redox potential is-100 ~-200mV, and sludge concentration is 3000 ~ 5000mg/L; The dissolved oxygen concentration in secondary O pond is 2.0 ~ 2.5mg/L, and hydraulic detention time is 10 ~ 20 hours, and sludge concentration is 3000 ~ 5000mg/L; The dissolved oxygen concentration in MBR pond is 3 ~ 5mg/L, and hydraulic detention time is 4 ~ 6 hours, and sludge concentration is 6000 ~ 8000mg/L; The nitrification liquid volume ratio refluxed to secondary A pond in secondary O pond is 2 ~ 4:1; The sludge volume ratio refluxed to secondary O pond in MBR pond is 0.5 ~ 1:1.
14. methods according to claim 1, wherein, described catalytic ozonation process is undertaken by the synergy of ozone/heterogeneous catalyst in catalytic ozonation tower.
15. methods according to claim 14, wherein, the condition of described catalytic ozonation process comprises: in catalytic ozonation tower, and the dosage of ozone is 60 ~ 90 grams of/ton of staying waters, and controlling catalytic ozonation tower hydraulic detention time is 20 ~ 30min; Fill heterogeneous catalyst in catalytic ozonation tower, the packing height of heterogeneous catalyst is 50 ~ 70% of tower body height.
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Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106186573A (en) * | 2016-08-31 | 2016-12-07 | 柳州市润广科技有限公司 | A kind of method processing heavy metal wastewater thereby |
| CN108726787A (en) * | 2017-04-21 | 2018-11-02 | 中国石油天然气股份有限公司 | The processing method of crude oil electric desalting sewage |
| CN109550771A (en) * | 2018-12-11 | 2019-04-02 | 中化环境控股有限公司 | The minimizing technology and removal device of organic pollutant in industrial waste salt |
| CN110803830A (en) * | 2019-10-30 | 2020-02-18 | 惠州学院 | Oil refining wastewater strengthening pretreatment process |
| CN109550771B (en) * | 2018-12-11 | 2024-04-26 | 中化环境控股有限公司 | Method and device for removing organic pollutants in industrial waste salt |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101857335A (en) * | 2009-04-08 | 2010-10-13 | 中国石油天然气股份有限公司 | Method for carrying out advanced treatment on extremely-viscous crude sewage |
| CN102079613A (en) * | 2010-12-22 | 2011-06-01 | 上海广联建设发展有限公司 | Ozone catalytic oxidation biological fluidized bed sewage treatment plant and treatment method using same |
| WO2012030427A1 (en) * | 2010-09-02 | 2012-03-08 | General Electric Company | Method to treat produced waters from thermally induced heavy crude oil production (tar sands) |
-
2013
- 2013-11-14 CN CN201310566472.9A patent/CN104628221B/en active Active
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101857335A (en) * | 2009-04-08 | 2010-10-13 | 中国石油天然气股份有限公司 | Method for carrying out advanced treatment on extremely-viscous crude sewage |
| WO2012030427A1 (en) * | 2010-09-02 | 2012-03-08 | General Electric Company | Method to treat produced waters from thermally induced heavy crude oil production (tar sands) |
| CN102079613A (en) * | 2010-12-22 | 2011-06-01 | 上海广联建设发展有限公司 | Ozone catalytic oxidation biological fluidized bed sewage treatment plant and treatment method using same |
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106186573A (en) * | 2016-08-31 | 2016-12-07 | 柳州市润广科技有限公司 | A kind of method processing heavy metal wastewater thereby |
| CN108726787A (en) * | 2017-04-21 | 2018-11-02 | 中国石油天然气股份有限公司 | The processing method of crude oil electric desalting sewage |
| CN109550771A (en) * | 2018-12-11 | 2019-04-02 | 中化环境控股有限公司 | The minimizing technology and removal device of organic pollutant in industrial waste salt |
| CN109550771B (en) * | 2018-12-11 | 2024-04-26 | 中化环境控股有限公司 | Method and device for removing organic pollutants in industrial waste salt |
| CN110803830A (en) * | 2019-10-30 | 2020-02-18 | 惠州学院 | Oil refining wastewater strengthening pretreatment process |
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Address after: 100010 Beijing, Chaoyangmen, North Street, No. 25, No. Co-patentee after: China National Offshore Oil Corporation Patentee after: China Offshore Oil Group Co., Ltd. Co-patentee after: CNOOC Huizhou Petrochemical Co., Ltd. Co-patentee after: China University of Petroleum (Beijing) Address before: 100010 Beijing, Chaoyangmen, North Street, No. 25, No. Co-patentee before: China National Offshore Oil Corporation Patentee before: China National Offshore Oil Corporation Co-patentee before: CNOOC Huizhou Petrochemical Co., Ltd. Co-patentee before: China University of Petroleum (Beijing) |