CN103663624A - Purification method for oilfield reinjection water - Google Patents
Purification method for oilfield reinjection water Download PDFInfo
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- CN103663624A CN103663624A CN201210341994.4A CN201210341994A CN103663624A CN 103663624 A CN103663624 A CN 103663624A CN 201210341994 A CN201210341994 A CN 201210341994A CN 103663624 A CN103663624 A CN 103663624A
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Abstract
The invention discloses a purification method for oilfield reinjection water. According to the method, at least one level of membrane filtration treatment is carried out on oilfield produced water through a cellular carrier type inorganic carbon membrane component so as to prepare the reinjection water suitable for low permeability and extra-low permeability oil reservoirs, wherein the filter precision of the membrane component for membrane filtration treatment is 0.001-100mu m. The purification method has high filtration accuracy, the membrane flux of the compound carbon membrane carrier is large, the capacity of the membrane in resisting oil contamination is strong, the integration level of the structure of the membrane core is high, the quality of the prepared reinjection water is stable, and fine filtrated oilfield reinjection water meets the requirement of the reinjection water for the oil reservoirs in low permeability and extra-low permeability block, and meets the A-grade standard of 'recommended index and analysis method for quality of oil reservoir injection water of clastic rock' (SY/T 5329-94).
Description
Technical field
The present invention relates to a kind for the treatment of process of oily(waste)water, particularly a kind of process for purification of oil field reinjection water, belongs to field of environment engineering technology.
Background technology
Along with domestic most oil fields enter secondary, tertiary recovery, hypotonic and special hypotonic block exploitation accounting improves year by year, and Produced Liquid water ratio is up to 90%, and water flood recovery is for maintaining sand pressure and keeping stable production of crude oil bringing into play increasing effect.Hypotonic and special hypotonic block reservoir water is had relatively high expectations, that domestic time injection water quality execution is industry standard < < petroclastic rock reservoir water water quality fertilizer index and analytical procedure > > (SY/T 5329-94) at present, wherein requiring the highest A1 grade standard is oil-contg≤5mg/L, suspension content≤1mg/L, suspended substance solid particle size intermediate value≤1 μ m.
Oil field extracted water contains petroleum-type organism, sulfide, organic phenol, cyanogen, bacterium and suspended solids etc., also contains the various chemical medicaments adding in water filling adopting process, as emulsion splitter, flocculation agent and sterilant etc.The saltiness of oil field extracted water, COD, salinity and water temperature are all higher, if directly outer row will cause serious environmental pollution. also wasted valuable water resources simultaneously.At present, recovered water after treatment, is mainly used in re-injection, a small amount of rear outer row up to standard.
At present. oil field at home produced water disposal technique is mainly to adopt traditional " old three covers " technique, as shown in Figure 1, i.e. " gravity settling-coagulant precipitation-filtration ", be aided with the chemical agents such as scale inhibition, inhibition, sterilization simultaneously, make to process rear product water and reach in re-injection water industry standard reinjection into reservoir after C level or B level.The A level water quality standard requiring for hypotonic or special LOW PERMEABILITY RESERVOIR, needs to increase fine filtering and processes, as shown in Figure 2.At present, fine filtering is mainly to adopt metallic membrane, metal or ceramic post sintering pipe and PE sintered pipes etc. in actual applications.The subject matter existing is: filtering accuracy is not high, and in product water, suspended substance solid particle size intermediate value is not up to standard; High to water water quality requirement, as require be all less than≤10mg/L of suspended substance and oil-contg; Water resistant matter impact capacity is poor, and the shock effect of water water quality is large.In order to address the above problem, the technology that some are new and process quilt propose.
Chinese utility model patent 03219467.6 discloses a kind of gravity settling+biochemistry pool+membrane filtration+deoxygenation combination water treatment process and equipment, the microorganism that biochemical treatment is wherein selected is obligate associating flora, and oil pollutant in water and CODcr are had to obvious degradation capability.Membrane sepn adopts organic or inorganic tubular fibre or tubular ultrafiltration, produces water and can reach re-injection water A3 standard-required after filtering.But this technique biochemical treatment is subject to water water quality and the water yield changes shock effect, responsive to water temperature and variation of ambient temperature, treatment effect stability cannot guarantee.Ultra-filtration membrane contamination resistance used and resistance of oxidation are poor, are difficult to guarantee long-period stable operation.Because biochemical treatment adopts open filter tank Air Exposure mode, cause dissolved oxygen in water to raise, need to increase deoxygenation processing unit, to solve handling equipment and corrosive pipeline problem.After the final processing of this technique, produce water and only reach A3 standard, cannot meet A1 standard-required.
Application number is that the application for a patent for invention of 201110101686.X discloses a kind of oil field reinjection water membrane treatment process, its technical process as shown in Figure 3, be specially: first oily(waste)water enters slurry tank and carry out natural subsidence, the suspended solids that remove portion is large and sump oil; Water after sedimentation directly enters ceramic membrane ultrafitration equipment, ceramic membrane channel diameter 1.5-3.5mm, filtering accuracy is 20-500 nanometer, in ceramic membrane equipment, adopt cross-flow mode circulating filtration, the penetrating fluid that sees through film can be directly used in re-injection, the circulation fluid that contains a large amount of suspended solidss and sump oil that does not see through film enters slurry tank and continues sedimentation, after mixing with water, entering ceramic membrane ultrafitration equipment filters again, control crossflow velocity 4-8m/s, dense water is got back to circulation tank, when concentration is concentrated into 300-1000 times in circulation tank, carry out automatic pollution discharge; Online detection instrument also can be adjusted crossflow velocity voluntarily according to water water quality situation, reaches energy-saving and cost-reducing object.Although this treatment process is simple, cost of investment is low, and membrane filtration system vulnerable to pollution in the method, is easily subject to water water quality impact, and.Adopt high crossflow velocity cross-flow operation scheme, process energy consumption high.
Chinese utility model patent 201120003222.0 discloses the oil field produced water treatment device of a kind of low-permeability high-salt; its treatment process is: oil removal sedimentary adjustive pool+tilted plate separator+coarse strainer+gravity coalescing separator+adsorption filter+Multi-stage precise strainer; wherein; adsorption filter has adopted active carbon filter core; accurate filter has been used titanium alloy sintered filter core, processes product water and can reach A1 level.This art breading long flow path, active carbon filter core absorption is saturated fast, easily dirty stifled, and membrane filtration aperture is large and distribute widely, and the filtering accuracy of sintered filter core is low, produce in water suspended solids median particle size and be difficult to up to standardly, process and produce shipwreck to reach the water quality requirement of LOW PERMEABILITY RESERVOIR re-injection water.
Application number is that 201110081609.2 application for a patent for invention discloses a kind for the treatment of Technology for Petroleum Water Flooding, at least comprise and regulate water pot, air-floating apparatus, line mixer, nitrogen dynamic response device, settling tank and supersonic filter, and the mode that adopts " oil removal by air bubbling oil removal ", " nitrogen preparation " and " ultrasonic wave filtration " to combine is processed oil field extracted water, its air supporting is processed and is comprised one-level air supporting and the air supporting of secondary nitrogen, before one-level air supporting by adding medicament, strengthen the removal effect of air supporting to oils and suspended substance, an oil removing can reach 96%.Secondary air-floatation is used nitrogen further to remove oils and suspended substance, suppresses aerobic bacteria in water simultaneously and, as iron bacteria and saprophytic microorganism, reduces oxygen level in water body, the etching problem of solution equipment and pipeline.Oil field reinjection water after this inventive method is processed can reach B grade standard, and the subject matter of existence is that processing accuracy is not high, uncontrollable to suspended solids particle diameter in water, cannot meet hypotonic or Oil in Super-low Permeability block injection water quality requirement.
Summary of the invention
The object of the invention is the above-mentioned technical problem particularly existing in the treatment process of LOW PERMEABILITY RESERVOIR re-injection water for existing oil field reinjection water, provide the inorganic carbon membrane assembly of a kind of employing honeycomb support formula to carry out fine filtering processing to oil field extracted water, preparation meets the oil field reinjection water method of oil field reinjection water water quality standard, the filtering accuracy of the inventive method is high, low to water water quality requirement, anti-water water quality impact capacity is strong, re-injection water quality stabilizing, oil field reinjection water after fine filtering meets the requirement of hypotonic and special hypotonic block oil reservoir re-injection water, reach the A grade standard of < < petroclastic rock reservoir water water quality fertilizer index and analytical procedure > > (SY/T 5329-94).
For realizing object of the present invention, one aspect of the present invention provides a kind of process for purification of oil field reinjection water, comprises that adopting carrier type membrane module to carry out at least one-level membrane filtration to oil field extracted water processes.
Wherein, in membrane filtration treating processes, crossflow velocity is 0 ~ 5m/s; The filtering accuracy of membrane filtration is 0.001-100 μ m, is preferably 0.01 ~ 20 μ m, and more preferably 0.01-10 μ m, is further preferably 0.01-3 μ m; Transmembrane pressure in membrane filtration processes is 0.01 ~ 0.5MPa.
Particularly, described membrane filtration is processed and is adopted cross-flow mode to carry out; Described carrier type membrane module is tubular membrane component.
Particularly, described membrane filtration is treated to and adopts hyperchannel tubular type membrane module to carry out secondary membrane filtration to oil field extracted water.
Wherein, the filtering accuracy of first step membrane filtration is 0.01 ~ 3 μ m, is preferably 0.1 ~ 1 μ m; The crossflow velocity of controlling in first step membrane filtration processes is 0.1 ~ 5m/s, is preferably 0.5 ~ 3m/s; Control transmembrane pressure is 0.05 ~ 0.5MPa, is preferably 0.1 ~ 0.3MPa, more preferably 0.15 ~ 0.20MPa.
Particularly, in membrane filtration treating processes described in the first step, controlling concentrated water drainage, high-volume to make the first step filter produce water yield be 90 ~ 99%, preferably 96 ~ 98%.
Wherein, the filtering accuracy of second stage membrane filtration is 0.01 ~ 0.1 μ m, is preferably 0.01 ~ 0.05 μ m; The crossflow velocity of controlling in the membrane filtration processes of the second stage is 0 ~ 0.2m/s, is preferably 0 ~ 0.014m/s, more preferably; Control transmembrane pressure is 0.01 ~ 0.1MPa, is preferably 0.05 ~ 0.095MPa, more preferably 0.07 ~ 0.095MPa.
Particularly, in membrane filtration treating processes described in the second stage, controlling concentrated water drainage, high-volume to make the first step filter produce water yield be 90 ~ 99%, preferably 96 ~ 98%.
The water inlet that the second stage of the present invention membrane filtration is processed is the product water that first step membrane filtration is processed, and utilizes the back pressure of first step filtration product water as second stage membrane filtration operating pressure, without increasing in addition intake pump.
After cascade filtration, produce water and reach A1 standard, be i.e. oil-contg≤1mg/L, suspension content≤1mg/L, suspended substance solid particle size intermediate value≤1 μ m.
Particularly, also comprise oil field extracted water is carried out carrying out described membrane filtration processing after pre-treatment again.
Wherein, the water quality of pretreated oil field extracted water is oleaginousness≤50mg/L, suspension content≤50mg/L, the current water quality oleaginousness≤50mg/L that carries out membrane filtration processing, suspension content≤50mg/L.
Particularly, in pretreated oil field extracted water (carrying out the water of membrane filtration processing), oleaginousness is 10-50mg/L, and suspension content is 10-50mg/L.
Particularly, described pre-treatment comprises and oil field extracted water is carried out successively to gravity settling processing, coagulant precipitation are processed and walnut shell filter is processed or carry out successively gravity settling processing, air supporting processing, media filtration processing or biochemical treatment or other any water treatment method.
Wherein, described carrier type membrane module is tubular membrane component; Be preferably hyperchannel tubular type membrane module.
Wherein, described membrane module comprises:
Film core;
Shell, the right cylinder of hollow or straightedge cylinder, be set in the periphery of film core;
Tightness system, is located between film core and shell, is arranged in two seal areas of film core;
Upper and lower end cap, is arranged at respectively shell upper and lower part, and wherein, lower end cover is connected with water inlet pipe, and upper end cover is connected with dense water rising pipe;
Produce water export mouth, be arranged on shell outside, between two tightness systems, for will be after filtering deriving membrane module from producing the product water that aquaporin enter diversion trench.
Particularly, described film core comprises:
Main body, membrane filtration supporter;
Filtration channel, described filtration channel is in a row distributed in main body, and along the described main body of longitudinal perforation of main body, every row's filtration channel is parallel to each other;
Produce aquaporin, be in a row distributed in main body, extending longitudinally along main body, interval 1-10 row filtration channel between adjacent two scheduling aquaporins, and produce the closure of openings that aquaporin is positioned at two end faces of main body, produce aquaporin and described filtration channel and be parallel to each other;
Diversion trench, is opened in the through hole of the perforation main body in main body wall, on the longitudinal direction along main body, is spaced with same scheduling aquaporin, collects the product water producing in aquaporin.
Wherein, rounded, oval, the rectangle in the cross section perpendicular to main body longitudinal direction of described main body or regular polygon or Polygons.
Particularly, described main body is by justifying, ellipse, and the solid that rectangle or regular polygon stretch and form, is preferably circle, square or regular hexagon.
Especially, described regular polygon is square, regular pentagon, regular hexagon or octagon.
Particularly, the diameter of the film core main body that cross section is rounded is 1-100cm, is preferably 5-20cm; Length is 5-200cm, is preferably 20-120cm.
Wherein, described film core main body is cylindrical shape, regular prism.
Particularly, described regular prism is four-prism, positive six prisms or positive eight prisms.
Especially, described film core main body is right cylinder; The diameter of main body is 1-100cm, is preferably 5-20cm; Length is 5-200cm, is preferably 20-120cm.
Wherein, described film core is tubular membrane or tubular membrane core.
Particularly, described film core is hyperchannel tubular type film or hyperchannel tubular type film core.
Especially, described film core is carrier type film core or the inorganic carbon membrane film of carrier type core.
Film core main body is by porous polymer materials, and porous ceramic film material or sintered metal materials form, and preferably aluminum oxide, zirconium white, titanium oxide, silicon carbide, stainless steel or titanium alloy, consist of.
Wherein, being evenly distributed on the filtration channel in the inorganic carbon membrane film of carrier type core main body and producing aquaporin number is 1 ~ 20/cm
2; Be preferably 2 ~ 10/cm
2, 6-10/cm more preferably
2.
Wherein, described filtration channel, rounded, oval, the rectangle in the cross section longitudinally perpendicular to main body, regular polygon or other Polygons that produce aquaporin.
Particularly, described regular polygon is square, regular pentagon, regular hexagon or octagon.
Particularly, the cross section longitudinally perpendicular to main body of described filtration channel, product aquaporin is preferably circle, square and regular hexagon.
Perpendicular to main body, the shape in cross section is identical longitudinally with producing aquaporin for the shape in the cross section longitudinally perpendicular to main body of described filtration channel, but for the ease of the resolution of two kinds of passages, the cross-sectional shape of described filtration channel also can be different from the cross-sectional shape that produces aquaporin.
Wherein, described is that circular filtration channel, the diameter that produces aquaporin are 0.1 ~ 10 millimeter perpendicular to main body longitudinal cross-section, preferably 1 ~ 5 millimeter, and 2 ~ 4mm more preferably; Described cross section is that foursquare filtration channel, the length of side of producing aquaporin are 0.1 ~ 10 millimeter, preferably 1 ~ 5 millimeter, and 1.5 ~ 3mm more preferably.
Particularly, the circumscribed circle diameter in the cross section of the filtration channel that described cross section is regular polygon, product aquaporin is 0.1 ~ 10mm, preferably 1 ~ 5mm, more preferably 2-5mm.
Especially, the filtration channel that described cross section is regular pentagon, product aquaporin, the external circular diameter in its cross section is 0.1 ~ 10mm, preferably 1 ~ 5mm; Described cross section is orthohexagonal filtration channel, produces aquaporin, and the external circular diameter in its cross section is 0.1 ~ 10mm, preferably 1 ~ 5mm; Described cross section is filtration channel, the product aquaporin of octagon, and the external circular diameter in its cross section is 0.1 ~ 10mm, preferably 1 ~ 5mm.
Film core of the present invention and the filtration channel on it, product aquaporin are generally by the moulding of extrusion moulding mode, also can be by other currently known methods moulding such as injection moulding or castings.Preferably extruding forming method is made multi-channel membrane core.Passage on film core of the present invention can be opening shape and measure-alike, also can be different, if the channel selecting as producing water collection is from different as the channel opening shape of filtering, and the size of producing aquaporin is also greater than filtration channel, be conducive to like this resolution to two kinds of passages, also increase product aquaporin volume, reduced the resistance to flow of producing water.
Wherein, interval 2-6 row filtration channel, further preferred interval 2-4 row filtration channel between adjacent two scheduling aquaporins.
Particularly, described product aquaporin is positioned at the closure of openings at film core main body two ends.
Use sizing agent, sealing plug or other known way to seal described product aquaporin.Preferably sealing means is that after using the material shutoff identical with film core main body, pyroprocessing reaches sealing effectiveness.Filtration channel is positioned at the opening of two end faces of main body to be opened, and is convenient to current and flows into film core main body, carries out membrane filtration, and the product water after filtration flows into and produces aquaporin, produces the closure of openings that aquaporin is positioned at the two ends of film core main body, prevents from producing water and mixes with water.
Wherein, at described filtration channel inwall, be also assembled with filtering layer.
Particularly, the pore size filter of filtering layer is 0.001-100 μ m, be preferably 0.01 ~ 20 μ m, 0.01-10 μ m more preferably, further be preferably 0.01-3 μ m, the filtering accuracy of the filtering layer forming is 0.001-100 μ m, is preferably 0.01 ~ 20 μ m, more preferably 0.01-10 μ m, is further preferably 0.01-3 μ m.
By one or more modes in sintering, bonding, coating, spraying, thermal treatment, crystallization treatment, chemical reaction, filtering layer material is assembled in to the inner side of described filtration channel, forms described filtering layer.Filtering layer material is selected a kind of in microfiltration membrane, ultra-filtration membrane, nanofiltration membrane, reverse osmosis membrane, gas separation membrane, gasification permeable membrane or ion-exchange membrane.
Wherein, described filtering layer material is elected inorganic materials or organic materials as.
Particularly, described inorganic materials is aluminum oxide, zirconium white, titanium oxide, silicon carbide, stainless steel or titanium alloy.
Particularly, described organic materials is polysulfones (PS), polyacrylonitrile (PAN), polyethersulfone (PES), polyvinylidene difluoride (PVDF) (PVDF), polyvinyl chloride (PVC), cellulose acetate (CA), polycarbonate (PC), polyethylene (PE), polypropylene (PP), polyvinylidene difluoride (PVDF) (PVDF), polytetrafluoroethylene (PTFE) or ion exchange resin.
Hyperchannel tubular type film core of the present invention, porous material high by porosity and that aperture is large forms, and it is little that product water transmits resistance in film core.Film core in the present invention can be used as supporter or the carrier of micro-filtration, ultrafiltration, nanofiltration, reverse osmosis, gas separation membrane, Pervaporation membrane and ion-exchange membrane, its method be film core for separating of filtration channel in assemble one deck filtering separation layer, assembling mode can adopt the array mode of sintering, bonding, coating, spraying, thermal treatment, crystallization treatment, chemical reaction or several modes.During assembling filter layer, assembling filter layer not in the product aquaporin on film core.
Wherein, diversion trench is to be opened in the through hole that runs through main body on the sidewall in main body outside, and it will be positioned at the locational product aquaporin of same row and partly be communicated with.Diversion trench is spaced along main body longitudinal direction and the product aquaporin that is positioned at same row.
Particularly, described diversion trench is along being trapezoidal or rectangle in cross section longitudinally perpendicular to main body.
Wherein, described diversion trench is 0.5-100cm along the length L of main body longitudinal direction, is preferably 1-20cm; The height h of diversion trench is 10-150:100 with the ratio that produces the height of aquaporin, be preferably 50-100:100, be diversion trench be that the circular diameter of product aquaporin or the ratio of the length of side that cross section is foursquare product aquaporin is 10-150:100 perpendicular to the width (the height h of diversion trench) of main body longitudinal direction and cross section, be preferably 50-100:100, be preferably 50-100:100.
Particularly, corresponding to same scheduling aquaporin, the diversion trench number that distributes along main body longitudinal direction, be 1-10, be preferably 2-4.
Outside at film core, by saw, bore, mill, plane or other known way are along the longitudinal direction that is parallel to film core, on the position of the same scheduling aquaporin of correspondence, keep at a certain distance away and offer diversion trench, diversion trench is trapezoidal or rectangle in cross section longitudinally perpendicular to main body, along connecting main body perpendicular to main body longitudinal direction, when main body is right cylinder, be that diversion trench connects main body perpendicular to main body radial direction along cylindrical tangential perforation main body, diversion trench is communicated with channel part corresponding to same scheduling aquaporin, on the position of same scheduling aquaporin, produce aquaporin and diversion trench is spaced, the product water producing in aquaporin flows out film core by diversion trench.
Diversion trench is that the sidewall in main body outside connects main body from the channel direction perpendicular to producing aquaporin, and the through hole extending along same scheduling aquaporin direction, through hole is rectangle or square along the cross section of main body longitudinal direction, wherein perpendicular to main body longitudinally width (being the height h of diversion trench) for perpendicular to the cross section of main body longitudinal direction, be circular product aquaporin diameter 50% ~ 150% or perpendicular to the cross section of main body longitudinal direction, be the 50-150% of the foursquare product aquaporin length of side; Diversion trench is 0.5-100cm along the length L of main body longitudinal direction.Diversion trench connects a same scheduling aquaporin part for correspondence, and each the product aquaporin in corresponding product aquaporin row is spatially communicated with corresponding diversion trench, and the product water producing in aquaporin can flow out body region by this diversion trench.
Wherein, on the outside sidewall at the two ends of film core main body, be respectively equipped with seal area.
Particularly, the width of described seal area is 2-20cm, is preferably 5-10cm.On the outside sidewall apart from film core end face 2-20cm, film core main body, offer diversion trench, diversion trench is not to start fluting from the end face of main body, and diversion trench is not set in seal area, and diversion trench is 2-20cm to the distance of the end face of main body, is preferably 5-10cm.
On the position of same scheduling aquaporin, two end faces of main body to distance separately the distance of immediate diversion trench be 2-20cm, at two end face >=2-20cm places apart from main body, offer diversion trench, in the scope that is 2-20cm along the longitudinal direction length of film core, seal area is set respectively on the outside sidewall at the two ends of film core main body.
Region between two end faces of film core main body and separately nearest diversion trench is seal area, be seal area along main body longitudinally width be 2-20cm, be preferably 5-10cm, two end faces that is to say main body to and its immediate diversion trench between distance be 2-20cm, be preferably 5-10cm.
Wherein, described shell selects the material of metal or non-metallic material to make; Described tightness system is selected organic rubber sealing-ring.
Particularly, sealing-ring is set in the outside, seal area at film core main body two ends, and the space between the outside of the inwall of shell, film core main body and the tightness system at film core two ends forms produces pool.
Particularly, described product water export mouth is opened in shell near dense water rising pipe one end.
The current that flow into from water inlet pipe enter film core by filtration channel, after filtering, infiltrate into product aquaporin, the current of same scheduling aquaporin conflux to corresponding diversion trench, and the current in diversion trench flow into and produce pool, then flow out membrane module through being positioned at the product water export mouth in shell outside.
Particularly, described upper and lower end cap is connected by flange with shell.
Wherein, upper and lower end cap is fixedly connected with and seals with shell by flange.
Particularly, end face of lower end cover, film core main body and sealing-ring form inhalant region; Another end face and the sealing-ring of upper end cover, film core main body form dense pool.
Particularly, at the middle part of shell, offer the import of backwashing water, while cleaning for membrane module, input back flushing current.
Oil field reinjection water process for purification tool of the present invention has the following advantages:
1, the carrier type carbon membrane film cored structure integrated level adopting in the inventive method is high, pore size filter narrowly distributing, and filtering accuracy is high, effectively after controlled filter, produce suspension content and the suspended substance median particle size of water, and membrane flux is large, and anti-pollution by oil ability is strong.
2, the water quality requirement that the inventive method is treated refining oil field extracted water is low, water water quality is little on producing the yield of water and the impact of water quality, in carrier type carbon membrane film core acceptable water water quality of the present invention, suspended substance and oil-contg are greater than 10mg/L, even the suspended substance in water and oil-contg all can be up to 50mg/L, and adopt the product water water quality after the inventive method is processed can reach oleaginousness≤5mg/L, suspension content≤1mg/L, suspended substance solid particle size intermediate value≤1 μ m, produce water quality stabilizing, compliance rate is high, meet the requirement of hypotonic and special hypotonic block oil reservoir re-injection water, reach the A grade standard of < < petroclastic rock reservoir water water quality fertilizer index and analytical procedure > > (SY/T5329-94), and it is harsh to water water quality requirement in prior art, to carry out membrane filtration treatment process, require suspended substance and the oil-contg of water to be all less than 10mg/L.
3, the anti-water water quality of the inventive method impact capacity is strong, the ability of existing metallic membrane or the anti-oil pollutant of ceramic membrane, the membrane flux of the inorganic carbon membrane assembly of carrier type of the present invention is the more than 2 times of conventional ceramic membrane flux, even can be up to 5 times of pottery membrane flux.The contact angle of described top layer membrane filtration layer and water is low, be only 0.3 °, good hydrophilic property, anti-pollution by oil ability is strong, adopt cross flow filter mode to carry out filtration treatment simultaneously, the impact of effectively avoiding pollution by oil and coming water slug to cause film itself, has significantly reduced and has come water slug on producing the impact of water water quality.
4, in the membrane filtration processes of the inventive method, transmembrane pressure is little, produces water transmission resistance little, and the resistance to flow difference of the product water that each filtration channel forms is little, and respectively evenly, the product discharge of membrane module is stable for the product discharge of each filtration channel, and membrane filtration efficiency is high.
5, in the inventive method, the film tamped density in the film core of carrier type membrane module is high, filtration channel in unit surface, to produce aquaporin quantity many, improve the membrane area in unit volume, improved the water production rate of unit volume membrane module, reduced the energy consumption and the production cost that produce water.
6, the filtration channel in unit surface on the film core of carrier type membrane module in the inventive method, to produce aquaporin quantity many, film core volume is little, it is simple, easy to make, when being assembled into membrane module, simple in structure, trim is few, good sealing effect, the filtration product water resistance difference that is beneficial to raising membrane filtration efficiency and different filtration channels is little, and transmembrane pressure is little, improve the working efficiency of membrane module, reduced production cost and the energy consumption of oil field reinjection water.
7, the yield of the inventive method refinement treatment oil field reinjection water is high, reaches more than 97%, and outer row's the dense water yield is few, has saved water resources, has reduced environmental pollution.
8, the inventive method adopts the cross flow filter mode of low crossflow velocity, has reduced the energy consumption of water treatment, and the inventive method is applied widely, can be used for traditional oil field extracted water old technology to process transformation, also can be used for the transformation of other traditional water technologies.
Accompanying drawing explanation
" old three covers " processing flow chart of Fig. 1 tradition oil field extracted water;
Fig. 2 LOW PERMEABILITY RESERVOIR re-injection water treatment process figure;
Fig. 3 ceramic membrane filter processing technological flow figure;
Fig. 4 is oil field extracted water fine filtering processing flow chart of the present invention;
Fig. 5 is the schematic perspective view of the embodiment of the present invention 1 carrier type film core;
Fig. 6 is the front schematic view of the embodiment of the present invention 1 carrier type film core;
Fig. 7 is the embodiment of the present invention 1 carrier type film core side schematic view;
Fig. 8 is partial schematic sectional view in Fig. 6;
Fig. 9 is the enlarged diagram of B portion in Fig. 8;
Figure 10 is the embodiment of the present invention 1 carrier type membrane module schematic diagram;
Figure 11 is the schematic perspective view of the embodiment of the present invention 4 carrier type film cores;
Figure 12 is the embodiment of the present invention 4 carrier type film core side schematic views.；
Description of reference numerals: 1, film core; 11, main body; 12, filtration channel; 13, produce aquaporin; 14, diversion trench; 15, filtering layer; 16, end face; 17, seal area; 2, shell; 21, tackiness agent; 22, backwashing water import; 3, upper end cover; 4, lower end cover; 5, water inlet pipe; 51, inhalant region; 6, dense water rising pipe; 61, dense pool; 7, produce water export mouth; 8, sealing-ring; 9, produce pool; 10 flanges.
Embodiment
Below in conjunction with specific embodiment, further describe the present invention, advantage and disadvantage of the present invention will be more clear along with description.But these embodiment are only exemplary, scope of the present invention are not formed to any restriction.It will be understood by those skilled in the art that lower without departing from the spirit and scope of the present invention and can the details of technical solution of the present invention and form be modified or be replaced, but these modifications and replacement all fall within the scope of protection of the present invention.
As shown in Figure 5-10, hyperchannel tubular type membrane module of the present invention is comprised of tubular membrane core 1, shell 2, upper and lower end cap 3,4, water inlet pipe 5, dense water rising pipe 6, product water export mouth 7 and sealing-ring 8, and the shell 2 of the cylindric or regular prism shape of hollow is set in the periphery of film core 1; Sealing-ring 8 is arranged between film core 1 and shell 2; Upper and lower end cap 3,4 is enclosed in the two ends of film core 1 and shell 2; Lower end cover 4 is connected with water inlet pipe 5, water current to be filtered is introduced to film core and carry out membrane sepn, and upper end cover 3 is connected with dense water rising pipe 6, and the dense water after filtration, through upper end cover 3, flows out membrane module from dense water rising pipe 6; The product water export mouth 7 that is opened in close dense water rising pipe 6 outsides, one end of shell 2 is connected with water pipe, and the product water through filtering is derived to membrane module.
The filtering layer 15 that film core 1 is by membrane filtration supportive body 11 and be in a row uniformly distributed in filtration channel 12 in main body 11, produce aquaporin 13 and produce the partially communicating diversion trench 14 of aquaporin 13 by collecting, be assembled in filtration channel 12 inwalls forms.Filtration channel 12, product aquaporin 13 are in a row uniformly distributed in main body, and every row's filtration channel 12, product aquaporin 13 are parallel to each other, and filtration channel 12 is along the described main body of longitudinal perforation of main body 11; At the inwall of filtration channel 12, pass through the array mode of sintering, bonding, coating, spraying, thermal treatment, crystallization treatment, chemical reaction or several modes, assembling film filtering layer 15, to entering the current of filtration channel 12, carry out membrane filtration processing, generate to filter and produce water and dense water; Diversion trench 14 is arranged on through hole on the outer side wall of main body perpendicular with the end face of main body 1, longitudinal direction along main body is spaced, the product aquaporin of same row corresponding position 13 is communicated with, product aquaporin 13 on same row is spaced with diversion trench 14, the locational product aquaporin of same row spatially with corresponding position on diversion trench be connected, the product water producing in aquaporin 13 confluxes to diversion trench.
Film core main body 11 is comprised of porous material, main body 11 perpendicular to main body rounded, oval, the rectangle in cross section, square, regular polygon or Polygons longitudinally, porous material is selected porous polymer materials, porous ceramic film material or sintered metal materials, for example selective oxidation aluminium, zirconium white, titanium oxide, silicon carbide, stainless steel or titanium alloy material.
The diameter of the main body 11 of the carrier type film core that cross section is rounded is 1-100cm, is preferably 5-20cm; Length is 5-200cm, is preferably 20-120cm.
The embodiment of the present invention be take film core main body and is described as cylindrical shape, and its length is 90cm, and diameter is 14cm.
Other cross-sectional shapes are that ellipse, rectangle, square, regular polygon or polygonal cylinder are all applicable to the present invention, such as Elliptic Cylinder, rectangular parallelepiped, square, positive five limit bodies, hexahedron etc.
Cross section is that circular filtration channel 12, the diameter of product aquaporin 13 are 0.1 ~ 10 millimeter, preferably 1 ~ 5 millimeter; Described cross section is that foursquare filtration channel 12, the length of side of producing aquaporin 13 are 0.1 ~ 10 millimeter, preferably 1 ~ 5 millimeter.
The filtering material of membrane filtration layer 15 that is assembled in filtration channel 12 inwalls is identical with the material that the inorganic carbon membrane film of carrier type core is used, also can be different.The material that filtering layer is used comprises the inorganic materials such as aluminum oxide, zirconium white, titanium oxide, silicon carbide; Or the metallic substance such as stainless steel and titanium alloy; Or the organic polymer material such as polysulfones (PS), polyacrylonitrile (PAN), polyethersulfone (PES), polyvinylidene difluoride (PVDF) (PVDF), polyvinyl chloride (PVC), cellulose acetate (CA), polycarbonate (PC), polyethylene (PE), polypropylene (PP), polyvinylidene difluoride (PVDF) (PVDF), polytetrafluoroethylene (PTFE); Or the functional materials such as ion exchange resin.
The pore size filter of filtering layer 15 is for being 0.001-100 μ m, be preferably 0.01 ~ 20 μ m, 0.01-10 μ m more preferably, further be preferably 0.01-3 μ m, the filtering accuracy that is filtering layer 15 is 0.001-100 μ m, be preferably 0.01 ~ 20 μ m, more preferably 0.01-10 μ m, is further preferably 0.01-3 μ m.
When the carrier type carbon membrane film core that employing the present invention porous material high by porosity and that aperture is large forms filters, it is little that product water transmits resistance in membrane carrier, and the filtering accuracy of film core 1 of the present invention reaches 0.001-100 μ m, can be used as the membrane treatment process of micro-filtration, ultrafiltration, nanofiltration, reverse osmosis, gas delivery, gasification infiltration and ion-exchange.
Interval 3 row's filtration channels 3 between adjacent two scheduling aquaporins in the embodiment of the present invention.
Film core main body 11 of the present invention and the filtration channel 12 on it, product aquaporin 13 are generally by the moulding of extrusion moulding mode, also can be by other currently known methods moulding such as injection moulding or castings.Preferably extruding forming method is made honeycomb support formula film core.In the present invention, the shape, the size dimension that perpendicular to main body 11, are longitudinally cross section of filtration channel 12, product aquaporin 13 can be identical, also can be different, but the resolution for the ease of two kinds of passages, conventionally the opening shape of filtration channel is not identical with product aquaporin opening shape, and the opening size that produces aquaporin 13 is greater than the opening size of filtration channel 12, is conducive to the resolution to two kinds of passages, has also increased product aquaporin space, reduce the resistance to flow of producing water, improved filtration efficiency.
As Fig. 5, 6, 8, shown in 9, outside sidewall in film core main body 11, two end face 2-20cm apart from film core main body 11, be preferably 5-10cm place, by saw, bore, mill, plane or other known way are along the longitudinal direction that is parallel to main body, on the position of the same scheduling aquaporin 13 of correspondence, from the outside of main body 11, offer through hole, connect main body, form diversion trench 14, diversion trench 14 is trapezoidal or rectangle in cross section longitudinally perpendicular to main body 11, diversion trench 14 connects to opposite side from a side of main body, the product aquaporin of same row's corresponding section is communicated with, in the corresponding position of same row's product aquaporin by saw, bore, mill, plane or other known way produce aquaporin from the outside of main body 11 by the part corresponding position and are communicated with, and connect main body 11, form through hole.Diversion trench 14 is mutually vertical with the end face of film core main body 11, and the product water producing in aquaporin flows out film core by diversion trench.
Two end faces of film core main body and the distance separately region between nearest diversion trench are seal area, be seal area along main body longitudinally width be 2-20cm, be preferably 5-10cm, two end faces that is to say main body to and its immediate diversion trench between length be 2-20cm, be preferably 5-15cm.
Be positioned at same row's diversion trench 14 and produce aquaporin 13 and be spaced, diversion trench 14 along main body 11 longitudinally length L be 0.5-100cm, be preferably 1-20cm; The height h of diversion trench is 10-150:100 with the ratio that produces the height of aquaporin, be preferably 50-100:100, be diversion trench 14 along the ratio of the height perpendicular to main body longitudinal direction, be 10-150:100 with producing aquaporin perpendicular to the height h of main body longitudinal direction, be preferably 50-100:100; And the number in the locational described diversion trench of same row is 1-10, be preferably 2-4.
As shown in figure 10, in membrane module of the present invention, sealing-ring 8 is arranged in the seal area 17 in film core main body 11 outsides, two ends, and the side surface of the main body 11 of sealing area is smooth, zero defect, by known seal modes such as sealing-rings, can guarantee sealing effectiveness.
Sealing-ring 8 installation sleeves are located at the outside of film core main body 11 seal areas 17.Space between the sealing-ring 8 at the outside of the inner side of shell 2, film core main body 11 and film core two ends forms produces pool 9.
One end of lower end cover 4 is connected with water inlet pipe 5, and the other end is fixedly connected with and is sealed by flange 10 with shell 2 with film core 1, and the end face 16 of lower end cover 4, film core main body 11 and sealing-ring 8 form inhalant region 51; One end of upper end cover 3 is connected with dense water rising pipe 6, and the other end is fixedly connected with and is sealed by flange 10 with shell 2 with film core 1, and the other end 16 of upper end cover 3, film core main body 11 and sealing-ring 8 form dense pool 61.
The current that flow into from water inlet pipe 5 enter film core by filtration channel 12, after filtering, infiltrate into and produce aquaporin 13, the current that produce aquaporin conflux to produce aquaporin in the diversion trench 14 of same row's corresponding position, current in diversion trench flow into and produce behind pool 9, then through being positioned at shell 2 near the product water export mouth 7 outflow membrane modules in the outside of dense water rising pipe 6 one end.
In order to facilitate the cleaning of membrane module, at the middle part of shell 2, offer backwashing water import 22, for inputting water for cleaning to membrane module, membrane module is carried out to back flushing, be beneficial to the Reusability of membrane module, the work-ing life of membrane component and prolong.
The working process of membrane module of the present invention: current to be filtered flow into behind inhalant region 51 from being positioned at the water inlet pipe 5 of membrane module bottom after lower end cover 4, owing to producing aquaporin 13 and be positioned at the closure of openings of two end faces of main body 11, current enter film core from the opening of the filtration channel 12 of film core, current see through from bottom to top the filtration of the filtering layer 15 in filtration channel 12 in flow process in film core under pressure, infiltrate into and produce aquaporin 13, and flow into diversion trench 14 along producing aquaporin 13, current in diversion trench 14 enter and produce pool 9, finally by producing water export mouth 7, flow out membrane module, after not being concentrated through the current that filter rete 15, flow into dense pool 61, through overrich water water outlet 6, flow out membrane module, reach the effect purifying water.
The embodiment of the present invention with oil field extracted water after pre-treatment, adopt the inorganic carbon membrane assembly of carrier type to carry out meticulous membrane filtration processing, wherein the pretreated current of embodiment 1-3 carry out the processing of two-stage membrane filtration successively, wherein after single filter is processed, produce water conservancy and directly enter second stage filtration with himself pressure (pressure head), without separately establishing second stage inlet water lifting pumps; The pretreated current of embodiment 4 carry out the processing of one-level membrane filtration.
While adopting two-stage membrane filtration to process in the present invention, through pretreated oil field extracted water, by pump, pump into first step membrane filtration module, in first step membrane filtration module, adopt the cross flow filter mode of high crossflow velocity to carry out filtration, purification processing, adjust circular flow, crossflow velocity while regulating thus the first step to filter is 0.1 ~ 5m/s, and transmembrane pressure is 0.05 ~ 0.5MPa.After the first step is filtered, concentrated water drainage enters sink drainage, regulates concentrated water drainage high-volume, to meet the product water rate of recovery of setting; The product water conservancy that the first step is filtered directly enters second stage membrane filtration module with himself pressure head (pressure), the second stage is filtered and is adopted low crossflow velocity or dead-end filtration pattern to carry out purifying treatment, crossflow velocity while controlling second stage filtration is 0 ~ 0.2m/s, transmembrane pressure is 0.01 ~ 0.1MPa, dense water after the membrane filtration of the second stage is back to first step membrane module, and the product water that filter the second stage enters and produces water reclaiming system.
After single filter is processed, produce water conservancy and directly enter second stage filtration with himself pressure (pressure head), without separately establishing second stage inlet water lifting pumps.
Embodiment 1
1, the pre-treatment of oil field extracted water
Oil field extracted water is processed and walnut shell filter processing through gravity settling processing, coagulant precipitation successively, adopt traditional " old three covers " treatment process oil field extracted water to be carried out to the pre-treatment such as oil removing, removal of impurities, make pre-treatment current, the water quality of pretreated current is that the influent quality of first step membrane filtration processing is as shown in table 1.
2, membrane filtration is processed
In the present embodiment, in the main body 11 of carrier type carbon membrane film core, offering altogether 1480 cross sections is foursquare filtration channel 12 and product aquaporin 13, and the length of side of filtration channel 12, product aquaporin 13 is 2mm, as shown in Fig. 5,6,7.The film core main body 1 of the embodiment of the present invention is right cylinder, its diameter 14cm, length 90cm, interval 3 row's filtration channels 12 between adjacent two scheduling aquaporins 13, in the outside of cylindric film core main body 1 corresponding to the corresponding position of producing aquaporin 13, the scope that is 15cm in the distance of two end faces 16 from film core main body 1 is outward by saw, bore, mill, 2 diversion trenchs 14 that plane or other known way are offered along the longitudinal direction of main body 11, same scheduling aquaporin 13 is divided into 3 sections, the length that same ranking is set up each diversion trench 14 is 20cm, spacing between diversion trench is 20cm, the height of diversion trench is 3mm, be each diversion trench be 20cm along the length of the longitudinal direction of cylinder body, along the spacing between adjacent two diversion trenchs of main body longitudinal direction, be 20cm, height along the radial direction of cylindrical body 11 is 3mm, and the height of diversion trench is 100:100 with the diameter ratio that produces aquaporin.
In the embodiment of the present invention, in first step membrane filtration treating processes, in the main body 11 of film core, the filtering accuracy of the filtering layer 15 in filtration channel 12 is 1 μ m, and in the membrane filtration treating processes of the second stage, in the main body 11 of film core, the filtering accuracy of the filtering layer 15 in filtration channel 12 is 0.04 μ m.Film core 1 is packed in the cylindric metal shell 2 of hollow, sealing-ring 8 is arranged in 17 regions, seal area at film core two ends, by film core and body seal, an end face 16 of film core is connected with upper end cover 3 by flange 10, and the other end of upper end cover 3 is connected with water inlet pipe 5; Another end face 16 of film core is connected with lower end cover 4 by flange 10, and the other end of lower end cover 4 is connected with dense water rising pipe 6; The water inlet pipe of membrane module 5 is connected with pretreated current, by the product water export mouth 7 of first step membrane filtration module with the water inlet pipe of second stage membrane filtration module to being connected.
Pretreated water stream flows into first step membrane filtration module by water inlet pipe 5, in cross-flow mode, carry out the processing of first step membrane filtration, wherein, the intake pressure of controlling the processing of first step membrane filtration is 0.4MPa, the dense water cycle flow that adjusting is flowed out from dense water rising pipe 6, controlling crossflow velocity in first step membrane filtration treating processes is 2.1m/s, and dense water pressure is 0.3MPa; Regulate the concentrated water drainage of first step membrane filtration processing high-volume, the water yield that first step membrane filtration is processed is 97% simultaneously, and the pressure of the product water that first step membrane filtration is processed is 0.17MPa, and transmembrane pressure is 0.18MPa.
Product water after first step membrane filtration enters second stage membrane module from producing water export mouth 7 flows out, in cross-flow mode, carry out second stage membrane filtration processing, wherein, the intake pressure of controlling second stage membrane filtration processing is 0.17MPa, regulating the dense water yield of second stage membrane filtration is 10% of second stage membrane filtration flooding quantity, controlling crossflow velocity in the membrane filtration treating processes of the second stage is 0.014m/s, dense water pressure is 0.12MPa, the pressure of the product water that second stage membrane filtration is processed is 0.05MPa, and transmembrane pressure is 0.095MPa.Product water after second stage membrane filtration is processed flows out second stage membrane carrier from producing water export mouth, and the water quality monitoring (WQM) result of producing water is as shown in table 1.
According to < < petroclastic rock reservoir water water quality fertilizer index and analytical procedure > > (SY/T 5329-94), measure suspended substance, median particle size and oil-contg.
Table 1 embodiment 1 Analysis Results of Water Quality
| Project | Membrane filtration water inlet | Produce water | A1 standard |
| Suspension content, mg/L | 29.0 | 0.60 | ≤1 |
| Oil-contg, mg/L | 17.5 | 0.58 | ≤5 |
| Suspended solids median particle size, μ m | 4.1 | 0.92 | ≤1 |
Embodiment 2
1, the pre-treatment of oil field extracted water
Oil field extracted water is processed and walnut shell filter processing through gravity settling processing, coagulant precipitation successively, adopt traditional " old three covers " treatment process oil field extracted water to be carried out to the pre-treatment such as oil removing, removal of impurities, make pre-treatment current, the water quality of pretreated current is that the influent quality of first step membrane filtration processing is as shown in table 2.
2, membrane filtration is processed
Pretreated water stream flows into first step membrane module by water inlet pipe 5, in cross-flow mode, carry out the processing of first step membrane filtration, wherein, except controlling the intake pressure of first step membrane filtration processing, be 0.4MPa, the dense water cycle flow that adjusting is flowed out from dense water rising pipe 6, controlling crossflow velocity in first step membrane filtration treating processes is 0.94m/s, and dense water pressure is 0.35MPa; Regulate the concentrated water drainage of first step membrane filtration processing high-volume, the water yield that first step membrane filtration is processed is 97.5% simultaneously, and the pressure of the product water that first step membrane filtration is processed is 0.20MPa, and transmembrane pressure is outside 0.18MPa, and all the other are identical with embodiment 1;
Product water after first step membrane filtration enters second stage membrane module from producing water export mouth 7 flows out, in cross-flow mode, carry out second stage membrane filtration processing, wherein, except controlling the intake pressure of second stage membrane filtration processing, be 0.20MPa, regulating the dense water yield of second stage membrane filtration is 1% of second stage membrane filtration flooding quantity, controlling crossflow velocity in the membrane filtration treating processes of the second stage is 0.014m/s, dense water pressure is 0.18MPa, the pressure of the product water that second stage membrane filtration is processed is 0.1MPa, outside transmembrane pressure 0.09MPa, all the other are identical with embodiment 1, product water after second stage membrane filtration is processed flows out second stage membrane carrier from producing water export mouth, the water quality monitoring (WQM) result of producing water is as shown in table 2.
Table 2 embodiment 2 Analysis Results of Water Quality
| Project | Water inlet | Produce water | A1 standard |
| Suspension content, mg/L | 26.0 | 0.30 | ≤1 |
| Oil-contg, mg/L | 20.7 | 0.33 | ≤5 |
| Suspended solids median particle size, μ m | 2.8 | 0.70 | ≤1 |
Embodiment 3
Except pretreated water flowing water matter is the influent quality that first step membrane filtration is processed; First step filtered water inlet pressure 0.43MPa, dense water pressure is 0.35MPa, and product water pressure is 0.2MPa, and transmembrane pressure is 0.19MPa; Second stage filtered water inlet pressure 0.2MPa, dense water pressure 0.18MPa, produces water pressure 0.12MPa, and outside transmembrane pressure 0.07MPa, all the other are identical with embodiment 2.Pretreated water flowing water matter and as shown in table 3 through the product water water quality after the processing of secondary membrane filtration.
Table 3 embodiment 3 Analysis Results of Water Quality
| Project | Water inlet | Produce water | A1 standard |
| Suspension content, mg/L | 31.5 | 0.93 | ≤1 |
| Oil-contg, mg/L | 29.8 | 0.86 | ≤5 |
| Suspended solids median particle size, μ m | 4.5 | 0.97 | ≤1 |
Embodiment 4
1, the pre-treatment of oil field extracted water
Oil field extracted water is carried out to the pre-treatment such as oil removing, removal of impurities through gravity settling processing, coagulant precipitation processing and biochemical treatment successively to recovered water, the water quality of the pretreated current that make is that the influent quality of first step membrane filtration processing is as shown in table 4.
2, membrane filtration is processed
In the present embodiment, in the main body 11 of carrier type carbon membrane film core, offer altogether the filtration channel 12 that 1010 cross sections are circular and produce aquaporin 13, the diameter of filtration channel 12, product aquaporin 13 is 3mm, as shown in Figure 11,12.The film core main body 1 of the embodiment of the present invention is right cylinder, its diameter 14cm, length 90cm, interval 3 row's filtration channels 12 between adjacent two scheduling aquaporins 13, in the outside of cylindric film core main body 1 corresponding to the corresponding position of producing aquaporin 3, the scope that is 15cm in the distance of two end faces 16 from film core main body 1 is outward by saw, bore, mill, 2 diversion trenchs 14 that plane or other known way are offered along the longitudinal direction of main body 11, same scheduling aquaporin 13 is divided into 3 sections, the length that same ranking is set up each diversion trench 14 is 20cm, spacing between diversion trench is 20cm, the height of diversion trench is 3mm, be each diversion trench be 20cm along the length of the longitudinal direction of cylinder body, along the spacing between adjacent two diversion trenchs of main body longitudinal direction, be 20cm, height along the radial direction of cylindrical body 11 is 3mm, and the height of diversion trench is 100:100 with the diameter ratio that produces aquaporin.
In embodiment, in first step membrane filtration treating processes, in the film core main body 11 of membrane module, the filtering accuracy of the filtering layer 15 in filtration channel 12 is 1 μ m, film core 1 is packed in the metal shell 2 of hollow, sealing-ring 8 is arranged in 17 regions, seal area at film core two ends, by film core and body seal, an end face 16 of film core is connected with upper end cover 3 by flange 10, and the other end of upper end cover 3 is connected with water inlet pipe 5; Another end face 16 of film core is connected with lower end cover 4 by flange 10, and the other end of lower end cover 4 is connected with dense water rising pipe 6; The water inlet pipe of membrane module 5 is connected with pretreated current.
Pretreated water stream flows into one-level membrane module by water inlet pipe 5, in cross-flow mode, carry out the processing of first step membrane filtration, wherein, the intake pressure of controlling the processing of first step membrane filtration is 0.4MPa, the dense water cycle flow that adjusting is flowed out from dense water rising pipe 6, controlling crossflow velocity in one-level membrane filtration treating processes is 1.8m/s, dense water pressure 0.3MPa; Regulate the concentrated water drainage of one-level membrane filtration processing high-volume, the water yield that one-level membrane filtration is processed is 97% simultaneously, and the pressure of the product water that one-level membrane filtration is processed is 0.18MPa, and transmembrane pressure is 0.17MPa.Product water after one-level membrane module filters flows out from the product water export mouth of membrane filtration module.Produce water water quality as shown in table 4.
Table 4 embodiment 4 Analysis Results of Water Quality
| Project | Water inlet | Produce water | A1 standard |
| Suspension content, mg/L | 11.8 | 0.95 | ≤1 |
| Oil-contg, mg/L | 6.7 | 0.75 | ≤5 |
| Suspended solids median particle size, μ m | 3.6 | 0.91 | ≤1 |
Claims (10)
1. a process for purification for oil field reinjection water, is characterized in that comprising that adopting carrier type membrane module to carry out at least one-level membrane filtration to oil field extracted water processes.
2. process for purification as claimed in claim 1, the filtering accuracy that it is characterized in that the carrier type membrane module in described membrane filtration treating processes is 0.001-100 μ m.
3. process for purification as claimed in claim 1, is characterized in that adopting cross-flow mode to carry out described membrane filtration and processes.
4. process for purification as claimed in claim 1, is characterized in that also comprising oil field extracted water is carried out carrying out described membrane filtration processing after pre-treatment again.
5. process for purification as claimed in claim 4, the water quality that it is characterized in that pretreated oil field extracted water is oleaginousness≤50mg/L, suspension content≤50mg/L.
6. process for purification as claimed in claim 1, is characterized in that described carrier type membrane module comprises:
Film core (1);
Shell (2), the cylindric or straightedge cylinder of hollow, is set in the periphery of film core;
Upper and lower end cap (3,4), is arranged at respectively the upper and lower part of shell (2), and wherein, lower end cover (4) is connected with water inlet pipe (5), and upper end cover (3) is connected with dense water rising pipe (6);
Produce water export mouth (7), be opened in shell (2) outside, for the product water after filtering is derived to membrane module.
7. be process for purification as claimed in claim 6, it is characterized in that described film core (1) comprising:
Main body (11), membrane filtration supporter;
Filtration channel (12), described filtration channel is in a row distributed in main body, and along the described main body of longitudinal perforation of main body, every row's filtration channel is parallel to each other;
Produce aquaporin (13), in a row be distributed in main body extending longitudinally along main body, interval 1-10 row filtration channel between adjacent two scheduling aquaporins, and produce the closure of openings that aquaporin is positioned at two end faces of main body, produce aquaporin and described filtration channel and be parallel to each other;
Diversion trench (14), is opened in main body wall, connects the through hole of main body, on the longitudinal direction along main body, is spaced with same scheduling aquaporin, collects the product water producing in aquaporin.
8. be process for purification as claimed in claim 7, it is characterized in that described main body (11) is rounded, oval perpendicular to the cross section of longitudinal direction, rectangle, square, regular polygon or Polygons.
9. be process for purification as claimed in claim 7, the cross section perpendicular to longitudinal direction of it is characterized in that described filtration channel (12), producing aquaporin (13) is rounded, oval, rectangle, regular polygon or other Polygons.
10. be process for purification as claimed in claim 3, it is characterized in that the inwall of described filtration channel (12) is also assembled with filtering layer (15).
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