CN1208719A - Gas solution adsorption type osmosis method for sea water desalination - Google Patents
Gas solution adsorption type osmosis method for sea water desalination Download PDFInfo
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- CN1208719A CN1208719A CN98103346A CN98103346A CN1208719A CN 1208719 A CN1208719 A CN 1208719A CN 98103346 A CN98103346 A CN 98103346A CN 98103346 A CN98103346 A CN 98103346A CN 1208719 A CN1208719 A CN 1208719A
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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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Abstract
The present invention relates to a new membrane desalination method of seawater. It is characterized by organically combining the seawater desalination by permeation process and gas-contained solution absorption power generation together. It utilizes the osmotic pressure formed by differential concentration of the high-concentration gas-contained solution and seawater in the membrane permeation water-absorbing zone to absorb the fresh water from seawater, then uses high-temp. to separate the water from gas solute being in the solution completely so as to obtain fresh water. Besides, the high-pressure gas separated out from high-temp. separator can be used to drive turbine-generator to make power generation. Said invention can obtain a large-quantity of fresh water, at the same time can make power generation, so that its energy consumption is less.
Description
The invention belongs to a branch of embrane method sea water desaltination.
Embrane method sea water desaltination mode mainly is electroosmose process and reverse osmosis method at present, and electroosmose process will consume more electric energy, and reverse osmosis method must be worked under condition of high voltage, influences the life-span of film, and structure is more complicated also, and the mechanical energy that consumes is also more.These two kinds of method energy expenditures are big, and water production rate is limited, can only be used for making water separately, and are relatively poor through turbid property.
Order of the present invention ground just provides a kind of new film method for desalting seawater, and it does not need electric energy needn't under high pressure work yet, the life-span length of film and a kind of desalination process that can combine with generating, and this technology water production rate is big, and energy expenditure is little.
Technical scheme of the present invention: the gas working medium solution of high density and seawater intersection, produce a kind of physical chemistry energy, can convert thereof into osmotic pressure, utilize the effect of semi-permeable membranes, fresh water under the effect of osmotic pressure in the seawater enters working medium solution by semi-permeable membranes, thereafter utilize the gas solute with the very big characteristics of variation of temperature changes in solubility rate, the gas working medium in the solution is separated with water, just obtain fresh water with high temperature.The high pressure gas impulsion gas-turbine generating of separating.Because the heat of being taken away when gas solute and solution separating is solution heat rather than vaporization heat, and the solution heat of gas working medium is very little, so efficiency of utilization is higher.Requirement to gas working medium: (1) solubleness is big, and (2) solution heat is little, the stable difficult decomposition of (3) chemical property.(4) permissible value of the pH value of solution and semi-permeable membranes is corresponding.
Specify below in conjunction with accompanying drawing, gas working medium is example with formaldehyde.
Accompanying drawing is a principle schematic of the present invention
Mark (1) membrane permeation suction zones among the figure, (2) high-temperature separator, (3) gas-liquid convection formula heat exchanger, (4) turbo-generator, (5) resorber, (6) resorber service pump, (7) liquid liquid convection type heat exchanger, (8) water outlet.
(1) the membrane permeation suction zones directly and contact with sea water, it is to be to absorb fresh water from seawater by its effect that semi-permeable membranes constitutes.Highly concentrated formaldehyde solution about 40% flows into from the import of membrane permeation suction zones, 40% highly concentrated formaldehyde solution and 3.5% lower concentration seawater have very high concentration difference, fresh water under the effect of osmotic pressure in the seawater enters formaldehyde solution by semi-permeable membranes, and salinity is then stayed in the seawater.The formaldehyde solution of high density is not broken and is absorbed fresh water in the seawater, concentration constantly descends, discharge from outlet at last, the concentration of formaldehyde of liquid effluent is about 8%, and the formaldehyde solution of lower concentration enters (2) high-temperature separator, and the temperature of high-temperature separator is about 95 ℃, utilize high temperature that formaldehyde gas is separated fully with water, many water-fast materials are housed as the nucleus of condensation in high-temperature separator, as charcoal, mountain sand etc., the nuclear energy that condenses improves the gasification rate of formaldehyde greatly.Formaldehyde is separated fully with water.Can use boiler to make high-temperature separator,, also can use other energy with the coal heating.The heat of being taken away when formaldehyde gas is vaporized separation from solution is very a spot of solution heat, rather than vaporization, so the heat that this process consumes seldom.The formaldehyde gas of High Temperature High Pressure is by (3) gas-liquid convection formula heat exchanger, given formaldehyde solution thermal energy transfer by heat exchanger, because what adopt is the convection type heat exchange method, the inlet of formaldehyde gas is suitable with the temperature out of formaldehyde solution, the outlet of formaldehyde gas is suitable with the temperature in of formaldehyde solution, and the heat energy that the high temperature formaldehyde gas is taken away obtains reclaiming like this.The generating of high pressure formaldehyde gas impulsion (4) turbo-generator.Formaldehyde gas enters (5) resorber after by turbo-generator, (6) the resorber service pump injects rare formaldehyde solution of 8% top spray from resorber, increased the absorption area of rare formaldehyde solution greatly, rare formaldehyde solution absorbs formaldehyde gas in a large number, its concentration is increased to about 40%, the formaldehyde solution of high density enters the membrane permeation suction zones, and osmotic absorbent from seawater is finished the working medium circulation.Effusive fresh water is by (7) liquid liquid convection type heat exchanger in the high-temperature separator, and cryogenic formaldehyde solution and high-temperature water carry out the convection type heat exchange in heat exchanger, the energy that the recovery high-temperature water is taken away.Cold water after is really discharged from (8) water outlet and has just been obtained a large amount of fresh water like this.
The maximum characteristics of technology of the present invention are osmosis method for sea water desalination and gas solution adsorption Generating combines, and can obtain a large amount of fresh water, can also generate electricity simultaneously. Gas What take away when solution is heated vaporization is a small amount of heat of solution, so the thermal efficiency of generating is higher. Owing to used gas-liquid convection formula heat exchanger and liquid convection type heat exchanger, energy is returned Receive, so energy consumption seldom. There are a large amount of water-fast materials to make the nuclei of condensation in the high-temperature separator, Greatly accelerated the vaporization rate of formaldehyde. Absorber and film osmotic absorbent distinguish, so greatly Improved the concentration of working medium methanol solution. 40% formalin and sea in the film osmotic absorbent district Water forms very big concentration difference, the osmotic pressure height, and the speed that absorbs fresh water is fast. This technology also has produces The characteristics such as the water yield is big, and the life-span of film is long.
Claims (5)
1. the present invention is a kind of brand-new film desalination process, its technical characterictic is, this technology combines osmosis method for sea water desalination and gas solution adsorption generating, it is to utilize the gas solution of high density and seawater intersection to produce osmotic pressure, utilize that the fresh water in the seawater enters working medium solution by semi-permeable membranes under the effect that acts on osmotic pressure of semi-permeable membranes, thereafter utilize high temperature that the gas solute in the gas solution is all separated, just obtain fresh water, the high pressure gas impulsion turbo-generator generating of separating.
2. be two kinds of gas liquid type and solution-types to be arranged in the system according to described its technical characterictic of claim 1 to system formula heat exchanger.
3. be that resorber and membrane permeation suction zones are separated according to described its technical characterictic of claim 1.
4. be that a large amount of water-fast nucleus of condensation are arranged in producer according to described its technical characterictic of claim 1.
5. be that requirement to working medium is according to described its technical characterictic of claim 1, solubleness is big, and solution heat is little, and chemical property is stable, and the pH value of its aqueous solution is corresponding with the film permissible value.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN98103346A CN1208719A (en) | 1998-07-30 | 1998-07-30 | Gas solution adsorption type osmosis method for sea water desalination |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN98103346A CN1208719A (en) | 1998-07-30 | 1998-07-30 | Gas solution adsorption type osmosis method for sea water desalination |
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| Publication Number | Publication Date |
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| CN1208719A true CN1208719A (en) | 1999-02-24 |
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| CN98103346A Pending CN1208719A (en) | 1998-07-30 | 1998-07-30 | Gas solution adsorption type osmosis method for sea water desalination |
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Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102596822A (en) * | 2009-12-25 | 2012-07-18 | 东丽株式会社 | Water production system and operation method therefor |
| CN104783340A (en) * | 2015-04-28 | 2015-07-22 | 苏州舒而适纺织新材料科技有限公司 | Heat-protective clothing moisture absorption air guide structure |
| US11502322B1 (en) | 2022-05-09 | 2022-11-15 | Rahul S Nana | Reverse electrodialysis cell with heat pump |
| US11502323B1 (en) | 2022-05-09 | 2022-11-15 | Rahul S Nana | Reverse electrodialysis cell and methods of use thereof |
| US11855324B1 (en) | 2022-11-15 | 2023-12-26 | Rahul S. Nana | Reverse electrodialysis or pressure-retarded osmosis cell with heat pump |
| US12040517B2 (en) | 2022-11-15 | 2024-07-16 | Rahul S. Nana | Reverse electrodialysis or pressure-retarded osmosis cell and methods of use thereof |
| US12107308B2 (en) | 2023-02-16 | 2024-10-01 | Rahul S Nana | Reverse electrodialysis cell and methods of use thereof |
-
1998
- 1998-07-30 CN CN98103346A patent/CN1208719A/en active Pending
Cited By (12)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102596822A (en) * | 2009-12-25 | 2012-07-18 | 东丽株式会社 | Water production system and operation method therefor |
| CN102596822B (en) * | 2009-12-25 | 2014-05-21 | 东丽株式会社 | Water production system and operation method therefor |
| CN104783340A (en) * | 2015-04-28 | 2015-07-22 | 苏州舒而适纺织新材料科技有限公司 | Heat-protective clothing moisture absorption air guide structure |
| CN104783340B (en) * | 2015-04-28 | 2017-04-05 | 苏州舒而适纺织新材料科技有限公司 | A kind of heat-protective clothing moisture absorption gas-guiding structure |
| US11502322B1 (en) | 2022-05-09 | 2022-11-15 | Rahul S Nana | Reverse electrodialysis cell with heat pump |
| US11502323B1 (en) | 2022-05-09 | 2022-11-15 | Rahul S Nana | Reverse electrodialysis cell and methods of use thereof |
| US11563229B1 (en) | 2022-05-09 | 2023-01-24 | Rahul S Nana | Reverse electrodialysis cell with heat pump |
| US11611099B1 (en) | 2022-05-09 | 2023-03-21 | Rahul S Nana | Reverse electrodialysis cell and methods of use thereof |
| US11699803B1 (en) | 2022-05-09 | 2023-07-11 | Rahul S Nana | Reverse electrodialysis cell with heat pump |
| US11855324B1 (en) | 2022-11-15 | 2023-12-26 | Rahul S. Nana | Reverse electrodialysis or pressure-retarded osmosis cell with heat pump |
| US12040517B2 (en) | 2022-11-15 | 2024-07-16 | Rahul S. Nana | Reverse electrodialysis or pressure-retarded osmosis cell and methods of use thereof |
| US12107308B2 (en) | 2023-02-16 | 2024-10-01 | Rahul S Nana | Reverse electrodialysis cell and methods of use thereof |
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