CN111186949A - Multistage flash evaporation seawater desalination and pressure delay permeation salt difference power generation coupling system and operation method - Google Patents
Multistage flash evaporation seawater desalination and pressure delay permeation salt difference power generation coupling system and operation method Download PDFInfo
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- CN111186949A CN111186949A CN202010029825.1A CN202010029825A CN111186949A CN 111186949 A CN111186949 A CN 111186949A CN 202010029825 A CN202010029825 A CN 202010029825A CN 111186949 A CN111186949 A CN 111186949A
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/02—Treatment of water, waste water, or sewage by heating
- C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
- C02F1/06—Flash evaporation
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/20—Treatment of water, waste water, or sewage by degassing, i.e. liberation of dissolved gases
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- H—ELECTRICITY
- H02—GENERATION; CONVERSION OR DISTRIBUTION OF ELECTRIC POWER
- H02N—ELECTRIC MACHINES NOT OTHERWISE PROVIDED FOR
- H02N11/00—Generators or motors not provided for elsewhere; Alleged perpetua mobilia obtained by electric or magnetic means
- H02N11/002—Generators
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2103/00—Nature of the water, waste water, sewage or sludge to be treated
- C02F2103/08—Seawater, e.g. for desalination
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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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- Hydrology & Water Resources (AREA)
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- Environmental & Geological Engineering (AREA)
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- Separation Using Semi-Permeable Membranes (AREA)
- Heat Treatment Of Water, Waste Water Or Sewage (AREA)
Abstract
The system comprises a salt water heater, a multi-stage flash evaporation heat recovery section, a multi-stage flash evaporation heat discharge section, a pressure exchanger, a booster pump, a pressure delay permeation membrane component, a water turbine, a natural seawater introducing pump, a cooling seawater discharge pump, a product fresh water leading-out pump, a CO removal pump and a salt difference power generation coupling system2The device comprises a device, a deaerating device and a vacuumizing device; and respectively introducing strong brine and seawater discharged by the multistage flash evaporation system into a liquid drawing side and a raw material liquid side of the pressure delay permeation membrane component to perform permeation power generation. Adjusting the flow ratio of the drawing liquid to the raw material liquid through a raw material liquid flow control valve; the pressure difference at two sides of the pressure delay permeation membrane component is adjusted by a booster pump; regulating the flow ratio of two sides of pressure exchanger by flow control valveFor example. The invention can improve the energy utilization efficiency of the whole system, reduce the salinity of the strong brine discharged by the system and reduce the influence on the ecological environment.
Description
Technical Field
The invention relates to the technical field of seawater desalination and salt difference energy, in particular to a multistage flash evaporation seawater desalination and pressure delay permeation salt difference power generation coupling system and an operation method.
Background
The multi-stage flash seawater desalination technology is a hot seawater desalination technology, and can produce fresh water in large quantities. However, the multi-stage flash evaporation seawater desalination technology has high heat consumption, is an energy-intensive seawater desalination mode, and can discharge a large amount of strong brine with concentration higher than the environmental concentration, thereby having negative effects on the surrounding ecological environment. The pressure delay infiltration power generation technology can utilize the solution concentration difference power generation technology and is mainly applied to areas with rich salt difference energy in nature, such as rivers, seaports, salt lakes and the like. However, the salt difference energy resource concentration difference is small, and the pretreatment cost is high due to more impurities in natural seawater, river water and lake water.
Disclosure of Invention
In order to solve the problems in the prior art, the invention provides a multistage flash evaporation seawater desalination and pressure delay permeation salt difference power generation coupling system and an operation method thereof, wherein the system introduces strong brine discharged by a multistage flash evaporation seawater desalination process into a pressure delay permeation system as an extraction liquid, introduces a low-concentration solution into the pressure delay permeation system as a raw material liquid, realizes concentration difference power generation and reduces the concentration of discharged water; the invention can improve the energy utilization efficiency of the whole system, reduce the salinity of the strong brine discharged by the system and reduce the influence on the ecological environment.
In order to achieve the purpose, the invention adopts the following technical scheme:
a multi-stage flash evaporation seawater desalination and pressure delay permeation salt difference power generation coupling system comprises a brine heater 1, a multi-stage flash evaporation heat recovery section 2, a multi-stage flash evaporation heat discharge section 3, a pressure exchanger 4, a booster pump 5, a pressure delay permeable membrane assembly 6, a water turbine 7, a natural seawater introducing pump 12, a cooling seawater discharge pump 11, a product fresh water extraction pump 13, a CO removal 2 device 8, a deoxygenation device 9 and a vacuum pumping device 10 which are connected, wherein the liquid side of the multi-stage flash evaporation heat discharge section 3 is connected with the low-pressure side of the pressure exchanger 4 through a strong brine discharge pipe; the low-pressure side of the pressure exchanger 4 is connected with the inlet of the liquid-drawing side of the pressure delay permeation membrane component 6 through a liquid-drawing pipeline and a booster pump 5; part of the natural seawater passes through a raw material liquid pipeline and is connected with a raw material liquid side inlet of the pressure delay permeable membrane assembly 6 through a raw material liquid flow control valve 14; the high-pressure side inlet of the pressure exchanger 4 is connected with the liquid-drawing side outlet of the pressure delay permeable membrane assembly 6 through a flow control valve 15 by a pipeline; the absorption liquid and the raw material liquid in the pressure delay permeable membrane component 6 absorb pure water from one side of the absorption liquid and push the water turbine 7 to do work; seawater enters the steam side of the multi-stage flash evaporation heat discharge section 3 through a natural seawater inlet pump 12 to serve as cooling water; part of the cooled seawater flows out of the multi-stage flash evaporation heat discharge section 3 and is directly discharged, the rest seawater serving as supplementary seawater enters a CO2 removal device 8, then enters a deoxygenation device 9, enters the liquid side of the multi-stage flash evaporation heat discharge section 3 after being deoxygenated, then enters the steam side of the multi-stage flash evaporation heat recovery section 2, is heated by a brine heater 1, enters the liquid side of the multi-stage flash evaporation heat recovery section 2, and then enters the liquid side of the multi-stage flash evaporation heat discharge section 3; the vacuum extractor 10 is connected to the multistage flash heat discharge section 3 via the oxygen removal device 9.
In the multi-stage flash evaporation seawater desalination and pressure delay permeation salt difference power generation coupling system, the volume flow ratio of raw material liquid and draw liquid entering the pressure delay permeation membrane component 6 is (0.9-1.1): 1.
in the multi-stage flash evaporation seawater desalination and pressure delay osmotic salt difference power generation coupling system, the drawn liquid at the inlet of the pressure delay osmotic membrane component 6 is from the seawater concentrated by the multi-stage flash evaporation heat recovery section (2) and the multi-stage flash evaporation heat discharge section 3, and the mass fraction of the drawn liquid is 6-8%; the raw material liquid is natural seawater which is introduced into a pump (12) to be conveyed, or pretreated urban wastewater.
In the multi-stage flash evaporation seawater desalination and pressure delay osmosis salt difference power generation coupling system, the pressure difference between two sides of the membrane of the pressure delay osmosis membrane component 6 is 0.4-0.6 times of the osmotic pressure difference between the drawing solution and the raw material solution.
The multi-stage flash evaporation seawater desalination and pressure delay permeation salt difference power generation coupling system is characterized in that the flow ratio of high-pressure fluid to low-pressure fluid on two sides of a pressure exchanger 4 is (0.9-1.1): 1.
the multi-stage flash evaporation seawater desalination and pressure delay permeation salt difference power generation coupling systemThe operation method comprises the steps that seawater enters the steam side of the multi-stage flash evaporation heat discharge section 3 through the natural seawater inlet pump 12 to be used as cooling water for cooling flash evaporation steam, part of the cooled seawater flows out of the multi-stage flash evaporation heat discharge section 3 and then is directly discharged through the cooling seawater discharge pump 11, and the rest seawater serving as supplementary seawater enters the CO removal section2The device 8 then enters a deaerator 9, enters the liquid side of the multistage flash evaporation heat discharge section 3 after being deaerated, then enters the steam side of the multistage flash evaporation heat recovery section 2, is heated by a brine heater 1, enters the liquid side of the multistage flash evaporation heat recovery section 2, and then enters the liquid side of the multistage flash evaporation heat discharge section 3 for flash evaporation concentration; controlling the salinity difference of the two sides of the pressure delay permeable membrane assembly 6 by adjusting the amount of the supplementary seawater entering the multistage flash heat discharge section 3, and simultaneously controlling the pressure difference of the two sides of the pressure delay permeable membrane assembly 6 to be 0.4-0.6 times of the osmotic pressure difference by adjusting the booster pump 5 according to the osmotic pressure difference; by adjusting the raw material liquid flow control valve 14, the ratio of the volume flow of the draw liquid and the raw material liquid entering the pressure-delay permeable membrane module 6 is controlled to be (0.9-1.1): 1; by adjusting the flow control valve 15, the ratio of the flow rates on both sides of the pressure exchanger 4 is controlled to be (0.9 to 1.1): 1; the vacuum degree in a multistage flash evaporation system consisting of the deaerating device 9, the brine heater 1, the multistage flash evaporation heat recovery section 2 and the multistage flash evaporation heat discharge section 3 is adjusted by the vacuumizing device 10; the product fresh water is led out by a product fresh water lead-out pump 13 and collected for water consumers to use.
Compared with the prior art, the invention has the following advantages:
(1) the invention utilizes the salt difference energy of the strong brine discharged by the multi-stage flash evaporation process by coupling the multi-stage flash evaporation seawater desalination and the salt difference power generation system, thereby improving the energy utilization efficiency of the whole system.
(2) The salt concentration generating system reduces the salinity of the strong brine discharged by the system and reduces the influence on the ecological environment.
Drawings
FIG. 1 is a diagram of a multi-stage flash desalination and pressure delay osmotic salt-difference power generation coupling system according to the present invention.
Detailed Description
The present invention will be described in further detail with reference to the accompanying drawings and specific embodiments.
As shown in fig. 1, the present invention provides a multistage flash evaporation seawater desalination and pressure delay osmosis salt difference power generation coupling system, which comprises a brine heater 1, a multistage flash evaporation heat recovery section 2, a multistage flash evaporation heat discharge section 3, a pressure exchanger 4, a booster pump 5, a pressure delay osmosis membrane assembly 6, a water turbine 7, a natural seawater introducing pump 12, a cooling seawater discharging pump 11, a product fresh water leading-out pump 13, a CO removal 2 removing device 8, a deaerating device 9 and a vacuum pumping device 10, which are connected with each other, wherein the liquid side of the multistage flash evaporation heat discharge section 3 is connected with the low-pressure side of the pressure exchanger 4 through a concentrated brine discharge pipe; the low-pressure side of the pressure exchanger 4 is connected with the inlet of the liquid-drawing side of the pressure delay permeation membrane component 6 through a liquid-drawing pipeline and a booster pump 5; part of the natural seawater passes through a raw material liquid pipeline and is connected with a raw material liquid side inlet of the pressure delay permeable membrane assembly 6 through a raw material liquid flow control valve 14; the high-pressure side inlet of the pressure exchanger 4 is connected with the liquid-drawing side outlet of the pressure delay permeable membrane assembly 6 through a flow control valve 15 by a pipeline; the absorption liquid and the raw material liquid in the pressure delay permeable membrane component 6 absorb pure water from one side of the absorption liquid and push the water turbine 7 to do work; seawater enters the steam side of the multi-stage flash evaporation heat discharge section 3 through a natural seawater inlet pump 12 to serve as cooling water; part of the cooled seawater flows out of the multi-stage flash evaporation heat discharge section 3 and is directly discharged, and the rest seawater is used as supplementary seawater and enters for removing CO2The device 8 then enters a deaerator 9, enters the liquid side of the multistage flash evaporation heat discharge section 3 after being deaerated, then enters the steam side of the multistage flash evaporation heat recovery section 2, is heated by a brine heater 1, enters the liquid side of the multistage flash evaporation heat recovery section 2, and then enters the liquid side of the multistage flash evaporation heat discharge section 3; the vacuum extractor 10 is connected to the multistage flash heat discharge section 3 via the oxygen removal device 9.
In a preferred embodiment of the present invention, the ratio of the volume flow rates of the raw material liquid and the draw liquid entering the pressure-retarded osmosis membrane module 6 is (0.9 to 1.1): 1.
as a preferred embodiment of the invention, the drawn liquid at the inlet of the pressure delay permeable membrane assembly 6 is from the seawater concentrated by the multi-stage flash evaporation heat recovery section 2 and the multi-stage flash evaporation heat discharge section 3, and the mass fraction of the drawn liquid is 6-8%; the raw material liquid is natural seawater which is introduced into a pump (12) to be conveyed, or pretreated urban wastewater.
In a preferred embodiment of the present invention, the pressure difference between both sides of the membrane of the pressure retarded osmosis membrane module 6 is 0.4 to 0.6 times of the osmotic pressure difference between the draw solution and the feed solution.
In a preferred embodiment of the present invention, the ratio of the flow rates of the high-pressure fluid and the low-pressure fluid on both sides of the pressure exchanger 4 is (0.9 to 1.1): 1, recovering pressure energy to the maximum extent.
As shown in figure 1, the operation method of the multi-stage flash evaporation seawater desalination and pressure delay permeation salt difference power generation coupling system is characterized in that seawater enters a steam side of a multi-stage flash evaporation heat discharge section 3 through a natural seawater introducing pump 12 to be used as cooling water for cooling flash evaporation steam, part of the cooled seawater flows out of the multi-stage flash evaporation heat discharge section 3 and then is directly discharged through a cooling seawater discharge pump 11, and the rest seawater serving as supplementary seawater enters a CO removal system2The device 8 then enters a deaerator 9, enters the liquid side of the multistage flash evaporation heat discharge section 3 after being deaerated, then enters the steam side of the multistage flash evaporation heat recovery section 2, is heated by a brine heater 1, enters the liquid side of the multistage flash evaporation heat recovery section 2, and then enters the liquid side of the multistage flash evaporation heat discharge section 3 for flash evaporation concentration; controlling the salinity difference of the two sides of the pressure delay permeable membrane assembly 6 by adjusting the amount of the supplementary seawater entering the multistage flash heat discharge section 3, and simultaneously controlling the pressure difference of the two sides of the pressure delay permeable membrane assembly 6 to be 0.4-0.6 times of the osmotic pressure difference by adjusting the booster pump 5 according to the osmotic pressure difference; by adjusting the raw material liquid flow control valve 14, the ratio of the volume flow of the draw liquid and the raw material liquid entering the pressure-delay permeable membrane module 6 is controlled to be (0.9-1.1): 1; by adjusting the flow control valve 15, the ratio of the flow rates on both sides of the pressure exchanger 4 is controlled to be (0.9 to 1.1): 1; the vacuum degree in a multistage flash evaporation system consisting of the deaerating device 9, the brine heater 1, the multistage flash evaporation heat recovery section 2 and the multistage flash evaporation heat discharge section 3 is adjusted by the vacuumizing device 10; the product fresh water is led out by a product fresh water lead-out pump 13 and collected for water consumers to use.
The invention provides a multistage flash evaporation seawater desalination and pressure delay permeation salt difference power generation coupling system and an operation method, wherein the system introduces strong brine discharged by a multistage flash evaporation seawater desalination process into a pressure delay permeation system to be used as an extraction liquid, and introduces a low-concentration solution into the pressure delay permeation system to be used as a raw material liquid, so that concentration difference power generation is realized, and the concentration of discharged water is reduced; the invention can improve the energy utilization efficiency of the whole system, reduce the salinity of the strong brine discharged by the system and reduce the influence on the ecological environment.
Claims (6)
1. The utility model provides a multistage flash distillation sea water desalination and pressure delay infiltration salt difference electricity generation coupled system, includes salt water heater (1) that link to each other, multistage flash distillation heat recovery section (2), multistage flash distillation heat discharge section (3), pressure exchanger (4), booster pump (5), pressure delay infiltration membrane module (6), hydraulic turbine (7) and natural sea water introducing pump (12), cooling sea water discharge pump (11), product fresh water extraction pump (13), remove CO2 device (8), deaerating plant (9) and evacuating device (10), its characterized in that: the liquid side of the multi-stage flash evaporation heat discharge section (3) is connected with the low-pressure side of the pressure exchanger (4) through a strong brine discharge pipe; the low-pressure side of the pressure exchanger (4) is connected with a liquid-drawing side inlet of the pressure delay permeation membrane component (6) through a liquid-drawing pipeline and a booster pump (5); part of the natural seawater passes through a raw material liquid pipeline and is connected with a raw material liquid side inlet of the pressure delay permeation membrane component (6) through a raw material liquid flow control valve (14); the high-pressure side inlet of the pressure exchanger (4) is connected with the liquid-drawing side outlet of the pressure delay permeation membrane component (6) through a flow control valve (15) by a pipeline; drawing pure water from one side of the drawing liquid by the drawing liquid and the raw material liquid in the pressure delay permeation membrane component (6) and pushing a water turbine (7) to do work; seawater enters a steam side of a multi-stage flash evaporation heat discharge section (3) through a natural seawater introducing pump (12) to be used as cooling water; part of the cooled seawater flows out of the multi-stage flash evaporation heat discharge section (3) and is directly discharged, the rest seawater serving as supplementary seawater enters a CO2 removal device (8), then enters a deoxygenation device (9), enters the liquid side of the multi-stage flash evaporation heat discharge section (3) after being deoxygenated, then enters the steam side of the multi-stage flash evaporation heat recovery section (2), is heated by a brine heater (1), enters the liquid side of the multi-stage flash evaporation heat recovery section (2), and then enters the liquid side of the multi-stage flash evaporation heat discharge section (3); the vacuum extractor (10) is connected with the multi-stage flash evaporation heat discharge section (3) through the oxygen removing device (9).
2. The multi-stage flash seawater desalination and pressure-delayed osmotic salt-difference power generation coupled system of claim 1, wherein: the ratio of the volume flow rates of the raw material solution and the draw solution is (0.9-1.1): 1.
3. the multi-stage flash seawater desalination and pressure-delayed osmotic salt-difference power generation coupled system of claim 1, wherein: the liquid drawn from the inlet of the pressure delay permeation membrane component (6) is from the seawater concentrated by the multi-stage flash evaporation heat recovery section (2) and the multi-stage flash evaporation heat discharge section (3), and the mass fraction of the drawn liquid is 6-8%; the raw material liquid is natural seawater which is introduced into a pump (12) to be conveyed, or pretreated urban wastewater.
4. The multi-stage flash seawater desalination and pressure-delayed osmotic salt-difference power generation coupled system of claim 1, wherein: the pressure difference of the two sides of the membrane of the pressure delay permeation membrane component (6) is 0.4-0.6 times of the osmotic pressure difference of the drawing liquid and the raw material liquid.
5. The multi-stage flash seawater desalination and pressure-delayed osmotic salt-difference power generation coupled system of claim 1, wherein: the ratio of the flow rates on both sides of the pressure exchanger (4) is (0.9-1.1): 1.
6. the operation method of the multi-stage flash evaporation seawater desalination and pressure delay permeation salt difference power generation coupled system as claimed in claims 1 to 5, characterized in that: seawater enters a steam side of the multi-stage flash evaporation heat discharge section (3) through a natural seawater introducing pump (12) to be used as cooling water for cooling flash evaporation steam, part of the cooled seawater flows out of the multi-stage flash evaporation heat discharge section (3) and is directly discharged through a cooling seawater discharge pump (11), and the rest seawater serving as supplementary seawater enters a CO removal system2The device (8) enters a deaerating device (9) later, enters the liquid side of the multi-stage flash evaporation heat discharge section (3) after being deaerated, then enters the steam side of the multi-stage flash evaporation heat recovery section (2), is heated by a brine heater (1), enters the liquid side of the multi-stage flash evaporation heat recovery section (2), and then enters the liquid side of the multi-stage flash evaporation heat discharge section (3) for flash evaporation concentration; the inlet pressure is controlled by adjusting the amount of supplementary seawater entering the multistage flash heat discharge section (3)Salinity difference on two sides of the force-delay osmosis membrane component (6), and simultaneously controlling the pressure difference on two sides of the pressure-delay osmosis membrane component (6) to be 0.4-0.6 times of the osmotic pressure difference according to the osmotic pressure difference regulation booster pump (5); by adjusting the raw material liquid flow control valve (14), the ratio of the volume flow of the drawing liquid and the raw material liquid entering the pressure delay permeation membrane component (6) is controlled to be (0.9-1.1): 1; controlling the flow rate ratio of the two sides of the pressure exchanger (4) to be (0.9-1.1) by adjusting the flow rate control valve (15): 1; the vacuum degree in a multistage flash evaporation system consisting of the deaerating device (9), the brine heater (1), the multistage flash evaporation heat recovery section (2) and the multistage flash evaporation heat discharge section (3) is adjusted by the vacuumizing device (10); the product fresh water is led out by a product fresh water lead-out pump (13) and collected for water consumers to use.
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| CN113562915A (en) * | 2021-07-26 | 2021-10-29 | 西安交通大学 | Low-pollution water and electricity cogeneration system utilizing solar energy and operation method thereof |
| CN115745287A (en) * | 2022-11-25 | 2023-03-07 | 中国科学院武汉岩土力学研究所 | High salinity saline water desalination treatment system and method |
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| CN115745287A (en) * | 2022-11-25 | 2023-03-07 | 中国科学院武汉岩土力学研究所 | High salinity saline water desalination treatment system and method |
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