CN103663624B - A kind of process for purification of oil field reinjection water - Google Patents
A kind of process for purification of oil field reinjection water Download PDFInfo
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- CN103663624B CN103663624B CN201210341994.4A CN201210341994A CN103663624B CN 103663624 B CN103663624 B CN 103663624B CN 201210341994 A CN201210341994 A CN 201210341994A CN 103663624 B CN103663624 B CN 103663624B
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Abstract
The invention discloses a kind of process for purification of oil field reinjection water, comprise and adopt the inorganic carbon membrane assembly of honeycomb support formula to carry out at least one-level membrane filtration process to oil field extracted water, wherein the filtering accuracy of the membrane module of membrane filtration process is 0.001-100 μm, obtains and is applicable to hypotonic and ultralow permeable reservoir reinjected water.The filtering accuracy of the inventive method is high, the membrane flux of activated carbon composite membrane carrier is large, film oil resistant class pollution capacity is strong, film cored structure integrated level is high, obtained reinjected water water stabilization, oil field reinjection water after fine filtering meets hypotonic and requirement that is spy's hypotonic block oil reservoir reinjected water, reach " clastic rock reservoir water water quality fertilizer index and analytical method " (SY/T? A grade standard 5329-94).
Description
Technical field
The present invention relates to a kind of processing method of oil-polluted 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 field enters secondary, tertiary recovery, hypotonic and spy hypotonic block exploitation accounting improves year by year, and Produced Liquid moisture content is up to 90%, and water flood recovery is for maintenance formation pressure and keep stable production of crude oil to play increasing effect.Hypotonic and spy's hypotonic block reservoir water requires higher, that current domestic reinjected water water quality performs is professional standard " clastic rock reservoir water water quality fertilizer index and analytical method " (SY/T5329-94), wherein require that the highest A1 grade standard is oil content≤5mg/L, suspension content≤1mg/L, suspended solids median particle size≤1 μm.
Oil field extracted water contains petroleum-type organic matter, sulfide, organic phenol, cyanogen, bacterium and SS etc., also adopts the various chemical medicaments added in technique containing water filling, as demulsifier, flocculant and bactericide etc.The salt content of oil field extracted water, COD, salinity and water temperature are all higher, if directly outer row will cause serious environmental pollution. waste valuable water resource 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 treatment technique mainly adopts traditional " old three covers " technique, as shown in Figure 1, i.e. " gravitational settling-coagulant precipitation-filtration ", be aided with the chemical agents such as scale inhibition, inhibition, sterilization simultaneously, make to process rear product water and to reach in reinjected water professional standard reinjection into reservoir after C level or B level.For the A level water standard that hypotonic or ultralow permeable reservoir require, then need to increase fine filtering process, as shown in Figure 2.At present, fine filtering mainly adopts metal film, metal or ceramic post sintering pipe and PE sintered pipes etc. in actual applications.The subject matter existed is: filtering accuracy is not high, produces suspended solids median particle size in water not up to standard; High to water water quality requirement, as required, suspension and oil content are all less than≤10mg/L; Water resistant matter impact capacity is poor, and it is large that water water quality impacts impact.In order to solve the problem, some new technology and technique are suggested.
Chinese utility model patent 03219467.6 discloses a kind of gravitational settling+biochemistry pool+membrane filtration+deoxygenation combination water treatment process and equipment, the microorganism that biochemical treatment is wherein selected is obligate associating flora, has obvious degradation capability to oil-in-water pollutant and CODcr.UF membrane adopts organic or inorganic doughnut or tubular ultrafiltration, produces water and can reach reinjected water A3 standard-required after filtering.But this technique biochemical treatment is subject to water water quality and impact is impacted in water yield change, to water temperature and variation of ambient temperature sensitivity, treatment effect stability cannot ensure.Milipore filter contamination resistance used and oxidation resistance poor, be difficult to ensure 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 conveying equipment and corrosive pipeline problem.This technique finally processes rear product water and only reaches 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 technological process as shown in Figure 3, be specially: first oil-polluted water enters settling tank and carry out natural subsidence, the SS 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, cross-flow mode circulating filtration is adopted in ceramic membrane equipment, penetrating fluid through film can be directly used in re-injection, the circulation fluid containing a large amount of suspended solid and sump oil not through film enters settling tank continuation sedimentation, enter ceramic membrane ultrafitration equipment after mixing with water again to filter, control crossflow velocity 4-8m/s, dense water gets back to circulating tank, when concentration is concentrated into 300-1000 times in circulating tank, carry out automatic pollution discharge; Online detection instrument also according to water water quality situation from Row sum-equal matrix crossflow velocity, can reach 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 the high crossflow velocity cross-flow method of operation, process energy consumption is high.
Chinese utility model patent 201120003222.0 discloses the oil field produced water treatment facilities of a kind of low-permeability high-salt; its treatment process is: oil removal sedimentary adjustive pool+inclined plate separator+coarse filter+gravity coalescing separator+adsorption filter+Multi-stage precise filter; wherein; adsorption filter have employed active carbon filter core; accurate filter employs titanium alloy sintered filter core, and water is produced in process can reach A1 level.This PROCESS FOR TREATMENT long flow path, active carbon filter core absorption is saturated fast, easily dirty stifled, and membrane filtration aperture is large and distribute wide, and the filtering accuracy of sintered filter core is low, producing SS median particle size in water is difficult to up to standard, and process produces shipwreck to reach the water quality requirement of LOW PERMEABILITY RESERVOIR reinjected water.
Application number be 201110081609.2 application for a patent for invention disclose a kind for the treatment of Technology for Petroleum Water Flooding, at least comprise and regulate water pot, air-floating apparatus, pipe-line mixer, nitrogen dynamic response device, sedimentation basin and supersonic filter, and adopt " oil removal by air bubbling oil removal ", mode process oil field extracted water that " nitrogen preparation " and " ultrasonic filtration " combines, its air-flotation process comprises one-level air supporting and the air supporting of secondary nitrogen, by adding medicament before one-level air supporting, strengthen the removal effect of air supporting to oils and suspension, an oil removing can reach 96%.Secondary air-floatation uses nitrogen to remove oils and suspension further, suppresses aerobic bacteria in water as iron bacteria and saprophytic bacteria, to reduce oxygen content in water body simultaneously, solves the etching problem of equipment and pipeline.Oil field reinjection water after this inventive method process can reach B grade standard, and the subject matter of existence is that processing accuracy is not high, uncontrollable to suspended solid 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 existed in the processing method for existing oil field reinjection water particularly LOW PERMEABILITY RESERVOIR reinjected water, a kind of inorganic carbon membrane assembly of honeycomb support formula that adopts is provided to carry out fine filtering process to oil field extracted water, preparation meets the oil field reinjection water method of oil field reinjection water water standard, the filtering accuracy of the inventive method is high, low to water water quality requirement, anti-water water quality impact capacity is strong, reinjected water water stabilization, oil field reinjection water after fine filtering meets hypotonic and requirement that is spy's hypotonic block oil reservoir reinjected water, reach the A grade standard of " clastic rock reservoir water water quality fertilizer index and analytical method " (SY/T5329-94).
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 and adopts carrier type membrane module to carry out at least one-level membrane filtration process to oil field extracted water.
Wherein, in membrane filtration processing procedure, crossflow velocity is 0 ~ 5m/s; The filtering accuracy of membrane filtration is 0.001-100 μm, is preferably 0.01 ~ 20 μm, more preferably 0.01-10 μm, is further preferably 0.01-3 μm; Transmembrane pressure in membrane filtration processes is 0.01 ~ 0.5MPa.
Particularly, described membrane filtration process adopts cross-current flow to carry out; Described carrier type membrane module is tubular membrane component.
Particularly, described membrane filtration is treated to and adopts multichannel tubular membrane component to carry out secondary membrane to oil field extracted water.
Wherein, the filtering accuracy of first order membrane filtration is 0.01 ~ 3 μm, is preferably 0.1 ~ 1 μm; The crossflow velocity controlled in first order 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 processing procedure described in the first order, control that concentrated water drainage high-volume make the first order filter to produce water yield is 90 ~ 99%, preferably 96 ~ 98%.
Wherein, the filtering accuracy of second level membrane filtration is 0.01 ~ 0.1 μm, is preferably 0.01 ~ 0.05 μm; The crossflow velocity controlled in the membrane filtration processes of the second level 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 processing procedure described in the second level, control that concentrated water drainage high-volume make the first order filter to produce water yield is 90 ~ 99%, preferably 96 ~ 98%.
The water inlet of the second level of the present invention membrane filtration process is the product water of first order membrane filtration process, and utilizes the first order to filter the back pressure of product water as second level membrane filtration operating pressure, without the need to increasing intake pump in addition.
After cascade filtration, produce water reach A1 standard, be i.e. oil content≤1mg/L, suspension content≤1mg/L, suspended solids median particle size≤1 μm.
Particularly, also comprise pretreatment is carried out to oil field extracted water after carry out described membrane filtration process again.
Wherein, the water quality of pretreated oil field extracted water is oil content≤50mg/L, suspension content≤50mg/L, namely carries out the current water quality oil content≤50mg/L of membrane filtration process, suspension content≤50mg/L.
Particularly, in pretreated oil field extracted water (namely carrying out the water of membrane filtration process), oil content is 10-50mg/L, and suspension content is 10-50mg/L.
Particularly, described pretreatment comprises and oil field extracted water is carried out successively gravitational settling process, coagulant precipitation process and walnut shell filter process or carry out gravitational settling process, air-flotation process, media filtration process or biochemical treatment or other any method for treating water successively.
Wherein, described carrier type membrane module is tubular membrane component; Be preferably multichannel tubular membrane component.
Wherein, described membrane module comprises:
Film core;
Shell, the cylinder of hollow or straightedge cylinder, be set in the periphery of film core;
Sealing device, is located between film core and shell, is arranged in two seal areas of film core;
Upper and lower end cap, is arranged at shell upper and lower part respectively, and wherein, bottom end cover is connected with water inlet pipe, and upper end cover is connected with dense water outlet pipe;
Produce water export mouth, be arranged on outer side, between two sealing devices, for deriving membrane module by entering the product water after guiding gutter from product aquaporin after filtering.
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 through described main body of longitudinal direction of main body, often arranges filtration channel and be parallel to each other;
Produce aquaporin, be in a row distributed in main body, extending longitudinally along main body, between adjacent two scheduling aquaporins, interval 1-10 arranges filtration channel, and produces the closure of openings that aquaporin is positioned at two end faces of main body, produces aquaporin and described filtration channel is parallel to each other;
Guiding gutter, is opened in the through hole of the through main body in main body wall, is being spaced along on the longitudinal direction of main body with same scheduling aquaporin, collects the product water produced 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 polygon.
Particularly, described main body is by justifying, oval, the solid that rectangle or regular polygon stretching are formed, and 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 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 multichannel tubular membrane or multichannel tubular membrane core.
Especially, described film core is carrier type film core or carrier type inorganic carbon membrane film core.
Film core main body is by porous polymer materials, and porous ceramic film material or sintered metal materials composition, be preferably made up of aluminium oxide, zirconia, titanium oxide, carborundum, stainless steel or titanium alloy.
Wherein, being evenly distributed on the filtration channel in carrier type inorganic carbon membrane film core main body and producing aquaporin number is 1 ~ 20/cm
2; Be preferably 2 ~ 10/cm
2, more preferably 6-10/cm
2.
Wherein, described filtration channel, the cross section of the longitudinal direction perpendicular to main body rounded, oval, rectangle, the regular polygon that produce aquaporin or other polygon.
Particularly, described regular polygon is square, regular pentagon, regular hexagon or octagon.
Particularly, the cross section of the longitudinal direction perpendicular to main body of described filtration channel, product aquaporin is preferably circular, square and regular hexagon.
The shape in the cross section of the longitudinal direction perpendicular to main body of described filtration channel is identical perpendicular to the shape in the cross section of main body longitudinal direction with product aquaporin, 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 producing aquaporin.
Wherein, described perpendicular to main body longitudinal cross-section be circular filtration channel, the diameter producing aquaporin is 0.1 ~ 10 millimeter, preferably 1 ~ 5 millimeter, more preferably 2 ~ 4mm; Described cross section is foursquare filtration channel, the length of side of producing aquaporin is 0.1 ~ 10 millimeter, preferably 1 ~ 5 millimeter, more preferably 1.5 ~ 3mm.
Particularly, described cross section is the filtration channel of regular polygon, the circumscribed circle diameter in the cross section of product aquaporin is 0.1 ~ 10mm, preferably 1 ~ 5mm, more preferably 2-5mm.
Especially, described cross section is filtration channel, the product aquaporin of regular pentagon, and the external diameter of a circle in its cross section is 0.1 ~ 10mm, preferably 1 ~ 5mm; Described cross section is orthohexagonal filtration channel, produces aquaporin, and the external diameter of a circle 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 diameter of a circle in its cross section is 0.1 ~ 10mm, preferably 1 ~ 5mm.
Film core of the present invention is generally shaping by extrusion molding mode with the filtration channel on it, product aquaporin, also can be shaping by other known method such as injection moulding or casting.Preferred extruding forming method makes multi-channel membrane core.Passage on film core of the present invention can be opening shape and measure-alike, also can be different, as different from as the access portal shape of filtering as the channel selecting of producing water collection, and the size of producing aquaporin is also greater than filtration channel, be conducive to the resolution to two kinds of passages like this, too increase and produce aquaporin volume, reduce the flow resistance of producing water.
Wherein, between adjacent two scheduling aquaporins, interval 2-6 arranges filtration channel, and further preferred interval 2-4 arranges filtration channel.
Particularly, described product aquaporin is positioned at the closure of openings at film core main body two ends.
Adhesive, sealing-plug or other known way is used to seal described product aquaporin.Preferred sealing means is that after using the material shutoff identical with film core main body, high-temperature process reaches sealing effectiveness.The opening that filtration channel is positioned at two end faces of main body is open, and be convenient to current and flow into film core main body, carry out membrane filtration, 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 producing water and mixes with water.
Wherein, also filter course is assembled with at described filtration channel inwall.
Particularly, the pore size filter of filter course is 0.001-100 μm, be preferably 0.01 ~ 20 μm, more preferably 0.01-10 μm, further be preferably 0.01-3 μm, the filtering accuracy of the filter course namely formed is 0.001-100 μm, is preferably 0.01 ~ 20 μm, more preferably 0.01-10 μm, is further preferably 0.01-3 μm.
By one or more modes in sintering, bonding, coating, spraying, heat treatment, crystallization treatment, chemical reaction, filter course material is assembled in the inner side of described filtration channel, forms described filter course.One in filter course Material selec-tion microfiltration membranes, milipore filter, NF membrane, reverse osmosis membrane, gas separation membrane, gasification permeable membrane or amberplex.
Wherein, described filter course material elects inorganic material or organic material as.
Particularly, described inorganic material is aluminium oxide, zirconia, titanium oxide, carborundum, stainless steel or titanium alloy.
Particularly, described organic material is polysulfones (PS), polyacrylonitrile (PAN), polyether sulfone (PES), Kynoar (PVDF), polyvinyl chloride (PVC), cellulose acetate (CA), Merlon (PC), polyethylene (PE), polypropylene (PP), Kynoar (PVDF), polytetrafluoroethylene (PTFE) or ion exchange resin.
Multichannel tubular membrane core of the present invention, and porous material that aperture large high by porosity forms, and it is little that product water transmits resistance in film core.Film core in the present invention can as the supporter of micro-filtration, ultrafiltration, nanofiltration, counter-infiltration, gas separation membrane, Pervaporation membrane and amberplex or carrier, its method be film core for separating of filtration channel in assemble one deck isolated by filtration layer, assembling mode can adopt the combination of sintering, bonding, coating, spraying, heat treatment, crystallization treatment, chemical reaction or several mode.During assembling filter layer, not assembling filter layer in the product aquaporin on film core.
Wherein, guiding gutter is opened in the through hole sidewall outside main body running through main body, and it is communicated with being positioned at the product aquaporin part that same ranking is set up.Guiding gutter is spaced along main body longitudinal direction and the product aquaporin being positioned at same row.
Particularly, described guiding gutter is trapezoidal or rectangle along the cross section perpendicular to main body longitudinal direction.
Wherein, described guiding gutter is 0.5-100cm along the length L of main body longitudinal direction, is preferably 1-20cm; The height h of guiding gutter is 10-150:100 with the ratio of the height producing aquaporin, be preferably 50-100:100, namely guiding gutter is 10-150:100 perpendicular to the ratio of to be the diameter of circular product aquaporin or cross section be width (the height h of guiding gutter) and the cross section of the main body longitudinal direction length of side of foursquare product aquaporin, be preferably 50-100:100, be preferably 50-100:100.
Particularly, be 1-10 corresponding to same scheduling aquaporin, along the guiding gutter number of main body longitudinal direction distribution, be preferably 2-4.
In the outside of film core, by saw, bore, mill, plane or other known way are along the longitudinal direction being parallel to film core, the position of the same scheduling aquaporin of correspondence keeps at a certain distance away and offers guiding gutter, guiding gutter is trapezoidal or rectangle perpendicular to the cross section of main body longitudinal direction, along perpendicular to the through main body of main body longitudinal direction, when main body is cylinder, namely guiding gutter along cylindrical tangential through main body namely perpendicular to the through main body of main body radial direction, channel part corresponding for same scheduling aquaporin is communicated with by guiding gutter, namely on the position of same scheduling aquaporin, aquaporin is produced and guiding gutter is spaced, the product water produced in aquaporin flows out film core by guiding gutter.
Guiding gutter is sidewall outside main body from perpendicular to the through main body of channel direction of producing aquaporin, and along the through hole that same scheduling aquaporin direction extends, through hole is rectangle or square along the cross section of main body longitudinal direction, is wherein be 50% ~ 150% of circular product aquaporin diameter perpendicular to the cross section of main body longitudinal direction or be the 50-150% of the foursquare product aquaporin length of side perpendicular to the cross section of main body longitudinal direction perpendicular to the width (i.e. the height h of guiding gutter) of main body longitudinal direction; Guiding gutter is 0.5-100cm along the length L of main body longitudinal direction.Guiding gutter is by through for a same scheduling aquaporin part for correspondence, and each product aquaporin in namely corresponding product aquaporin row is spatially communicated with corresponding guiding gutter, and the product water produced in aquaporin can flow out body region by this guiding gutter.
Wherein, the outside side wall at the two ends of film core main body is respectively equipped with seal area.
Particularly, the width of described seal area is 2-20cm, is preferably 5-10cm.Namely on the outside side wall of distance film core end face 2-20cm, film core main body, offer guiding gutter, guiding gutter is not slot from the end face of main body, and do not arrange guiding gutter in seal area, guiding gutter 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 are 2-20cm to the distance apart from respective immediate guiding gutter, distance main body two end faces >=2-20cm place offer guiding gutter, namely on the outside side wall at the two ends of film core main body along the longitudinal direction length of film core be 2-20cm scope in seal area is set respectively.
Region between two end faces of film core main body and guiding gutter nearest is separately seal area, namely seal area is 2-20cm along the width of main body longitudinal direction, be preferably 5-10cm, that is two end faces of main body are 2-20cm to the distance between its immediate guiding gutter, are preferably 5-10cm.
Wherein, described shell selects the material of metal or non-metallic material to make; Organic rubber sealing ring selected by described sealing device.
Particularly, sealing ring is set in outside the seal area at film core main body two ends, and the inwall of shell, space between the outside of film core main body and the sealing device at film core two ends are formed and produce pool.
Particularly, described product water export mouth is opened in shell near dense water outlet pipe one end.
The current flowed into from water inlet pipe enter film core by filtration channel, product aquaporin is infiltrated into after filtering, the current of same scheduling aquaporin conflux in corresponding guiding gutter, and the current in guiding gutter flow into and produce pool, then flow out membrane module through the product water export mouth being positioned at outer side.
Particularly, described upper and lower end cap and shell pass through Flange joint.
Wherein, upper and lower end cap to be fixedly connected with shell by flange and to seal.
Particularly, an end face of bottom 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, offer the import of backwashing water at the middle part of shell, when cleaning for membrane module, input backwash 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 adopted in the inventive method is high, pore size filter narrowly distributing, and filtering accuracy is high, effectively produces suspension content and the suspension median particle size of water after controlled filter, and membrane flux is large, and oil resistant class pollution capacity is strong.
2, the water quality requirement that the inventive method treats refining oil field extracted water is low, the impact of water water quality on the yield and water quality that produce water is little, in carrier type carbon membrane film core acceptable water water quality of the present invention, suspension and oil content are greater than 10mg/L, suspension even in water and oil content all can up to 50mg/L, and adopt the product water water quality after the inventive method process can reach oil content≤5mg/L, suspension content≤1mg/L, suspended solids median particle size≤1 μm, produce water quality stabilizing, compliance rate is high, meet hypotonic and requirement that is spy's hypotonic block oil reservoir reinjected water, reach the A grade standard of " clastic rock reservoir water water quality fertilizer index and analytical method " (SY/T5329-94), and it is harsh to water water quality requirement to carry out membrane filtration processing method in prior art, require that the suspension of water and oil content are all less than 10mg/L.
3, the inventive method anti-water water quality impact capacity is strong, the ability of existing metal film or ceramic membrane oil resistant pollutant, the membrane flux of the inorganic carbon membrane assembly of carrier type of the present invention is more than 2 times of conventional ceramic membrane flux, even can up to 5 of pottery membrane flux times.The contact angle of described top layer membrane filtration layer and water is low, be only 0.3 °, good hydrophilic property, oil resistant class pollution capacity is strong, adopt cross-flow filtration mode to carry out filtration treatment simultaneously, effectively avoid oil pollution and carry out the impact that water slug causes film itself, significantly reduce water slug to the impact of producing water water quality.
In the membrane filtration processes of 4, the inventive method, transmembrane pressure is little, produces Water transport resistance little, and the flow resistance difference of the product water that each filtration channel is formed is little, and the product discharge of each filtration channel respectively evenly, stablize, and membrane filtration efficiency is high by the product discharge of membrane module.
5, in the inventive method carrier type membrane module film core in film packed density high, filtration channel in unit are, product aquaporin quantity are many, improve the membrane area in unit volume, improve the aquifer yield of unit volume membrane module, reduce the energy consumption and production cost of producing water.
6, in the inventive method carrier type membrane module film core on filtration channel in unit are, to produce aquaporin quantity many, film core volume is little, it is simple, easy to make, and when being assembled into membrane module, structure is simple, sealing surface is few, good sealing effect, be beneficial to the filtration product water resistance difference improving membrane filtration efficiency and different filtration channel little, transmembrane pressure is little, improve the operating efficiency of membrane module, reduce 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 the dense water yield of outer row is few, saves water resource, decreases environmental pollution.
8, the inventive method adopts the cross-flow filtration mode of low crossflow velocity, reduces the energy consumption of water treatment, and the inventive method is applied widely, can be used for, to traditional oil field extracted water old technology process transformation, also can be used for the transformation of other traditional water treatment technologies.
Accompanying drawing explanation
" old three covers " process chart of Fig. 1 tradition oil field extracted water;
Fig. 2 LOW PERMEABILITY RESERVOIR reinjected water process chart;
Fig. 3 ceramic membrane filter processing technological flow figure;
Fig. 4 is oil field extracted water fine filtering process 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 in 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 core;
Figure 12 is the embodiment of the present invention 4 carrier type film core side schematic view.；
Description of reference numerals: 1, film core; 11, main body; 12, filtration channel; 13, aquaporin is produced; 14, guiding gutter; 15, filter course; 16, end face; 17, seal area; 2, shell; 21, adhesive; 22, backwashing water import; 3, upper end cover; 4, bottom end cover; 5, water inlet pipe; 51, inhalant region; 6, dense water outlet pipe; 61, dense pool; 7, water export mouth is produced; 8, sealing ring; 9, is produced from pool; 10 flanges.
Detailed description of the invention
Further describe the present invention below in conjunction with specific embodiment, advantage and disadvantage of the present invention will be more clear along with description.But these embodiments are only exemplary, do not form any restriction to scope of the present invention.It will be understood by those skilled in the art that and can modify to the details of technical solution of the present invention and form or replace down without departing from the spirit and scope of the present invention, but these amendments and replacement all fall within the scope of protection of the present invention.
As shown in Figure 5-10, multichannel tubular membrane component of the present invention by tubular membrane core 1, shell 2, upper and lower end cap 3,4, water inlet pipe 5, dense water outlet pipe 6, produce water export mouth 7 and sealing ring 8 forms, 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; Bottom end cover 4 is connected with water inlet pipe 5, and water current to be filtered are introduced film core and carries out UF membrane, upper end cover 3 is connected with dense water outlet pipe 6, and the dense water after filtration, through upper end cover 3, flows out membrane module from dense water outlet pipe 6; Product water export mouth 7 outside close dense water outlet pipe 6 one end being opened in shell 2 is connected with water pipe, will derive membrane module through the product water filtered.
Film core 1 is by membrane filtration supportive body 11 and the filtration channel 12, the product aquaporin 13 that are in a row uniformly distributed in main body 11 and produce the partially communicating guiding gutter 14 of aquaporin 13 by collecting, be assembled in the filter course 15 of filtration channel 12 inwall forms.Filtration channel 12, product aquaporin 13 are in a row uniformly distributed in main body, often arrange filtration channel 12, product aquaporin 13 is parallel to each other, and filtration channel 12 is along the through described main body of longitudinal direction of main body 11; At the inwall of filtration channel 12 by the combination of sintering, bonding, coating, spraying, heat treatment, crystallization treatment, chemical reaction or several mode, assembling film filter course 15, membrane filtration process is carried out to the current entering filtration channel 12, generates to filter and produce water and dense water; Guiding gutter 14 is arranged on through hole on the lateral wall of main body and perpendicular with the end face of main body 1, longitudinal direction along main body is spaced, the product aquaporin 13 of same row relevant position is communicated with, product aquaporin 13 on same row is spaced with guiding gutter 14, the product aquaporin that same ranking is set up spatially is connected with the guiding gutter on relevant position, and the product water produced in aquaporin 13 confluxes to guiding gutter.
Film core main body 11 is made up of porous material, the cross section perpendicular to main body longitudinal direction of main body 11 is rounded, oval, rectangle, square, regular polygon or polygon, porous polymer materials selected by porous material, porous ceramic film material or sintered metal materials, such as selective oxidation aluminium, zirconia, titanium oxide, carborundum, 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 is with film core main body for cylindrical shape is described, 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, cuboid, square, positive five limit bodies, hexahedron etc.
Filtration channel 12 is along the through described main body of longitudinal direction of main body 11, often arrange filtration channel to be parallel to each other and the opening being positioned at two end faces of main body 11 be open state, without closed, enter the current in filtration channel 12, through the filtration of filter course 15, be separated into filter and produce water and dense water.
The cross section perpendicular to main body 11 longitudinal direction of filtration channel 12, product aquaporin 13 is rounded, oval, square, rectangle, and regular polygon or other polygon, the embodiment of the present invention is described for circular or square.
Cross section is the filtration channel 12 of circle, the diameter of product aquaporin 13 is 0.1 ~ 10 millimeter, preferably 1 ~ 5 millimeter; Described cross section is foursquare filtration channel 12, the length of side of producing aquaporin 13 is 0.1 ~ 10 millimeter, preferably 1 ~ 5 millimeter.
The filtering material being assembled in the membrane filtration layer 15 of filtration channel 12 inwall is identical with the material that carrier type inorganic carbon membrane film core uses, also can be different.The material that filter course uses comprises the inorganic material such as aluminium oxide, zirconia, titanium oxide, carborundum; Or the metal material such as stainless steel and titanium alloy; Or the high-molecular organic material such as polysulfones (PS), polyacrylonitrile (PAN), polyether sulfone (PES), Kynoar (PVDF), polyvinyl chloride (PVC), cellulose acetate (CA), Merlon (PC), polyethylene (PE), polypropylene (PP), Kynoar (PVDF), polytetrafluoroethylene (PTFE); Or the functional material such as ion exchange resin.
The pore size filter of filter course 15 is for being 0.001-100 μm, be preferably 0.01 ~ 20 μm, more preferably 0.01-10 μm, further be preferably 0.01-3 μm, namely the filtering accuracy of filter course 15 is 0.001-100 μm, be preferably 0.01 ~ 20 μm, more preferably 0.01-10 μm, be further preferably 0.01-3 μm.
During the carrier type carbon membrane film core filtration adopting the present invention's and porous material that aperture large high by porosity form, 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 μm, can as the membrane treatment process of micro-filtration, ultrafiltration, nanofiltration, counter-infiltration, gas separaion, gasification infiltration and ion-exchange.
Produce extending longitudinally along main body of aquaporin 13, between adjacent two scheduling aquaporins, interval 1-10 arranges filtration channel, and preferred interval 2-6 arranges filtration channel; The encapsulant such as opening adhesive 21 grade that product aquaporin 13 is positioned at two end faces of main body 11 is closed, and the opening that filtration channel 12 is positioned on two end faces of main body 11 is open state, current to be filtered can only enter main body 11 inside of film core from filtration channel 12.
In the embodiment of the present invention, between adjacent two scheduling aquaporins, filtration channel 3 is arranged at interval 3.
Film core main body 11 of the present invention is generally shaping by extrusion molding mode with the filtration channel 12 on it, product aquaporin 13, also can be shaping by other known method such as injection moulding or casting.Preferred extruding forming method makes honeycomb support formula film core.Filtration channel 12 in the present invention, produce aquaporin 13 perpendicular to main body 11 be longitudinally cross section shape, size dimension can be identical, also can be different, but for the ease of the resolution of two kinds of passages, the opening shape of usual filtration channel is not identical with product aquaporin opening shape, and the opening size producing aquaporin 13 is greater than the opening size of filtration channel 12, be conducive to the resolution to two kinds of passages, too increase and produce aquaporin space, reduce the flow resistance of producing water, improve filter efficiency.
As Fig. 5, 6, 8, shown in 9, at the outside side wall of film core main body 11, two end face 2-20cm of distance film core main body 11, be preferably 5-10cm place, by saw, bore, mill, plane or other known way are along the longitudinal direction being parallel to main body, through hole is offered from the outside of main body 11 in the position of the same scheduling aquaporin 13 of correspondence, through main body, form guiding gutter 14, guiding gutter 14 is trapezoidal or rectangle perpendicular to the cross section of main body 11 longitudinal direction, guiding gutter 14 is through to opposite side from the side of main body, the product aquaporin of the appropriate section of same row is communicated with, namely saw is passed through in the relevant position of the product aquaporin of same row, bore, mill, part relevant position is produced aquaporin from the outside of main body 11 and is communicated with by plane or other known way, and through main body 11, form through hole.Guiding gutter 14 is mutually vertical with the end face of film core main body 11, and the product water produced in aquaporin flows out film core by guiding gutter.
Guiding gutter 14 is the seal area 6 of film core to the exterior lateral area of two end faces 16 of film core main body 11, namely being respectively equipped with along main body longitudinal direction length at the two ends of film core main body 11 is the seal area of 2-20cm, that is in the scope of two end face 2-20cm of distance film core main body 11, guiding gutter is not offered, but offer guiding gutter 14 in the distance that the distance of two end faces of distance film core main body 11 is respectively greater than 2-20cm along the longitudinal direction of main body, guiding gutter is 2-20cm to the distance of the end face 16 of main body, is preferably 5-10cm.
Region between two end faces of film core main body and the nearest separately guiding gutter of distance is seal area, namely seal area is 2-20cm along the width of main body longitudinal direction, be preferably 5-10cm, that is two end faces of main body are 2-20cm to the length between its immediate guiding gutter, are preferably 5-15cm.
The guiding gutter 14 and the product aquaporin 13 that are positioned at same row are spaced, and guiding gutter 14 is 0.5-100cm along the length L of main body 11 longitudinal direction, is preferably 1-20cm; The height h of guiding gutter is 10-150:100 with the ratio of the height producing aquaporin, be preferably 50-100:100, namely guiding gutter 14 is 10-150:100 perpendicular to the height h of main body longitudinal direction with producing aquaporin along the ratio of the height perpendicular to main body longitudinal direction, is preferably 50-100:100; And the number being in the described guiding gutter that same ranking is set up is 1-10, is 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 outside film core main body 11 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 ensure sealing effectiveness.
Sealing ring 8 installation sleeve is located at the outside of film core main body 11 seal area 17.The inner side of shell 2, space between the outside of film core main body 11 and the sealing ring 8 at film core two ends are formed produces pool 9.
One end of bottom end cover 4 is connected with water inlet pipe 5, and the other end and film core 1 and shell 2 are fixedly connected with by flange 10 and seal, and end face 16 and the sealing ring 8 of bottom end cover 4, film core main body 11 form inhalant region 51; One end of upper end cover 3 is connected with dense water outlet pipe 6, and the other end and film core 1 and shell 2 are fixedly connected with by flange 10 and seal, and other end 16 and the sealing ring 8 of upper end cover 3, film core main body 11 form dense pool 61.
The current flowed into from water inlet pipe 5 enter film core by filtration channel 12, infiltrate into after filtering and produce aquaporin 13, produce the current of aquaporin conflux to product aquaporin in the guiding gutter 14 of the relevant position of same row, after current in guiding gutter flow into and produce pool 9, then flow out membrane module through being positioned at the product water export mouth 7 of shell 2 near the outside of dense water outlet pipe 6 one end.
The conveniently cleaning of membrane module, offers backwashing water import 22 at the middle part of shell 2, for inputting water for cleaning in membrane module, carrying out backwash to membrane module, being beneficial to the Reusability of membrane module, the service life of membrane component and prolong.
The course of work of membrane module of the present invention: after current to be filtered flow into inhalant region 51 from the water inlet pipe 5 being positioned at membrane module bottom after bottom end cover 4, the closure of openings of two end faces of main body 11 is positioned at owing to producing aquaporin 13, current enter film core from the opening of the filtration channel 12 of film core, under pressure current in film core from bottom to top in flow process through the filtration of the filter course 15 in filtration channel 12, infiltrate into and produce aquaporin 13, and flow into guiding gutter 14 along producing aquaporin 13, current in guiding gutter 14 enter and produce pool 9, membrane module is flowed out finally by product water export mouth 7, after not being concentrated through the current filtering rete 15, flow into dense pool 61, membrane module is flowed out through overrich water delivery port 6, reach the effect purified water.
The embodiment of the present invention with oil field extracted water after pretreatment, carrier type inorganic carbon membrane assembly is adopted to carry out meticulous membrane filtration process, wherein the pretreated current of embodiment 1-3 carry out the process of two-stage membrane filtration successively, after single filter process, wherein producing himself pressure of water conservancy (pressure head) directly entering second level filtration, without the need to separately establishing second level inlet water lifting pumps; The pretreated current of embodiment 4 carry out the process of one-level membrane filtration.
When adopting the process of two-stage membrane filtration in the present invention, first order membrane filtration module is pumped into by pump through pretreated oil field extracted water, in first order membrane filtration module, adopt the cross-flow filtration mode of high crossflow velocity to carry out filtration, purification process, adjustment circular flow, crossflow velocity when regulating the first order to filter thus is 0.1 ~ 5m/s, and transmembrane pressure is 0.05 ~ 0.5MPa.After the first order is filtered, concentrated water drainage enters sewerage, regulates concentrated water drainage high-volume, with the product Water Sproading rate of satisfied setting; The product water conservancy that the first order is filtered directly enters second level membrane filtration module with himself pressure head (pressure), the second level is filtered and is adopted low crossflow velocity or dead end filtration mode to carry out purified treatment, the crossflow velocity controlled when the second level is filtered is 0 ~ 0.2m/s, transmembrane pressure is 0.01 ~ 0.1MPa, dense water after the membrane filtration of the second level is back to first order membrane module, and the product water that the second level is filtered enters and produces Water circulation system.
After single filter process, producing himself pressure of water conservancy (pressure head) directly entering second level filtration, without the need to separately establishing second level inlet water lifting pumps.
Embodiment 1
1, the pretreatment of oil field extracted water
By oil field extracted water successively through gravitational settling process, coagulant precipitation process and walnut shell filter process, namely traditional " old three covers " treatment process is adopted to carry out the pretreatment such as oil removing, removal of impurities to oil field extracted water, obtained pretreatment current, the water quality of pretreated current and the influent quality of first order membrane filtration process as shown in table 1.
2, membrane filtration process
In the present embodiment carrier type carbon membrane film core main body 11 on to offer 1480 cross sections be altogether foursquare filtration channel 12 and produce aquaporin 13, filtration channel 12, the length of side of producing aquaporin 13 are 2mm, as shown in Fig. 5,6,7.The film core main body 1 of the embodiment of the present invention is cylinder, its diameter 14cm, length 90cm, between adjacent two scheduling aquaporins 13, filtration channel 12 is arranged at interval 3, the corresponding position of producing aquaporin 13 is corresponded in the outside of cylindric film core main body 1, the scope being 15cm in the distance of two end faces 16 from film core main body 1 passes through saw outward, bore, mill, 2 guiding gutters 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 guiding gutter 14 is 20cm, spacing between guiding gutter is 20cm, the height of guiding gutter is 3mm, namely each guiding gutter is 20cm along the length of the longitudinal direction of cylinder body, be 20cm along the spacing between adjacent two guiding gutters of main body longitudinal direction, height along the radial direction of cylindrical body 11 is 3mm, and the height of guiding gutter is 100:100 with the diameter ratio of product aquaporin.
In the embodiment of the present invention in the first order membrane filtration processing procedure film core main body 11 on the filtering accuracy of filter course 15 in filtration channel 12 be 1 μm, in the membrane filtration processing procedure of the second level film core main body 11 on the filtering accuracy of filter course 15 in filtration channel 12 be 0.04 μm.Film core 1 is loaded in the cylindrical metal shell 2 of hollow, sealing ring 8 is arranged in seal area 17 region 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 bottom end cover 4 by flange 10, and the other end of bottom end cover 4 is connected with dense water outlet pipe 6; The water inlet pipe 5 of membrane module is connected with pretreated current, by the product water export mouth 7 of first order membrane filtration module and the water inlet pipe of second level membrane filtration module to being connected.
Pretreated water flows through water inlet pipe 5 and flows into first order membrane filtration module, the process of first order membrane filtration is carried out with cross-current flow, wherein, the intake pressure controlling the process of first order membrane filtration is 0.4MPa, regulate the dense water circulation flow flowed out from dense water outlet pipe 6, controlling crossflow velocity in first order membrane filtration processing procedure is 2.1m/s, and dense water pressure is 0.3MPa; Regulate the concentrated water drainage of first order membrane filtration process high-volume, make the water yield of first order membrane filtration process be 97%, the pressure of the product water of first order membrane filtration process is 0.17MPa, and transmembrane pressure is 0.18MPa simultaneously.
Product water after first order membrane filtration enters second level membrane module after product water export mouth 7 flows out, second level membrane filtration process is carried out with cross-current flow, wherein, the intake pressure controlling second level membrane filtration process is 0.17MPa, the dense water yield regulating second level membrane filtration is 10% of second level membrane filtration inflow, controlling crossflow velocity in the membrane filtration processing procedure of the second level is 0.014m/s, dense water pressure is 0.12MPa, the pressure of the product water of second level membrane filtration process is 0.05MPa, and transmembrane pressure is 0.095MPa.Product water after the membrane filtration process of the second level flows out second level membrane carrier from product water export mouth, and the water quality monitoring result of producing water is as shown in table 1.
Suspension, median particle size and oil content is measured according to " clastic rock reservoir water water quality fertilizer index and analytical method " (SY/T5329-94).
Table 1 embodiment 1 Analysis Results of Water Quality
| Project | Membrane filtration is intake | Produce water | A1 standard |
| Suspension content, mg/L | 29.0 | 0.60 | ≤1 |
| Oil content, mg/L | 17.5 | 0.58 | ≤5 |
| Suspended solid median particle size, μm | 4.1 | 0.92 | ≤1 |
Embodiment 2
1, the pretreatment of oil field extracted water
By oil field extracted water successively through gravitational settling process, coagulant precipitation process and walnut shell filter process, namely traditional " old three covers " treatment process is adopted to carry out the pretreatment such as oil removing, removal of impurities to oil field extracted water, obtained pretreatment current, the water quality of pretreated current and the influent quality of first order membrane filtration process as shown in table 2.
2, membrane filtration process
Pretreated water flows through water inlet pipe 5 and flows into first order membrane module, the process of first order membrane filtration is carried out with cross-current flow, wherein, except the intake pressure controlling the process of first order membrane filtration is 0.4MPa, regulate the dense water circulation flow flowed out from dense water outlet pipe 6, controlling crossflow velocity in first order membrane filtration processing procedure is 0.94m/s, and dense water pressure is 0.35MPa; Regulate the concentrated water drainage of first order membrane filtration process high-volume, make the water yield of first order membrane filtration process be 97.5%, the pressure of the product water of first order membrane filtration process is 0.20MPa, and transmembrane pressure is outside 0.18MPa, and all the other are identical with embodiment 1 simultaneously;
Product water after first order membrane filtration enters second level membrane module after product water export mouth 7 flows out, second level membrane filtration process is carried out with cross-current flow, wherein, except the intake pressure controlling second level membrane filtration process is 0.20MPa, the dense water yield regulating second level membrane filtration is 1% of second level membrane filtration inflow, controlling crossflow velocity in the membrane filtration processing procedure of the second level is 0.014m/s, dense water pressure is 0.18MPa, the pressure of the product water of second level membrane filtration process is 0.1MPa, outside transmembrane pressure 0.09MPa, all the other are identical with embodiment 1, product water after the membrane filtration process of the second level flows out second level membrane carrier from product water export mouth, the water quality monitoring 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 content, mg/L | 20.7 | 0.33 | ≤5 |
| Suspended solid median particle size, μm | 2.8 | 0.70 | ≤1 |
Embodiment 3
Except the influent quality of pretreated water flowing water matter and the process of first order membrane filtration; First order 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 level filtered water inlet pressure 0.2MPa, dense water pressure 0.18MPa, produce water pressure 0.12MPa, outside transmembrane pressure 0.07MPa, all the other are identical with embodiment 2.Pretreated water flowing water matter and the product water water quality after secondary membrane process as shown in table 3.
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 content, mg/L | 29.8 | 0.86 | ≤5 |
| Suspended solid median particle size, μm | 4.5 | 0.97 | ≤1 |
Embodiment 4
1, the pretreatment of oil field extracted water
Oil field extracted water is carried out the pretreatment such as oil removing, removal of impurities through gravitational settling process, coagulant precipitation process and biochemical treatment to recovered water successively, the water quality of obtained pretreated current and the influent quality of first order membrane filtration process as shown in table 4.
2, membrane filtration process
In the present embodiment carrier type carbon membrane film core main body 11 on offer filtration channel 12 that 1010 cross sections are circular altogether and produce aquaporin 13, filtration channel 12, the diameter producing aquaporin 13 are 3mm, as shown in Figure 11,12.The film core main body 1 of the embodiment of the present invention is cylinder, its diameter 14cm, length 90cm, between adjacent two scheduling aquaporins 13, filtration channel 12 is arranged at interval 3, the corresponding position of producing aquaporin 3 is corresponded in the outside of cylindric film core main body 1, the scope being 15cm in the distance of two end faces 16 from film core main body 1 passes through saw outward, bore, mill, 2 guiding gutters 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 guiding gutter 14 is 20cm, spacing between guiding gutter is 20cm, the height of guiding gutter is 3mm, namely each guiding gutter is 20cm along the length of the longitudinal direction of cylinder body, be 20cm along the spacing between adjacent two guiding gutters of main body longitudinal direction, height along the radial direction of cylindrical body 11 is 3mm, and the height of guiding gutter is 100:100 with the diameter ratio of product aquaporin.
In embodiment in the first order membrane filtration processing procedure membrane module film core main body 11 on the filtering accuracy of filter course 15 in filtration channel 12 be 1 μm, film core 1 is loaded in the metal shell 2 of hollow, sealing ring 8 is arranged in seal area 17 region 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 bottom end cover 4 by flange 10, and the other end of bottom end cover 4 is connected with dense water outlet pipe 6; The water inlet pipe 5 of membrane module is connected with pretreated current.
Pretreated water flows through water inlet pipe 5 and flows into one-level membrane module, the process of first order membrane filtration is carried out with cross-current flow, wherein, the intake pressure controlling the process of first order membrane filtration is 0.4MPa, regulate the dense water circulation flow flowed out from dense water outlet pipe 6, controlling crossflow velocity in one-level membrane filtration processing procedure is 1.8m/s, dense water pressure 0.3MPa; Regulate the concentrated water drainage of one-level membrane filtration process high-volume, make the water yield of one-level membrane filtration process be 97%, the pressure of the product water of one-level membrane filtration process is 0.18MPa, and transmembrane pressure is 0.17MPa simultaneously.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 content, mg/L | 6.7 | 0.75 | ≤5 |
| Suspended solid median particle size, μm | 3.6 | 0.91 | ≤1 |
Claims (8)
1. the process for purification of an oil field reinjection water, it is characterized in that comprising and adopt carrier type membrane module to carry out at least one-level membrane filtration process to oil field extracted water, described carrier type membrane module comprises: film core (1), shell (2), upper and lower end cap (3,4), water inlet pipe (5), outlet pipe (6) and product water export mouth (7), wherein:
Described film core comprises:
Membrane filtration supporter main body (11);
In a row to be distributed in main body, and the filtration channel (12) of the through described main body of longitudinal direction along main body, and often to arrange filtration channel and be parallel to each other;
In a row be distributed in main body, along the product aquaporin (13) extending longitudinally of 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, product aquaporin and described filtration channel are parallel to each other;
Be opened in the guiding gutter (14) in main body wall, described guiding gutter is the through hole of through main body, be spaced along on the longitudinal direction of main body with same scheduling aquaporin, collect the product water produced in aquaporin, wherein, corresponding to same scheduling aquaporin, along main body longitudinal direction distribution 1-10 guiding gutter, and the height of guiding gutter is 10-150:100 with the ratio of the height producing aquaporin;
Described shell is the cylindric of hollow or straightedge cylinder, is set in the periphery of film core;
Described upper and lower end cap, is arranged at the upper and lower part of shell respectively, and wherein, bottom end cover is connected with water inlet pipe, and upper end cover is connected with dense water outlet pipe;
Described product water export mouth, is opened in outer side, for the product water after filtering is derived membrane module.
2. process for purification as claimed in claim 1, is characterized in that the filtering accuracy of the carrier type membrane module in described membrane filtration processing procedure is 0.001-100 μm.
3. process for purification as claimed in claim 1, is characterized in that adopting cross-current flow to carry out described membrane filtration process.
4. process for purification as claimed in claim 1, it is characterized in that also comprising pretreatment is carried out to oil field extracted water after carry out described membrane filtration process again.
5. process for purification as claimed in claim 4, is characterized in that the water quality of pretreated oil field extracted water is oil content≤50mg/L, suspension content≤50mg/L.
6. the process for purification as described in as arbitrary in claim 1-5, is characterized in that described main body (11) is rounded, oval perpendicular to the cross section of longitudinal direction, rectangle, square, regular polygon or polygon.
7. the process for purification as described in as arbitrary in claim 1-5, is characterized in that described filtration channel (12), produces that the cross section perpendicular to longitudinal direction of aquaporin (13) is rounded, oval, rectangle, regular polygon or other polygon.
8. the process for purification as described in as arbitrary in claim 1-5, is characterized in that the inwall of described filtration channel (12) is also assembled with filter course (15).
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Denomination of invention: A refining method of oilfield reinjection water Effective date of registration: 20211015 Granted publication date: 20151216 Pledgee: South Taihu New Area sub branch of Huzhou Wuxing Rural Commercial Bank Co.,Ltd. Pledgor: ZHEJIANG CATHAYRIPE ENVIRONMENTAL ENGINEERING Co.,Ltd. Registration number: Y2021330001922 |
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