CN103657413B - A kind of purification method of condensed water in high temperature - Google Patents
A kind of purification method of condensed water in high temperature Download PDFInfo
- Publication number
- CN103657413B CN103657413B CN201210341530.3A CN201210341530A CN103657413B CN 103657413 B CN103657413 B CN 103657413B CN 201210341530 A CN201210341530 A CN 201210341530A CN 103657413 B CN103657413 B CN 103657413B
- Authority
- CN
- China
- Prior art keywords
- water
- main body
- aquaporin
- membrane
- filtration
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
Landscapes
- Separation Using Semi-Permeable Membranes (AREA)
Abstract
The invention discloses a kind of condensation water purification method, process including condensed water in high temperature adopts the inorganic carbon membrane assembly of honeycomb support formula carry out at least one-level membrane filtration, wherein the filtering accuracy of the membrane module that membrane filtration processes is 0.001-100 μm, prepares the boiler feedwater being suitable to reuse.The filtering accuracy of the inventive method is high, the membrane flux of honeycomb support formula film core is big, anti-water water quality impact capacity is strong, oil resistant class pollution capacity is strong, and film cored structure integrated level is high, and preparation method is simple, without complicated online discrimination system, the condensation water quality stabilizing prepared, temperature is high, meets boiler feedwater water quality requirement, and saves substantial amounts of heat energy.
Description
Technical field
The present invention relates to the processing method of a kind of sewage, particularly to the purification method of a kind of condensed water in high temperature, belong to water and process 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 made up of sensible heat and latent heat two parts, is generally only the latent heat utilizing steam and a small amount of sensible heat, and after release latent heat and a small amount of sensible heat, steam is transformed into condensed water in high temperature, and the temperature of condensed water in high temperature is typically in more than 50 DEG C.Condense the heat energy of water and be worth account for that steam thermal energy is worth about 25%, be the good distilled water of a kind of water quality, it is possible to as boiler feedwater, it is achieved 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, the corrosion product that condensation water is contaminated and contains a small amount of oils and solid corrosion product such as ferrum and copper.Therefore, condense water have to pass through process remove contained pollutant could as boiler feedwater.At present, condensate-water polishing utilization rate is relatively low, and a large amount of condensed water in high temperature are taken as sewage discharge, not only causes water resource waste, and also large losses energy, causes a degree of thermal pollution.
The main cause that the condensed water in high temperature response rate is low is to be difficult under the high temperature conditions effectively remove oil, ferrum, reprocesses, thus result in a large amount of wastes of heat energy after removing the oil condensed in water and ferrum needs cooling.In condensed water in high temperature, oil is main to be existed with dissolved oil and oil emulsion form, and molecular activity is big, it is difficult to realize oil-water separation.The material of steam pipeline is carbon steel, easily corrodes under aerobic and sour environment.Corrosion product has the Fe of suspended state and colloidal attitude3O4、Fe2O3, and ionic state Fe2+、Fe3 +, it is difficult to remove by blocking materials or filter membrane.
Application number be 200410030636.7 application for a patent for invention disclose a kind of containing micro oil and organic steam condensate reuse method, will containing micro oil and organic steam condensate, pass into water to process workshop section and lost efficacy in the resin anion (R.A.) bed that not yet regenerates micro oil and Organic substance in elimination steam condensate, then again by resin regeneration；Being stripped of micro oil and organic steam condensate and remove cation, resin anion (R.A.) bed elimination anion through cationic resin bed, last blended bed removes positive and negative ion further, reaches high pressure boiler water supply index.Although this invention has the industrial feature that easily puts into, but the method is subject to resin contamination resistance and thermal stability limit, can only adopt andnon-continuous operation manner, it is necessary to the regeneration chemicals accumulatings such as loaded down with trivial details resin regeneration process and soda acid.
US Patent No. P4,638,766 disclose a kind of using technology as boiler feedwater after Ion exchange resin, first pass through the such as degreasing units such as coalescing filter and remove most non-the dissolved oils, then adopting reverse-osmosis treated to remove residue organic pollution and ion, boiler feedwater requirement is reached.The method adopts two stages for the treatment of technique, the first order process after still a certain amount of oil pollutant of oil-containing in water, reverse osmosis membrane impact is big；Meanwhile, the method needs high temperature reverse osmosis, and cost of investment is higher；Finally, the method can only process the condensation water of 80 ° of below C.
Application number be 200710024847.3 application for a patent for invention disclose a kind of membrance separation purify steam condensed water in high temperature method, by condensed water in high temperature successively through microfiltration or ultrafilter membrane pretreatment and NF membrane advanced treating, remove the impurity such as the float in water, oil, colloid, dissolubility small organic molecule and inorganic ions.Although the method realization processes standard water discharge reuse, save a large amount of boiler feed water, reclaim heat energy in condensed water in high temperature, but the method needs high temperature resistant nanofiltration, simultaneously ceramic membrane oil resistant class pollution capacity is general, and water resistant matter impact capacity is poor, it is necessary to higher crossflow velocity and cause that energy consumption is higher.
Application number is application for a patent for invention a kind of disclose processing high temperature condensed water by integration technique of membrane the method for 200710024848.8, with the microfiltration that aperture is 0.01～1 μm or ultrafilter membrane, under 0.01～1.5MPa pressure, it is that the condensed water in high temperature of 50 DEG C～95 DEG C is filtered to temperature, most of oil in trap water, colloid and suspended contamination, then carry out follow-up absorption or adopt ion-exchange treatment further, although the method realization processes standard water discharge reuse, but the method exists membrane filtration water resistant matter, and impact is poor, during adsorption treatment condensed water in high temperature, adsorbing material is likely to have mineral and organic loss to ooze out, cause secondary water pollution, finally need high-temperature resin deironing, relatively costly.
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, complexation produces the dissolubility ion of conductance, then the method adopting ceramic membrane filter retains polymeric complexing agent, remove the dissolubility ionic impurity in water, wherein the rejection of polymeric complexing agent is reached more than 99% by ceramic membrane, can ensure that and penetrate electrical conductivity of water at 10 below μ S/cm, and secondary pollution will not be introduced, although the method is suitable for the dissolubility ion in purifying high-temperature condensed water, but the method needs to add water soluble polymer chelating agent, follow-up filter membrane can be produced to pollute by chelating agent, once stick to film surface, it is difficult to be removed it by backwash and Chemical cleaning, make the pollution being difficult to recover of pair of films.
The patent No. be 200820078652.7 utility model patent disclose and a kind of condense water combined type high temperature oil-removing iron-removing apparatus, including automaton, alarm device, the water inlet monitor, pressure and temp actuator, filter and the water outlet monitor that are sequentially connected with by pipeline, it is connected with in turn condensed water oil-removing device and condensed water deironing device by pipeline between described filter and described water outlet monitor, described water outlet monitor has two outlets, is connected with the water inlet of described pressure and temp actuator and the equipment of use respectively；Described water inlet monitor is connected with water inlet and the external bypass of described pressure and temp actuator by three-way valve.This device adopts powder precoat filter deironing, although can remove the iron ion of condensation water, reach recovery standard, but adopt product water yield prepared by this device low, and high-temperature resin, and powdered resin precoat filter easily causes the chemical contamination of water quality.
The patent No. be 201120184305.4 utility model patent disclose a kind of high-temperature iron removing filter of condensed water in boiler, there are air vent and water inlet in tank body upper end, there are sewage draining exit and outlet in tank body lower end, being fixed with top board and base plate in tank body, between top board and base plate, longitudinal arrangement has filter element；Filter element is porosity be 0.2～10 μm stainless steel metal sintering filter element；Tank body upper end has backwash outlets, lower end to have backwash import；Water inlet, outlet, backwash outlets, backwash import, air vent and sewage draining exit place are mounted on electromagnetic valve, and electromagnetic valve is connected with the outfan of PLC.Although adopting this filter can remove the magnetic and non-magnetic impurities ferrum in steam condensate (SC), but owing to the filtering accuracy of metal sintering filter element is relatively low, and pore-size distribution is wider, therefore that the removal effect of float is poor；And the ability of the anti-oil pollution of metal sintering filter element is poor, it can be caused the pollution being difficult to recover by water quality impact.
In any of the above condensed water in high temperature processing method, condensed water in high temperature oil removal treatment method mainly having active carbon adsorption, resin adsorption method, high-temperature resin class extracts and ceramic membrane filter method etc..Wherein absorption method is subject to saturated adsorption capacity and material is affected restriction by oils dirt is stifled, and water quality is unstable；High-temperature resin class extracts and ceramic membrane rule tolerance water water quality impact capacity is poor, and water quality impact can cause the degree of depth of resin or film to pollute, and causes the destruction being difficult to recover.Condensed water in high temperature deironing processing method is mainly had ion exchange, powdex Filtration, high temperature nanofiltration and high temperature hyperfiltration, complexation-filtration combination method, metal sintering pipe Filtration etc..Its ion exchange methods and powdex method need to use high-temperature resin, and resin contamination resistance is poor, powdered resin precoat filter complex process, relatively costly；High temperature nanofiltration and reverse osmosis rule are higher to the requirement of film, and the investment of film and operating cost are high；Complexation-filter rule needs to add medicament, re-uses microfiltration or complex is removed in ultrafiltration, and institute's adding medicine is a kind of water-soluble high-molecular material, and subsequent film filter process can be caused the pollution being difficult to recover by these medicaments；Metal sintering pipe filter rule is not high due to the filtering accuracy of sintered pipes, and pore-size distribution is wider, all removal float weak effects.And water resistant matter impact capacity is poor in existing condensed water in high temperature processing procedure, complex process, it is necessary to efficiently online water quality monitoring system.
Condensed water in high temperature is a kind of pure water being subject to oils and metallic corrosion products slight pollution, the target that condensed water in high temperature processes is to process without cooling, under the high temperature conditions it is being carried out oil removing deironing process, purification reaches boiler feedwater water quality requirement (generally requiring oil content≤1mg/L, iron content≤50 μ g/L).Sealing of the system of process is just proposed significantly high requirement by this highly purified product water, and therefore the sealing of system is up to standard just extremely important to whole process system and technique.
Summary of the invention
It is an object of the invention to the above-mentioned technical problem existed in the processing method for existing condensation water particularly condensed water in high temperature, thering is provided a kind of adopts honeycomb support formula membrane module that high-temperature steam is condensed the method that water carries out fine filtering process, preparation meets the condensation water of boiler feedwater water standard, the filtering accuracy of the inventive method is high, water water quality requirement is low, anti-water water quality impact capacity is strong, processing method is simple, without complicated online discrimination system, condensing water quality stabilizing, the condensation water after fine filtering meets boiler feedwater water quality requirement.
For realizing the purpose of the present invention, one aspect of the present invention provides the purification method of a kind of condensed water in high temperature, processes including adopting carrier type membrane module that condensed water in high temperature carries out at least one-level membrane filtration.
Wherein, the temperature of described condensed water in high temperature is 50-120 DEG C.
Particularly, described membrane filtration processing procedure controls treatment temperature and be 50-120 DEG C.
Wherein, in membrane filtration processing procedure, crossflow velocity is 0 ~ 5m/s；The filtering accuracy of membrane filtration is 0.001-100 μm, it is preferred to 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；Filtration temperature in membrane filtration processes is 50-120 DEG C.
Wherein, described membrane filtration processes and adopts cross-current flow to carry out；Described carrier type membrane module is tubular membrane component.
Particularly, described membrane filtration processes as adopting multichannel tubular membrane component that condensed water in high temperature is carried out secondary membrane.
Particularly, the crossflow velocity that in membrane filtration processing procedure, the first order filters is 0 ~ 5m/s；The crossflow velocity that the second level is filtered is 0 ~ 0.1m/s.
Wherein, the filtering accuracy of first order membrane filtration is 0.01 ~ 3 μm, it is preferred to 0.1 ~ 1 μm；The crossflow velocity controlled in first order membrane filtration processes is 0 ~ 5m/s, it is preferred to 0.1 ~ 5m/s, more preferably 0.5 ~ 3m/s；Control transmembrane pressure is 0.01 ~ 0.5MPa, it is preferred to 0.05 ~ 0.3MPa, more preferably 0.1-0.25MPa.
Particularly, controlling concentrated water drainage in membrane filtration processing procedure described in the first order high-volume makes first order filtration product water yield be 90 ~ 99%, it is preferable that 96 ~ 98%.
Wherein, the filtering accuracy of second level membrane filtration is 0.01 ~ 0.1 μm, it is preferred to 0.01 ~ 0.05 μm；The crossflow velocity controlled in the membrane filtration processes of the second level is 0 ~ 0.1m/s, it is preferred to 0 ~ 0.007m/s, more preferably dead-end filtration；Control transmembrane pressure is 0.01 ~ 0.2MPa, it is preferred to 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 the 0 ~ 10% of second level flow of inlet water, it is preferred to 1 ~ 5%.
The product water that the water inlet that the second level membrane filtration of the present invention processes processes for first order membrane filtration, and utilize the first order to filter the back pressure producing water as second level membrane filtration operating pressure, it is not necessary to additionally increase intake pump.
After cascade filtration, produce water reach boiler feedwater water standard, i.e. oil content≤1mg/L, iron content≤50 μ g/L.
Wherein, described carrier type membrane module is tubular membrane component；It is preferably multichannel tubular membrane component.
Wherein, described membrane module includes:
Film core；
Shell, the cylinder of hollow or straightedge cylinder, be set in the periphery of film core；
Sealing device, in being located between film core and shell, being arranged on two seal areas of film core；
Upper and lower end cap, is respectively arranged at 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 outer side, between two sealing devices, for membrane module will be derived from producing the product water after aquaporin enters guiding gutter after filtering.
Particularly, described film core includes:
Main body, membrane filtration supporter；
Filtration channel, described filtration channel is in a row distributed in main body, and along main body longitudinally through described main body, often row filtration channel be parallel to each other；
Producing aquaporin, be in a row distributed in main body, along the longitudinal extension of main body, between adjacent two scheduling aquaporins, at least 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 is parallel to each other with described filtration channel；
Guiding gutter, the through hole of the through main body being opened in main body wall, it is being spaced with same scheduling aquaporin along the longitudinal direction of main body, is collecting the product water produced in aquaporin.
Wherein, the cross section being perpendicular to main body longitudinal direction of described main body is rounded, oval, rectangle or regular polygon.
Particularly, described main body is by justifying, oval, and rectangle or regular polygon stretch the solid formed, it is preferred to circular, 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, it is preferred to 5-20cm；Length is 5-200cm, it is preferred to 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, it is preferred to 5-20cm；Length is 5-200cm, it is preferred to 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 the inorganic carbon membrane film core of carrier type.
Film core main body is by porous polymer materials, porous ceramic film material or sintered metal materials composition, it is preferable that be made up of aluminium oxide, zirconium oxide, titanium oxide, carborundum, rustless steel or titanium alloy.
Wherein, it is evenly distributed on the filtration channel in carrier type inorganic carbon membrane film core main body and product aquaporin number is 1 ~ 20/cm2；It is preferably 2 ~ 10/cm2, more preferably 6-10/cm2。
Wherein, described filtration channel, produce aquaporin the longitudinal cross section being perpendicular to main body is rounded, oval, rectangle, regular polygon or other polygon.
Particularly, described regular polygon is square, regular pentagon, regular hexagon or octagon.
Particularly, described filtration channel, produce that the longitudinal cross section being perpendicular to main body of aquaporin is preferably circular, square and regular hexagon.
Described filtration channel, the longitudinal cross section being perpendicular to main body producing aquaporin shape can be identical, it is also possible to different, but for the ease of the resolution of two kinds of passages, the cross sectional shape of described filtration channel is different with the cross sectional shape of product aquaporin.
Wherein, being perpendicular to main body longitudinal cross-section described in be circular filtration channel, the diameter producing aquaporin is 0.1 ~ 10 millimeter, it will be preferred that 1 ~ 5 millimeter, more preferably 2 ~ 4mm；Described cross section be foursquare filtration channel, produce aquaporin the length of side be 0.1 ~ 10 millimeter, it will be preferred that 1 ~ 5 millimeter, more preferably 1.5 ~ 3mm.
Particularly, described cross section is the circumscribed circle diameter in the cross section of the filtration channel of regular polygon, product aquaporin is 0.1 ~ 10mm, it will be preferred that 1 ~ 5mm, more preferably 2-5mm.
Especially, described cross section is the filtration channel of regular pentagon, produces aquaporin, and the external diameter of a circle in its cross section is 0.1 ~ 10mm, it will be preferred that 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, it will be preferred that 1 ~ 5mm；Described cross section is the filtration channel of octagon, produces aquaporin, and the external diameter of a circle in its cross section is 0.1 ~ 10mm, it will be preferred that 1 ~ 5mm.
The film core of the present invention and filtration channel thereon, product aquaporin are generally by extrusion molding mode molding, it is also possible to by other known method molding such as injection moulding or casting.Preferred extruding forming method makes multi-channel membrane core.Passage on inventive film core can be opening shape and equivalently-sized, can also be different, as different from as the access portal shape filtered as the channel selecting producing water collection, and the size of product aquaporin is also greater than filtration channel, so be conducive to the resolution to two kinds of passages, too increase product aquaporin volume, reduce the flow resistance producing water.
Wherein, between adjacent two scheduling aquaporins, interval 3-6 arranges filtration channel.
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 that described product aquaporin is sealed.Preferred sealing means is that after using the material closure 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, it is simple to current flow into film core main body, carry 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, it is prevented that produces water and mixes with water.
Wherein, filter course also it is assembled with at described filtration channel inwall.
Particularly, the pore size filter of filter course is 0.001-100 μm, it is preferably 0.01 ~ 20 μm, more preferably 0.01-10 μm, further being preferably 0.01-3 μm, the filtering accuracy of the filter course namely formed is 0.001-100 μm, it is preferred to 0.01 ~ 20 μm, more preferably 0.01-10 μm, further it is 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.Described filter course material selects the one in micro-filtration membrane, ultrafilter membrane, NF membrane, reverse osmosis membrane, gas separation membrane, gasification permeable membrane or ion exchange membrane.
Wherein, described filter course material elects inorganic material or organic material as.
Particularly, described inorganic material is aluminium oxide, zirconium oxide, titanium oxide, carborundum, rustless steel or titanium alloy.
The tubular type multi-channel membrane core of the present invention, is made up of the porous material that porosity is high and aperture is big, and it is little that product water transmits resistance in film core.Film core in the present invention can as the supporter of microfiltration, ultrafiltration, nanofiltration, reverse osmosis, gas separation membrane, Pervaporation membrane and ion exchange membrane or carrier, its method is that assembling mode can adopt the compound mode of sintering, bonding, coating, spraying, heat treatment, crystallization treatment, chemical reaction or several ways for assembling one layer of isolated by filtration layer in the filtration channel that separates at film core.During assembling filter layer, not assembling filter layer in the product aquaporin on film core.
Wherein, guiding gutter is the through hole being opened in and running through main body on the sidewall outside main body, and it will be located in the product aquaporin part connection that same ranking is put.Guiding gutter is spaced along main body longitudinal direction and the product aquaporin being positioned at same row.
Particularly, the longitudinal cross section of main body is trapezoidal or rectangle along being perpendicular to for described guiding gutter.
Wherein, described guiding gutter is 0.5-100cm along the length L of main body longitudinal direction, it is preferred to 1-20cm；The height h of guiding gutter is with to produce the ratio of height of aquaporin be 10-150:100, it is preferably 50-100:100, namely guiding gutter is perpendicular to the ratio of the length of side that the width (height h of guiding gutter) of main body longitudinal direction and cross section are the circular diameter producing aquaporin or cross section is foursquare product aquaporin is 10-150:100, it is preferably 50-100:100, it is preferred to 50-100:100.
Particularly, corresponding to same scheduling aquaporin, be 1-10 along the guiding gutter number that main body longitudinal direction is spaced apart, it is preferred to 2-4.
Outside at film core, by sawing, bore, mill, plane or other known way are along the longitudinal direction being parallel to film core, the position of corresponding same scheduling aquaporin keeps at a certain distance away and offers guiding gutter, guiding gutter is along being perpendicular to the overall trapezoidal or rectangle in the longitudinal cross section of main body, along being perpendicular to the through main body of main body longitudinal direction, when main body is cylinder, namely guiding gutter is perpendicular to the through main body of main body radial direction along tangential through main body, by channel part connection corresponding for same scheduling aquaporin, namely on the position of same scheduling aquaporin, produce aquaporin be spaced with guiding gutter, the product water produced in aquaporin flows out film core by guiding gutter.
Guiding gutter is that the sidewall outside main body is from being perpendicular to the through main body of channel direction producing aquaporin, and the through hole extended along same scheduling aquaporin direction, through hole is rectangle or square along the cross section of main body longitudinal direction, is wherein perpendicular to width (i.e. height h of guiding gutter) is the product aquaporin diameter that cross section is circle being perpendicular to main body longitudinal direction the 50% ~ 150% of main body longitudinal direction or is perpendicular to the 50-150% that cross section is the foursquare product aquaporin length of side 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 part for corresponding same scheduling aquaporin, and the namely corresponding each product aquaporin produced in aquaporin row spatially connects with corresponding guiding gutter, and the product water in product aquaporin can pass through this guiding gutter and flow out body region.
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, it is preferred to 5-10cm.Namely distance film core end face 2-20cm, film core main body outside side wall on offer guiding gutter, guiding gutter be not the end face from main body start fluting, be not provided with guiding gutter in seal area, guiding gutter is 2-20cm to the distance of the end face of main body, it is preferred to 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, start to offer guiding gutter at two end faces >=2-20cm place of distance main body, namely on the outside side wall at the two ends of film core main body, in the scope that longitudinal direction length is 2-20cm of film core, be respectively provided with seal area.
Region between two end faces and each nearest guiding gutter of film core main body is seal area, namely seal area is 2-20cm along the width that main body is longitudinal, it is preferably 5-10cm, say, that two end faces of main body are 2-20cm to the distance between its immediate guiding gutter, it is preferred to 5-10cm.
Wherein, described shell selects the material of metal or non-metallic material to make；Described sealing device selects resistant to elevated temperatures inorganic, organic and metallic sealing material, it is preferable that the inorganic sealing material such as graphite and carbon fiber, it is preferable that fiber, nitrile rubber, polytetrafluoro rubber and other rubber seal, it is preferable that metallic lead, copper and other alloy sealant material.
Particularly, sealing ring is set in outside the seal area at film core main body two ends, the inwall of shell, film core main body outside and the sealing device at film core two ends between space formed 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, it is filtered infiltrating into product aquaporin afterwards, the current of same scheduling aquaporin converge in corresponding guiding gutter, and the current in guiding gutter flow into and produce pool, flow out membrane module then 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 is connected by flange and shell are fixing and seal.
Particularly, bottom end cover, an end face of film core main body and sealing ring form inhalant region；Upper end cover, another end face of film core main body and sealing ring form dense pool.
Particularly, offer the import of backwashing water at the middle part of shell, when cleaning for membrane module, input backwash current.
The condensed water in high temperature purification method of the present invention has the advantage that
1, the multichannel tubular membrane cored structure integrated level adopted in the inventive method is high, pore size filter narrowly distributing, film packed density is high, filtration channel, product aquaporin quantity in unit are 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.
2, in the film core in the present invention, main body is identical with the constituent of sealing coat, through high-temperature process, seamless combination is integrally forming, both thermal coefficient of expansions are identical, the mechanical strength of film core is high, the process of filtration treatment condensed water in high temperature does not result in alternate stress and structural deterioration, is suitable to separation and the refinement treatment of high-temperature material.
3, the film cored structure in the present invention is cellular multi-channel structure, and main body mechanical strength is high, the Stability Analysis of Structures of carrier type film core under the high temperature conditions, mechanical strength is high, and on membrane module, seal point is few, adopts sealing ring sealing means, improve the sealing property of film core, decrease the probability of leakage.
4, the inventive method adopts two-stage cross flow filter mode to process pending condensed water in high temperature, improve anti-water water quality impact capacity, the first order filters the cross flow filter pattern adopting high crossflow velocity, the cross flow filter pattern adopting low crossflow velocity is filtered in the second level, it is effectively prevented from oil pollution and carrys out the impact that film itself is caused by water slug, significantly reducing the water slug impact on producing water water quality.
5, the film core oil resistant class pollution capacity in the inventive method is good, pending water water quality requirement is low, tolerance water water quality impact capacity is strong, the condensation water purification high suitable in temperature processes, the temperature condensing water processed can up to 120 DEG C, and the contact angle of the membrane material of the carrier type film core of the present invention is only 0.4 °, the minima in known various membrane materials.The membrane module of the present invention can be used to process the water of oil content up to 100mg/L, water water quality of producing after adopting the inventive method to process reaches the water standard of boiler feedwater, and condensed water in high temperature being carried out by prior art when membrane filtration processes water water quality requirement is harsh, it is desirable to the oil content of water is both less than 10mg/L.
6, in the membrane filtration processes of the inventive method, transmembrane pressure is little, produces Water transport resistance little, and the flow resistance difference producing water that each filtration channel is formed is little, and respectively uniformly, the product discharge of membrane module is stable for the product discharge of each filtration channel, and membrane filtration efficiency is high.
7, the filtration channel in unit are on the film core of the tubular membrane component used in the inventive method, to produce aquaporin quantity many, film core volume is little, it is simple, easy to make, when being assembled into membrane module, and simple in construction, sealing surface is few, good sealing effect, is beneficial to raising membrane filtration efficiency and the filtration product water resistance difference of different filtration channel is little, and transmembrane pressure is little, improve the work efficiency of membrane module, reduce 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 the dense water yield of outer row is few, saves water resource, decreases environmental pollution.
Accompanying drawing explanation
Fig. 1 conventional ceramic film high-temp. Condensate Water Treatment Process；
Fig. 2 inventive film assembly purified treatment 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 in 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 core；
Figure 10 is the embodiment of the present invention 4 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；52, elevator pump；53, circulating pump；54, former water tank；55, first order membrane module；56, second level membrane module；57, valve is regulated；58, intermediate water tank；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
Below in conjunction with specific embodiment further describe the present invention, advantages of the present invention and feature will be with describe and apparent.But these embodiments are only exemplary, the scope of the present invention is not constituted any restriction.It will be understood by those skilled in the art that and the details of technical solution of the present invention and form can be modified or replace lower without departing from the spirit and scope of the present invention, but these amendments and replacement each fall within protection scope of the present invention.
As shown in figures 3-8, the multichannel tubular membrane component of the present invention by film 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, water current to be filtered is introduced film core and carries out membrance 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；It is opened in the product water export mouth 7 outside close dense water outlet pipe 6 one end of shell 2 to be connected with water pipe, the product water through filtering is derived membrane module.
Film core 1 by membrane filtration supportive body 11 and the filtration channel 12 being in a row uniformly distributed in main body 11, produce aquaporin 13 and by collect produce the partially communicating guiding gutter 14 of aquaporin 13, the filter course 15 that is assembled in filtration channel 12 inwall forms.Filtration channel 12, produce aquaporin 13 be in a row uniformly distributed in main body, often row filtration channel 12, produce aquaporin 13 be parallel to each other, and filtration channel 12 along main body 11 longitudinally through described main body；Inwall at filtration channel 12 passes through the compound mode of sintering, bonding, coating, spraying, heat treatment, crystallization treatment, chemical reaction or several ways, assembling film filter course 15, the current entering filtration channel 12 are carried out membrane filtration process, generates to filter and produce water and dense water；Guiding gutter 14 is provided in the through hole on the sidewall 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 connected, product aquaporin 13 on same row is spaced with guiding gutter 14, what same ranking was put produce aquaporin spatially with the guiding gutter on relevant position to UNICOM, the product water produced in aquaporin 13 converges into guiding gutter.
Film core main body 11 is made up of porous material, main body 11 be perpendicular to that the longitudinal cross section of main body is rounded, oval, rectangle, square, regular polygon or polygon, porous material selects porous polymer materials, porous ceramic film material or sintered metal materials, for instance selective oxidation aluminum, zirconium oxide, titanium oxide, carborundum, rustless 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, it is preferred to 5-20cm；Length is 5-200cm, it is preferred to 20-120cm.
The embodiment of the present invention illustrates with film core main body for 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 suitable in the present invention, for instance Elliptic Cylinder, cuboid, square, positive five limit bodies, hexahedron etc..
Filtration channel 12 along main body 11 longitudinally through described main body, often the opening of two end faces that row's filtration channel is parallel to each other and is positioned at main body 11 is open state, without closing, enters the current in filtration channel 12, through the filtration of filter course 15, it is separated into filtration and produces water and dense water.
Filtration channel 12, produce aquaporin 13 the cross section being perpendicular to main body 11 longitudinal direction is rounded, oval, square, rectangle, regular polygon or other polygon, the embodiment of the present invention illustrates for circular or square.
Cross section is circular filtration channel 12, the diameter producing aquaporin 13 is 0.1 ~ 10 millimeter, it will be preferred that 1 ~ 5 millimeter；Described cross section be foursquare filtration channel 12, produce aquaporin 13 the length of side be 0.1 ~ 10 millimeter, it will be preferred that 1 ~ 5 millimeter.
The filtering material of the membrane filtration layer 15 being assembled in filtration channel 12 inwall is identical with the material that carrier type inorganic carbon membrane film core uses, it is also possible to different.The material that filter course uses includes the inorganic material such as aluminium oxide, zirconium oxide, titanium oxide, carborundum；Or the metal material such as rustless steel and titanium alloy；Or the functional material such as ion exchange resin.
The pore size filter of filter course 15 is 0.001-100 μm, it is preferably 0.01 ~ 20 μm, more preferably 0.01-10 μm, further it is preferably 0.01-3 μm, namely the filtering accuracy of filter course 15 is 0.001-100 μm, it is preferably 0.01 ~ 20 μm, more preferably 0.01-10 μm, is further preferably 0.01-3 μm.
When adopting the carrier type carbon membrane film core that the present invention is made up of the porous material that porosity is high and aperture is big to filter, it is little that product water transmits resistance in membrane carrier, and the filtering accuracy of the film core 1 of the present invention reaches 0.001-100 μm, it is possible to as the membrane treatment process of microfiltration, ultrafiltration, nanofiltration, reverse osmosis, gas separation, gasification infiltration and ion exchange.
Producing the aquaporin 13 longitudinal extension along main body, between adjacent two scheduling aquaporins, interval 1-10 arranges filtration channel, it is preferable that interval 2-4 arranges filtration channel；Opening adhesive 21 encapsulant such as grade producing two end faces that aquaporin 13 is positioned at 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 12 is arranged at interval 3.
The film core main body 11 of the present invention and filtration channel thereon 12, product aquaporin 13 are generally by extrusion molding mode molding, it is also possible to by other known method molding such as injection moulding or casting.Preferred extruding forming method makes cellular tubular membrane core.Filtration channel 12 in the present invention, produce aquaporin 13 be perpendicular to main body 11 be longitudinally the shape in cross section, size dimension can be identical, can also be different, but the resolution for the ease of two kinds of passages, usual filtration channel is positioned at the cross sectional shape of film two end faces of core main body and differs with producing aquaporin cross sectional shape, and produce the sectional dimension sectional dimension more than filtration channel 12 of aquaporin 13, be conducive to the resolution to two kinds of passages, too increase product aquaporin space, reduce the flow resistance producing water, improve filter efficiency.
Such as Fig. 3, 4, 6, shown in 7, outside in film core main body 11, two end face 2-20cm of distance film core main body 11, it is preferably 5-10cm place, by sawing, 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 corresponding same scheduling aquaporin 13, through main body, form guiding gutter 14, guiding gutter 14 is perpendicular to that the cross section of main body 11 longitudinal direction is trapezoidal or rectangle, guiding gutter 14 is through to opposite side from the side of main body, the corresponding part of same row is produced aquaporin connection, namely in the relevant position producing aquaporin of same row by sawing, bore, mill, part relevant position is produced aquaporin connection by plane or other known way from the outside of main body 11, and through main body 11, form through hole.The end face of guiding gutter 14 and film core main body 11 is mutually perpendicular to, and the product water produced in aquaporin flows out film core by guiding gutter.
Guiding gutter 14 is to the seal area that exterior lateral area is film core 6 of two end faces 16 of film core main body 11, namely it is the seal area of 2-20cm being respectively arranged at two ends with along main body longitudinal direction length of film core main body 11, 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 distance more than 2-20cm of the distance of two end faces of distance film core main body 11 respectively along the longitudinal direction of main body, guiding gutter is 2-20cm to the distance of the end face 16 of main body, it is preferred to 5-10cm.
Two end faces of film core main body and the region between each nearest guiding gutter are seal area, namely seal area is 2-20cm along the width that main body is longitudinal, it is preferably 5-10cm, that is two end faces of main body are 2-20cm to the length between its immediate guiding gutter, it is preferred to 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 of main body 11 longitudinal direction, it is preferred to 1-20cm；The height h of guiding gutter is with to produce the ratio of height of aquaporin be 10-150:100, it is preferably 50-100:100, namely guiding gutter 14 is perpendicular to the height h of main body longitudinal direction and the ratio producing aquaporin along the height being perpendicular to main body longitudinal direction is 10-150:100, it is preferred to 50-100:100；And the number being in the described guiding gutter that same ranking is put is 1-10, it is preferred to 2-4.
As shown in Figure 8, in the membrane module of the present invention, sealing ring 8 is arranged in the seal area 6 outside film core main body 11 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, it is ensured that sealing effectiveness.
The outside being set in film core main body 11 seal area 17 installed by sealing ring 8.The inner side of shell 2, film core main body 11 outside and the sealing ring 8 at film core two ends between space formed produce 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 connected by flange 10 is fixing and seals, and bottom end cover 4, the end face 16 of 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 and film core 1 and shell 2 are connected by flange 10 is fixing and seals, and upper end cover 3, the other end 16 of film core main body 11 and sealing ring 8 form dense pool 61.
The current flowed into from water inlet pipe 5 enter film core by filtration channel 12, it is filtered infiltrating into product aquaporin 13 afterwards, the current producing aquaporin converge into and produce aquaporin in the guiding gutter 14 of the relevant position of same row, current in guiding gutter flow into after producing pool 9, flow out membrane module then through being positioned at the shell 2 product water export mouth 7 near the outside of dense water outlet pipe 6 one end.
In order to facilitate the cleaning of membrane module, offer backwashing water import 22 at the middle part of shell 2, for inputting water for cleaning in membrane module, membrane module is carried out backwash, be beneficial to the Reusability of membrane module, extend the service life of membrane module.
The present invention carries out after the condensed water in high temperature of membrane filtration flows into inhalant region 51 from the water inlet pipe 5 being positioned at membrane module bottom after bottom end cover 4, owing to producing the closure of openings that aquaporin 13 is positioned at two end faces of main body 11, 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 product 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 producing 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 outlet 6, reach the effect purified water.
The embodiment of the present invention adopts the condensed water in high temperature that high-temperature steam is transformed into by multichannel tubular membrane component to carry out the fine membrane filtration of two-stage and processes, 2 multichannel tubular membrane components (first order membrane module 55, second level membrane module 56) are sequentially passed through by condensed water in high temperature, carry out fine film process, processing in the present invention and the condensed water in high temperature that temperature is 100 DEG C is carried out purified treatment, the condensed water in high temperature that other temperature are 50-120 DEG C is also applied for adopting the inventive method to carry out purified treatment.
The work process of inventive film assembly: condensed water in high temperature current to be filtered enter former water tank 54, when being 50-120 DEG C when keeping temperature, condensed water in high temperature pumps into first order membrane filtration module from former water tank 54 through inlet water lifting pumps 52, the cross flow filter mode adopting high crossflow velocity in first order membrane filtration module is filtered purified treatment, circular flow is adjusted by controlling circulating pump 53, thus regulating the crossflow velocity when first order filters is 0 ~ 5m/s, and transmembrane pressure is 0.01 ~ 0.5MPa.After the first order filters, 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 filters is directly entered 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, controlling the crossflow velocity when second level is filtered 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 the second level is filtered enters and produces Water circulation system.
After single filter processes, produce water conservancy himself pressure (pressure head) be directly entered second level filtration, it is not necessary to separately set second level inlet water lifting pumps.
Embodiment 1
Offering 1480 cross sections in the present embodiment in the main body 11 of film core 1 altogether to be foursquare filtration channel 12 and produce aquaporin 13, filtration channel 12, the length of side producing aquaporin 13 are 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, between adjacent two scheduling aquaporins 13, filtration channel 12 is arranged at interval 3, in the outside of cylindric film core main body 1 corresponding to producing the corresponding position of aquaporin 13, by sawing outside the scope that distance is 15cm of two end faces 16 from film core main body 1, 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, it is 20cm that the length of each guiding gutter 14 is put in same ranking, spacing between guiding gutter is 20cm, the height h of guiding gutter is 3mm, namely each guiding gutter is 20cm along the length of the longitudinal direction of cylinder body；It is 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 and the diameter ratio producing aquaporin are 100:100.
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 μm, 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 μm.Being loaded by film core 1 in the cylindrical metal shell 2 of hollow, sealing ring 8 is arranged in the region, seal area 17 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 5 of membrane module is connected with pretreated current, by the water inlet pipe producing water export mouth 7 and second level membrane filtration module of first order membrane filtration module to being connected, as shown in Figure 8.
When being 100 DEG C keeping temperature, condensed water in high temperature (100 DEG C) is flowed into first order film core by water inlet pipe 5, first order membrane filtration process is carried out with cross-current flow, wherein, the intake pressure controlling the process of first order membrane filtration is 0.45MPa, regulating the dense water circular 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 0.30MPa；Regulating the concentrated water drainage of first order membrane filtration process high-volume so that the water yield that first order membrane filtration processes is 98%, the pressure producing water that first order membrane filtration processes is 0.22MPa, and transmembrane pressure is 0.155MPa simultaneously.
Product water after first order membrane filtration is from producing entrance second level membrane module after 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 0.22MPa, the dense water rate control of cross-flow is at the 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 producing water that second level membrane filtration processes is 0.1MPa, and transmembrane pressure is 0.1MPa.Product water after the membrane filtration process of the second level flows out second level membrane carrier from producing water export mouth, and the water quality monitoring result producing water is as shown in table 1.
The oil content in current is measured according to GB " mensuration of boiler feed water and cooling water analysis method oil " (GB/T12153-1989)；The iron content in current is measured according to GB " mensuration of boiler feed water and cooling water analysis method ferrum " (GB/T14427-1993)；Electrical conductivity of water is measured according to GB " mensuration of boiler feed water and cooling water analysis method electrical conductivity " (GB/T6908-1986).
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/cm | 51 | 9.2 |
| COD,mg/L | 45.0 | 4.0 |
| Ferrum, 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, first order membrane filtration process is carried out with cross-current flow, wherein, the intake pressure processed except controlling first order membrane filtration is 0.4MPa, regulate the dense water circular flow 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；Regulating the concentrated water drainage of first order membrane filtration process high-volume so that the water yield that first order membrane filtration processes is 97.5%, the pressure producing water that first order membrane filtration processes is 0.18MPa, and transmembrane pressure is outside 0.195MPa, and all the other are identical with embodiment 1 simultaneously；
Product water after first order membrane filtration is from producing entrance second level membrane module after 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 0.18MPa, regulate the dense water yield is second level membrane filtration inflow the 5% of second level membrane filtration, 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 producing water that second level membrane filtration processes is 0.06MPa, transmembrane pressure is outside 0.11MPa, 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 producing water export mouth, the water quality monitoring result 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 |
| Ferrum, μ g/L | 179 | 13.0 |
Embodiment 3
Except the influent quality that condensed water in high temperature current water quality and first order membrane filtration process；Intake pressure 0.41MPa, the dense water pressure 0.34MPa that the first order filters, produces water pressure 0.17MPa, and transmembrane pressure is 0.205MPa；Intake pressure 0.17MPa, the dense water pressure 0.15MPa that the second level is filtered, 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 the product water water quality after secondary membrane processes are as shown in table 3.
Table 3 embodiment 3 Analysis Results of Water Quality
| Project | Water inlet | Produce water 12--> |
| 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 |
| Ferrum, μ g/L | 201 | 17.0 |
Embodiment 4
Offering filtration channel 12 that 1010 cross sections are circular in the present embodiment in the main body 11 of film core altogether and produce aquaporin 13, filtration channel 12, the diameter producing aquaporin 13 are 3mm, such as Fig. 9, shown in 10.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, in the outside of cylindric film core main body 1 corresponding to producing the corresponding position of aquaporin 13, by sawing outside the scope that distance is 15cm of two end faces 16 from film core main body 1, 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, it is 20cm that the length of each guiding gutter 14 is put in same ranking, spacing between guiding gutter is 20cm, the height h of guiding gutter is 3mm, namely each guiding gutter is 20cm along the length of the longitudinal direction of cylinder body；It is 20cm along the spacing between adjacent two guiding gutters of main body longitudinal direction；Height h along the radial direction of cylindrical body 11 is 3mm, and the height of guiding gutter and the diameter ratio producing aquaporin are 100:100.
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 μm, 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 μm.Being loaded by film core 1 in the metal shell 2 of hollow, sealing ring 8 is arranged in the region, seal area 17 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 5 of membrane module is connected with pretreated current.
The condensed water in high temperature that temperature is 100 DEG C flows into first order membrane module by water inlet pipe 5, first order membrane filtration process is carried out with cross-current flow, wherein, the intake pressure processed except controlling first order membrane filtration is 0.42MPa, regulate the dense water circular flow 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；Regulating the concentrated water drainage of first order membrane filtration process high-volume so that the water yield that first order membrane filtration processes is 98%, the pressure producing water that first order membrane filtration processes is 0.19MPa, and transmembrane pressure is outside 0.175MPa, and all the other are identical with embodiment 1 simultaneously；
Product water after first order membrane filtration is from producing entrance second level membrane module after 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 0.19MPa, the dense water rate control of cross-flow is at the 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 producing water that second level membrane filtration processes is 0.065MPa, outside transmembrane pressure 0.115MPa, 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 producing water export mouth, the water quality monitoring result 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 13 --> |
| Oil content, mg/L | 13.0 | 0.2 |
| Electrical conductivity, μ S/cm | 63.0 | 8.4 |
| COD,mg/L | 45.0 | 4.0 |
| Ferrum, μ g/L | 150 | 13.0 |
Embodiment 5
Except the influent quality that condensed water in high temperature current water quality and first order membrane filtration process；The first order filtered water inlet pressure 0.44MPa, dense water pressure 0.32MPa, produce water pressure 0.2MPa, transmembrane pressure 0.185MPa；The second level filtered water inlet pressure 0.2MPa, dense water pressure 0.18MPa, produce 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 the product water water quality after secondary membrane processes are as shown in table 5.
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 |
| Ferrum, μ g/L | 190 | 14.5 |
Claims (9)
1. condensing a water purification method, it is characterized in that adopting carrier type membrane module that condensed water in high temperature carries out at least one-level membrane filtration processes, wherein, described carrier type membrane module includes:
Film core (1)；
Shell (2), the cylindric or straightedge cylinder of hollow, it is set in the periphery of film core；
Upper and lower end cap (3,4), is respectively arranged at 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 membrane module；
Wherein, film core (1) including:
Main body (11), membrane filtration supporter；
Filtration channel (12), described filtration channel is in a row distributed in main body, and along main body longitudinally through described main body, often row filtration channel be parallel to each other；
Produce aquaporin (13), in a row being distributed in main body, along the longitudinal extension of main body, between adjacent two scheduling aquaporins, interval 1-10 arranges filtration channel, and produce the closure of openings that aquaporin is positioned at two end faces of main body, produce aquaporin and be parallel to each other with described filtration channel；
Guiding gutter (14), is opened in main body wall, the through hole of through main body, is being spaced with same scheduling aquaporin, collects the product water produced in aquaporin along the longitudinal direction of main body.
2. purification method as claimed in claim 1, is characterized in that the temperature of described condensed water in high temperature is 50-120 DEG C.
3. purification method as claimed in claim 1 or 2, is characterized in that the filtering accuracy of the carrier type membrane module in described membrane filtration processing procedure is 0.001-100 μm.
4. purification method as claimed in claim 1 or 2, is characterized in that adopting cross-current flow to carry out described membrane filtration 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 or 2, is characterized in that described main body (11) is transversely to the machine direction that the cross section in direction is rounded, oval, rectangle, square.
7. purification method as claimed in claim 1 or 2, it is characterized in that described main body (11) is transversely to the machine direction the cross section in direction is regular polygon.
8. purification method as claimed in claim 1 or 2, the cross section being transversely to the machine direction direction it is characterized in that described filtration channel (12), producing aquaporin (13) is rounded, oval, rectangle, regular polygon or other polygon.
9. purification method as claimed in claim 1 or 2, is characterized in that the inwall of described filtration channel (12) is also assembled with filter course (15).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201210341530.3A CN103657413B (en) | 2012-09-14 | 2012-09-14 | A kind of purification method of condensed water in high temperature |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201210341530.3A CN103657413B (en) | 2012-09-14 | 2012-09-14 | A kind of purification method of condensed water in high temperature |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN103657413A CN103657413A (en) | 2014-03-26 |
| CN103657413B true CN103657413B (en) | 2016-07-06 |
Family
ID=50296907
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201210341530.3A Active CN103657413B (en) | 2012-09-14 | 2012-09-14 | A kind of purification method of condensed water in high temperature |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN103657413B (en) |
Families Citing this family (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105923804B (en) * | 2016-05-23 | 2019-02-01 | 浙江中凯瑞普环境工程股份有限公司 | A kind of condensed water in high temperature oil removing process |
| 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 |
| 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 |
| 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 |
| 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 |
| 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 |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN2461650Y (en) * | 2000-10-27 | 2001-11-28 | 杨德武 | Inorganic composite film separator for molecular class separtion |
| CN101088922A (en) * | 2007-07-05 | 2007-12-19 | 南京九思高科技有限公司 | Membrane separating process for purifying high temperature condensated water |
| CN101092258A (en) * | 2007-07-05 | 2007-12-26 | 南京九思高科技有限公司 | Method for processing high temperature condensed water by integration technique of membrane |
Family Cites Families (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2000218110A (en) * | 1999-01-28 | 2000-08-08 | Japan Organo Co Ltd | Operation of condensed water filter apparatus in power plant |
-
2012
- 2012-09-14 CN CN201210341530.3A patent/CN103657413B/en active Active
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN2461650Y (en) * | 2000-10-27 | 2001-11-28 | 杨德武 | Inorganic composite film separator for molecular class separtion |
| CN101088922A (en) * | 2007-07-05 | 2007-12-19 | 南京九思高科技有限公司 | Membrane separating process for purifying high temperature condensated water |
| CN101092258A (en) * | 2007-07-05 | 2007-12-26 | 南京九思高科技有限公司 | Method for processing high temperature condensed water by integration technique of membrane |
Also Published As
| Publication number | Publication date |
|---|---|
| CN103657413A (en) | 2014-03-26 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN103657413B (en) | A kind of purification method of condensed water in high temperature | |
| CN103663624B (en) | A kind of process for purification of oil field reinjection water | |
| CN105271622B (en) | A kind of electroplating wastewater zero handling process and system | |
| CN103933860B (en) | A kind of preparation system of urea for vehicle | |
| KR101513250B1 (en) | Central baffle, pressurized hollow fiber membrane module having the same and cleaning method thereof | |
| WO2012026373A1 (en) | Hollow fiber type reverse osmosis membrane and process for production thereof | |
| CN101935118A (en) | Process for purifying and recycling hot water by membrane method | |
| CN105000755A (en) | Wastewater zero-emission industrial sewage treatment system and treatment method | |
| CN103055701B (en) | Cleanable security filter and its application | |
| CN205933453U (en) | High recovery pit water recycling system | |
| CN108467140A (en) | A kind of coking wastewater combination desalinating process | |
| WO2012056668A1 (en) | Reverse osmosis membrane structure for water treatment and reverse osmosis membrane module | |
| CN108178360A (en) | A kind of waste emulsified mixture purifying processing device of waste emulsified mixture purifying treatment method and adopting said method | |
| CN203498181U (en) | System for recycling waste acid and waste alkali | |
| CN203955038U (en) | A kind of preparation system of automobile-used urea | |
| CN103657422B (en) | A kind of film core and consisting of membrane module | |
| CN201942583U (en) | Ceramic membrane filter device with oil partition tank | |
| CN104828929A (en) | An anti-pollution multifunctional ceramic flat sheet membrane | |
| CN105923804B (en) | A kind of condensed water in high temperature oil removing process | |
| CN209564851U (en) | A kind of graphene concentrated separation system | |
| CN204529559U (en) | The reverse osmosis concentrated water system of a kind of photocatalysis oxidation technique associating iron-carbon micro-electrolysis process | |
| CN103787539B (en) | A kind of method of membrane separation nitro-chlorobenzene hot wastewater | |
| CN106517604A (en) | Electromembrane coupling type dyeing waste water deep treatment and component recycling method | |
| CN206266336U (en) | A kind of oil-containing condensate-scavenging installation | |
| CN206935136U (en) | A kind of external-compression type tubular membrane component for wastewater treatment |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| PE01 | Entry into force of the registration of the contract for pledge of patent right | ||
| PE01 | Entry into force of the registration of the contract for pledge of patent right |
Denomination of invention: A purification method of high temperature condensate Effective date of registration: 20211015 Granted publication date: 20160706 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 |
|
| PC01 | Cancellation of the registration of the contract for pledge of patent right | ||
| PC01 | Cancellation of the registration of the contract for pledge of patent right |
Date of cancellation: 20230321 Granted publication date: 20160706 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 |