CN105540893A - Cross flow coalescence-cavitation air floatation reactor and ternary produced water cross flow coalescence air floatation-A/O biological treatment method - Google Patents

Cross flow coalescence-cavitation air floatation reactor and ternary produced water cross flow coalescence air floatation-A/O biological treatment method Download PDF

Info

Publication number
CN105540893A
CN105540893A CN201511022237.0A CN201511022237A CN105540893A CN 105540893 A CN105540893 A CN 105540893A CN 201511022237 A CN201511022237 A CN 201511022237A CN 105540893 A CN105540893 A CN 105540893A
Authority
CN
China
Prior art keywords
water
sections
section
air
pipe
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Granted
Application number
CN201511022237.0A
Other languages
Chinese (zh)
Other versions
CN105540893B (en
Inventor
魏利
魏超
魏东
李春颖
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Harbin Institute of Technology
Original Assignee
Harbin Institute of Technology
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Harbin Institute of Technology filed Critical Harbin Institute of Technology
Priority to CN201511022237.0A priority Critical patent/CN105540893B/en
Publication of CN105540893A publication Critical patent/CN105540893A/en
Application granted granted Critical
Publication of CN105540893B publication Critical patent/CN105540893B/en
Active legal-status Critical Current
Anticipated expiration legal-status Critical

Links

Classifications

    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F9/00—Multistage treatment of water, waste water or sewage
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/24—Treatment of water, waste water, or sewage by flotation
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/40—Devices for separating or removing fatty or oily substances or similar floating material
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2103/00—Nature of the water, waste water, sewage or sludge to be treated
    • C02F2103/10—Nature of the water, waste water, sewage or sludge to be treated from quarries or from mining activities
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2301/00—General aspects of water treatment
    • C02F2301/08—Multistage treatments, e.g. repetition of the same process step under different conditions
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F3/00—Biological treatment of water, waste water, or sewage
    • C02F3/30—Aerobic and anaerobic processes

Abstract

The invention relates to a cross flow coalescence-cavitation air floatation reactor and a ternary produced water cross flow coalescence air floatation-A/O biological treatment method, belonging to the field of the oil field sewage treatment. The invention in particular relates to a method for treating the high-calcium ternary produced water of the oil field. The invention aims at solving the problems of the existing oil field high-calcium ternary produced water that the oil and water are difficult to separate, the emulsification degree of the produced water is high, the oil content is relatively high, and the suspended solids are difficult to remove. The cross flow coalescence-cavitation air floatation reactor comprises a cross flow coalescence oil remover, a primary-section air floatation reactor, a secondary-section air floatation reactor, a water dispensing device, a primary-section water dispensing corridor, a water outlet storage device, a settling device and a secondary-section water dispensing corridor. The treatment method comprises the following steps: I, cross flow coalescence air floatation treatment; II, anaerobic treatment; and III, aerobic treatment. The cross flow coalescence-cavitation air floatation reactor has the advantages that the recycled ternary produced water of the oil field reaches the standard: the oil content is less than or equal to 5 mg/L, the content of the suspended solids is less than or equal to 5mg/L, and the mid-value of the particle size is less than or equal to 1 micrometer. The cross flow coalescence-cavitation air floatation reactor and the ternary produced water cross flow coalescence air floatation-A/O biological treatment method are mainly used for treating the high-calcium ternary produced water of the oil field.

Description

Transverse flow is coalescent-cavitation air flotation reactor and ternary recovered water transverse flow agglomerated air floatation-A/O bioremediation
Technical field
The invention belongs to field of oilfield sewage treatment, be specifically related to a kind for the treatment of process of oil-field high-calcium type ternary recovered water.
Technical background
How to improve the problem that recovery ratio is institute's general concern in Oil extraction process, there are some researches show, after primary oil recovery and secondary oil recovery, still have the crude oil of 2/3rds to be retained in the middle of stratum.In order to improve the recovery ratio in oil field, driving with the ternary of adding chemically composited medicament the technology of adopting in the last few years and be taken as the representative of tertiary oil recovery technology and be applied.
Ternary drive adopt in the technology of adopting alkali, tensio-active agent, in polymkeric substance three kinds of medicaments, often kind of medicament has all played different effects.The interpolation of alkali can improve the emulsifying property of crude oil by the surface tension of reduction water-oil interface, the interpolation of alkali simultaneously can reduce the consumption of tensio-active agent and reduce medicament use cost.The interpolation of tensio-active agent can reduce the surface tension of profit equally.Drive in the technology of adopting in ternary, polymkeric substance can increase the viscosity of aqueous phase, reduces mobility ratio and the perviousness of aqueous phase.
Recovered water is regarded as the factory effluent of petroleum industry, and in present field produces, the multiple treatment processs such as physics, chemistry, biology is independent or conbined usage is applied to the process of recovered water.Although ternary drives the technology of adopting can increase recovery ratio more than 20%, but the chemical agent wherein added, water and oil is made to define more stable emulsified state, oil droplet is stablized more and volume reduces, thus make oily water separation become more difficult, in addition, in ternary recovered water, the volume of suspended solids and concentration are higher than the recovered water of water-drive oil recovery, and therefore the process of ternary recovered water is that petroleum industry is produced and proposed new challenge.Daqing oil field is China oil field that cumulative recovery is maximum so far, and produced quantity continuous more than 20 years in year are more than 4.3 × 10 7ton, therefore the annual recovered water produced is up to 3 × 10 8, these recovered waters need to reach reinjection standard after treatment.In recent years, different oily water separation techniques is applied to the process of oil field extracted water, in report in the past, sedimentation, air supporting, biological treatment, membrane separation technique are widely used in the process of water drive recovered water, but the related data being seen in the relevant ternary produced water disposal of report is still deficienter.
At present, domestic investigator mainly from physics sedimentation, add chemical agent, three aspects of carrying out a biological disposal upon start with and to process ternary recovered water.For the water quality characteristics of ternary recovered water, some investigators have emphatically carried out some researchs to chemical agent in ternary recovered water and suspended solids, oleaginousness, the impact of metal ion on recovered water oily water separation characteristic, and main progress is as follows:
The people such as the Wang Fanglin of Shanghai Communications University are according to the processing feature of ternary composite flooding water extraction, have developed degreaser DO1001, stirring intensity when having carried out deoiling effect, degreaser throwing amount, medicament strengthening reaction in laboratory experiment and the research such as churning time, and on the basis of desk research, carried out the research of on-the-spot small-sized process experimental installation.Investigator have studied the impact of ternary medicament on recovered water oily water separation characteristic by simulation alkali system ternary composite flooding water extraction in its academic dissertation, investigate water-oil interface characteristic, metal ion, soda acid, sequestrant and aeration, on the impact of ternary composite driving suspended solids content, study various physical separation method and chemical process targetedly to the centrifugation of ternary composite flooding water extraction.Sulfide scavenger is applied to the process of ternary recovered water by the Liu Wenjie of Daqing oil field designing institute, determines chemical feeding quantity and operational conditions.
Ye Qing have studied the factors such as ternary composite flooding water extraction medium viscosity, ternary content, oil bead diameter, ionic strength to the impact of ternary recovered water oily water separation characteristic in its academic dissertation, and have studied ternary recovered water water-oil interface character and rheological characteristics by the mode of indoor water distribution, analyze ternary recovered water oil droplet stable mechanism.Investigator adopts centrifuging, coagulation-air floatation, ultrasonic emulsion breaking method and electrolysis-By Bubble-floating Method to carry out process experimental study to ternary drive water exit in this research.
The Liu Shumeng of Shanghai Communications University starts with from oil removing, filtration, fine filtering three aspect, at efficient degreasing technical elements, carry out gas and take liquid-liquid rotational flow separation theory and applied research, at high efficiency filter technical elements, carry out hydrophilic fibre ball and filter ternary composite flooding water extraction experimental study, in Fine Filtration Technology, carry out the research of poly-drive water exit ultra-filtration membrane further treatment technique.
Wang Biao analyzes the impact of ASP oil-displacing agent component on ternary recovered water oily water separation characteristic and interfacial rheological characteristic matter in its academic dissertation, prepare lime mud treatment agent simultaneously, study the impact on treatment effect of its dosage, pH, agitation condition, settling time, initial oil content and temperature.
Wang Aijun simulates aeration sedimentation process in its academic dissertation, investigate the changing conditions of the indexs such as suspended solids, oleaginousness, polymer content, sulfide, silicate in ternary recovered water, analyze the composition of suspended solids, characterize the pattern of suspended solids, and have studied the principal element affecting suspended solids content change in ternary recovered water.
According to the water quality characteristics of ternary recovered water, built-up type sedimentation-tripping device is applied in the middle of the site disposal experiment of ternary recovered water by Many researchers.Such as, the people such as Cao Zhenkun apply force combination formula settling separation device, by field experiment, determine processing parameter, illustrate the process advantage compared with independent sedimentation process.Investigator Liu Wen application combination sedimentation filtration device process weak base type ternary recovered water, determines corresponding processing parameter.
The people such as Liu Changli by the applying filler being loaded with aerobic microbiological of having tamed in the process of ternary recovered water, analyze and to oil, usefulness is utilized to the degradation effect of oleaginousness and microorganism, explore the feasibility of microbe application in ternary produced water disposal.
From studying above, up to the present, the research of China to ternary produced water disposal is still in the starting stage.The medicament added in ternary recovered water, one side is that the productive life of the mankind provides extremely useful help, on the other hand but for the process of recovered water proposes new baptism in raising recovery ratio.At present for ternary recovered water use with sedimentation be core technology physical sepn technique and based on the chemical technology adding various medicament, need the auxiliary of a large amount of medicament on the one hand, add processing cost, on the other hand not in the decrement truly realizing pollutent, be not eco-friendly.The plurality of advantages such as microbe application has efficiently in sewage disposal, low cost, the materials such as the polymkeric substance in ternary medicament, tensio-active agent have extremely strong biotic resistance and toxicity, if process is not good at, serious destruction can be caused to storage environment, based on these characteristics, there is more suffering in its biological degradation, but microorganism has higher aberration rate and environmental compatibility, microbiological deterioration and innoxiously will become the effective means solving ternary medicament process.Can be found by research in the past, the process being applied to ternary recovered water is still in the starting exploratory stage and does not sum up the easy-to-use treatment process of complete set.In research in the past, processing intent for ternary recovered water is all in order to field produces service, thus formulated processing target is mostly the water quality standard reaching re-injection, the water-quality guideline paid close attention to, based on oleaginousness, suspended solids, viscosity, median particle size etc., have ignored the toxicant in ternary recovered water and hazardous and noxious substances.But a problem that can not be ignored is, the oilfield exploitation of current China has entered the High water cut stage, wastewater discharge will be a problem that cannot avoid, therefore make produced water disposal reach new demand that higher water quality requirement is field produces.
Summary of the invention
It is large that object of the present invention will solve present oil-field high-calcium type ternary produced water disposal difficulty, be mainly manifested in oily water separation difficulty, recovered water emulsification degree is high, oleaginousness is wherein higher, suspended substance is difficult to the problem removed, and provide a kind of transverse flow coalescent-cavitation air flotation reactor and ternary recovered water transverse flow agglomerated air floatation-A/O bioremediation.
Transverse flow is coalescent-and cavitation air flotation reactor comprises lateral flow coalescence oil remover, one section of air supporting reactor, two sections of air supporting reactors, water dispensing apparatus, one section of water distribution vestibule, water outlet holder, sedimentation device, water inlet pipe, flow coalescent oil exit pipe, flow coalescent collection tank, upper hold-down grid, baffle plate, flow coalescent perforated sludge discharge pipe, one section of slag receiving trough, one section of scum pipe, one section of effluent trough, one section of rising pipe, one section is held air water pipe, one section of perforated sludge discharge pipe, two sections are held air water pipe, sedimentation oil exit pipe, sedimentation rising pipe, two sections of water distribution vestibules, sedimentation perforated sludge discharge pipe, two sections of perforated sludge discharge pipes, lower hold-down grid, two sections of water inlet pipes, two sections of scum pipes, two sections of slag receiving troughs and sedimentation collection tank,
By described upper hold-down grid and lower hold-down grid, lateral flow coalescence oil remover is separated into oil extraction district from top to bottom successively, packing area and the coalescent Ji Yu district of stream, described water dispensing apparatus is arranged on the side of lateral flow coalescence oil remover, at the opposite side of lateral flow coalescence oil remover, one section of water distribution vestibule is set, and packing area is communicated with one section of water distribution vestibule with water dispensing apparatus, the coalescent collection tank of stream is set above water dispensing apparatus, the coalescent collection tank of described stream is communicated with by flowing coalescent draining valve with oil extraction district, bottom water dispensing apparatus, water inlet pipe is set, the coalescent oil exit pipe of stream is set bottom the coalescent collection tank of stream, at lower hold-down grid, baffle plate is set towards stream side, coalescent Ji Yu district, the coalescent perforated sludge discharge pipe of stream is set bottom the coalescent Ji Yu district of stream,
By one section of dividing plate, one section of air supporting reactor is separated into one section of air flotation zone and point pool, in one section of air flotation zone, one section of dividing plate top arranges one section of slag receiving trough, in point pool, one section of air supporting sidewall of reactor top arranges one section of effluent trough, one section of described air flotation zone is communicated with one section of water distribution vestibule by one section of water intaking valve, one section of described slag receiving trough is communicated with one section of air flotation zone by one section of residual cake valve, and one section of scum pipe is set at one section of slag receiving trough, one section of described effluent trough is communicated with a point pool by one section of outlet valve, and bottom one section of effluent trough, one section of rising pipe is set, one section of described air supporting reactor bottom is provided with a Duan Jiyu district, one section of perforated sludge discharge pipe is set bottom a Duan Jiyu district,
Described one section is held air water pipe and runs through one section of air supporting reactor, one section of one end holding air water pipe is communicated with one section of water distribution vestibule, one section of the other end holding air water pipe and two sections hold gas cross current, described two sections are held air water pipe and run through two sections of air supporting reactors, and two sections of the other ends holding air water pipe are communicated with two sections of water distribution vestibules;
By two sections of dividing plates, two sections of air supporting reactors are separated into inhalant region and two sections of air flotation zones, in two sections of air flotation zones, two sections of dividing plate tops arrange two sections of slag receiving troughs, in inhalant region, two sections of air supporting sidewall of reactor tops arrange two sections of inlet flumes, two sections of described air flotation zones are communicated with two sections of water distribution vestibules by two sections of outlet valves, two sections of described slag receiving troughs are communicated with two sections of air flotation zones by two sections of residual cake valves, and two sections of scum pipes are set at two sections of slag receiving troughs, two sections of described inlet flumes are communicated with inhalant region by two sections of water intaking valves, two sections of water inlet pipes are set bottom two sections of inlet flumes, and two sections of water inlet pipes are communicated with one section of rising pipe, two sections of described air supporting reactor bottoms are provided with two Duan Jiyu districts, arrange two sections of perforated sludge discharge pipes bottom two Duan Jiyu districts,
The opposite side of described two sections of water distribution vestibules is communicated with sedimentation device by sedimentary province water entry, at the opposite side of sedimentation device, water outlet holder is set, sedimentation collection tank is set above water outlet holder, described sedimentation collection tank is communicated with sedimentation device by sedimentation draining valve, described water outlet holder is communicated with sedimentation device by sedimentation outlet valve, sedimentation rising pipe is set bottom water outlet holder, sedimentation oil exit pipe is set bottom sedimentation collection tank, settlement volume silt district is provided with bottom described sedimentation device, bottom settlement volume silt district, sedimentation perforated sludge discharge pipe is set.
Utilize above-mentioned transverse flow coalescent-cavitation air flotation reactor carries out ternary recovered water transverse flow agglomerated air floatation-A/O bioremediation, specifically completes according to the following steps:
One, transverse flow agglomerated air floatation process: oil field ternary recovered water is passed into transverse flow coalescent-cavitation air flotation reactor in process, obtain transverse flow agglomerated air floatation process water;
Two, anaerobic treatment: utilize UASB reactor, IC reactor or anaerobism sbr reactor device to carry out anaerobic treatment to transverse flow agglomerated air floatation process water, obtain anaerobic treatment water, utilize in anaerobic treatment process and tamed the anaerobic activated sludge with efficient degradation usefulness and carry out biological reinforced process, hydraulic detention time is 12h ~ 24h;
Three, aerobic treatment: utilize aerobic activated sludge or aerobe biofilm to carry out aerobic treatment to anaerobic treatment water, namely complete ternary recovered water transverse flow agglomerated air floatation-A/O to carry out a biological disposal upon, obtain processing rear sewage, utilize in Aerobic and tamed the capable biological reinforced process of the microorganism species with higher biological degradation activity, hydraulic detention time is 8h ~ 16h.
Advantage of the present invention: the characteristic that the present invention is directed to ternary recovered water, air flotation technology is first adopted to carry out the separation of profit, the follow-up profit for remaining carries out A/O Biochemical method, the standard of the re-injection of recovered water can be reached, wherein innovative point is, the air supporting mode that this change is traditional, employing be transverse flow coalescent-cavitation air flotation reactor, the efficiency of air supporting and petroleum-type recovery can be improved greatly, adopt biological method can realize the advanced treatment of oil-containing simultaneously.Suspended substance also can reduce greatly.Finally realize the up to standard of oil field ternary produced-water reinjection: oleaginousness≤5mg/L, suspended substance≤5mg/L, median particle size≤1 micron.
Accompanying drawing explanation
Fig. 1 be transverse flow coalescent-cavitation air flotation reactor in the structural representation of water dispensing apparatus, lateral flow coalescence oil remover, one section of water distribution vestibule and one section of air supporting reactor;
Fig. 2 be transverse flow coalescent-cavitation air flotation reactor in two sections of air supporting reactors, two sections of water distribution vestibules, sedimentation device and water outlet holders structural representation;
Fig. 3 is oleaginousness clearance graphic representation, in figure ● represent oleaginousness clearance curve in one section of water distribution vestibule 8, and in figure, ■ represents oleaginousness clearance curve in two sections of water distribution vestibules 26, in figure ▲ represent oleaginousness clearance curve in water outlet holder 9;
Fig. 4 is removal efficiency graphic representation, in figure ● represent suspended substance removal rate curve in one section of water distribution vestibule 8, in figure, ■ represents suspended substance removal rate curve in two sections of water distribution vestibules 26, in figure ▲ represent suspended substance removal rate curve in water outlet holder 9;
Fig. 5 be treatment time-oleaginousness graphic representation, in figure, ■ represents oleaginousness curve in oil field ternary recovered water, in figure ● represent oleaginousness curve in transverse flow agglomerated air floatation process water described in step one, in figure ▲ represent described in step 3 process after oleaginousness curve in sewage;
Fig. 6 be treatment time-concentration of suspension graphic representation, in figure, ■ represents concentration of suspension curve in oil field ternary recovered water, in figure ● represent concentration of suspension curve in transverse flow agglomerated air floatation process water described in step one, in figure ▲ represent described in step 3 process after concentration of suspension curve in sewage;
Fig. 7 be treatment time-median particle size graphic representation, in figure, ■ represents median particle size curve in oil field ternary recovered water, in figure ● represent median particle size curve in transverse flow agglomerated air floatation process water described in step one, in figure ▲ represent described in step 3 process after median particle size curve in sewage.
Embodiment
Embodiment one: composition graphs 1 and Fig. 2, present embodiment be transverse flow coalescent-cavitation air flotation reactor comprises lateral flow coalescence oil remover 1, one section of air supporting reactor 2, two sections of air supporting reactors 3, water dispensing apparatus 7, one section of water distribution vestibule 8, water outlet holder 9, sedimentation device 10, water inlet pipe 11, flow coalescent oil exit pipe 12, flow coalescent collection tank 13, upper hold-down grid 14, baffle plate 15, flow coalescent perforated sludge discharge pipe 16, one section of slag receiving trough 17, one section of scum pipe 18, one section of effluent trough 19, one section of rising pipe 20, one section is held air water pipe 21, one section of perforated sludge discharge pipe 22, two sections are held air water pipe 23, sedimentation oil exit pipe 24, sedimentation rising pipe 25, two sections of water distribution vestibules 26, sedimentation perforated sludge discharge pipe 28, two sections of perforated sludge discharge pipes 29, lower hold-down grid 31, two sections of water inlet pipes 32, two sections of scum pipes 33, two sections of slag receiving troughs 34 and sedimentation collection tank 40,
By described upper hold-down grid 14 and lower hold-down grid 31, lateral flow coalescence oil remover 1 is separated into oil extraction district 4 from top to bottom successively, packing area 1-1 and the coalescent Ji Yu district 5 of stream, described water dispensing apparatus 7 is arranged on the side of lateral flow coalescence oil remover 1, at the opposite side of lateral flow coalescence oil remover 1, one section of water distribution vestibule 8 is set, and packing area 1-1 is communicated with one section of water distribution vestibule 8 with water dispensing apparatus 7, the coalescent collection tank 13 of stream is set above water dispensing apparatus 7, the coalescent collection tank of described stream 13 is communicated with by flowing coalescent draining valve 41 with oil extraction district 4, water inlet pipe 11 is set bottom water dispensing apparatus 7, the coalescent oil exit pipe 12 of stream is set bottom the coalescent collection tank 13 of stream, at lower hold-down grid 31, baffle plate 15 is set towards stream side, coalescent Ji Yu district 5, the coalescent perforated sludge discharge pipe 16 of stream is set bottom the coalescent Ji Yu district 5 of stream,
By one section of dividing plate 37, one section of air supporting reactor 2 is separated into one section of air flotation zone 2-1 and point pool 2-2, in one section of air flotation zone 2-1, one section of dividing plate 37 top arranges one section of slag receiving trough 17, in point pool 2-2, one section of air supporting reactor 2 side wall upper part arranges one section of effluent trough 19, one section of described air flotation zone 2-1 is communicated with one section of water distribution vestibule 8 by one section of water intaking valve 42, described one section of slag receiving trough 17 is communicated with one section of air flotation zone 2-1 by one section of residual cake valve 43, and one section of scum pipe 18 is set at one section of slag receiving trough 17, described one section of effluent trough 19 is communicated with a point pool 2-2 by one section of outlet valve 44, and bottom one section of effluent trough 19, one section of rising pipe 20 is set, a Duan Jiyu district 6 is provided with bottom one section of described air supporting reactor 2, one section of perforated sludge discharge pipe 22 is set bottom a Duan Jiyu district 6,
Described one section is held air water pipe 21 and runs through one section of air supporting reactor 2, one section of one end holding air water pipe 21 is communicated with one section of water distribution vestibule 8, one section of the other end holding air water pipe 21 holds air water pipe 23 be communicated with two section, described two sections are held air water pipe 23 and run through two sections of air supporting reactors 3, and two sections of the other ends holding air water pipe 23 are communicated with two sections of water distribution vestibules 26;
By two sections of dividing plates 38, two sections of air supporting reactors 3 are separated into inhalant region 3-1 and two section of air flotation zone 3-2, in two sections of air flotation zone 3-2, two sections of dividing plate 38 tops arrange two sections of slag receiving troughs 34, in the 3-1 of inhalant region, two sections of air supporting reactor 3 side wall upper part arrange two sections of inlet flumes 45, two sections of described air flotation zone 3-2 are communicated with two sections of water distribution vestibules 26 by two sections of outlet valves 48, described two sections of slag receiving troughs 34 are communicated with two sections of air flotation zone 3-2 by two sections of residual cake valves 47, and two sections of scum pipes 33 are set at two sections of slag receiving troughs 34, described two sections of inlet flumes 45 are communicated with inhalant region 3-1 by two sections of water intaking valves 46, two sections of water inlet pipes 32 are set bottom two sections of inlet flumes 45, and two sections of water inlet pipes 32 are communicated with one section of rising pipe 20, be provided with two Duan Jiyu districts 30 bottom two sections of described air supporting reactors 3, two sections of perforated sludge discharge pipes 29 are set bottom two Duan Jiyu districts 30,
The opposite side of described two sections of water distribution vestibules 26 is communicated with sedimentation device 10 by sedimentary province water entry 39, at the opposite side of sedimentation device 10, water outlet holder 9 is set, sedimentation collection tank 40 is set above water outlet holder 9, described sedimentation collection tank 40 is communicated with sedimentation device 10 by sedimentation draining valve 49, described water outlet holder 9 is communicated with sedimentation device 10 by sedimentation outlet valve 50, sedimentation rising pipe 25 is set bottom water outlet holder 9, sedimentation oil exit pipe 24 is set bottom sedimentation collection tank 40, settlement volume silt district 27 is provided with bottom described sedimentation device 10, bottom settlement volume silt district 27, sedimentation perforated sludge discharge pipe 28 is set.
Fig. 1 be transverse flow coalescent-cavitation air flotation reactor in the structural representation of water dispensing apparatus, lateral flow coalescence oil remover, one section of water distribution vestibule and one section of air supporting reactor, in figure, 1 is lateral flow coalescence oil remover, 2 is one section of air supporting reactor, 4 is oil extraction district, 5 is the coalescent Ji Yu district of stream, 6 is a Duan Jiyu district, 7 is water dispensing apparatus, 8 is one section of water distribution vestibule, 11 is water inlet pipe, 12 is the coalescent oil exit pipe of stream, 13 is the coalescent collection tank of stream, 14 is upper hold-down grid, 15 is baffle plate, 16 is the coalescent perforated sludge discharge pipe of stream, 17 is one section of slag receiving trough, 18 is one section of scum pipe, 19 is one section of effluent trough, 20 is one section of rising pipe, 21 are one section holds air water pipe, 22 is one section of perforated sludge discharge pipe, 31 is lower hold-down grid, 35 is water inlet reverse checkvalve, 37 is one section of dividing plate, 41 is the coalescent draining valve of stream, 42 is one section of water intaking valve, 43 is one section of residual cake valve, 44 is one section of outlet valve, 1-1 is packing area, 2-1 is one section of air flotation zone, 2-2 is a point pool.
Fig. 2 be transverse flow coalescent-cavitation air flotation reactor in two sections of air supporting reactors, two sections of water distribution vestibules, sedimentation device and water outlet holders structural representation, 3 is two sections of air supporting reactors, 9 is water outlet holder, 10 is sedimentation device, 23 are two sections holds air water pipe, 24 is sedimentation oil exit pipe, 25 is sedimentation rising pipe, 26 is two sections of water distribution vestibules, 27 is settlement volume silt district, 28 is sedimentation perforated sludge discharge pipe, 29 is two sections of perforated sludge discharge pipes, 30 is two Duan Jiyu districts, 32 is two sections of water inlet pipes, 33 is two sections of scum pipes, 34 is two sections of slag receiving troughs, 36 is water outlet reverse checkvalve, 38 is two sections of dividing plates, 39 is sedimentary province water entry, 40 is sedimentation collection tank, 45 is two sections of inlet flumes, 46 is two sections of water intaking valves, 47 is two sections of residual cake valves, 48 is two sections of outlet valves, 49 is sedimentation draining valve, 50 is sedimentation outlet valve, 3-1 is inhalant region, 3-2 is two sections of air flotation zones.
Embodiment two: composition graphs 1 and Fig. 2, present embodiment with the difference of embodiment one is: described one section is held air water pipe 21 and is communicated with one section of water distribution vestibule 8 by reverse checkvalve 35 of intaking, described two sections are held air water pipe 23 and are communicated with two sections of water distribution vestibules 26 by water outlet reverse checkvalve 36, and two sections of appearance air water pipes 23 and the backflow of one section of appearance air water pipe 21 enter one section of water distribution vestibule 8 successively to ensure two sections of interior two sections of air supporting water outlets of water distribution vestibule 26.Other are identical with embodiment one.
Embodiment three: composition graphs 1 and Fig. 2, present embodiment be utilize the transverse flow described in embodiment one coalescent-cavitation air flotation reactor carries out ternary recovered water transverse flow agglomerated air floatation-A/O bioremediation, specifically completes according to the following steps:
One, transverse flow agglomerated air floatation process: oil field ternary recovered water is passed into transverse flow coalescent-cavitation air flotation reactor in process, obtain transverse flow agglomerated air floatation process water;
Two, anaerobic treatment: utilize UASB reactor, IC reactor or anaerobism sbr reactor device to carry out anaerobic treatment to transverse flow agglomerated air floatation process water, obtain anaerobic treatment water, utilize in anaerobic treatment process and tamed the anaerobic activated sludge with efficient degradation usefulness and carry out biological reinforced process, hydraulic detention time is 12h ~ 24h;
Three, aerobic treatment: utilize aerobic activated sludge or aerobe biofilm to carry out aerobic treatment to anaerobic treatment water, namely complete ternary recovered water transverse flow agglomerated air floatation-A/O to carry out a biological disposal upon, obtain processing rear sewage, utilize in Aerobic and tamed the capable biological reinforced process of the microorganism species with higher biological degradation activity, hydraulic detention time is 8h ~ 16h.
The method of the domestication of the anaerobic activated sludge of having tamed described in present embodiment is as follows:
1., check anaerobic reaction device equipment, ensure anaerobic reaction device Plant in good condition;
2., the medicament of preparation domestication:
Concentration add-on according to 1 hydrargyrum oxydatum crudum agent: 0.5 gram, urea, white sugar 2 grams; 0.2 gram, ferrous sulfate; Potassium primary phosphate 0.1 gram; SODIUMNITRATE 0.1 gram; 0.1 gram, magnesium sulfate; Sodium.alpha.-hydroxypropionate 2 milliliters; 2 grams, sodium sulfate, the water of 0.01 gram, calcium chloride and surplus;
3., by the mud of the second pond of municipal sewage plant stir, remove the particulate matter that diameter is greater than 2mm, then add ternary recovered water, obtain concentration and reach 3000mg/L mud;
4., then add step medicament 2., the volume ratio that medicament and concentration reach 3000mg/L mud is 1:20, stirs, and pours in anaerobic reaction device;
5., close the lid fermentation; Every day stirs twice, controls the content of dissolved oxygen lower than 0.05mg/L;
6., to COD monitor, supplement medicament during COD value <200mg/L, the volume ratio of medicament and oil field ternary recovered water is 1:20; Ensure sludge quantity, the height of quiet heavy rear mud is at more than 3/5 of container height simultaneously;
7., cultivate 72h, change an oil field ternary recovered water;
8., by changing an oil field ternary recovered water as COD value <100mg/L carrying out Cyclic culture, when being 24h to HRT, having been tamed the anaerobic activated sludge with efficient degradation usefulness.
The acclimation method of the microorganism species (aerobic activated sludge) that taming described in present embodiment has higher biological degradation activity:
1., be 10% inoculation by the inoculum size of aerobic reactor mud, described aerobic reactor mud is Daqing oil field east wind secondary sedimentation tank of sewage treatment work, and the concentration of aerobic reactor mud is 3000mg/L;
2., reactor run when fracturing liquid is full of reactor after, quiet sink 24 hours, start to add ternary recovered water and carry out aeration, carry out aeration, aeration control is at 16:1, and dissolved oxygen content controls at 6mg/L;
3., tame 7 days, namely obtain having tamed the microorganism species (aerobic activated sludge) with higher biological degradation activity.
Embodiment four: the difference of present embodiment and embodiment three is: in step one, transverse flow agglomerated air floatation process detailed process is as follows:
Oil field ternary recovered water enters water dispensing apparatus 7 by water inlet pipe 11, the packing area 1-1 entering lateral flow coalescence oil remover 1 again filters, in oil field ternary recovered water, part oil enters oil extraction district 4 through upper hold-down grid 14, entering in the coalescent collection tank 13 of stream by the coalescent draining valve 41 of stream, finally sent by the coalescent oil exit pipe 12 of stream, in oil field ternary recovered water, mud is deposited in the coalescent Ji Yu district 5 of stream by lower hold-down grid 31, discharges by flowing coalescent perforated sludge discharge pipe 16;
The oil field ternary recovered water being carried out one section of water distribution vestibule 8 by packing area 1-1 is filtered water, filtered water sends into one section of air flotation zone 2-1 of one section of air supporting reactor 2 by one section of water intaking valve 42, air-flotation process is carried out in one section of air flotation zone 2-1, the dregs of fat that one section of air flotation zone 2-1 produces carry out a point pool 2-2 to utilize one section of dividing plate 37 to stop, by one section of residual cake valve 43, the dregs of fat are collected in one section of slag receiving trough 17, discharged by one section of scum pipe 18 again, the silting of one section of air flotation zone 2-1 generation in a Duan Jiyu district 6, and is discharged by one section of perforated sludge discharge pipe 22;
Water after one section of air-flotation process to be pooled in point pool 2-2 in one section of effluent trough 19, undertaken in two sections of inlet flumes 45 by one section of rising pipe 20 and two sections of water inlet pipes 32 successively, undertaken in the inhalant region 3-1 of two sections of air supporting reactors 3 by two sections of water intaking valves 46 again, finally flow in two sections of air flotation zone 3-2 of two sections of air supporting reactors 3, air-flotation process is carried out in two sections of air flotation zone 3-2, the dregs of fat that two sections of air flotation zone 3-2 produce carry out inhalant region 3-1 to utilize two sections of dividing plates 38 to stop, by two sections of residual cake valves 47, the dregs of fat are collected in two sections of slag receiving troughs 34, discharged by two sections of scum pipes 33 again, the silting of two sections of air flotation zone 3-2 generations is in two Duan Jiyu districts 6, and two sections of perforated sludge discharge pipes 29 are discharged,
Water after two sections of air-flotation process enters in two sections of water distribution vestibules 26 by two sections of outlet valves 48, enter in sedimentation device 10 by sedimentary province water entry 39 again, stratification is carried out at sedimentation device 10, upper strata is oil reservoir, oil reservoir is collected in sedimentation collection tank 40 by sedimentation draining valve 49, bottom is silt seam, silt seam is deposited in settlement volume silt district 27, and discharged by sedimentation perforated sludge discharge pipe 28, centre is water layer, the process water that water layer obtains is transverse flow agglomerated air floatation process water, transverse flow agglomerated air floatation process water is collected in water outlet holder 9 by sedimentation outlet valve 50, and send into anaerobic treatment stage by sedimentation rising pipe 25.Other are identical with embodiment three.
Embodiment five: one of present embodiment and embodiment three or four difference is: in step one, the water treatment capacity of transverse flow agglomerated air floatation process is 2m 3/ h, the packing area 1-1 water-carrying section volumetric loading of lateral flow coalescence oil remover 1 is 3.75m 3/ m 2h, the hydraulic detention time of lateral flow coalescence oil remover 1 is 1h ~ 2h, and the hydraulic detention time of one section of air supporting reactor 2 is 0.5h ~ 1h, the hydraulic detention time of two sections of air supporting reactors 3 is 0.25h ~ 0.5h.Other are identical with embodiment three or four.
Embodiment six: one of present embodiment and embodiment three to five difference is: when the process of transverse flow agglomerated air floatation refluxes in step one, water now after two sections of interior two sections of air-flotation process of water distribution vestibule 26 holds air water pipe 23 through carrying out two sections according to water outlet reverse checkvalve 36, hold air water pipe 23 through two sections again to enter in one section of appearance air water pipe 21, enter in one section of water distribution vestibule 8 finally by water inlet reverse checkvalve 35.Other are identical with embodiment three to five.
Embodiment seven: one of present embodiment and embodiment three to six difference is: the reflux ratio <50% when the process of transverse flow agglomerated air floatation refluxes in step one.Other are identical with embodiment three to six.
Embodiment eight: one of present embodiment and embodiment three to seven difference is: reflux ratio is 30% when the process of transverse flow agglomerated air floatation refluxes in step one.Other are identical with embodiment three to seven.
Embodiment nine: one of present embodiment and embodiment three to seven difference is: reflux ratio is 40% when the process of transverse flow agglomerated air floatation refluxes in step one.Other are identical with embodiment three to seven.
Adopt following verification experimental verification effect of the present invention
Embodiment 1: utilize transverse flow coalescent-cavitation air flotation reactor carries out ternary recovered water transverse flow agglomerated air floatation-A/O bioremediation, specifically completes according to the following steps:
One, transverse flow agglomerated air floatation process: oil field ternary recovered water enters water dispensing apparatus 7 by water inlet pipe 11, the packing area 1-1 entering lateral flow coalescence oil remover 1 again filters, in oil field ternary recovered water, part oil enters oil extraction district 4 through upper hold-down grid 14, entering in the coalescent collection tank 13 of stream by the coalescent draining valve 41 of stream, finally sent by the coalescent oil exit pipe 12 of stream, in oil field ternary recovered water, mud is deposited in the coalescent Ji Yu district 5 of stream by lower hold-down grid 31, discharges by flowing coalescent perforated sludge discharge pipe 16;
The oil field ternary recovered water being carried out one section of water distribution vestibule 8 by packing area 1-1 is filtered water, filtered water sends into one section of air flotation zone 2-1 of one section of air supporting reactor 2 by one section of water intaking valve 42, air-flotation process is carried out in one section of air flotation zone 2-1, the dregs of fat that one section of air flotation zone 2-1 produces carry out a point pool 2-2 to utilize one section of dividing plate 37 to stop, by one section of residual cake valve 43, the dregs of fat are collected in one section of slag receiving trough 17, discharged by one section of scum pipe 18 again, the silting of one section of air flotation zone 2-1 generation in a Duan Jiyu district 6, and is discharged by one section of perforated sludge discharge pipe 22;
Water after one section of air-flotation process to be pooled in point pool 2-2 in one section of effluent trough 19, undertaken in two sections of inlet flumes 45 by one section of rising pipe 20 and two sections of water inlet pipes 32 successively, undertaken in the inhalant region 3-1 of two sections of air supporting reactors 3 by two sections of water intaking valves 46 again, finally flow in two sections of air flotation zone 3-2 of two sections of air supporting reactors 3, air-flotation process is carried out in two sections of air flotation zone 3-2, the dregs of fat that two sections of air flotation zone 3-2 produce carry out inhalant region 3-1 to utilize two sections of dividing plates 38 to stop, by two sections of residual cake valves 47, the dregs of fat are collected in two sections of slag receiving troughs 34, discharged by two sections of scum pipes 33 again, the silting of two sections of air flotation zone 3-2 generations is in two Duan Jiyu districts 6, and two sections of perforated sludge discharge pipes 29 are discharged,
Water after two sections of air-flotation process enters in two sections of water distribution vestibules 26 by two sections of outlet valves 48, enter in sedimentation device 10 by sedimentary province water entry 39 again, stratification is carried out at sedimentation device 10, upper strata is oil reservoir, oil reservoir is collected in sedimentation collection tank 40 by sedimentation draining valve 49, bottom is silt seam, silt seam is deposited in settlement volume silt district 27, and discharged by sedimentation perforated sludge discharge pipe 28, centre is water layer, the process water that water layer obtains is transverse flow agglomerated air floatation process water, transverse flow agglomerated air floatation process water is collected in water outlet holder 9 by sedimentation outlet valve 50, obtain transverse flow agglomerated air floatation process water, and send into anaerobic treatment stage by sedimentation rising pipe 25,
Two, anaerobic treatment: utilize UASB reactor, IC reactor or anaerobism sbr reactor device to carry out anaerobic treatment to transverse flow agglomerated air floatation process water, obtain anaerobic treatment water, utilize in anaerobic treatment process and tamed the anaerobic activated sludge with efficient degradation usefulness and carry out biological reinforced process, hydraulic detention time is 18h;
Three, aerobic treatment: utilize aerobic activated sludge or aerobe biofilm to carry out aerobic treatment to anaerobic treatment water, namely complete ternary recovered water transverse flow agglomerated air floatation-A/O to carry out a biological disposal upon, obtain processing rear sewage, utilize in Aerobic and tamed the capable biological reinforced process of the microorganism species with higher biological degradation activity, hydraulic detention time is 12h.
In embodiment 1 step one, the water treatment capacity of transverse flow agglomerated air floatation process is 2m 3/ h, the packing area 1-1 water-carrying section volumetric loading of lateral flow coalescence oil remover 1 is 3.75m 3/ m 2h, the hydraulic detention time of lateral flow coalescence oil remover 1 is 1h, and the hydraulic detention time of one section of air supporting reactor 2 is 0.5h, the hydraulic detention time of two sections of air supporting reactors 3 is 0.5h.
Transverse flow described in embodiment 1 step one is coalescent-and cavitation air flotation reactor comprises lateral flow coalescence oil remover 1, one section of air supporting reactor 2, two sections of air supporting reactors 3, water dispensing apparatus 7, one section of water distribution vestibule 8, water outlet holder 9, sedimentation device 10, water inlet pipe 11, flow coalescent oil exit pipe 12, flow coalescent collection tank 13, upper hold-down grid 14, baffle plate 15, flow coalescent perforated sludge discharge pipe 16, one section of slag receiving trough 17, one section of scum pipe 18, one section of effluent trough 19, one section of rising pipe 20, one section is held air water pipe 21, one section of perforated sludge discharge pipe 22, two sections are held air water pipe 23, sedimentation oil exit pipe 24, sedimentation rising pipe 25, two sections of water distribution vestibules 26, sedimentation perforated sludge discharge pipe 28, two sections of perforated sludge discharge pipes 29, lower hold-down grid 31, two sections of water inlet pipes 32, two sections of scum pipes 33, two sections of slag receiving troughs 34 and sedimentation collection tank 40,
By described upper hold-down grid 14 and lower hold-down grid 31, lateral flow coalescence oil remover 1 is separated into oil extraction district 4 from top to bottom successively, packing area 1-1 and the coalescent Ji Yu district 5 of stream, described water dispensing apparatus 7 is arranged on the side of lateral flow coalescence oil remover 1, at the opposite side of lateral flow coalescence oil remover 1, one section of water distribution vestibule 8 is set, and packing area 1-1 is communicated with one section of water distribution vestibule 8 with water dispensing apparatus 7, the coalescent collection tank 13 of stream is set above water dispensing apparatus 7, the coalescent collection tank of described stream 13 is communicated with by flowing coalescent draining valve 41 with oil extraction district 4, water inlet pipe 11 is set bottom water dispensing apparatus 7, the coalescent oil exit pipe 12 of stream is set bottom the coalescent collection tank 13 of stream, at lower hold-down grid 31, baffle plate 15 is set towards stream side, coalescent Ji Yu district 5, the coalescent perforated sludge discharge pipe 16 of stream is set bottom the coalescent Ji Yu district 5 of stream,
By one section of dividing plate 37, one section of air supporting reactor 2 is separated into one section of air flotation zone 2-1 and point pool 2-2, in one section of air flotation zone 2-1, one section of dividing plate 37 top arranges one section of slag receiving trough 17, in point pool 2-2, one section of air supporting reactor 2 side wall upper part arranges one section of effluent trough 19, one section of described air flotation zone 2-1 is communicated with one section of water distribution vestibule 8 by one section of water intaking valve 42, described one section of slag receiving trough 17 is communicated with one section of air flotation zone 2-1 by one section of residual cake valve 43, and one section of scum pipe 18 is set at one section of slag receiving trough 17, described one section of effluent trough 19 is communicated with a point pool 2-2 by one section of outlet valve 44, and bottom one section of effluent trough 19, one section of rising pipe 20 is set, a Duan Jiyu district 6 is provided with bottom one section of described air supporting reactor 2, one section of perforated sludge discharge pipe 22 is set bottom a Duan Jiyu district 6,
Described one section is held air water pipe 21 and runs through one section of air supporting reactor 2, one section of one end holding air water pipe 21 is communicated with one section of water distribution vestibule 8, one section of the other end holding air water pipe 21 holds air water pipe 23 be communicated with two section, described two sections are held air water pipe 23 and run through two sections of air supporting reactors 3, and two sections of the other ends holding air water pipe 23 are communicated with two sections of water distribution vestibules 26;
By two sections of dividing plates 38, two sections of air supporting reactors 3 are separated into inhalant region 3-1 and two section of air flotation zone 3-2, in two sections of air flotation zone 3-2, two sections of dividing plate 38 tops arrange two sections of slag receiving troughs 34, in the 3-1 of inhalant region, two sections of air supporting reactor 3 side wall upper part arrange two sections of inlet flumes 45, two sections of described air flotation zone 3-2 are communicated with two sections of water distribution vestibules 26 by two sections of outlet valves 48, described two sections of slag receiving troughs 34 are communicated with two sections of air flotation zone 3-2 by two sections of residual cake valves 47, and two sections of scum pipes 33 are set at two sections of slag receiving troughs 34, described two sections of inlet flumes 45 are communicated with inhalant region 3-1 by two sections of water intaking valves 46, two sections of water inlet pipes 32 are set bottom two sections of inlet flumes 45, and two sections of water inlet pipes 32 are communicated with one section of rising pipe 20, be provided with two Duan Jiyu districts 30 bottom two sections of described air supporting reactors 3, two sections of perforated sludge discharge pipes 29 are set bottom two Duan Jiyu districts 30,
The opposite side of described two sections of water distribution vestibules 26 is communicated with sedimentation device 10 by sedimentary province water entry 39, at the opposite side of sedimentation device 10, water outlet holder 9 is set, sedimentation collection tank 40 is set above water outlet holder 9, described sedimentation collection tank 40 is communicated with sedimentation device 10 by sedimentation draining valve 49, described water outlet holder 9 is communicated with sedimentation device 10 by sedimentation outlet valve 50, sedimentation rising pipe 25 is set bottom water outlet holder 9, sedimentation oil exit pipe 24 is set bottom sedimentation collection tank 40, settlement volume silt district 27 is provided with bottom described sedimentation device 10, bottom settlement volume silt district 27, sedimentation perforated sludge discharge pipe 28 is set,
Described one section is held air water pipe 21 and is communicated with one section of water distribution vestibule 8 by water inlet reverse checkvalve 35, described two sections are held air water pipe 23 and are communicated with two sections of water distribution vestibules 26 by water outlet reverse checkvalve 36, and two sections of appearance air water pipes 23 and the backflow of one section of appearance air water pipe 21 enter one section of water distribution vestibule 8 successively to ensure two sections of interior two sections of air supporting water outlets of water distribution vestibule 26.
Embodiment 2: the difference of the present embodiment and embodiment 1 is: in step one, the process of transverse flow agglomerated air floatation is 30% to reflux by reflux ratio, water now after two sections of interior two sections of air-flotation process of water distribution vestibule 26 holds air water pipe 23 through carrying out two sections according to water outlet reverse checkvalve 36, hold air water pipe 23 through two sections again to enter in one section of appearance air water pipe 21, enter in one section of water distribution vestibule 8 finally by water inlet reverse checkvalve 35.Other are identical with embodiment 1.
Embodiment 3: the difference of the present embodiment and embodiment 1 is: in step one, the process of transverse flow agglomerated air floatation is 40% to reflux by reflux ratio, water now after two sections of interior two sections of air-flotation process of water distribution vestibule 26 holds air water pipe 23 through carrying out two sections according to water outlet reverse checkvalve 36, hold air water pipe 23 through two sections again to enter in one section of appearance air water pipe 21, enter in one section of water distribution vestibule 8 finally by water inlet reverse checkvalve 35.Other are identical with embodiment 1.
Embodiment 4: the difference of the present embodiment and embodiment 1 is: in step one, the process of transverse flow agglomerated air floatation is 50% to reflux by reflux ratio, water now after two sections of interior two sections of air-flotation process of water distribution vestibule 26 holds air water pipe 23 through carrying out two sections according to water outlet reverse checkvalve 36, hold air water pipe 23 through two sections again to enter in one section of appearance air water pipe 21, enter in one section of water distribution vestibule 8 finally by water inlet reverse checkvalve 35.Other are identical with embodiment 1.
Two days are run according to embodiment 1 to 4 method, detect the oleaginousness in oil field ternary recovered water, as shown in Figure 3, Fig. 3 is oleaginousness clearance graphic representation, in figure ● represent oleaginousness clearance curve in one section of water distribution vestibule 8, in figure, ■ represents oleaginousness clearance curve in two sections of water distribution vestibules 26, in figure ▲ represent oleaginousness clearance curve in water outlet holder 9; As shown in Figure 3, the total removal rate of embodiment 1 pair of oleaginousness reaches 47.89% and 54.84% respectively, wherein in one section of water distribution vestibule 8, oleaginousness clearance reaches 2.07% and 3.06% respectively, and in two sections of water distribution vestibules 26, oleaginousness clearance reaches 45.82% and 51.78% respectively; The total removal rate of embodiment 2 pairs of oleaginousness reaches 68.63% and 71.30% respectively, and wherein in one section of water distribution vestibule 8, oleaginousness clearance reaches 7.35% and 7.71% respectively, and in two sections of water distribution vestibules 26, oleaginousness clearance reaches 61.28% and 63.59% respectively; The total removal rate of embodiment 3 pairs of oleaginousness reaches 75.37% and 79.67% respectively, and wherein in one section of water distribution vestibule 8, oleaginousness clearance reaches 12.49% and 16.04% respectively, and in two sections of water distribution vestibules 26, oleaginousness clearance reaches 62.89% and 63.63% respectively; The total removal rate of embodiment 4 pairs of oleaginousness reaches 37.13% and 47.21% respectively, and wherein in one section of water distribution vestibule 8, oleaginousness clearance reaches 2.29% and 5.48% respectively, and in two sections of water distribution vestibules 26, oleaginousness clearance reaches 34.83% and 41.74% respectively.Known by contrasting, in step one process of transverse flow agglomerated air floatation by reflux ratio be 40% carry out refluxing when, best deoiling effect can be obtained.
Two days are run according to embodiment 1 to 4 method, detect the suspended substance in oil field ternary recovered water, as shown in Figure 4, Fig. 4 is removal efficiency graphic representation, in figure ● represent suspended substance removal rate curve in one section of water distribution vestibule 8, in figure, ■ represents suspended substance removal rate curve in two sections of water distribution vestibules 26, in figure ▲ represent suspended substance removal rate curve in water outlet holder 9; As shown in Figure 4, the total removal rate of embodiment 1 pair of suspended substance reaches 38.73% and 40.86% respectively, wherein in one section of water distribution vestibule 8, removal efficiency reaches 19.06% and 18.60% respectively, and in two sections of water distribution vestibules 26, removal efficiency reaches 19.67% and 22.26% respectively; The total removal rate of embodiment 2 pairs of suspended substances reaches 59.29% and 62.24% respectively, and wherein in one section of water distribution vestibule 8, removal efficiency reaches 26.22% and 28.55% respectively, and in two sections of water distribution vestibules 26, removal efficiency reaches 33.07% and 33.69% respectively; The total removal rate of embodiment 3 pairs of suspended substances reaches 69.59% and 71.34% respectively, and wherein in one section of water distribution vestibule 8, removal efficiency reaches 32.62% and 33.17% respectively, and in two sections of water distribution vestibules 26, removal efficiency reaches 36.96% and 38.16% respectively; The total removal rate of embodiment 4 pairs of suspended substances reaches 42.79% and 45.6% respectively, and wherein in one section of water distribution vestibule 8, removal efficiency reaches 19.12% and 20.15% respectively, and in two sections of water distribution vestibules 26, removal efficiency reaches 23.67% and 25.45% respectively.Known by contrasting, in step one process of transverse flow agglomerated air floatation by reflux ratio be 40% carry out refluxing when, the effect of best oil removal can be obtained.
Embodiment 5: utilize transverse flow coalescent-cavitation air flotation reactor carries out ternary recovered water transverse flow agglomerated air floatation-A/O bioremediation, specifically completes according to the following steps:
One, transverse flow agglomerated air floatation process: oil field ternary recovered water enters water dispensing apparatus 7 by water inlet pipe 11, the packing area 1-1 entering lateral flow coalescence oil remover 1 again filters, in oil field ternary recovered water, part oil enters oil extraction district 4 through upper hold-down grid 14, entering in the coalescent collection tank 13 of stream by the coalescent draining valve 41 of stream, finally sent by the coalescent oil exit pipe 12 of stream, in oil field ternary recovered water, mud is deposited in the coalescent Ji Yu district 5 of stream by lower hold-down grid 31, discharges by flowing coalescent perforated sludge discharge pipe 16;
The oil field ternary recovered water being carried out one section of water distribution vestibule 8 by packing area 1-1 is filtered water, filtered water sends into one section of air flotation zone 2-1 of one section of air supporting reactor 2 by one section of water intaking valve 42, air-flotation process is carried out in one section of air flotation zone 2-1, the dregs of fat that one section of air flotation zone 2-1 produces carry out a point pool 2-2 to utilize one section of dividing plate 37 to stop, by one section of residual cake valve 43, the dregs of fat are collected in one section of slag receiving trough 17, discharged by one section of scum pipe 18 again, the silting of one section of air flotation zone 2-1 generation in a Duan Jiyu district 6, and is discharged by one section of perforated sludge discharge pipe 22;
Water after one section of air-flotation process to be pooled in point pool 2-2 in one section of effluent trough 19, undertaken in two sections of inlet flumes 45 by one section of rising pipe 20 and two sections of water inlet pipes 32 successively, undertaken in the inhalant region 3-1 of two sections of air supporting reactors 3 by two sections of water intaking valves 46 again, finally flow in two sections of air flotation zone 3-2 of two sections of air supporting reactors 3, air-flotation process is carried out in two sections of air flotation zone 3-2, the dregs of fat that two sections of air flotation zone 3-2 produce carry out inhalant region 3-1 to utilize two sections of dividing plates 38 to stop, by two sections of residual cake valves 47, the dregs of fat are collected in two sections of slag receiving troughs 34, discharged by two sections of scum pipes 33 again, the silting of two sections of air flotation zone 3-2 generations is in two Duan Jiyu districts 6, and two sections of perforated sludge discharge pipes 29 are discharged,
Water after two sections of air-flotation process enters in two sections of water distribution vestibules 26 by two sections of outlet valves 48, enter in sedimentation device 10 by sedimentary province water entry 39 again, stratification is carried out at sedimentation device 10, upper strata is oil reservoir, oil reservoir is collected in sedimentation collection tank 40 by sedimentation draining valve 49, bottom is silt seam, silt seam is deposited in settlement volume silt district 27, and discharged by sedimentation perforated sludge discharge pipe 28, centre is water layer, the process water that water layer obtains is transverse flow agglomerated air floatation process water, transverse flow agglomerated air floatation process water is collected in water outlet holder 9 by sedimentation outlet valve 50, obtain transverse flow agglomerated air floatation process water, and send into anaerobic treatment stage by sedimentation rising pipe 25,
In step one, the process of transverse flow agglomerated air floatation is 40% to reflux by reflux ratio, water now after two sections of interior two sections of air-flotation process of water distribution vestibule 26 holds air water pipe 23 through carrying out two sections according to water outlet reverse checkvalve 36, hold air water pipe 23 through two sections again to enter in one section of appearance air water pipe 21, enter in one section of water distribution vestibule 8 finally by water inlet reverse checkvalve 35;
Two, anaerobic treatment: utilize UASB reactor, IC reactor or anaerobism sbr reactor device to carry out anaerobic treatment to transverse flow agglomerated air floatation process water, obtain anaerobic treatment water, utilize in anaerobic treatment process and tamed the anaerobic activated sludge with efficient degradation usefulness and carry out biological reinforced process, hydraulic detention time is 18h;
Three, aerobic treatment: utilize aerobic activated sludge or aerobe biofilm to carry out aerobic treatment to anaerobic treatment water, namely complete ternary recovered water transverse flow agglomerated air floatation-A/O to carry out a biological disposal upon, obtain processing rear sewage, utilize in Aerobic and tamed the capable biological reinforced process of the microorganism species with higher biological degradation activity, hydraulic detention time is 12h.
In embodiment 5 step one, the water treatment capacity of transverse flow agglomerated air floatation process is 2m 3/ h, the packing area 1-1 water-carrying section volumetric loading of lateral flow coalescence oil remover 1 is 3.75m 3/ m 2h, the hydraulic detention time of lateral flow coalescence oil remover 1 is 1h, and the hydraulic detention time of one section of air supporting reactor 2 is 0.5h, the hydraulic detention time of two sections of air supporting reactors 3 is 0.5h.
Transverse flow described in embodiment 5 step one is coalescent-and cavitation air flotation reactor comprises lateral flow coalescence oil remover 1, one section of air supporting reactor 2, two sections of air supporting reactors 3, water dispensing apparatus 7, one section of water distribution vestibule 8, water outlet holder 9, sedimentation device 10, water inlet pipe 11, flow coalescent oil exit pipe 12, flow coalescent collection tank 13, upper hold-down grid 14, baffle plate 15, flow coalescent perforated sludge discharge pipe 16, one section of slag receiving trough 17, one section of scum pipe 18, one section of effluent trough 19, one section of rising pipe 20, one section is held air water pipe 21, one section of perforated sludge discharge pipe 22, two sections are held air water pipe 23, sedimentation oil exit pipe 24, sedimentation rising pipe 25, two sections of water distribution vestibules 26, sedimentation perforated sludge discharge pipe 28, two sections of perforated sludge discharge pipes 29, lower hold-down grid 31, two sections of water inlet pipes 32, two sections of scum pipes 33, two sections of slag receiving troughs 34 and sedimentation collection tank 40,
By described upper hold-down grid 14 and lower hold-down grid 31, lateral flow coalescence oil remover 1 is separated into oil extraction district 4 from top to bottom successively, packing area 1-1 and the coalescent Ji Yu district 5 of stream, described water dispensing apparatus 7 is arranged on the side of lateral flow coalescence oil remover 1, at the opposite side of lateral flow coalescence oil remover 1, one section of water distribution vestibule 8 is set, and packing area 1-1 is communicated with one section of water distribution vestibule 8 with water dispensing apparatus 7, the coalescent collection tank 13 of stream is set above water dispensing apparatus 7, the coalescent collection tank of described stream 13 is communicated with by flowing coalescent draining valve 41 with oil extraction district 4, water inlet pipe 11 is set bottom water dispensing apparatus 7, the coalescent oil exit pipe 12 of stream is set bottom the coalescent collection tank 13 of stream, at lower hold-down grid 31, baffle plate 15 is set towards stream side, coalescent Ji Yu district 5, the coalescent perforated sludge discharge pipe 16 of stream is set bottom the coalescent Ji Yu district 5 of stream,
By one section of dividing plate 37, one section of air supporting reactor 2 is separated into one section of air flotation zone 2-1 and point pool 2-2, in one section of air flotation zone 2-1, one section of dividing plate 37 top arranges one section of slag receiving trough 17, in point pool 2-2, one section of air supporting reactor 2 side wall upper part arranges one section of effluent trough 19, one section of described air flotation zone 2-1 is communicated with one section of water distribution vestibule 8 by one section of water intaking valve 42, described one section of slag receiving trough 17 is communicated with one section of air flotation zone 2-1 by one section of residual cake valve 43, and one section of scum pipe 18 is set at one section of slag receiving trough 17, described one section of effluent trough 19 is communicated with a point pool 2-2 by one section of outlet valve 44, and bottom one section of effluent trough 19, one section of rising pipe 20 is set, a Duan Jiyu district 6 is provided with bottom one section of described air supporting reactor 2, one section of perforated sludge discharge pipe 22 is set bottom a Duan Jiyu district 6,
Described one section is held air water pipe 21 and runs through one section of air supporting reactor 2, one section of one end holding air water pipe 21 is communicated with one section of water distribution vestibule 8, one section of the other end holding air water pipe 21 holds air water pipe 23 be communicated with two section, described two sections are held air water pipe 23 and run through two sections of air supporting reactors 3, and two sections of the other ends holding air water pipe 23 are communicated with two sections of water distribution vestibules 26;
By two sections of dividing plates 38, two sections of air supporting reactors 3 are separated into inhalant region 3-1 and two section of air flotation zone 3-2, in two sections of air flotation zone 3-2, two sections of dividing plate 38 tops arrange two sections of slag receiving troughs 34, in the 3-1 of inhalant region, two sections of air supporting reactor 3 side wall upper part arrange two sections of inlet flumes 45, two sections of described air flotation zone 3-2 are communicated with two sections of water distribution vestibules 26 by two sections of outlet valves 48, described two sections of slag receiving troughs 34 are communicated with two sections of air flotation zone 3-2 by two sections of residual cake valves 47, and two sections of scum pipes 33 are set at two sections of slag receiving troughs 34, described two sections of inlet flumes 45 are communicated with inhalant region 3-1 by two sections of water intaking valves 46, two sections of water inlet pipes 32 are set bottom two sections of inlet flumes 45, and two sections of water inlet pipes 32 are communicated with one section of rising pipe 20, be provided with two Duan Jiyu districts 30 bottom two sections of described air supporting reactors 3, two sections of perforated sludge discharge pipes 29 are set bottom two Duan Jiyu districts 30,
The opposite side of described two sections of water distribution vestibules 26 is communicated with sedimentation device 10 by sedimentary province water entry 39, at the opposite side of sedimentation device 10, water outlet holder 9 is set, sedimentation collection tank 40 is set above water outlet holder 9, described sedimentation collection tank 40 is communicated with sedimentation device 10 by sedimentation draining valve 49, described water outlet holder 9 is communicated with sedimentation device 10 by sedimentation outlet valve 50, sedimentation rising pipe 25 is set bottom water outlet holder 9, sedimentation oil exit pipe 24 is set bottom sedimentation collection tank 40, settlement volume silt district 27 is provided with bottom described sedimentation device 10, bottom settlement volume silt district 27, sedimentation perforated sludge discharge pipe 28 is set,
Described one section is held air water pipe 21 and is communicated with one section of water distribution vestibule 8 by water inlet reverse checkvalve 35, described two sections are held air water pipe 23 and are communicated with two sections of water distribution vestibules 26 by water outlet reverse checkvalve 36, and two sections of appearance air water pipes 23 and the backflow of one section of appearance air water pipe 21 enter one section of water distribution vestibule 8 successively to ensure two sections of interior two sections of air supporting water outlets of water distribution vestibule 26.
Run 7 days according to embodiment 5 method, treatment effect is as shown in Fig. 5, Fig. 6 and Fig. 7.
Fig. 5 be treatment time-oleaginousness graphic representation, in figure, ■ represents oleaginousness curve in oil field ternary recovered water, in figure ● represent oleaginousness curve in transverse flow agglomerated air floatation process water described in step one, in figure ▲ represent described in step 3 process after oleaginousness curve in sewage; As shown in Figure 5, run 7 days continuously, when (oil field ternary recovered water) oleaginousness of intaking is about 300mg/L, after the present embodiment process, in water outlet, oleaginousness is lower than 5mg/L.
Fig. 6 be treatment time-concentration of suspension graphic representation, in figure, ■ represents concentration of suspension curve in oil field ternary recovered water, in figure ● represent concentration of suspension curve in transverse flow agglomerated air floatation process water described in step one, in figure ▲ represent described in step 3 process after concentration of suspension curve in sewage; As shown in Figure 6, run 7 days continuously, when intake (oil field ternary recovered water) middle concentration of suspension is higher than 100mg/L, after the present embodiment process, in water outlet, concentration of suspension is lower than 20mg/L.
Fig. 7 be treatment time-median particle size graphic representation, in figure, ■ represents median particle size curve in oil field ternary recovered water, in figure ● represent median particle size curve in transverse flow agglomerated air floatation process water described in step one, in figure ▲ represent described in step 3 process after median particle size curve in sewage; As shown in Figure 7, run 7 days continuously, after this enforcement process, the median particle size of water outlet is lower than 1 μm.

Claims (9)

1. transverse flow coalescent-cavitation air flotation reactor, it is characterized in that transverse flow coalescent-cavitation air flotation reactor comprises lateral flow coalescence oil remover (1), one section of air supporting reactor (2), two sections of air supporting reactors (3), water dispensing apparatus (7), one section of water distribution vestibule (8), water outlet holder (9), sedimentation device (10), water inlet pipe (11), flow coalescent oil exit pipe (12), flow coalescent collection tank (13), upper hold-down grid (14), baffle plate (15), flow coalescent perforated sludge discharge pipe (16), one section of slag receiving trough (17), one section of scum pipe (18), one section of effluent trough (19), one section of rising pipe (20), one section is held air water pipe (21), one section of perforated sludge discharge pipe (22), two sections are held air water pipe (23), sedimentation oil exit pipe (24), sedimentation rising pipe (25), two sections of water distribution vestibules (26), sedimentation perforated sludge discharge pipe (28), two sections of perforated sludge discharge pipes (29), lower hold-down grid (31), two sections of water inlet pipes (32), two sections of scum pipes (33), two sections of slag receiving troughs (34) and sedimentation collection tank (40),
By described upper hold-down grid (14) and lower hold-down grid (31), lateral flow coalescence oil remover (1) is separated into oil extraction district (4) from top to bottom successively, packing area (1-1) and the coalescent Ji Yu district (5) of stream, described water dispensing apparatus (7) is arranged on the side of lateral flow coalescence oil remover (1), at the opposite side of lateral flow coalescence oil remover (1), one section of water distribution vestibule (8) is set, and packing area (1-1) is communicated with one section of water distribution vestibule (8) with water dispensing apparatus (7), in water dispensing apparatus (7) top, the coalescent collection tank of stream (13) is set, the coalescent collection tank of described stream (13) is communicated with by flowing coalescent draining valve (41) with oil extraction district (4), in water dispensing apparatus (7) bottom, water inlet pipe (11) is set, in the coalescent collection tank of stream (13) bottom, the coalescent oil exit pipe of stream (12) is set, at lower hold-down grid (31), baffle plate (15) is set towards stream coalescent Ji Yu district (5) side, in stream coalescent Ji Yu district (5) bottom, the coalescent perforated sludge discharge pipe of stream (16) is set,
By one section of dividing plate (37), one section of air supporting reactor (2) is separated into one section of air flotation zone (2-1) and point pool (2-2), on one section of interior one section of dividing plate (37) top of air flotation zone (2-1), one section of slag receiving trough (17) is set, in a point pool (2-2) interior one section of air supporting reactor (2) side wall upper part, one section of effluent trough (19) is set, one section of described air flotation zone (2-1) is communicated with one section of water distribution vestibule (8) by one section of water intaking valve (42), one section of described slag receiving trough (17) is communicated with one section of air flotation zone (2-1) by one section of residual cake valve (43), and one section of scum pipe (18) is set one section of slag receiving trough (17), one section of described effluent trough (19) is communicated with a point pool (2-2) by one section of outlet valve (44), and one section of effluent trough (19) bottom arranges one section of rising pipe (20), one section of described air supporting reactor (2) bottom is provided with a Duan Jiyu district (6), in a bottom, Duan Jiyu district (6), one section of perforated sludge discharge pipe (22) is set,
Described one section is held air water pipe (21) and runs through one section of air supporting reactor (2), one section of one end holding air water pipe (21) is communicated with one section of water distribution vestibule (8), one section of the other end holding air water pipe (21) holds air water pipe (23) be communicated with two section, described two sections are held air water pipe (23) and run through two sections of air supporting reactors (3), and two sections of the other ends holding air water pipe (23) are communicated with two sections of water distribution vestibules (26);
By two sections of dividing plates (38), two sections of air supporting reactors (3) are separated into inhalant region (3-1) and two sections of air flotation zones (3-2), on two sections of interior two sections of dividing plate (38) tops of air flotation zone (3-2), two sections of slag receiving troughs (34) are set, in inhalant region (3-1) interior two sections of air supporting reactor (3) side wall upper part, two sections of inlet flumes (45) are set, two sections of described air flotation zones (3-2) are communicated with two sections of water distribution vestibules (26) by two sections of outlet valves (48), two sections of described slag receiving troughs (34) are communicated with two sections of air flotation zones (3-2) by two sections of residual cake valves (47), and two sections of scum pipes (33) are set two sections of slag receiving troughs (34), two sections of described inlet flumes (45) are communicated with inhalant region (3-1) by two sections of water intaking valves (46), two sections of inlet flume (45) bottoms, two sections of water inlet pipes (32) are set, and two sections of water inlet pipes (32) are communicated with one section of rising pipe (20), two sections of described air supporting reactor (3) bottoms are provided with two Duan Jiyu districts (30), arrange two sections of perforated sludge discharge pipes (29) in two bottoms, Duan Jiyu district (30),
The opposite side of described two sections of water distribution vestibules (26) is communicated with sedimentation device (10) by sedimentary province water entry (39), at the opposite side of sedimentation device (10), water outlet holder (9) is set, in water outlet holder (9) top, sedimentation collection tank (40) is set, described sedimentation collection tank (40) is communicated with sedimentation device (10) by sedimentation draining valve (49), described water outlet holder (9) is communicated with sedimentation device (10) by sedimentation outlet valve (50), in water outlet holder (9) bottom, sedimentation rising pipe (25) is set, in sedimentation collection tank (40) bottom, sedimentation oil exit pipe (24) is set, described sedimentation device (10) bottom is provided with settlement volume silt district (27), in bottom, settlement volume silt district (27), sedimentation perforated sludge discharge pipe (28) is set.
2. transverse flow according to claim 1 coalescent-cavitation air flotation reactor, it is characterized in that one section of described appearance air water pipe (21) is communicated with one section of water distribution vestibule (8) by water inlet reverse checkvalve (35), described two sections are held air water pipe (23) and are communicated with two sections of water distribution vestibules (26) by water outlet reverse checkvalve (36), and two sections of appearances air water pipe (23) and one section of appearance air water pipe (21) backflow enter one section of water distribution vestibule (8) successively to ensure two sections of interior two sections of air supporting water outlets of water distribution vestibule (26).
3. utilize the transverse flow described in claim 1 coalescent-cavitation air flotation reactor carries out ternary recovered water transverse flow agglomerated air floatation-A/O bioremediation, it is characterized in that utilizing transverse flow coalescent-cavitation air flotation reactor carries out ternary recovered water transverse flow agglomerated air floatation-A/O bioremediation to be completed according to the following steps:
One, transverse flow agglomerated air floatation process: oil field ternary recovered water is passed into transverse flow coalescent-cavitation air flotation reactor in process, obtain transverse flow agglomerated air floatation process water;
Two, anaerobic treatment: utilize UASB reactor, IC reactor or anaerobism sbr reactor device to carry out anaerobic treatment to transverse flow agglomerated air floatation process water, obtain anaerobic treatment water, utilize in anaerobic treatment process and tamed the anaerobic activated sludge with efficient degradation usefulness and carry out biological reinforced process, hydraulic detention time is 12h ~ 24h;
Three, aerobic treatment: utilize aerobic activated sludge or aerobe biofilm to carry out aerobic treatment to anaerobic treatment water, namely complete ternary recovered water transverse flow agglomerated air floatation-A/O to carry out a biological disposal upon, obtain processing rear sewage, utilize in Aerobic and tamed the capable biological reinforced process of the microorganism species with higher biological degradation activity, hydraulic detention time is 8h ~ 16h.
4. according to claim 3 utilize transverse flow coalescent-cavitation air flotation reactor carries out ternary recovered water transverse flow agglomerated air floatation-A/O bioremediation, it is characterized in that in step one, transverse flow agglomerated air floatation process detailed process is as follows:
Oil field ternary recovered water enters water dispensing apparatus (7) by water inlet pipe (11), the packing area (1-1) entering lateral flow coalescence oil remover (1) is again filtered, in oil field ternary recovered water, part oil enters oil extraction district (4) through upper hold-down grid (14), entering in the coalescent collection tank of stream (13) by the coalescent draining valve of stream (41), finally sent by the coalescent oil exit pipe of stream (12), in oil field ternary recovered water, mud is deposited the coalescent Ji Yu district (5) of stream by lower hold-down grid (31), discharge by flowing coalescent perforated sludge discharge pipe (16),
The oil field ternary recovered water being carried out one section of water distribution vestibule (8) by packing area (1-1) is filtered water, filtered water sends into one section of air flotation zone (2-1) of one section of air supporting reactor (2) by one section of water intaking valve (42), air-flotation process is carried out in one section of air flotation zone (2-1), the dregs of fat that one section of air flotation zone (2-1) produces carry out a point pool (2-2) to utilize one section of dividing plate (37) to stop, by one section of residual cake valve (43), the dregs of fat are collected in one section of slag receiving trough (17), discharged by one section of scum pipe (18) again, the silting that one section of air flotation zone (2-1) produces is in a Duan Jiyu district (6), and discharged by one section of perforated sludge discharge pipe (22),
Water after one section of air-flotation process is pooled in the interior one section of effluent trough (19) in a point pool (2-2), undertaken in two sections of inlet flumes (45) by one section of rising pipe (20) and two sections of water inlet pipes (32) successively, undertaken in the inhalant region (3-1) of two sections of air supporting reactors (3) by two sections of water intaking valves (46) again, finally flow in two sections of air flotation zones (3-2) of two sections of air supporting reactors (3), air-flotation process is carried out in two sections of air flotation zones (3-2), the dregs of fat that two sections of air flotation zones (3-2) produce carry out inhalant region (3-1) to utilize two sections of dividing plates (38) to stop, by two sections of residual cake valves (47), the dregs of fat are collected in two sections of slag receiving troughs (34), discharged by two sections of scum pipes (33) again, the silting that two sections of air flotation zones (3-2) produce is in two Duan Jiyu districts (6), and two sections of perforated sludge discharge pipes (29) are discharged,
Water after two sections of air-flotation process enters in two sections of water distribution vestibules (26) by two sections of outlet valves (48), enter in sedimentation device (10) by sedimentary province water entry (39) again, stratification is carried out at sedimentation device (10), upper strata is oil reservoir, oil reservoir is collected in sedimentation collection tank (40) by sedimentation draining valve (49), bottom is silt seam, silt seam is deposited in settlement volume silt district (27), and discharged by sedimentation perforated sludge discharge pipe (28), centre is water layer, the process water that water layer obtains is transverse flow agglomerated air floatation process water, transverse flow agglomerated air floatation process water is collected in water outlet holder (9) by sedimentation outlet valve (50), and send into anaerobic treatment stage by sedimentation rising pipe (25).
5. according to claim 4 utilize transverse flow coalescent-cavitation air flotation reactor carries out ternary recovered water transverse flow agglomerated air floatation-A/O bioremediation, it is characterized in that the water treatment capacity of transverse flow agglomerated air floatation process in step one is 2m3/h, packing area (1-1) the water-carrying section volumetric loading of lateral flow coalescence oil remover (1) is 3.75m 3/ m 2h, the hydraulic detention time of lateral flow coalescence oil remover (1) is 1h ~ 2h, and the hydraulic detention time of one section of air supporting reactor (2) is 0.5h ~ 1h, the hydraulic detention time of two sections of air supporting reactors (3) is 0.25h ~ 0.5h.
6. according to claim 3 or 4 utilize transverse flow coalescent-cavitation air flotation reactor carries out ternary recovered water transverse flow agglomerated air floatation-A/O bioremediation, it is characterized in that when in step one, the process of transverse flow agglomerated air floatation refluxes, water now after two sections of interior two sections of air-flotation process of water distribution vestibule (26) holds air water pipe (23) through carrying out two sections according to water outlet reverse checkvalve (36), hold air water pipe (23) through two sections again to enter in one section of appearance air water pipe (21), enter in one section of water distribution vestibule (8) finally by water inlet reverse checkvalve (35).
7. according to claim 6 utilize transverse flow coalescent-cavitation air flotation reactor carries out ternary recovered water transverse flow agglomerated air floatation-A/O bioremediation, it is characterized in that the reflux ratio <50% when the process of transverse flow agglomerated air floatation refluxes in step one.
8. according to claim 7 utilize transverse flow coalescent-cavitation air flotation reactor carries out ternary recovered water transverse flow agglomerated air floatation-A/O bioremediation, it is characterized in that reflux ratio is 30% when the process of transverse flow agglomerated air floatation refluxes in step one.
9. according to claim 7 utilize transverse flow coalescent-cavitation air flotation reactor carries out ternary recovered water transverse flow agglomerated air floatation-A/O bioremediation, it is characterized in that reflux ratio is 40% when the process of transverse flow agglomerated air floatation refluxes in step one.
CN201511022237.0A 2015-12-29 2015-12-29 Laterally stream coalescence cavitation air flotation reactor and ternary recovered water laterally flow agglomerated air floatation A/O bioremediations Active CN105540893B (en)

Priority Applications (1)

Application Number Priority Date Filing Date Title
CN201511022237.0A CN105540893B (en) 2015-12-29 2015-12-29 Laterally stream coalescence cavitation air flotation reactor and ternary recovered water laterally flow agglomerated air floatation A/O bioremediations

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
CN201511022237.0A CN105540893B (en) 2015-12-29 2015-12-29 Laterally stream coalescence cavitation air flotation reactor and ternary recovered water laterally flow agglomerated air floatation A/O bioremediations

Publications (2)

Publication Number Publication Date
CN105540893A true CN105540893A (en) 2016-05-04
CN105540893B CN105540893B (en) 2017-11-17

Family

ID=55820524

Family Applications (1)

Application Number Title Priority Date Filing Date
CN201511022237.0A Active CN105540893B (en) 2015-12-29 2015-12-29 Laterally stream coalescence cavitation air flotation reactor and ternary recovered water laterally flow agglomerated air floatation A/O bioremediations

Country Status (1)

Country Link
CN (1) CN105540893B (en)

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN111285532A (en) * 2019-12-24 2020-06-16 大庆油田有限责任公司 Corrosion inhibitor-containing gas field water reinjection treatment device and process
CN114105421A (en) * 2022-01-27 2022-03-01 新疆科力新技术发展股份有限公司 Efficient purification reinjection treatment system and treatment method for complex wastewater in oil field

Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN2672039Y (en) * 2004-01-12 2005-01-19 大庆油田有限责任公司 Coalescence gas float oil removing device
RU2264993C1 (en) * 2004-04-27 2005-11-27 Государственное образовательное учреждение высшего профессионального образования Уфимский государственный нефтяной технический университет (ГОУ ВПО УГНТУ) Method of purification of oily waste waters
CN101863562A (en) * 2010-05-28 2010-10-20 胜利油田胜利勘察设计研究院有限公司 Method and device for treating polymer-containing sewage by using high-gradient agglomerated air floatation
CN101972559A (en) * 2010-10-21 2011-02-16 天津大学 Oil-water separating device and method
CN202379771U (en) * 2011-12-12 2012-08-15 中国石油天然气股份有限公司 Multi-point air floatation polymer-containing sewage treatment device for shallow layer

Patent Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN2672039Y (en) * 2004-01-12 2005-01-19 大庆油田有限责任公司 Coalescence gas float oil removing device
RU2264993C1 (en) * 2004-04-27 2005-11-27 Государственное образовательное учреждение высшего профессионального образования Уфимский государственный нефтяной технический университет (ГОУ ВПО УГНТУ) Method of purification of oily waste waters
CN101863562A (en) * 2010-05-28 2010-10-20 胜利油田胜利勘察设计研究院有限公司 Method and device for treating polymer-containing sewage by using high-gradient agglomerated air floatation
CN101972559A (en) * 2010-10-21 2011-02-16 天津大学 Oil-water separating device and method
CN202379771U (en) * 2011-12-12 2012-08-15 中国石油天然气股份有限公司 Multi-point air floatation polymer-containing sewage treatment device for shallow layer

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN111285532A (en) * 2019-12-24 2020-06-16 大庆油田有限责任公司 Corrosion inhibitor-containing gas field water reinjection treatment device and process
CN114105421A (en) * 2022-01-27 2022-03-01 新疆科力新技术发展股份有限公司 Efficient purification reinjection treatment system and treatment method for complex wastewater in oil field

Also Published As

Publication number Publication date
CN105540893B (en) 2017-11-17

Similar Documents

Publication Publication Date Title
CN101870544B (en) Method for treating petroleum refining waste water
CN101898854B (en) Method and device for treatment of high-sulfur content and low-permeability oil reservoir produced wastewater
CA2707573C (en) Centralized sump oil and acid oil treatment process and system
CN102642884B (en) Oil-contained sewage treatment method and eddy energy fast-cyclone separating system of special equipment for method
CN101195074B (en) Electromagnetism filtering and separating method for oil-water and device thereof
CN107082506A (en) A kind of processing method of oil field extracted water and technological process
CN102838256A (en) Buried sewage treatment system
CN105084615B (en) Oil field wastewater treatment technique based on special membrane
CN101264999A (en) Process and apparatus for treating sewage
CN205347057U (en) Oil field tertiary oil recovery effluent disposal system
CN104016520B (en) Device for pre-treating coal chemical industry wastewater by air flotation coupled with coagulation and method for pre-treating coal chemical industry wastewater by device
CN201793456U (en) Oily sewage treatment system
CN105540893A (en) Cross flow coalescence-cavitation air floatation reactor and ternary produced water cross flow coalescence air floatation-A/O biological treatment method
CN104773880B (en) Sewage treatment technology and equipment for well drilling
CN107235588A (en) Produced Water In Oil-gas Fields, Ngi reinjection treatment method and equipment
Zhu et al. Optimization of reinjection treatment technology for oilfield wastewater in Longdong area
CN113683257B (en) Organic sewage treatment system of food and beverage
CN2661683Y (en) Oil field recovered water treatment device by internal electrolysis reaction
CN107365008A (en) A kind of vehicular pressure break returns waste discharge and abandons liquid treating system
CN206437971U (en) A kind of environment-friendly high-efficiency pickling waste waters processing system
CN112374684A (en) Oil and gas field drilling waste liquid recycling treatment device and method
CN106167294A (en) A kind of sewage auxiliary dephosphorization device
CN101007683A (en) High salinity oil extraction waste water treating process
CN110330186A (en) A kind of processing method suitable for greasy filth station greasy filth waste water and oil-gas field fracturing waste water
CN205313286U (en) Sled dress formula acidizing fracturing effluent disposal system

Legal Events

Date Code Title Description
C06 Publication
PB01 Publication
C10 Entry into substantive examination
SE01 Entry into force of request for substantive examination
GR01 Patent grant
GR01 Patent grant