CN102329019B - Ultralow-pressure membrane separation device for desalinating bitter and salty water - Google Patents
Ultralow-pressure membrane separation device for desalinating bitter and salty water Download PDFInfo
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- CN102329019B CN102329019B CN201110264658XA CN201110264658A CN102329019B CN 102329019 B CN102329019 B CN 102329019B CN 201110264658X A CN201110264658X A CN 201110264658XA CN 201110264658 A CN201110264658 A CN 201110264658A CN 102329019 B CN102329019 B CN 102329019B
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- 239000012528 membrane Substances 0.000 title claims abstract description 119
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 title claims abstract description 57
- 238000000926 separation method Methods 0.000 title claims abstract description 23
- 238000000108 ultra-filtration Methods 0.000 claims abstract description 69
- 238000001728 nano-filtration Methods 0.000 claims abstract description 64
- 238000001223 reverse osmosis Methods 0.000 claims abstract description 62
- 238000000502 dialysis Methods 0.000 claims description 21
- 238000010612 desalination reaction Methods 0.000 claims description 19
- 239000007788 liquid Substances 0.000 claims description 11
- 230000001737 promoting effect Effects 0.000 claims description 6
- 238000011010 flushing procedure Methods 0.000 claims description 5
- 230000008676 import Effects 0.000 claims description 3
- 239000013505 freshwater Substances 0.000 abstract description 6
- 238000011034 membrane dialysis Methods 0.000 abstract description 4
- 238000001914 filtration Methods 0.000 abstract description 3
- 238000011001 backwashing Methods 0.000 abstract 2
- 230000000694 effects Effects 0.000 abstract 1
- 238000004064 recycling Methods 0.000 abstract 1
- 238000000034 method Methods 0.000 description 17
- 239000000243 solution Substances 0.000 description 14
- 230000003204 osmotic effect Effects 0.000 description 6
- 238000005265 energy consumption Methods 0.000 description 5
- 239000000463 material Substances 0.000 description 5
- 238000004519 manufacturing process Methods 0.000 description 4
- 238000011033 desalting Methods 0.000 description 3
- 238000005516 engineering process Methods 0.000 description 3
- JEGUKCSWCFPDGT-UHFFFAOYSA-N h2o hydrate Chemical compound O.O JEGUKCSWCFPDGT-UHFFFAOYSA-N 0.000 description 3
- 238000012545 processing Methods 0.000 description 3
- 238000011084 recovery Methods 0.000 description 3
- 150000003839 salts Chemical class 0.000 description 3
- 230000003750 conditioning effect Effects 0.000 description 2
- 230000007797 corrosion Effects 0.000 description 2
- 238000005260 corrosion Methods 0.000 description 2
- 239000000385 dialysis solution Substances 0.000 description 2
- 230000004907 flux Effects 0.000 description 2
- 238000005374 membrane filtration Methods 0.000 description 2
- 235000019600 saltiness Nutrition 0.000 description 2
- PXGOKWXKJXAPGV-UHFFFAOYSA-N Fluorine Chemical compound FF PXGOKWXKJXAPGV-UHFFFAOYSA-N 0.000 description 1
- FAPWRFPIFSIZLT-UHFFFAOYSA-M Sodium chloride Chemical compound [Na+].[Cl-] FAPWRFPIFSIZLT-UHFFFAOYSA-M 0.000 description 1
- 238000013459 approach Methods 0.000 description 1
- 229910052785 arsenic Inorganic materials 0.000 description 1
- RQNWIZPPADIBDY-UHFFFAOYSA-N arsenic atom Chemical compound [As] RQNWIZPPADIBDY-UHFFFAOYSA-N 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 239000012267 brine Substances 0.000 description 1
- 239000000356 contaminant Substances 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 238000011161 development Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000004821 distillation Methods 0.000 description 1
- 239000002384 drinking water standard Substances 0.000 description 1
- 239000003814 drug Substances 0.000 description 1
- 229920006351 engineering plastic Polymers 0.000 description 1
- 239000011737 fluorine Substances 0.000 description 1
- 229910052731 fluorine Inorganic materials 0.000 description 1
- 231100001261 hazardous Toxicity 0.000 description 1
- 230000036571 hydration Effects 0.000 description 1
- 238000006703 hydration reaction Methods 0.000 description 1
- 229910052500 inorganic mineral Inorganic materials 0.000 description 1
- 239000011707 mineral Substances 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 239000005416 organic matter Substances 0.000 description 1
- 229920003023 plastic Polymers 0.000 description 1
- 239000004033 plastic Substances 0.000 description 1
- 231100000614 poison Toxicity 0.000 description 1
- 230000007096 poisonous effect Effects 0.000 description 1
- 238000005381 potential energy Methods 0.000 description 1
- 238000002203 pretreatment Methods 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 238000011160 research Methods 0.000 description 1
- 230000035945 sensitivity Effects 0.000 description 1
- 239000011780 sodium chloride Substances 0.000 description 1
- HPALAKNZSZLMCH-UHFFFAOYSA-M sodium;chloride;hydrate Chemical compound O.[Na+].[Cl-] HPALAKNZSZLMCH-UHFFFAOYSA-M 0.000 description 1
- 239000010935 stainless steel Substances 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
- Y02A20/00—Water conservation; Efficient water supply; Efficient water use
- Y02A20/124—Water desalination
- Y02A20/131—Reverse-osmosis
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- Separation Using Semi-Permeable Membranes (AREA)
Abstract
The invention discloses an ultralow-pressure membrane separation device for desalinating bitter and salty water. The ultralow-pressure membrane separation device comprises a precise filter, an ultrafiltration membrane system, an ultrafiltration membrane dialysis tank, a nanofiltration (or low-removal-rate reverse osmosis) membrane system, a nanofiltration (or low-removal-rate reverse osmosis) membrane dialysis tank, a reverse osmosis membrane system, a pump and pipelines for connecting various parts; after raw water (the bitter and salty water) is filtered through the precise filter and then introduced to an ultrafiltration membrane for filtration, after the filtration of the ultrafiltration of the ultrafiltration, ultrafiltration dialyzate is introduced into a first-stage nanofiltration (or low-removal-rate reverse osmosis) membrane for treatment, a first-stage concentrated solution is discharged outwards or is used for a backwashing ultrafiltration membrane, or is processed by an energy recycling device so as to increase the pressure for the ultrafiltration dialyzate to undergo first-stage nanofiltration (or reverse osmosis), and water produced from the first-stage nanofiltration membrane is then introduced into a second-stage reverse osmosis membrane system; and second-stage dialyzate is qualified fresh water, and a second-stage concentrated solution is applied to the backwashing ultrafiltration membrane or is discharged outwards or recycled. The ultralow-pressure membrane separation device has the advantages of extremely low equipment operation pressure, good effect on desalinating the bitter and salty water, low equipment operation cost and the like.
Description
Technical field
The present invention discloses a kind of ultra-low-pressure brackish water desalination membrane separation device, by International Patent Classification (IPC) (IPC), divides and belongs to brackish water desalination film device manufacturing technology field, especially relates to a kind of film separating system of the ultralow pressure for brackish water desalination.
Background technology
Obtaining of Freshwater resources is a great environment and the problem of surviving that people face, and various countries take much count of the technical research of this respect and input.The desalination techniques of brackish water is an important channel that obtains Freshwater resources, and particularly China's Freshwater resources lack, but the brackish water resource distribution is very wide, so technique of desalinating saline water becomes China and obtains very real approach highly significant of water resources.The method of brackish water desalination at present is a lot, mainly membrane separation process, distillation method, cold method, sun power method, electroosmose process, chemical desalting method etc., wherein the membrane separation process desalting is effective, water conditioning and be much higher than drinking water standard, simple to operate, level of automation is high, and therefore development is very fast.
Current membrane separation process equipment, because the brackish water saltiness of processing is high, so equipment must under high pressure move to overcome the high osmotic pressure of brackish water, the necessary resistance to corrosion of parts that simultaneously contacts brackish water is strong, this has just proposed higher requirement to the material of equipment, and the pipeline, pump etc. that particularly contact brackish water need corrosion-resistant, high pressure resistant, cause equipment making raw material material to require high, device fabrication requires high, and manufacturing cost is high.The technical process of existing membrane separation process desalination brackish water is long, too complicated in addition, needs to consume various medicaments simultaneously, the desalination core process is only used one reverse osmosis or nanofiltration membrane, can not tackle the water quality of variation, produce the water variation water quality larger, must use special, membrane element stable performance.
China document CN 201284253 discloses a kind of nano filter membrane bitter brine desalting system apparatus, workflow is as follows: brackish water → water tank → water pump → cartridge filter → ultrafiltration module → water tank → water pump → one-level nanofiltration membrane demineralizer → water tank → water pump secondary nanofiltration membrane demineralizer → water tank → fresh water, yet, said apparatus repeated application nanofiltration membrane is filtered, and the nanofiltration membrane molecular weight cut-off is bigger than normal, can only partly remove in brackish water the poisonous and hazardous mineral ion of human body (as fluorine, arsenic etc.) and low-molecular-weight organic matter, it is qualified that product water water quality is difficult for, and the high-recovery of declaring in this invention is impossible realize.
Summary of the invention
For the deficiencies in the prior art, the invention provides a kind of desalination effective, the ultra-low-pressure brackish water desalination membrane separation device of water conditioning, this membrane separation plant adopts two step desalinating process, thereby reduces the osmotic pressure of every step membrane filtration, flow process is succinct, the equipment operating pressure is extremely low, and equipment is used material general, and apparatus processing requires low, membrane element requires low, good separation.
For achieving the above object, the present invention is achieved by the following technical solutions:
A kind of ultra-low-pressure brackish water desalination membrane separation device, comprise accurate filter, ultrafiltration membrane system, ultra-filtration membrane dialysate tank, nanofiltration (or low rejection reverse osmosis) film system, nanofiltration (or low rejection reverse osmosis) film dialysate tank, reverse osmosis membrane system, pump and connect the pipeline of each several part; Described accurate filter is connected with the brackish water transferpump, accurate filter is connected with ultrafiltration membrane system by recycle pump, the ultrafiltration membrane system dialyzate is connected to the ultrafiltration dialysis tank, ultrafiltration dialysis liquid is connected with nanofiltration (or low rejection reverse osmosis) film system by topping-up pump, the dialyzate of nanofiltration (or low rejection reverse osmosis) film system is connected to nanofiltration (or low rejection reverse osmosis membrane) dialysate tank, and nanofiltration (or low rejection reverse osmosis) film dialysate tank is connected with reverse osmosis membrane system by topping-up pump again.
Further, the concentrated solution outlet of described nanofiltration (or low rejection reverse osmosis) film system connects an energy recycle device for promoting the pressure of a part of ultrafiltration membrane system dialyzate, and the ultrafiltration dialysis liquid after the acquisition supercharging enters the import of nanofiltration (or low rejection reverse osmosis) film system by pipeline.
The concentrated solution of further, described nanofiltration (or low rejection reverse osmosis) film system is directly discharged or is turned back to ultrafiltration membrane system and carries out back flushing.
Further, the concentrated solution of described reverse osmosis membrane system can be connected in the dialysis side of ultra-filtration membrane separation system for recoiling or returning to nanofiltration or the reuse of low rejection reverse osmosis membrane system by pipeline by pipeline.
Further, it is 0.002-0.05um or molecular weight cut-off 2000D-500KD that the film of described ultra-filtration membrane separation system is held back aperture, first step nanofiltration (or low rejection reverse osmosis) film to the ensemble average rejection of brackish water salinity between 40-95%, the ensemble average rejection of second stage reverse osmosis membrane system to the brackish water salinity > 90%.
In the present invention, former water (brackish water) is after accurate filter filters, enter again ultrafiltration membrance filter, after ultrafiltration membrance filter, ultrafiltration dialysis liquid enters low rejection nanofiltration (or the low rejection reverse osmosis) film of the first step and is processed, the concentrated solution of the first step or efflux or for the ultra-filtration membrane that recoils, or be used for promoting the pressure that ultrafiltration dialysis liquid enters first step reverse osmosis through energy recycle device, the product water of the nanofiltration of the first step (or low rejection reverse osmosis) film enters second stage reverse osmosis membrane system again; The dialyzate of the second stage is qualified fresh water, the concentrated solution of the second stage or for recoiling ultra-filtration membrane or efflux or reuse.
The present invention has following beneficial effect:
A. the characteristics of utilizing ultra-filtration membrane not hold back, membrane contaminant is held back soluble salt, can realize that the pre-treatment of brackish water under utmost point less energy-consumption purifies, and simplified pretreatment technology, for the continual and steady operation of the film system of back lays the foundation;
B. the brackish water after super-filtration purifying is only containing soluble salt, and under the prerequisite of controlling the rate of recovery, the film surface circular flow in nanofiltration and reverse osmosis membrane system can be very low, and relevant with the rate of recovery, this just greatly reduces energy consumption;
C. the characteristics of utilizing nanofiltration (or low rejection reverse osmosis) film to hold back the salt portions, can share the osmotic pressure of part, reduces the burden of back reverse osmosis system, and simultaneity factor self-operating pressure also so significantly reduces.In the occasion of energy consumption sensitivity, the potential energy available energy retrieving arrangement of concentrated solution is reclaimed, and enters pressure and the flow velocity of nanofiltration (or low rejection reverse osmosis) film for promoting ultrafiltration dialysis liquid; Also can the intermittent back flushing for ultrafiltration system, maintain the ultrafiltration system flux stabilized;
D. through the brackish water of nanofiltration (or low rejection reverse osmosis) after film has been removed the major part salinity, osmotic pressure significantly reduces, and saltiness reduces, can use the reverse osmosis of common specification to carry out desalination work, can under extremely low working pressure, just can realize desalination desalination, the purpose of producing the hydration lattice.The concentrated solution of reverse osmosis can efflux takes away salinity, also can be used for the back flushing of ultrafiltration system, maintains the ultrafiltration system flux stabilized;
E. utilize the two-stage film except sharing osmotic pressure, reduce outside system energy consumption, can form the double shield that produces water water quality, the trickle fluctuation of the rejection of twin-stage film can be inresponsive as the single stage membrane system yet, and wherein the slight variations of the rejection of one film can not cause very large fluctuation to producing water water quality;
F. the most important thing is to use the method for dividing potential drop membrane sepn, desalination film system running pressure is extremely low, and most of pipe fitting can use cheap engineering plastics to substitute the high corrosion-resistant steel of price and make pressure line and parts, easy to process, low cost of manufacture.
The accompanying drawing explanation
Fig. 1 is structural representation of the present invention.
Fig. 2 is energy content retrieving arrangement schematic diagram.
Parts in figure: 1. dehvery pump, 2. accurate filter, 3. recycle pump, 4. ultrafiltration membrane system, 5. ultrafiltration dialysis flow container, 6. topping-up pump, 7. nanofiltration (low rejection reverse osmosis) film system, 8. nanofiltration or low rejection reverse osmosis membrane dialysate tank, 9. topping-up pump, 10. reverse osmosis membrane system.
Parts in Fig. 2: 1. dehvery pump, 2. accurate filter, 3. recycle pump, 4. ultrafiltration membrane system, 5. ultrafiltration dialysis flow container, 6. topping-up pump, 7. nanofiltration (or low rejection reverse osmosis) film system, 8. nanofiltration or low rejection reverse osmosis membrane dialysate tank, 9. topping-up pump, 10. reverse osmosis membrane system, 11. energy recycle devices.
Embodiment
Below in conjunction with accompanying drawing, the invention will be further described:
Embodiment: refer to Fig. 1, a kind of ultra-low-pressure brackish water desalination membrane separation device, comprise accurate filter 2, ultrafiltration membrane system 3, ultra-filtration membrane dialysate tank 5, nanofiltration membrane system 7, nanofiltration membrane dialysate tank 8, reverse osmosis membrane system 10, pump and connect the pipeline of each several part; Described accurate filter 2 is connected with brackish water transferpump 1, accurate filter 2 is connected with ultrafiltration membrane system 4 by recycle pump 3, ultrafiltration membrane system 4 dialyzates are connected to ultrafiltration dialysis tank 5, ultrafiltration dialysis liquid is connected with nanofiltration membrane system 7 by topping-up pump 6, the dialyzate of nanofiltration membrane system is connected to nanofiltration dialysate tank 8, and nanofiltration dialysate tank 8 is connected with reverse osmosis membrane system 10 by topping-up pump 9 again.
In the present invention, the concentrated solution outlet of nanofiltration membrane system 7 can connect an energy recycle device 11(referring to Fig. 2) for promoting the pressure of a part of ultrafiltration membrane system 4 dialyzates, the ultrafiltration dialysis liquid obtained after supercharging enters the import of nanofiltration membrane system by pipeline, also recovered energy not.The concentrated solution of described nanofiltration membrane system is directly discharged or is turned back to ultrafiltration membrane system and carries out back flushing, as Fig. 1.
As Fig. 1, the concentrated solution of reverse osmosis membrane system 10 can be connected in the dialysis side of ultra-filtration membrane separation system 4 for recoiling or returning to the reuse of nanofiltration membrane system by pipeline by pipeline.It is 0.002-0.05um or molecular weight cut-off 2000D-500KD that the film of described ultra-filtration membrane separation system 4 is held back aperture, first step nanofiltration membrane to the ensemble average rejection of brackish water salinity between 40-95%, the ensemble average rejection of second stage reverse osmosis membrane system to the brackish water salinity > 90%.
The present invention puts the each several part explanation:
A. the pipeline that system of the present invention has comprised accurate filter, ultrafiltration membrane separating device, ultra-filtration membrane dialysate tank, nanofiltration (or low rejection reverse osmosis) film system, nanofiltration (or low rejection reverse osmosis) film dialysate tank, reverse osmosis membrane system, reverse osmosis membrane dialysate tank, pump, energy recycle device and connection each several part;
B. the brackish water transferpump connects accurate filter; Accurate filter is connected with ultrafiltration membrane system by pump, and the ultrafiltration membrane system dialyzate is connected to the ultrafiltration dialysis tank; Ultrafiltration dialysis liquid is connected with nanofiltration (or low rejection reverse osmosis) film system by pump, and the dialysis tubing of nanofiltration (or low rejection reverse osmosis) film system is connected to nanofiltration (or low rejection reverse osmosis) film dialysate tank; Nanofiltration (or low rejection reverse osmosis) dialysate tank is connected with reverse osmosis system by pump again;
The concentrated solution of C. nanofiltration (or low rejection reverse osmosis) film system can connect energy recycle device according to the requirement of energy consumption, for promoting the pressure of a part of ultrafiltration dialysis liquid, the ultrafiltrated after the acquisition supercharging enters nanofiltration (or low rejection reverse osmosis) film system by pipeline.If concentrated solution not recovered energy can be connected in ultra-filtration membrane dialysis side for recoil or discharge by pipeline;
D. the concentrated solution of reverse osmosis membrane system can be connected in ultra-filtration membrane dialysis side for recoil or return to nanofiltration (or low rejection reverse osmosis) film system reuse by pipeline by pipeline;
E. to hold back aperture be 0.002-0.05um or molecular weight cut-off 2000D-500KD to ultra-filtration membrane, first step nanofiltration or low-pressure reverse osmosis membrane to the ensemble average rejection of brackish water salinity between 40-95%, the second stage > 90%;
F. the film operating pressure is extremely low, can use the pipeline of plastic material.
The present invention relates to a kind of device of membrane sepn of brackish water desalination, this membrane separation plant adopts two step desalinating process, reduces the osmotic pressure of every step membrane filtration, flow process is succinct, and the equipment operating pressure is extremely low, and equipment is used material general, apparatus processing requires low, and membrane element requires low, good separation.
The above record, only, for utilizing the embodiment of this origination techniques content, modification, variation that any those skilled in the art use this creation to do, all belong to the scope of the claims that this creation is advocated, and be not limited to those disclosed embodiments.
Claims (2)
1. a ultra-low-pressure brackish water desalination membrane separation device, is characterized in that: the pipeline that comprises accurate filter, ultrafiltration membrane system, ultra-filtration membrane dialysate tank, nanofiltration membrane system, nanofiltration membrane dialysate tank, reverse osmosis membrane system, pump and connection each several part; Described accurate filter is connected with the brackish water transferpump, accurate filter is connected with ultrafiltration membrane system by recycle pump, the ultrafiltration membrane system dialyzate is connected to the ultrafiltration dialysis tank, ultrafiltration dialysis liquid is connected with the nanofiltration membrane system by topping-up pump, the dialyzate of nanofiltration membrane system is connected to the nanofiltration membrane dialysate tank, and the nanofiltration membrane dialysate tank is connected with reverse osmosis membrane system by topping-up pump again;
The concentrated solution of described nanofiltration membrane system is directly discharged or is turned back to ultrafiltration membrane system and carries out back flushing;
The concentrated solution of described reverse osmosis membrane system is connected in the dialysis side of ultrafiltration membrane system for recoiling or returning to the reuse of nanofiltration membrane system by pipeline by pipeline; The concentrated solution outlet of described nanofiltration membrane system connects an energy recycle device for promoting the pressure of a part of ultrafiltration membrane system dialyzate, and the ultrafiltration dialysis liquid after the acquisition supercharging enters the import of nanofiltration membrane system by pipeline;
It is 0.002-0.05um or molecular weight cut-off 2000D-500KD that the film of described ultrafiltration membrane system is held back aperture, nanofiltration membrane to the ensemble average rejection of brackish water salinity between 40-95%, the ensemble average rejection of reverse osmosis membrane system to the brackish water salinity > 90%.
2. ultra-low-pressure brackish water desalination membrane separation device according to claim 1 is characterized in that: described nanofiltration membrane system can be replaced by low rejection reverse osmosis membrane system.
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| CN201110264658XA CN102329019B (en) | 2011-09-08 | 2011-09-08 | Ultralow-pressure membrane separation device for desalinating bitter and salty water |
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| CN201110264658XA CN102329019B (en) | 2011-09-08 | 2011-09-08 | Ultralow-pressure membrane separation device for desalinating bitter and salty water |
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| CN102329019B true CN102329019B (en) | 2013-12-11 |
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| CN103936202B (en) * | 2014-05-04 | 2015-11-18 | 河南师范大学 | A kind of method for desalting brackish water and device thereof |
| CN109020040A (en) * | 2018-08-02 | 2018-12-18 | 上海雷鸣水处理技术有限公司 | A kind of desalination plant and method |
| CN112915790B (en) * | 2021-02-09 | 2021-11-26 | 杭州佰迈医疗科技有限公司 | Ultralow pressure generating device, use method and application |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1994904A (en) * | 2006-11-24 | 2007-07-11 | 陈益棠 | Sea water nanofiltration desalination method and device |
| CN201292269Y (en) * | 2008-11-14 | 2009-08-19 | 中国人民解放军海军节能技术研究中心 | Membrane separation device, in particular reverse osmosis sea water desalting apparatus |
| CN201485337U (en) * | 2009-04-02 | 2010-05-26 | 黄松青 | Seawater desalination device with low pressure membrane separation method |
| CN101767894A (en) * | 2009-06-09 | 2010-07-07 | 张世文 | Method for desalting brackish water and device thereof |
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Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1994904A (en) * | 2006-11-24 | 2007-07-11 | 陈益棠 | Sea water nanofiltration desalination method and device |
| CN201292269Y (en) * | 2008-11-14 | 2009-08-19 | 中国人民解放军海军节能技术研究中心 | Membrane separation device, in particular reverse osmosis sea water desalting apparatus |
| CN201485337U (en) * | 2009-04-02 | 2010-05-26 | 黄松青 | Seawater desalination device with low pressure membrane separation method |
| CN101767894A (en) * | 2009-06-09 | 2010-07-07 | 张世文 | Method for desalting brackish water and device thereof |
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