CN103657413A - Purifying method of high-temperature condensed water - Google Patents
Purifying method of high-temperature condensed water Download PDFInfo
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- CN103657413A CN103657413A CN201210341530.3A CN201210341530A CN103657413A CN 103657413 A CN103657413 A CN 103657413A CN 201210341530 A CN201210341530 A CN 201210341530A CN 103657413 A CN103657413 A CN 103657413A
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Abstract
The invention discloses a purifying method of condensed water. The purifying method comprises the steps of adopting a honeycomb-shaped carrier type inorganic carbon membrane assembly to carry out at least one stage of membrane filtering treatment on high-temperature condensed water, wherein the filtering accuracy of the membrane assembly treated by membrane filtering is 0.001-100mum, and preparing the boiler supplementing water suitable for recycling. The purifying method disclosed by the invention has the advantages that the filtering accuracy is high, the membrane flux of a honeycomb-shaped carrier type membrane core is large, the impact resistance of incoming water is strong, the resistance to oil pollution is strong, the integration level of the membrane core structure is high, the preparation method is simple, a complex online discrimination system is not needed, and the prepared condensed water is stable in quality and high in temperature, meets the requirement on water quality of the boiler supplementing water and saves a great amount of heat.
Description
Technical field
The present invention relates to a kind of processing method of sewage, particularly a kind of purification method of condensed water in high temperature, belongs to water treatment and energy recovery technical field.
Background technology
In the industries such as thermoelectricity, chemical industry and petrochemical industry, steam is widely used as a kind of power and thermal source.The heat energy of steam is comprised of sensible heat and latent heat two parts, conventionally just utilizes the latent heat of steam and a small amount of sensible heat, discharges after latent heat and a small amount of sensible heat, and steam is transformed into condensed water in high temperature, and the temperature of condensed water in high temperature is generally more than 50 ℃.The heat energy of condensate water is worth and accounts for 25% left and right that steam thermal energy is worth, and is the good distilled water of a kind of water quality, can be used as boiler feedwater, realizes water-saving and emission-reducing and energy-saving and emission-reduction.But in actual application, due to corrosion and the leakage of heat transmission equipment and pipeline, condensate water is polluted and is contained a small amount of oils and solid corrosion product as the corrosion product of iron and copper.Therefore, condensate water must through processing remove contained pollutant could be as boiler feedwater.At present, condensate water recovery utilization rate is lower, and a large amount of condensed water in high temperature are used as sewage discharge, not only cause water resource waste, also lose large energy, cause thermal pollution to a certain degree.
The main cause that the condensed water in high temperature rate of recovery is low is under hot conditions, to be difficult to effectively remove oil, iron, and the oil in removal condensate water and iron are processed after need to lowering the temperature again, therefore cause a large amount of wastes of heat energy.In condensed water in high temperature, oil mainly exists with dissolved oil and oil emulsion form, and molecular activity is large, is difficult to realize water-oil separating.The material of steam pipeline is carbon steel, easily under aerobic and sour environment, corrodes.Corrosion product has the Fe of suspended state and colloidal attitude
3o
4, Fe
2o
3, and ionic state Fe
2+, Fe
3+, by stopping material or filter membrane, be difficult to remove.
It is a kind of containing micro oil and organic steam condensate reuse method that application number is that 200410030636.7 application for a patent for invention discloses, will be containing micro oil and organic steam condensate, pass into water treatment workshop section and lost efficacy in the resin anion (R.A.) bed of not yet regeneration and remove micro oil and organic matter in steam condensate, and then by resin regeneration; Removed micro oil and organic steam condensate through resin cation bed remove cation, resin anion (R.A.) bed removes anion, finally by mixed bed, further removes positive and negative ion, reaches high pressure boiler water supply index.Although this invention has the industrial feature of easy input, the method is subject to resin contamination resistance and thermal stability limit, can only adopt andnon-continuous operation manner, needs the regeneration chemicals accumulatings such as loaded down with trivial details resin regeneration processing and soda acid.
US Patent No. P4,638,766 disclose a kind of after condensate water is processed the technology as boiler feedwater, first by removing most non-solubilised state oils as degreasing units such as coalescing filters, then adopting reverse-osmosis treated to remove residue organic pollution and ion, reach boiler feedwater requirement.The method adopts bi-level treatment technique, the first order process after a certain amount of oil pollutant of oil-containing still in water, large on reverse osmosis membrane impact; Meanwhile, the method needs high temperature counter-infiltration, and cost of investment is higher; Finally, the method can only be processed 80 ° of condensate water below C.
Application number is a kind of method that 200710024847.3 application for a patent for invention discloses film isolation of purified steam condensed water in high temperature, condensed water in high temperature is successively passed through to micro-filtration or milipore filter pretreatment and NF membrane advanced treating, remove the impurity such as suspension, oil, colloid, dissolubility small organic molecule and inorganic ions in water.Although the method realizes, process water outlet reuse up to standard, saved a large amount of boiler feed waters, reclaim heat energy in condensed water in high temperature, but the method needs high temperature resistant nanofiltration, the anti-oil pollution ability of ceramic membrane is general simultaneously, and water resistant matter impact capacity is poor, need to cause energy consumption higher compared with high crossflow velocity.
Application number is a kind of method that 200710024848.8 application for a patent for invention discloses processing high temperature condensed water by integration technique of membrane, with aperture, be micro-filtration or the milipore filter of 0.01～1 μ m, under 0.01～1.5MPa pressure, the condensed water in high temperature that is 50 ℃～95 ℃ to temperature filters, most of oil in trap water, colloid and suspended contamination, then carry out follow-up absorption or further adopt ion-exchange treatment, although realizing, the method processes water outlet reuse up to standard, it is poor that but the method exists membrane filtration water resistant matter to impact, during adsorption treatment condensed water in high temperature, sorbing material may have mineral matter and organic loss to ooze out, cause secondary water pollution, finally need high-temperature resin deironing, cost is higher.
Application number is a kind of method that the application for a patent for invention of 200810023494.X discloses purifying high-temperature condensed water, adopt polymeric complexing agent, complexing produces the dissolubility ion that electricity is led, then adopt the method for ceramic membrane filter to hold back polymeric complexing agent, remove the dissolubility ionic impurity in water, wherein ceramic membrane reaches more than 99% the rejection of polymeric complexing agent, can guarantee to penetrate electrical conductivity of water below 10 μ S/cm, and can not introduce secondary pollution, although the method is applicable to the dissolubility ion in purifying high-temperature condensed water, but the method need to be added water soluble polymer complexing agent, complexing agent can produce and pollute follow-up filter membrane, once stick to film surface, be difficult to be removed by backwash and Chemical cleaning, make the pollution that is difficult to recovery of pair of films.
The patent No. is that 200820078652.7 utility model patent discloses a kind of condensate water combined type high temperature oil-removing iron-removing apparatus, comprise automaton, warning device, the water inlet monitor connecting successively by pipeline, pressure and temp adjuster, filter and water outlet monitor, between described filter and described water outlet monitor, by pipeline, be connected with condensed water oil-removing device and condensed water deironing device in turn, described water outlet monitor has two delivery ports, respectively with the water inlet of described pressure and temp adjuster with use equipment connection; Described water inlet monitor is communicated with water inlet and the external bypass of described pressure and temp adjuster by triple valve.This device adopts the deironing of powder precoat filter, although can remove the iron ion of condensate water, reaches recovery standard, adopts the product water yield of this device preparation low, and high-temperature resin, and powdered resin precoat filter easily causes the chemical contamination of water quality.
The patent No. is that 201120184305.4 utility model patent discloses a kind of high-temperature iron removing filter of condensed water in boiler, there are exhaust outlet and water inlet in tank body upper end, there are sewage draining exit and delivery port in tank body lower end, in tank body, be fixed with top board and base plate, between top board and base plate, longitudinal arrangement has filter element; Filter element is that porosity is the stainless steel metal sintering filter element of 0.2～10 μ m; There is backwash outlet tank body upper end, and there is backwash import lower end; Water inlet, delivery port, backwash outlet, backwash import, exhaust outlet and sewage draining exit place are all provided with magnetic valve, and magnetic valve is connected with the output of PLC.Although adopt this filter can remove the magnetic and non-magnetic impurities iron in steam condensate (SC), because the filtering accuracy of metal sintering filter element is lower, and pore-size distribution is wider, therefore poor to the removal effect of suspension; And the ability of the anti-oil pollution of metal sintering filter element is poor, water quality impact meeting causes to it pollution that is difficult to recovery.
In various condensed water in high temperature processing methods, condensed water in high temperature oil removal treatment method is mainly contained to active carbon adsorption above, resin adsorption method, the extraction of high-temperature resin class and ceramic membrane filter method etc.Wherein absorption method is subject to saturated adsorption capacity and material and is subject to that oils is dirty stifledly affects restriction, and water quality is unstable; The extraction of high-temperature resin class and ceramic membrane rule tolerance water water quality impact capacity are poor, and water quality impact can cause the degree of depth of resin or film to pollute, and causes being difficult to the destruction of recovery.Condensed water in high temperature deironing processing method is mainly contained to ion-exchange, powdex filtration method, high temperature nanofiltration and high temperature hyperfiltration, complexing-filtration combined method, metal sintering pipe filtration method etc.Wherein ion-exchange and powdex method need to be used high-temperature resin, and resin contamination resistance is poor, powdered resin precoat filter complex process, and cost is higher; High temperature nanofiltration and counter-infiltration rule are had relatively high expectations to film, and investment and the operating cost of film are high; Complexing-filter rule need to add medicament, re-use micro-filtration or ultrafiltration and remove complex compound, and institute's adding medicine is a kind of water-soluble high-molecular material, and these medicaments can cause the pollution that is difficult to recovery to subsequent film filter process; Metal sintering pipe filter rule is because the filtering accuracy of sintered pipes is not high, and pore-size distribution is wider, all removal suspension weak effects.And water resistant matter impact capacity is poor in existing condensed water in high temperature processing procedure, complex process, needs efficient online water quality monitoring system.
Condensed water in high temperature is a kind of pure water that is subject to oils and metallic corrosion products slight pollution, the target that condensed water in high temperature is processed is to process, under hot conditions, it is being carried out to oil removing deironing processing without cooling, purification reaches boiler feedwater water quality requirement (General Requirements oil content≤1mg/L, iron content≤50 μ g/L).This highly purified product water just proposes very high requirement to the sealing for the treatment of system, so the sealing of system is up to standard just extremely important to whole treatment system and technique.
Summary of the invention
The object of the invention is the above-mentioned technical problem particularly existing in the processing method of condensed water in high temperature for existing condensate water, provide a kind of honeycomb support formula membrane module that adopts high-temperature steam condensate water to be carried out to the method for fine filtering processing, preparation meets the condensate water of boiler feedwater 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, processing method is simple, online discrimination system without complexity, condensate water water stabilization, the condensate water after fine filtering meets boiler feedwater water quality requirement.
For realizing object of the present invention, one aspect of the present invention provides a kind of purification method of condensed water in high temperature, comprises that adopting carrier type membrane module to carry out at least one-level membrane filtration to condensed water in high temperature processes.
Wherein, the temperature of described condensed water in high temperature is 50-120 ℃.
Particularly, in described membrane filtration processing procedure, controlling treatment temperature is 50-120 ℃.
Wherein, in membrane filtration processing procedure, 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; Filtration temperature in membrane filtration processes is 50-120 ℃.
Wherein, 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 multichannel tubular type membrane module to carry out secondary membrane filtration to condensed water in high temperature.
Particularly, the crossflow velocity that in membrane filtration processing procedure, the first order is filtered is 0 ~ 5m/s; The crossflow velocity that filter the second level is 0 ~ 0.1m/s.
Wherein, the filtering accuracy of first order membrane filtration is 0.01 ~ 3 μ m, is preferably 0.1 ~ 1 μ m; The crossflow velocity of controlling in first order membrane filtration processes is 0 ~ 5m/s, is preferably 0.1 ~ 5m/s, more preferably 0.5 ~ 3m/s; Control transmembrane pressure is 0.01 ~ 0.5MPa, is preferably 0.05 ~ 0.3MPa, more preferably 0.1-0.25MPa.
Particularly, in membrane filtration processing procedure described in the first order, controlling concentrated water drainage, high-volume to make the first order filter produce water yield be 90 ~ 99%, preferably 96 ~ 98%.
Wherein, the filtering accuracy of second level 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 level is 0 ~ 0.1m/s, is preferably 0 ~ 0.007m/s, more preferably dead-end filtration; Control transmembrane pressure is 0.01 ~ 0.2MPa, is preferably 0.05 ~ 0.2MPa, more preferably 0.075-0.15MPa.
Particularly, in the membrane filtration processes of the described second level, concentrated water discharge enters the former water tank of the first order, and controlling concentrated water drainage is high-volume 0 ~ 10% of second level flow of inlet water, is preferably 1 ~ 5%.
The water inlet that the second level of the present invention membrane filtration is processed is the product water that first order membrane filtration is processed, and utilizes the back pressure of first order filtration product water as second level membrane filtration operating pressure, without increasing in addition intake pump.
After cascade filtration, produce water and reach boiler feedwater water standard, be i.e. oil content≤1mg/L, iron content≤50 μ g/L.
Wherein, described carrier type membrane module is tubular membrane component; Be preferably multichannel tubular type membrane module.
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 respectively shell upper and lower part, 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 shell outside, between two sealing devices, for will be after filtering deriving membrane module from producing the product water that aquaporin enter guiding gutter.
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, in a row be distributed in main body extending longitudinally along main body, interval 1-10 row filtration channel at least 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;
Guiding gutter, 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.
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 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 type film or multichannel 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 aluminium oxide, zirconia, titanium oxide, carborundum, 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 polygon 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.
The shape in the cross section longitudinally perpendicular to main body of described filtration channel, product aquaporin can be identical, also can be different, and still, for the ease of the resolution of two kinds of passages, the cross sectional shape of described filtration channel is 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 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 and the filtration channel on it, product aquaporin are generally by the moulding of extrusion molding mode, also can be by other known method 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 flow resistance of producing water.
Wherein, interval 3-6 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 adhesive, 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, high-temperature process 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 filter course.
Particularly, the pore size filter of filter course 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 filter course 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, heat treatment, crystallization treatment, chemical reaction, filter course material is assembled in to the inner side of described filtration channel, forms described filter course.Described filter course material is selected a kind of in microfiltration membranes, milipore filter, NF membrane, reverse osmosis membrane, gas separation membrane, gasification permeable membrane or amberplex.
Wherein, described filter course material is elected inorganic material or organic material as.
Particularly, described inorganic material is aluminium oxide, zirconia, titanium oxide, carborundum, stainless steel or titanium alloy.
Tubular type multi-channel membrane 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, counter-infiltration, gas separation membrane, Pervaporation membrane and amberplex, 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 modes.During assembling filter layer, assembling filter layer not in the product aquaporin on film core.
Wherein, guiding gutter 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.Guiding gutter is spaced along main body longitudinal direction and the product aquaporin that is positioned at same row.
Particularly, described guiding gutter is along being trapezoidal or rectangle in cross section longitudinally perpendicular to main body.
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 that produces the height of aquaporin, be preferably 50-100:100, be guiding gutter 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 guiding gutter) of main body longitudinal direction and cross section, be preferably 50-100:100, be preferably 50-100:100.
Particularly, corresponding to same scheduling aquaporin, along main body longitudinal direction guiding gutter number spaced apart, 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 guiding gutter, guiding gutter along perpendicular to main body longitudinally cross section integral body be trapezoidal or rectangle, along connecting main body perpendicular to main body longitudinal direction, when main body is cylinder, guiding gutter connects main body perpendicular to main body radial direction along tangential perforation main body, the channel part that same scheduling aquaporin is corresponding is communicated with, on the position of same scheduling aquaporin, produce aquaporin and guiding gutter is spaced, the product water producing in aquaporin flows out film core by guiding gutter.
Guiding gutter 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 guiding gutter) 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; Guiding gutter is 0.5-100cm along the length L of main body longitudinal direction.Guiding gutter connects a part for the same scheduling aquaporin of correspondence, and each the product aquaporin in corresponding product aquaporin row is spatially communicated with corresponding guiding gutter, and the product water producing in aquaporin can flow out body region by this guiding gutter.
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 guiding gutter, guiding gutter is not to start fluting from the end face of main body, and guiding gutter is not set in seal area, and 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 to distance separately the distance of immediate guiding gutter be 2-20cm, at two end face >=2-20cm places apart from main body, start to offer guiding gutter, 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 guiding gutter 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 guiding gutter between distance be 2-20cm, be preferably 5-10cm.
Wherein, described shell selects the material of metal or non-metallic material to make; Described sealing device is selected resistant to elevated temperatures inorganic, organic and metal sealing material, the inorganic encapsulants such as preferred graphite and carbon fiber, optimum fiber, nitrile rubber, polytetrafluoro rubber and other rubber seal, preferable alloy lead, copper and other alloy encapsulant.
Particularly, sealing ring is set in the seal area outside at film core main body two ends, and the space between the outside of the inwall of shell, film core main body and the sealing device at film core two ends forms produces pool.
Particularly, described product water export mouth is opened in shell near dense water outlet 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 guiding gutter, and the current in guiding gutter 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 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, at the middle part of shell, offer the import of backwashing water, while cleaning for membrane module, input backwash current.
Condensed water in high temperature purification method tool of the present invention has the following advantages:
1, the multichannel tubular type film cored structure integrated level adopting in the inventive method is high, pore size filter narrowly distributing, film packed density is high, filtration channel in unit are, to produce aquaporin quantity many, improved the membrane area in unit volume, improve the aquifer yield of unit volume membrane module, reduced the energy consumption and the production cost that produce water.
2, in the film core in the present invention, main body is identical with the constituent of separation layer, through high-temperature process, seamless combination becomes one, both thermal coefficient of expansions are identical, the mechanical strength of film core is high, in the process of filtration treatment condensed water in high temperature, can not cause alternate stress and structural deterioration, be suitable for separation and the refinement treatment of high-temperature material.
3, the film cored structure in the present invention is cellular multi-channel structure, main body mechanical strength is high, the Stability Analysis of Structures of carrier type film core under hot conditions, mechanical strength is high, and on membrane module, seal point is few, adopt sealing ring sealing means, improved the sealing property of film core, reduced the possibility of leaking.
4, the inventive method adopts two-stage cross-flow filtration mode to process pending condensed water in high temperature, improved anti-water water quality impact capacity, the first order is filtered the cross-flow filtration pattern that adopts high crossflow velocity, the cross-flow filtration pattern that adopts low crossflow velocity is filtered in the second level, the impact of effectively avoiding oil pollution and coming water slug to cause film itself, has significantly reduced and has come water slug on producing the impact of water water quality.
5, the anti-oil pollution ability of the film core in the inventive method is good, low to pending water water quality requirement, tolerance water water quality impact capacity is strong, be applicable to the purified treatment of the condensate water that temperature is high, the temperature of the condensate water of processing can be up to 120 ℃, and the contact angle of the membrane material of carrier type film core of the present invention is only 0.4 °, the minimum of a value in known various membrane materials.Membrane module of the present invention can be used for processing oil content up to the water of 100mg/L, product water water quality after employing the inventive method is processed reaches the water standard of boiler feedwater, and it is harsh to water water quality requirement while processing in prior art, condensed water in high temperature to be carried out to membrane filtration, require the oil content of water to be all less than 10mg/L.
6, in the membrane filtration processes of the inventive method, transmembrane pressure is little, produces water transmission resistance little, and the flow resistance 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.
Filtration channel on the film core of the tubular membrane component 7, using in the inventive method in unit are, 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, sealing surface 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 operating efficiency of membrane module, reduced processing cost and the energy consumption of condensed water in high temperature.
8, 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 resource, has reduced environmental pollution.
Accompanying drawing explanation
Fig. 1 conventional ceramic film high-temp. Condensate Water Treatment Process;
Fig. 2 membrane module purified treatment of the present invention condensed water in high temperature process chart;
Fig. 3 is the schematic perspective view of the embodiment of the present invention 1 film core;
Fig. 4 is the front schematic view of the embodiment of the present invention 1 film core;
Fig. 5 is the embodiment of the present invention 1 film core side schematic view;
Fig. 6 is partial schematic sectional view in Fig. 4;
Fig. 7 is the enlarged diagram of B portion in Fig. 6;
Fig. 8 is the embodiment of the present invention 1 membrane module schematic diagram;
Fig. 9 is the schematic perspective view of the embodiment of the present invention 4 film cores;
Figure 10 is the embodiment of the present invention 4 film core side schematic views.
Description of reference numerals: 1, film core; 11, main body; 12, filtration channel; 13, produce aquaporin; 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; 52, elevator pump; 53, circulating pump; 54, former water tank; 55, first order membrane module; 56, second level membrane module; 57, control valve; 58, intermediate water tank; 6, dense water outlet pipe; 61, dense pool; 7, produce water export mouth; 8, sealing ring; 9, produce pool; 10 flanges.
The specific 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 Fig. 3-8, multichannel tubular type membrane module of the present invention is comprised of film core 1, shell 2, upper and lower end cap 3,4, water inlet pipe 5, dense water outlet 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; Bottom end cover 4 is connected with water inlet pipe 5, water current to be filtered is introduced to film core and carry out film separation, and 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; The product water export mouth 7 that is opened in close dense water outlet 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 filter course 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 guiding gutter 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 combination of sintering, bonding, coating, spraying, heat treatment, crystallization treatment, chemical reaction or several modes, assembling film filter course 15, to entering the current of filtration channel 12, carry out membrane filtration processing, generate to filter and produce water and dense water; Guiding gutter 14 is arranged on through hole on the sidewall 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 relevant position 13 is communicated with, product aquaporin 13 on same row is spaced with guiding gutter 14, the locational product aquaporin of same row spatially with relevant position on guiding gutter to UNICOM, the product water producing in aquaporin 13 confluxes to guiding gutter.
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 polygon longitudinally, porous material is selected porous polymer materials, porous ceramic film material or sintered metal materials, for example 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 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, cuboid, 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 filter course is used 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 functional material such as ion exchange resin.
The pore size filter of filter course 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 filter course 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 that micro-filtration, ultrafiltration, nanofiltration, counter-infiltration, gas are separated, the membrane treatment process of gasification infiltration and ion-exchange.
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 molding mode, also can be by other known method moulding such as injection moulding or castings.Preferably extruding forming method is made cellular tubular membrane 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, the cross sectional shape that common filtration channel is positioned at two end faces of film core main body is not identical with product aquaporin cross sectional shape, and the sectional dimension of producing aquaporin 13 is greater than the sectional dimension of filtration channel 12, be conducive to the resolution to two kinds of passages, also increased product aquaporin space, reduce the flow resistance of producing water, improved filter efficiency.
As Fig. 3, 4, 6, shown in 7, outside 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 guiding gutter 14, guiding gutter 14 is trapezoidal or rectangle in cross section longitudinally perpendicular to main body 11, guiding gutter 14 connects to opposite side from a side of main body, same row's corresponding part is produced to aquaporin to be communicated with, in the relevant 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 relevant position and are communicated with, and connect 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 producing 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, the seal area that to be respectively equipped with along main body longitudinal direction length at the two ends of film core main body 11 be 2-20cm, that is to say in the scope of two end face 2-20cm apart from film core main body 11 and do not offer guiding gutter, but along main body, longitudinally offer guiding gutter 14 in the distance that is greater than 2-20cm apart from the distance of two end faces of film core main body 11 respectively, guiding gutter is 2-20cm to the distance of the end face 16 of main body, is preferably 5-10cm.
Two end faces of film core main body and the distance separately region between nearest guiding gutter 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 guiding gutter between length be 2-20cm, be preferably 5-15cm.
Be positioned at same row's guiding gutter 14 and produce aquaporin 13 and be spaced, guiding gutter 14 along main body 11 longitudinally length be 0.5-100cm, be preferably 1-20cm; The height h of guiding gutter is 10-150:100 with the ratio that produces the height of aquaporin, be preferably 50-100:100, be guiding gutter 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 guiding gutter of same row is 1-10, be preferably 2-4.
As shown in Figure 8, in membrane module of the present invention, sealing ring 8 is arranged in the seal area 6 in film core main body 11 outsides, two ends, and the side surface of the main body 1 of sealing area is smooth, zero defect, by known seal modes such as sealing rings, can guarantee sealing effectiveness.
One end of bottom 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 bottom 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 outlet 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 guiding gutter 14 of same row's relevant position, current in guiding gutter 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 outlet 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 backwash, be beneficial to the Reusability of membrane module, the service life of membrane component and prolong.
The condensed water in high temperature that the present invention carries out membrane filtration flows into after inhalant region 51 from being positioned at the water inlet pipe 5 of membrane module bottom after bottom 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 filter course 15 in filtration channel 12 in flow process in film core under pressure, 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, 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 delivery port 6, flow out membrane module, reach the effect purifying water.
The condensed water in high temperature that the embodiment of the present invention adopts multichannel tubular type membrane module to be transformed into high-temperature steam carries out the meticulous membrane filtration of two-stage to be processed, be about to condensed water in high temperature successively through 2 multichannel tubular type membrane modules (first order membrane module 55, second level membrane module 56), carry out meticulous film processing, in the present invention, process the condensed water in high temperature that is 100 ℃ to temperature and carry out purified treatment, other temperature are that the condensed water in high temperature of 50-120 ℃ is also applicable to adopt the inventive method to carry out purified treatment.
The course of work of membrane module of the present invention: condensed water in high temperature current to be filtered enter former water tank 54, in the situation that keeping temperature to be 50-120 ℃, condensed water in high temperature pumps into first order membrane filtration module from former water tank 54 through inlet water lifting pumps 52, in first order membrane filtration module, adopt the cross-flow filtration mode of high crossflow velocity to carry out filtration, purification processing, by controlled circulation pump 53, adjust circular flow, crossflow velocity while regulating thus the first order to filter is 0 ~ 5m/s, and transmembrane pressure is 0.01 ~ 0.5MPa.After the first order is filtered, concentrated water drainage enters sewerage, regulates concentrated water drainage high-volume, to meet the product water rate of recovery of 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 pattern to carry out purified treatment, crossflow velocity while controlling second level filtration is 0 ~ 0.1m/s, transmembrane pressure is 0.01 ~ 0.2MPa, dense water after the membrane filtration of the second level is back to former water tank 54, and the product water that filter the second level enters and produces water reclaiming system.
After single filter is processed, produce water conservancy and directly enter second level filtration with himself pressure (pressure head), without separately establishing second level inlet water lifting pumps.
In the present embodiment, in the main body 11 of film core 1, 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. 3,4,5.The film core main body 1 of the embodiment of the present invention is 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 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 h of guiding gutter is 3mm, be each guiding gutter be 20cm along the length of the longitudinal direction of cylinder body, along the spacing between adjacent two guiding gutters of main body longitudinal direction, be 20cm, height along the radial direction of cylindrical body 11 is 3mm, and the height of guiding gutter is 100:100 with the diameter ratio that produces aquaporin.
In the embodiment of the present invention, in first order membrane filtration processing procedure, in the main body 11 of film core, the filtering accuracy of the filter course 15 in filtration channel 12 is 0.1 μ m, and in the membrane filtration processing procedure of the second level, in the main body 11 of film core, the filtering accuracy of the filter course 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 seal area 17 regions 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 of membrane module 5 is connected with pretreated current, by the product water export mouth 7 of first order membrane filtration module with the water inlet pipe of second level membrane filtration module to being connected, as shown in Figure 8.
Keeping temperature, be under the condition of 100 ℃, condensed water in high temperature (100 ℃) is flowed into first order film core by water inlet pipe 5, in cross-flow mode, carry out the processing of first order membrane filtration, wherein, the intake pressure of controlling the processing of first order membrane filtration is 0.45MPa, the dense water circulation flow that adjusting is flowed out from dense water outlet pipe 6, controlling crossflow velocity in first order membrane filtration processing procedure is 2.1m/s, dense water pressure is 0.30MPa; Regulate the concentrated water drainage of first order membrane filtration processing high-volume, the water yield that first order membrane filtration is processed is 98% simultaneously, and the pressure of the product water that first order membrane filtration is processed is 0.22MPa, and transmembrane pressure is 0.155MPa.
Product water after first order membrane filtration enters second level membrane module from producing water export mouth 7 flows out, in cross-flow mode, carry out second level membrane filtration processing, wherein, the intake pressure of controlling second level membrane filtration processing is 0.22MPa, the dense water yield of cross-flow is controlled at 5% of inflow, the concentrate recirculation of second level membrane filtration is to first order membrane module, controlling crossflow velocity in the membrane filtration processing procedure of the second level is 0.007m/s, dense water pressure is 0.18MPa, the pressure of the product water that second level membrane filtration is processed is 0.1MPa, and transmembrane pressure is 0.1MPa.Product water after second level membrane filtration is processed flows out second level membrane carrier from producing water export mouth, and the water quality monitoring result of producing water is as shown in table 1.
According to the mensuration > > (GB/T 12153-1989) of GB < < boiler feed water and cooling water analytical method oil, measure the oil content in current; According to the mensuration > > (GB/T14427-1993) of GB < < boiler feed water and cooling water analytical method iron, measure the iron content in current; According to the mensuration > > (GB/T 6908-1986) of GB < < boiler feed water and cooling water analytical method electrical conductivity, measure electrical conductivity of water.
Table 1 embodiment 1 Analysis Results of Water Quality
| Project | Water inlet | Produce water |
| Suspension content, mg/L | 19.0 | 0.6 |
| Oil content, mg/L | 15.5 | 0.5 |
| Electrical conductivity, μ S/ |
51 | 9.2 |
| COD,mg/L | 45.0 | 4.0 |
| Iron, μ g/L | 109 | 10.0 |
Embodiment 2
Condensed water in high temperature current flow into first order film core by water inlet pipe 5, in cross-flow mode, carry out the processing of first order membrane filtration, wherein, except controlling the intake pressure of first order membrane filtration processing, be 0.4MPa, the dense water circulation flow that adjusting is flowed out from dense water outlet pipe 6, controlling crossflow velocity in first order membrane filtration processing procedure is 0.95m/s, and dense water pressure is 0.3MPa; Regulate the concentrated water drainage of first order membrane filtration processing high-volume, the water yield that first order membrane filtration is processed is 97.5% simultaneously, and the pressure of the product water that first order membrane filtration is processed is 0.18MPa, and transmembrane pressure is outside 0.195MPa, and all the other are identical with embodiment 1;
Product water after first order membrane filtration enters second level membrane module from producing water export mouth 7 flows out, in cross-flow mode, carry out second level membrane filtration processing, wherein, the intake pressure of controlling second level membrane filtration processing is 0.18MPa, regulating the dense water yield of second level membrane filtration is 5% of second level membrane filtration inflow, controlling crossflow velocity in the membrane filtration processing procedure of the second level is 0.007m/s, dense water pressure is 0.16MPa, the pressure of the product water that second level membrane filtration is processed is 0.06MPa, transmembrane pressure is outside 0.11MPa, all the other are identical with embodiment 1, product water after second level membrane filtration is processed flows out second level membrane carrier from producing 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 |
| Suspension content, mg/L | 18.0 | 0.4 |
| Oil content, mg/L | 13.0 | 0.65 |
| Electrical conductivity, μ S/cm | 70.0 | 11.2 |
| COD，mg/L | 55.0 | 6.0 |
| Iron, μ g/L | 179 | 13.0 |
Except condensed water in high temperature current water quality is the influent quality that first order membrane filtration is processed; The intake pressure 0.41MPa that the first order is filtered, dense water pressure 0.34MPa, produces water pressure 0.17MPa, and transmembrane pressure is 0.205MPa; The intake pressure 0.17MPa that filter the second level, dense water pressure 0.15MPa, produces water pressure 0.06MPa, and outside transmembrane pressure 0.1MPa, 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 |
| Suspension content, mg/L | 28.0 | 0.9 |
| Oil content, mg/L | 33.0 | 0.82 |
| Electrical conductivity, μ S/cm | 58.0 | 10.4 |
| COD,mg/L | 75.0 | 7.0 |
| Iron, μ g/L | 201 | 17.0 |
Embodiment 4
In the present embodiment, in the main body 11 of 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 Fig. 9,10.The film core main body 1 of the embodiment of the present invention is 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 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 h of guiding gutter is 3mm, be each guiding gutter be 20cm along the length of the longitudinal direction of cylinder body, along the spacing between adjacent two guiding gutters of main body longitudinal direction, be 20cm, height h along the radial direction of cylindrical body 11 is 3mm, and the height of guiding gutter is 100:100 with the diameter ratio that produces aquaporin.
In the embodiment of the present invention, in first order membrane filtration processing procedure, in the main body 11 of film core, the filtering accuracy of the filter course 15 in filtration channel 12 is 0.1 μ m, and in the membrane filtration processing procedure of the second level, in the main body 11 of film core, the filtering accuracy of the filter course 15 in filtration channel 12 is 0.04 μ m.Film core 1 is packed in the metal shell 2 of hollow, sealing ring 8 is arranged in seal area 17 regions at film core two ends, and 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 of membrane module 5 is connected with pretreated current.
Temperature is that the condensed water in high temperature of 100 ℃ flows into first order membrane module by water inlet pipe 5, in cross-flow mode, carry out the processing of first order membrane filtration, wherein, except controlling the intake pressure of first order membrane filtration processing, be 0.42MPa, the dense water circulation flow that adjusting is flowed out from dense water outlet pipe 6, controlling crossflow velocity in first order membrane filtration processing procedure is 1.9m/s, and dense water pressure is 0.31MPa; Regulate the concentrated water drainage of first order membrane filtration processing high-volume, the water yield that first order membrane filtration is processed is 98% simultaneously, and the pressure of the product water that first order membrane filtration is processed is 0.19MPa, and transmembrane pressure is outside 0.175MPa, and all the other are identical with embodiment 1;
Product water after first order membrane filtration enters second level membrane module from producing water export mouth 7 flows out, in cross-flow mode, carry out second level membrane filtration processing, wherein, the intake pressure of controlling second level membrane filtration processing is 0.19MPa, the dense water yield of cross-flow is controlled at 1% of inflow, the concentrate recirculation of second level membrane filtration is to first order membrane module, controlling crossflow velocity in the membrane filtration processing procedure of the second level is 0.007m/s, dense water pressure is 0.17MPa, the pressure of the product water that second level membrane filtration is processed is 0.065MPa, outside transmembrane pressure 0.115MPa, all the other are identical with embodiment 1, product water after second level membrane filtration is processed flows out second level membrane carrier from producing water export mouth, the water quality monitoring result of producing water is as shown in table 4.
Table 4 embodiment 4 Analysis Results of Water Quality
| Project | Water inlet | Produce water |
| Suspension content, mg/L | 15.0 | 0.65 |
| Oil content, mg/L | 13.0 | 0.2 |
| Electrical conductivity, μ S/cm | 63.0 | 8.4 |
| COD,mg/L | 45.0 | 4.0 |
| Iron, μ g/L | 150 | 13.0 |
Embodiment 5
Except condensed water in high temperature current water quality is the influent quality that first order membrane filtration is processed; First order filtered water inlet pressure 0.44MPa, dense water pressure 0.32MPa, produces water pressure 0.2MPa, transmembrane pressure 0.185MPa; Second level filtered water inlet pressure 0.2MPa, dense water pressure 0.18MPa, produces water pressure 0.1MPa, and transmembrane pressure is outside 0.09MPa, and all the other are identical with embodiment 4.Pretreated water flowing water matter and as shown in table 5 through the product water water quality after the processing of secondary membrane filtration.
Table 5 embodiment 5 Analysis Results of Water Quality
| Project | Water inlet | Produce water |
| Suspension content, mg/L | 35.0 | 0.85 |
| Oil content, mg/L | 75.0 | 0.88 |
| Electrical conductivity, μ S/cm | 63.0 | 13.4 |
| COD，mg/L | 95.0 | 11.0 |
| Iron, μ g/L | 190 | 14.5 |
Claims (10)
1. the water purification method that condenses, is characterized in that adopting carrier type membrane module to carry out at least one-level membrane filtration to condensed water in high temperature and processes.
2. purification method as claimed in claim 1, the temperature that it is characterized in that described condensed water in high temperature is 50-120 ℃.
3. purification method as claimed in claim 1 or 2, the filtering accuracy that it is characterized in that the carrier type membrane module in described membrane filtration processing procedure is 0.001-100 μ m.
4. purification method as claimed in claim 1 or 2, is characterized in that adopting cross-flow mode to carry out described membrane filtration and processes.
5. purification method as claimed in claim 1 or 2, is characterized in that the crossflow velocity in carrying out described membrane filtration processing procedure is 0 ~ 5m/s.
6. purification method 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, bottom end cover (4) is connected with water inlet pipe (5), and upper end cover (3) is connected with dense water outlet 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 purification method 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 at least 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;
Guiding gutter (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 purification method 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 polygon.
9. be purification method 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 polygon.
10. be purification method as claimed in claim 3, it is characterized in that the inwall of described filtration channel (12) is also assembled with filter course (15).
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| CN105967368A (en) * | 2016-06-25 | 2016-09-28 | 安徽升华新奥特化工有限公司 | Green and safe wastewater treatment method for methyl tin mercaptide |
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| CN106007027A (en) * | 2016-06-25 | 2016-10-12 | 安徽升华新奥特化工有限公司 | Environment-friendly wastewater treatment process for methyl tin mercaptide stabilizer |
| CN106045084A (en) * | 2016-06-25 | 2016-10-26 | 安徽升华新奥特化工有限公司 | Environment-friendly methyltin wastewater treatment process |
| CN111484162A (en) * | 2020-04-17 | 2020-08-04 | 莱特莱德（北京）环境技术股份有限公司 | Oil refinery condensed water oil removing system and oil removing method thereof |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN105923804A (en) * | 2016-05-23 | 2016-09-07 | 浙江中凯瑞普环境工程股份有限公司 | High-temperature-condensed-water oil removing technology |
| CN105885089A (en) * | 2016-06-25 | 2016-08-24 | 安徽升华新奥特化工有限公司 | Environment-friendly process for treating wastewater by aid of methyl tin mercaptide combinations |
| CN105967368A (en) * | 2016-06-25 | 2016-09-28 | 安徽升华新奥特化工有限公司 | Green and safe wastewater treatment method for methyl tin mercaptide |
| CN106007027A (en) * | 2016-06-25 | 2016-10-12 | 安徽升华新奥特化工有限公司 | Environment-friendly wastewater treatment process for methyl tin mercaptide stabilizer |
| CN106045084A (en) * | 2016-06-25 | 2016-10-26 | 安徽升华新奥特化工有限公司 | Environment-friendly methyltin wastewater treatment process |
| CN105999876A (en) * | 2016-06-29 | 2016-10-12 | 西安利能科技有限责任公司 | Non-detachable chemical washing method for powder resin covered filter element and detergent |
| CN111484162A (en) * | 2020-04-17 | 2020-08-04 | 莱特莱德（北京）环境技术股份有限公司 | Oil refinery condensed water oil removing system and oil removing method thereof |
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| CN103657413B (en) | 2016-07-06 |
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