WO2010026953A1 - Procédé éco-énergétique et dispositif de fabrication d'eau distillée et/ou d'eau concentrée - Google Patents

Procédé éco-énergétique et dispositif de fabrication d'eau distillée et/ou d'eau concentrée Download PDF

Info

Publication number
WO2010026953A1
WO2010026953A1 PCT/JP2009/065229 JP2009065229W WO2010026953A1 WO 2010026953 A1 WO2010026953 A1 WO 2010026953A1 JP 2009065229 W JP2009065229 W JP 2009065229W WO 2010026953 A1 WO2010026953 A1 WO 2010026953A1
Authority
WO
WIPO (PCT)
Prior art keywords
water
evaporator
concentrated
condenser
distilled water
Prior art date
Application number
PCT/JP2009/065229
Other languages
English (en)
Japanese (ja)
Inventor
誠一 竹田
Original Assignee
Takeda Seiichi
Priority date (The priority date 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 date listed.)
Filing date
Publication date
Application filed by Takeda Seiichi filed Critical Takeda Seiichi
Priority to JP2010527781A priority Critical patent/JPWO2010026953A1/ja
Publication of WO2010026953A1 publication Critical patent/WO2010026953A1/fr

Links

Images

Classifications

    • 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
    • C02F1/041—Treatment of water, waste water, or sewage by heating by distillation or evaporation by means of vapour compression
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D1/00—Evaporating
    • B01D1/0088—Cascade evaporators
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D1/00—Evaporating
    • B01D1/28—Evaporating with vapour compression
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D5/00—Condensation of vapours; Recovering volatile solvents by condensation
    • B01D5/0057—Condensation of vapours; Recovering volatile solvents by condensation in combination with other processes
    • B01D5/006—Condensation of vapours; Recovering volatile solvents by condensation in combination with other processes with evaporation or distillation
    • 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
    • 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
    • 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
    • Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
    • Y02W10/00—Technologies for wastewater treatment
    • Y02W10/30—Wastewater or sewage treatment systems using renewable energies
    • Y02W10/37—Wastewater or sewage treatment systems using renewable energies using solar energy

Definitions

  • the present invention relates generally to the production of distilled water and / or concentrated water from raw water containing impurities such as salt, and more particularly to the production of distilled water from raw water using a heat exchanger to increase energy efficiency.
  • the present invention relates to a method and an apparatus thereof, and a method for obtaining concentrated water generated with distillation.
  • the latent heat of steam generation is about 540 cal / g at 98 ° C. and about 570 cal / g at 48 ° C., and only about 1/8 of hot water can be evaporated by the multistage flash method. For this reason, in order to increase energy efficiency, the concentrated water of about 40 to 50 ° C.
  • An object of this invention is to solve such a problem and to provide the distilled water manufacturing method and apparatus excellent in energy efficiency.
  • distilled water is produced, water concentration always occurs, so it is easy to think that the distilled water production apparatus is also a production apparatus for concentrated water.
  • the multi-stage flash method which is the mainstream of seawater desalination, has a low concentration rate of residual water remaining after distillation and is low for the purpose of salt production. There is little to be done.
  • salt water with a high concentration rate for the production of salt can be obtained as a by-product of seawater desalination, the energy usage rate for salt / salt production can be greatly reduced. Therefore, it is also an object of the present invention to provide a raw water concentration method and apparatus.
  • a method for producing distilled water and / or concentrated water from raw water is provided.
  • This manufacturing method is (I) supplying raw water having a temperature 5 ° C. lower than the boiling point or higher to the evaporator; (Ii) evaporating at least a portion of the raw water as water vapor in an evaporator; (Iii) discharging concentrated water; (Iv) pressurizing the steam so that the condensation temperature of the steam is higher than the boiling point of the raw water by 1.01 to 2.0 times higher than the pressure in the evaporator; (V) condensing the pressurized water vapor in a condenser to form distilled water.
  • the evaporator and the condenser are partitioned by a heat transfer plate, and the heat of condensation due to the condensation of water vapor in the condenser is transferred from the condenser to the evaporator through the heat transfer plate, thereby Bring the raw water to a boil.
  • the step (ii) may further include a step of separating raw water evaporated at least partially as water vapor into water vapor and concentrated water.
  • the method may further include (vi) cooling the condensed distilled water and / or (vii) cooling the discharged concentrated water.
  • the method may further include preheating the raw water supplied to the evaporator to a temperature lower than the boiling point by 5 ° C. or higher.
  • the steps of preheating raw water, cooling distilled water, and cooling concentrated water are performed in at least one counter-flow heat exchanger, and distilled water and / or concentration is performed.
  • the raw water can be preheated to a temperature 5 ° C. lower than the boiling point.
  • this heat exchanger can be a plate heat exchanger.
  • a part of the pressurized water vapor can be sent to the evaporator to become a boiling nucleus.
  • the water concentrated in the evaporator is used as raw water, and the steps (ii), (iii), (iv), and (v) are repeated in one or more cycles. it can.
  • the raw water can be seawater or saltwater lake water, in which case the pressurizing stage is 1.02 to 2. It is preferable to pressurize so that it becomes higher by 0 times.
  • the raw water can also be treated water containing heavy metals or treated water containing substances that are not volatile.
  • an apparatus for producing distilled water and / or concentrated water comprises: Raw water supply means for supplying the stock solution; An evaporator that evaporates at least a portion of the raw water supplied from the raw water supply means; A condenser that communicates with the evaporator and that condenses water vapor to produce distilled water; An apparatus for producing distilled water and concentrated water, comprising pressurizing means provided in a line leading from the evaporator to the condenser.
  • This pressurizing means pressurizes the water vapor in the condenser so that the condensation temperature of the water vapor is higher than the boiling point of the raw water, and the evaporator and the condenser are partitioned by a heat transfer plate.
  • the raw water is boiled in the evaporator by transmitting the heat of condensation due to the condensation of water vapor in the condenser through the heat transfer plate from the condenser to the evaporator.
  • the apparatus for producing distilled water and / or concentrated water further includes a gas-liquid separation device provided between the evaporator and the condenser for separating raw water into steam and concentrated water. Can be included.
  • the apparatus for producing distilled water and / or concentrated water further includes at least one plate heat exchanger provided between the raw water supply means and the evaporator, Concentrated water discharged from the gas-liquid separator and / or distilled water discharged from the condenser can be subjected to heat exchange with the raw water in the plate heat exchanger.
  • an apparatus for producing distilled water and / or concentrated water comprises at least one set of evaporators, pressurizing means communicating with the evaporators, condensing communicating with the pressurizing means.
  • Each set can be connected so that the concentrated water discharged from the previous set of condensers is introduced into the next set of evaporators as raw water.
  • the pressurizing means pressurizes the pressure in the condenser 0.01 to 1.0 atm higher than the pressure in the evaporator.
  • the pressurizing means preferably pressurizes the pressure in the condenser to be 0.02 to 1.0 atmosphere higher than the pressure in the evaporator.
  • Water containing a salt such as seawater has a boiling point increase corresponding to the concentration of the salt, and it is necessary to increase the minimum pressure with an increase in the concentration of the salt.
  • Distillation and concentration are a pair of actions, and this method can be advantageously used as a concentration means.
  • this method is a method for producing a salt using as a raw material concentrated water obtained by the method for producing distilled water and concentrated water.
  • wastewater and wastewater containing heavy metals and other substances that exceed the environmental standards discharged from factories, or wastewater containing pesticides that exceed environmental standards among wastewater from golf courses, farms, livestock facilities, or poultry farms can be used for concentration as a preliminary treatment for detoxifying or extracting valuable substances.
  • the figure showing the basic composition for dividing raw water into distilled water and concentrated water The figure which shows the structure of an example of the distilled water manufacturing apparatus which concerns on this invention. The figure which shows another structure of the distilled water manufacturing apparatus which concerns on this invention. The figure which shows the structure of an example of the multistage distilled water manufacturing apparatus which concerns on this invention. Schematic of the experimental device for confirming the performance of the evaporator / condenser.
  • One of the principles of the present invention is to directly use the heat of condensation of the generated water vapor for evaporation of raw water.
  • the condensing (liquefaction) temperature increases as the pressure increases. Therefore, if the water vapor pressure is increased to increase the condensing temperature, the raw water on the low pressure side can be boiled at this temperature.
  • P the pressure
  • V the volume
  • ⁇ is said to be a specific heat ratio
  • the boiling point (condensation temperature) becomes 102.67 ° C. That is, the water vapor evaporated at 1 atm and 100 ° C. is raised to about 109 ° C. when the pressure is increased by 10% (if 1.1 atm), and is cooled to 102.67 ° C. when touching the heat transfer plate at 100 ° C. It is condensed into water while maintaining 102.67 ° C. The amount of heat released by water vapor while being cooled from 109 ° C. to 102.67 ° C. by 6.33 ° C.
  • the heat transfer coefficient at the heat transfer surface of the gas fluid is smaller than that of condensation heat transfer or boiling heat transfer, but since the amount of heat to be transferred is small, the heat transfer area up to the condensation temperature is small, and most heat transfer is performed.
  • the hot surface is used for condensation while transferring a large amount of heat during condensation to the evaporator.
  • the present invention uses this phenomenon to use the condensation of water vapor as a heat source for boiling raw water.
  • condensation and evaporation can occur simultaneously on the front and back of the metal heat transfer plate having high thermal conductivity.
  • the difference between the actual boiling temperature and boiling point is called the degree of heating, and it is desirable to make this degree of heating as small as possible and 0 to increase energy efficiency (the amount of water obtained divided by the required energy). .
  • boiling nuclei there is a method of leaving bubbles in the dents by roughening the boiling heat transfer surface or the like. As another means, it is also effective to inject gas into boiling nuclei. If pressurized steam is present as in this apparatus, this method is a very effective means, and it is preferable to employ this method. However, other boiling nuclei may be arranged or formed.
  • the evaporation / condensing device 2 that performs heat exchange between steam and high-temperature raw water is a kind of heat exchanger that includes an evaporator 10 and a condenser 11 and is partitioned by a heat transfer plate 4 therebetween.
  • a blower (turbine) 8 is provided at the uppermost part, and water vapor can be fed from the evaporator 10 to the condenser 11 while applying pressure.
  • the heat exchanger 20 described on the lower side of the evaporation / condensing device 2 in the figure is a counterflow heat exchanger for heating the raw water taken in and cooling the distilled water and the concentrated water. Distilled water and concentrated water (residual water) that have finished supplying heat are discharged.
  • the heated raw water is sent from the heat exchanger 20 to the evaporator 10.
  • the heater 30 is provided in the middle of the line which sends high temperature raw water. The heater 30 is necessary for increasing the heat in the initial operation of the apparatus.
  • the steam pipe may pass through the condenser as shown in FIG. 1 or through the outside of the condenser, but it goes without saying that heat insulation is necessary in the case of the outside.
  • the amount of steam for the boiling nuclei may be small if the water in the evaporation chamber reaches the boiling point, but if it is slightly lower than the boiling point, send more steam so that the vapor nuclei will not disappear due to condensation. Is desired.
  • FIG. 1 if a plurality of air inlets are installed so that the optimum air inlet can be selected, it is possible to select an air inlet having an appropriate temperature in the evaporator according to the operating conditions.
  • the piping valve leading to it can be opened to adjust the steam flow rate.
  • the water vapor whose energy has increased due to the compression has a heat quantity that evaporates the high-temperature water in the evaporator 10, and a portion of the water vapor is not condensed in the condenser 11 and is heated. It reaches the exchanger 20 and condenses. Distilled water and concentrated water can pass through the heat exchanger 20 to raise the raw water to a temperature near the boiling point (above 5 ° C. below the boiling point). If the heat insulation is increased so that heat does not escape to the outside, and the water vapor compression rate is increased, the heater 30 can be hardly heated when a steady state is reached after a certain period of time.
  • the pressure when the pressure is increased by 10% from 1 atm to 1.1 atm, the amount of heat of the water vapor increases by 2.99 cal / g as described above, so that water sufficient to supplement the condensate is continuously supplied from the boiling water side. If the water vapor pressure is increased by 0.1 atm, the heat retention is improved, and the overall heat loss including the loss of the heat exchanger is kept below the 3 ° C temperature drop of water, it will depend on the heater in the steady state. Distilled water can be continuously produced without heating.
  • the evaporation in the evaporator 10 and the condensation in the condenser 11 correspond to the evaporation end and the condensation end in the case of a heat pipe, and the temperature of the condensation end is higher than the temperature of the evaporation end.
  • a blower 8 such as a blower
  • the heat pipe is extremely excellent in heat transfer due to the high heat transfer between evaporation heat and condensation heat transfer, and the high speed of water vapor movement, but in the present invention, the thickness of the heat transfer plate is also reduced.
  • the material is titanium or highly corrosion-resistant stainless steel, and the thinner the thickness, the better.
  • 0.3 to 1.0 mm is generally used due to the problem of the strength of the apparatus. is there.
  • the boiling point rise due to concentration hardly changes at a concentration rate of several times.
  • the boiling point of seawater is about 0.5 ° C.
  • the boiling point of seawater concentrated twice is about 1 ° C. higher than that of pure water.
  • the condensation temperature is 111.6 ° C.
  • the water vapor condenses after the temperature has dropped by 28.2 ° C.
  • it raises to 2 atm it will rise to 170.6 degreeC and a volume will be 0.595 times.
  • the condensation temperature at this time is 120.4 ° C.
  • the water vapor will condense after the temperature drops by 50.2 ° C., and the amount of heat released at this time is calculated using a constant pressure specific heat of 1.95 J / g ⁇ ° C.
  • FIG. 2A shows an assembling configuration of an example of an apparatus for producing distilled water and concentrated water according to the present invention.
  • the apparatus for producing distilled water and concentrated water according to the present invention can be produced by combining commercially available heat exchangers, pipes, pumps and the like.
  • the actual device needs to be easy to operate and easy to maintain. Therefore, the blower 8 was disconnected from the evaporation / condensing device 2.
  • the configuration of the distilled water and concentrated water manufacturing apparatus 1 shown in FIG. 2A will be described according to the flow of raw water, distilled water, and water vapor.
  • the flow of cold water (including raw water and distilled water) is indicated by thin solid arrows
  • the flow of hot water (including raw water and distilled water) is indicated by thick solid arrows
  • the flow of water vapor is indicated by dashed arrows.
  • the structure of the manufacturing apparatus 1 of the shown distilled water and concentrated water is demonstrated according to the flow of raw
  • the flow of cold water (including raw water and distilled water) is indicated by thin solid arrows
  • the flow of hot water (including raw water and distilled water) is indicated by thick solid arrows
  • the flow of water vapor is indicated by dashed arrows.
  • the raw water 40 can be natural water such as fresh water such as river water, sea water, salt water such as salt water lake water, and the like.
  • concentration is not only to concentrate useful substances, such as obtaining concentrated seawater and salt lake water for salt production, but also to contain hazardous heavy metals or hazardous substances that exceed environmental standards.
  • the treatment load of treated water may be reduced.
  • Raw water 40 is fed into the apparatus by a supply means (not shown) such as a pump.
  • a supply means such as a pump.
  • the speed at which water vapor condenses varies greatly depending on whether or not non-condensable gas is contained in the water vapor. Therefore, it is desirable to remove (degas) in advance a non-condensable gas (air component) that lowers the condensation rate in order to efficiently condense.
  • the degassing device 22 a method for depressurizing low-temperature raw water with a vacuum pump to release dissolved gas has already been established. Therefore, it is convenient and preferable to use these devices, but other devices may be used. .
  • the heat exchangers 24 and 26 for raising the temperature of the raw water are arranged in two or more stages, and gas bubbles separated at an intermediate temperature are collected. A method may be adopted.
  • the raw water is divided into heat exchangers 24 and 26 and flows.
  • heat is exchanged with distilled water discharged from the condenser of the evaporation / condensing device 2, and the temperature of the raw water is heated to a temperature that is 5 ° C. lower than the boiling point.
  • the reason why the temperature is set to 5 ° C. is that a calorie of 5 cal / g is necessary to raise the temperature from this temperature to the boiling point, and a calorie of 10 cal / g is necessary for the produced water when the gas-liquid separation rate is 50%. This is because the energy efficiency is lowered when the temperature is lowered by 5 ° C. or more from the boiling point.
  • the compression corresponding to the calorie of 5 cal / g is pressurized from 1. atm to 1.172 atm, and from 0.5 atm to 0.586 atm.
  • heat exchanger 26 heat exchange is performed with the concentrated water (residual water) discharged from the gas-liquid separator 6, and the temperature of the raw water is heated to a temperature that is 5 ° C. lower than the boiling point of the raw water. .
  • heat exchangers 24 and 26 used for exchanging heat between raw water and high-temperature distilled water and concentrated water, counter-flow type heat exchangers are desirable, and plate type heat exchangers are particularly suitable.
  • the heat exchanger is not limited.
  • the temperature difference between the primary and secondary sides can be as low as 1 ° C, and operation is possible at a temperature difference of 2 to 3 ° C. .
  • the degassed raw water approaches the boiling temperature near the outlet of the heat exchanger, but when the pressure difference is large and the temperature on the condenser side is high, condensed water higher than the boiling temperature flows into the heat exchanger, It is also possible to start boiling before entering the evaporator.
  • Hot water for heat exchange includes concentrated water (residual water) and distilled water so that they are not mixed.
  • two plate-type heat exchangers are used, but three or more may be used, or a partition plate (a blind plate) that divides the flow path by one can be attached, Alternatively, other methods can be adopted.
  • the raw water heated by the heat exchangers 24 and 26 merges and passes through the heating heater 30 and enters the evaporation / condensing device 2 from the high-temperature raw water inflow line 12, but the heater 30 hardly works after the steady state. May be.
  • the heater 30 hardly works after the steady state. May be.
  • at least a part of the raw water is evaporated by being heated by the condensation heat of water vapor in the evaporator.
  • the water vapor generating heater 32 is used to generate water vapor at the time of start-up, this heater may be hardly operated when the steady state is reached.
  • the gas-liquid separator 6 separates the water vapor and the concentrated water, and the concentrated water is sent from the concentrated water discharge line 16 to the heat exchanger 26 for heat recovery and cooled.
  • the steam is pressurized by a turbine type blower (blower) 8 and sent to the condenser of the evaporator / condenser 2, and the produced distilled water is discharged from the distilled water discharge line 14 and sent to the heat exchanger 24. It is done.
  • the pressure of water vapor is preferably 1.01 to 2.0, depending on the type of raw water. If it is atmospheric pressure, it corresponds to a pressure of 0.01 to 1.0 atm. The reason for this is that if the pressure under atmospheric pressure is 0.01 atm or less, even if it is distillation of fresh water, the pressure is practically too low, and the temperature difference between the condenser and the evaporator is small, so the distilled water production capacity is low. Because.
  • the greater the pressurization the greater the temperature difference between the condenser and the evaporator, the faster the condensation rate and the evaporation rate, and the higher the production rate of distilled water, but at pressures where the pressure ratio of pressurization exceeds 2.0. This is because the energy to raise the water by 20 ° C. or more is supplied, and the energy cost increases.
  • the pressurization is reduced, and if the demand for water increases and the supply capacity is no longer sufficient, a flexible operation for increasing the pressurization is possible.
  • the plate heat exchanger can be easily disassembled and inspected, and the direction of the fluid can be easily changed. Therefore, it is preferable that the line (flow path) through which raw water flows and the line (flow path) through which distilled water or concentrated water flows can be exchanged. After the operation is stopped and cleaned, the scale attached to the raw water side dissolves in the hot water by flowing hot water through the flow path where the raw water flows, and then flowing the raw water through the flow path on the hot water side. There is no need, and maintenance becomes easy.
  • the boiling portion of the evaporator may be at atmospheric pressure or may be depressurized. At atmospheric pressure, there is an advantage that there are few problems of strength of the apparatus. However, since the boiling temperature is 100 ° C. at atmospheric pressure, heat loss is more likely to occur than in the case of reduced pressure, and when corrosive seawater is used as raw water, the corrosion resistance of the material constituting the heat exchanger is only high. However, the material cost is slightly increased. Lowering the pressure enables distillation at a low temperature, and the scale adhesion to the equipment is not strong, the amount is small, and there is an advantage of less heat loss, but the distillation rate is reduced, or a vacuum pump for decompression There is a problem that is necessary.
  • FIG. 2B shows an example in which two plate heat exchangers 3 as evaporation / condensation devices are connected, and pressurized steam as boiling nuclei can be blown into the connecting portion through the steam pipe 17.
  • the evaporation / condensing device 2 is a plate heat exchanger, a partition plate (a blind plate) that divides the flow path by a single unit can be attached.
  • FIG. 3 shows an example of an apparatus according to the present invention in which evaporation / condensing apparatuses are combined in multiple stages.
  • Each set includes an evaporating / condensing device 2, 2 ', 2 ", a gas-liquid separating device 6, 6', 6", a blower 8, 8 ', 8 “, and a distilled water discharge line 14, 14', 14".
  • the high-temperature raw water heated by the heat exchanger flows into the first stage evaporation / condensing device 2 from the high-temperature raw water inflow line 12, having the concentrated water discharge lines 16, 16 ′, 16 ′′.
  • the concentrated water discharged from the first-stage and second-stage gas-liquid separators 6 and 6 ' is introduced as raw water into the second-stage and third-stage evaporator / condenser 2, 2' and 2 ", respectively.
  • the concentrated water discharged from the third-stage gas-liquid separator 6 ′′ and the distilled water discharged from each stage of the evaporating / condensing devices 2, 2 ′, 2 ′′ are sent to a heat exchanger to preheat raw water. Heat exchange is performed.
  • the concentrated water discharged from the gas-liquid separators 6 and 6 ′ does not need to be preheated because of high temperature.
  • FIG. 3 the concentrated water discharged from the gas-liquid separators 6 and 6 ′ does not need to be preheated because of high temperature.
  • the evaporator / condenser is combined in three stages, but the combination may be two stages, or four or more stages.
  • the efficiency can be increased by introducing steam as boiling nuclei.
  • the concentrated water remaining after distillation such as seawater is concentrated to saturation, the boiling point rises by about 10 ° C., so that it becomes necessary to increase the applied pressure and the energy consumption increases.
  • the concentration rate should be about 2 to 8 times, considering that increasing the concentration of the concentrated water is disadvantageous in terms of energy, and recovering the heat of the concentrated water with a heat exchanger. It is.
  • the concentration rate can be increased 9 times even in 2 stages of about 3 times, and the efficiency is increased.
  • concentrated water remaining after distillation such as seawater
  • the concentration process is divided into two or more as shown in FIG. 3 is advantageous. .
  • the higher the degree of concentration and the higher the pressure required the smaller the amount of water, so a smaller heat exchanger is required, and the energy efficiency is increased by the multi-stage.
  • the degree of concentration increases, clogging due to salt precipitation is more likely to occur.
  • the cost of the apparatus, the cost of maintenance, and the like are reduced as a whole, such as taking measures for clogging only at the final stage.
  • distilled water and / or concentrated water With the apparatus and method for producing distilled water and / or concentrated water according to the present invention, it is possible to obtain distilled water with low energy use by an apparatus that is easy to maintain. Low-cost water can be obtained from use to use as industrial high-purity water. Compared with the reverse osmosis membrane method, energy efficiency can be increased and maintenance is easy. Concentrated water can be produced at a lower cost than ever for wide use such as production of concentrated seawater as a salt production raw material and pretreatment of various water treatments. Use of both distilled water production equipment and method and concentrated water production equipment and method is desirable from the viewpoint of energy efficiency, but it is sufficient to use either one according to the user's environment and necessity. Of course, only one of them can be used.
  • the evaporator 10 is a stainless steel cylinder having an outer diameter of 122 mm, an inner diameter of 121 mm, and a height of 400 mm. In order to secure a flow path width of about 5 mm inside, the upper part having a diameter of 111 mm and a height of 300 mm is rounded.
  • a stainless steel cylinder (inner cylinder) 5 was fixed at several points in a state where it was floated 5 mm from the bottom.
  • a blower 8 was attached to the evaporator outlet portion of about 100 mm above the cylindrical container 5 in the condenser. Water droplets contained in the steam were collected by a mist trap 9 installed at the top of the evaporator and returned to the evaporator wall.
  • a condenser 11 having an inner diameter of about 180 mm and a height of 430 mm was arranged on the outside so as to wrap the entire blower 8 and the evaporator, and a heat insulating material was arranged around the condenser 11 and necessary places on the piping.
  • reference numeral 35 denotes a pressure gauge
  • four steam pipes 17 are attached to the evaporator in the circumferential direction at a position about 1/5 from the bottom of the evaporator height.
  • the steam pipe 17 was provided with an adjustment valve and adjusted in advance so that a small amount of steam passed.
  • the heat exchanger 20 is not used, but instead, the raw water at a desired temperature can be supplied to the evaporator 4 from the raw water tank 27 with a temperature controller. .
  • Distilled water produced by the condenser was discharged from the outlet pipe, cooled by the cooler 29, led to the distilled water reservoir 39, and the amount of distilled water produced was measured by a weigh scale 47 '. Further, the raw water tank 27 with temperature controller and the raw water flow rate control valve 43 are connected by a soft silicone rubber hose so that the weight of the raw water including the tank can be measured. Regarding the pressure, the condensation side was set to atmospheric pressure, and the inside of the evaporator could be lowered to 0.8 atm by adjusting the input voltage of the blower (turbine) 8 and the raw water flow rate adjusting valve 43. In the test, the following results were obtained when the inside of the evaporator was 0.9 atm and the inside of the condenser was 1 atm.
  • thermometer 36 and the thermometer 36 in the condenser indicate 100 ° C, and water vapor comes out of the pressure relief valve 18.
  • the steam supply valve 32 is closed and the raw water weight is measured by the weigh scale 47.
  • the blower 8 is operated to adjust the voltage of the blower motor so that the evaporator internal pressure becomes 0.9 atm, and the flow rate adjusting valve 43 is opened little by little to supply 97 ° C. raw water into the evaporator.
  • the pressure in the evaporator slightly approaches 1 atm, but the raw water at 97 ° C.
  • the flow control valve 43 Thin until just before closing. Then, the pressure in the evaporator almost returns to 0.9 atm, and a flow 38 of distilled water can be observed. At this time, the distilled water flow rate adjusting valve 44 is opened so as not to disturb the flow of distilled water. (7) Thereafter, the flow rate adjustment valve 43 is adjusted so that the total weight of the raw water and the distilled water becomes equal. This is to keep the water level in the evaporator constant.
  • the heat transfer areas were about 0.05 m 2 and 0.1 m 2 , and about 1.6 liters / h and 3 liters / h with an energy input of 240 to 250 W / h for this heat transfer area. Distilled water was obtained. It was also found that even when water having a temperature lower by 1 to 2 ° C. than the boiling point was sent to the evaporator, it was heated to the boiling point by the heat from the condenser, and distilled water having the same level as that at the boiling point was obtained.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Hydrology & Water Resources (AREA)
  • Engineering & Computer Science (AREA)
  • Environmental & Geological Engineering (AREA)
  • Water Supply & Treatment (AREA)
  • Organic Chemistry (AREA)
  • Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
  • Heat Treatment Of Water, Waste Water Or Sewage (AREA)

Abstract

L'invention porte sur un procédé et sur un dispositif de fabrication d'eau distillée et/ou d'eau concentrée à partir d'eau brute. Le procédé de fabrication comprend (i) une étape de distribution d'eau brute, dont la température est supérieure ou égale à une température inférieure de cinq degrés au point d'ébullition, à un évaporateur, (ii) une étape d'évaporation d'au moins une partie de l'eau brute sous forme de vapeur d'eau dans l'évaporateur, (iii) une étape de décharge d'eau concentrée, (iv) une étape de mise sous pression de la vapeur d'eau de telle sorte que la pression de la vapeur d'eau devient 1,01 à 2 fois supérieure à la pression dans l'évaporateur, de telle sorte que la température de condensation de la vapeur d'eau devient supérieure au point d'ébullition de l'eau brute, et (v) une étape de condensation de la vapeur d'eau pressurisée dans un condenseur pour transformer la vapeur d'eau en eau distillée. L'évaporateur et le condenseur sont séparés par une plaque de transfert de chaleur, et l'eau brute est amenée à ébullition dans l'évaporateur par transfert de la chaleur de condensation, générée par la condensation de la vapeur d'eau dans le condenseur, du condenseur à l'évaporateur par l'intermédiaire de la plaque de transfert de chaleur.
PCT/JP2009/065229 2008-09-04 2009-09-01 Procédé éco-énergétique et dispositif de fabrication d'eau distillée et/ou d'eau concentrée WO2010026953A1 (fr)

Priority Applications (1)

Application Number Priority Date Filing Date Title
JP2010527781A JPWO2010026953A1 (ja) 2008-09-04 2009-09-01 エネルギー効率の高い蒸留水及び／又は濃縮水の製造方法と装置

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
JP2008227249 2008-09-04
JP2008-227249 2008-09-04

Publications (1)

Publication Number Publication Date
WO2010026953A1 true WO2010026953A1 (fr) 2010-03-11

Family

ID=41797121

Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/JP2009/065229 WO2010026953A1 (fr) 2008-09-04 2009-09-01 Procédé éco-énergétique et dispositif de fabrication d'eau distillée et/ou d'eau concentrée

Country Status (2)

Country Link
JP (1) JPWO2010026953A1 (fr)
WO (1) WO2010026953A1 (fr)

Cited By (12)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JP2012200661A (ja) * 2011-03-25 2012-10-22 M Hikari Energy Kaihatsu Kenkyusho:Kk 気圧差を利用した脱水方法及び真水の回収装置
JP2014516780A (ja) * 2011-05-16 2014-07-17 ピエール、マルヴィン 水圧式脱塩装置および方法
JP2014188399A (ja) * 2013-03-26 2014-10-06 Ihi Corp 海水の淡水化システム及び方法
KR20140133517A (ko) * 2012-01-11 2014-11-19 후이 멍 창 정수용 방법 및 장치
CN104709953A (zh) * 2014-12-15 2015-06-17 北京理工大学 热能梯级利用的多级回热加湿除湿海水淡化装置
JPWO2014196610A1 (ja) * 2013-06-05 2017-02-23 大川原化工機株式会社 海水淡水化装置および海水淡水化方法
JPWO2014196611A1 (ja) * 2013-06-05 2017-02-23 大川原化工機株式会社 濃縮装置および濃縮方法
JP2018122266A (ja) * 2017-02-02 2018-08-09 鹿島環境エンジニアリング株式会社 濃縮システム及び濃縮方法
EP3351512A3 (fr) * 2011-09-09 2018-10-17 Sylvan Source, Inc. Purification et dessalement d'eau industrielle
WO2019086979A1 (fr) * 2017-10-30 2019-05-09 Chandan Kumar Évaporateur à compression de vapeur mécanique sans chaudière
WO2020045662A1 (fr) * 2018-08-30 2020-03-05 国立大学法人佐賀大学 Échangeur de chaleur
JP2021505370A (ja) * 2017-12-05 2021-02-18 ダブリュージーエイ ウォーター グローバル アクセス ソシエダッド デ レスポンサビリダッド リミターダ 低圧縮比を有する機械的蒸気圧縮装置

Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPS6125601A (ja) * 1984-07-14 1986-02-04 Hitachi Kiden Kogyo Ltd 有機溶剤の回収方法及びその装置
JPH0263592A (ja) * 1988-08-31 1990-03-02 Hitachi Ltd 蒸留装置
JP2005205337A (ja) * 2004-01-23 2005-08-04 Taikisha Ltd 廃水処理設備

Patent Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPS6125601A (ja) * 1984-07-14 1986-02-04 Hitachi Kiden Kogyo Ltd 有機溶剤の回収方法及びその装置
JPH0263592A (ja) * 1988-08-31 1990-03-02 Hitachi Ltd 蒸留装置
JP2005205337A (ja) * 2004-01-23 2005-08-04 Taikisha Ltd 廃水処理設備

Cited By (17)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JP2012200661A (ja) * 2011-03-25 2012-10-22 M Hikari Energy Kaihatsu Kenkyusho:Kk 気圧差を利用した脱水方法及び真水の回収装置
JP2014516780A (ja) * 2011-05-16 2014-07-17 ピエール、マルヴィン 水圧式脱塩装置および方法
EP3351512A3 (fr) * 2011-09-09 2018-10-17 Sylvan Source, Inc. Purification et dessalement d'eau industrielle
KR102212070B1 (ko) * 2012-01-11 2021-02-05 후이 멍 창 정수용 방법 및 장치
KR20140133517A (ko) * 2012-01-11 2014-11-19 후이 멍 창 정수용 방법 및 장치
JP2015518412A (ja) * 2012-01-11 2015-07-02 チャン, フエイメンCHANG, Huei Meng 浄水の方法および装置
JP2014188399A (ja) * 2013-03-26 2014-10-06 Ihi Corp 海水の淡水化システム及び方法
JPWO2014196610A1 (ja) * 2013-06-05 2017-02-23 大川原化工機株式会社 海水淡水化装置および海水淡水化方法
JPWO2014196611A1 (ja) * 2013-06-05 2017-02-23 大川原化工機株式会社 濃縮装置および濃縮方法
US10294122B2 (en) 2013-06-05 2019-05-21 Ohkawara Kakohki Co., Ltd. Seawater desalination device and seawater desalination method
CN104709953A (zh) * 2014-12-15 2015-06-17 北京理工大学 热能梯级利用的多级回热加湿除湿海水淡化装置
CN104709953B (zh) * 2014-12-15 2023-03-21 北京理工大学 热能梯级利用的多级回热加湿除湿海水淡化装置
JP2018122266A (ja) * 2017-02-02 2018-08-09 鹿島環境エンジニアリング株式会社 濃縮システム及び濃縮方法
WO2019086979A1 (fr) * 2017-10-30 2019-05-09 Chandan Kumar Évaporateur à compression de vapeur mécanique sans chaudière
JP2021505370A (ja) * 2017-12-05 2021-02-18 ダブリュージーエイ ウォーター グローバル アクセス ソシエダッド デ レスポンサビリダッド リミターダ 低圧縮比を有する機械的蒸気圧縮装置
JP7333522B2 (ja) 2017-12-05 2023-08-25 ダブリュージーエイ ウォーター グローバル アクセス ソシエダッド デ レスポンサビリダッド リミターダ 低圧縮比を有する機械的蒸気圧縮装置
WO2020045662A1 (fr) * 2018-08-30 2020-03-05 国立大学法人佐賀大学 Échangeur de chaleur

Also Published As

Publication number Publication date
JPWO2010026953A1 (ja) 2012-02-02

Similar Documents

Publication Publication Date Title
WO2010026953A1 (fr) Procédé éco-énergétique et dispositif de fabrication d'eau distillée et/ou d'eau concentrée
El-Dessouky et al. Plastic/compact heat exchangers for single-effect desalination systems
WO2011085669A1 (fr) Appareil de séparation à distillation provoquée par une chaleur à basse température pour évaporer une solution aqueuse sous une pression négative et procédé pour obtenir de l'eau distillée
JP2011050860A (ja) 含水有機物の無水化方法
CN201587871U (zh) 多级真空蒸馏海水淡化装置
US7811420B2 (en) Isothermal gas-free water distillation
KR101402482B1 (ko) 소형선박 부착용 해수 담수화장치
AU2005284554A1 (en) Seawater desalination plant
JP2013523439A (ja) 蒸気吸収システム
CN201834781U (zh) 单级真空蒸馏海水淡化装置
WO2011135724A1 (fr) Dispositif de production d'un liquide pur
US9345986B2 (en) Method for evaporation and possible distillation of fluids using a heat pump
US3300392A (en) Vacuum distillation including predegasification of distilland
JP5975208B2 (ja) 海水の淡水化装置及びこれを用いた海水の淡水化方法
JP6199428B2 (ja) 過熱水蒸気発生器
US11465068B2 (en) Multi-stage flash (MSF) reversal system and method
US9441279B2 (en) Maple or birch water evaporator system
CN102115221B (zh) 可在线调节产水量的低温多效海水淡化装置
CN206108947U (zh) 一种高效海水淡化装置
CN215946814U (zh) 一种海水淡化系统
TW201315687A (zh) 海水淡化裝置
JPS6142390A (ja) ボイラ給水製造法
CN201952319U (zh) 可在线调节产水量的低温多效海水淡化装置
CN214512757U (zh) 一种基于热平衡原理的多联式热泵蒸发浓缩系统
CN207324110U (zh) 降膜蒸发系统及其真空装置

Legal Events

Date Code Title Description
121 Ep: the epo has been informed by wipo that ep was designated in this application

Ref document number: 09811479

Country of ref document: EP

Kind code of ref document: A1

WWE Wipo information: entry into national phase

Ref document number: 2010527781

Country of ref document: JP

NENP Non-entry into the national phase

Ref country code: DE

122 Ep: pct application non-entry in european phase

Ref document number: 09811479

Country of ref document: EP

Kind code of ref document: A1