CN1297491C - Method and equipment for solution separation and seawater desalination - Google Patents
Method and equipment for solution separation and seawater desalination Download PDFInfo
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- CN1297491C CN1297491C CNB021567174A CN02156717A CN1297491C CN 1297491 C CN1297491 C CN 1297491C CN B021567174 A CNB021567174 A CN B021567174A CN 02156717 A CN02156717 A CN 02156717A CN 1297491 C CN1297491 C CN 1297491C
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- 238000004821 distillation Methods 0.000 claims abstract description 85
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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
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- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
- Heat Treatment Of Water, Waste Water Or Sewage (AREA)
Abstract
The invention relates to a constant temperature distillation method, a multistage vacuum distillation, cooling and icing solution separation and seawater desalination method and equipment using the method, the method utilizes a multistage vacuum distillation device, a multistage vacuum cooling device and a multistage vacuum icing device, under the initial state, the constant temperature distillation method, a liquid discharge vacuum icing method, solution transfer and regeneration of a thermal cycle solution are matched to separate the solution, the temperature of each stage of vacuum distillation is set according to the temperature gradient of the thermal cycle solution, the solution is separated into the multistage vacuum distillation, certain energy is recycled for repeated use, in order to increase the stage number of the vacuum distillation, the temperature of the thermal cycle solution flowing out from the last stage of the multistage vacuum distillation is reduced, therefore, the multistage vacuum cooling and the multistage vacuum icing are utilized to assist the multistage vacuum distillation, the thermal cycle of evaporation and condensation is kept balanced, the method and the equipment can reduce the cost of seawater desalination.
Description
Technical field
The present invention relates to a kind of constant temperature distillation method, and use the multilevel vacuum distilling, cooling of this method, icing solution separating and sea water desaltination and equipment thereof, particularly relate to a kind of vacuum environment that vacuum vessel provided of utilizing liquid-discharge vacuumizing method to produce, make de-gassed solution through liquid gas interface or liquid-solid interface and with de-gassed solution evaporation, cooling, and the multilevel vacuum distilling that freezes, cooling, the method for icing solution separating and the method and the equipment thereof of sea water desaltination.
Background technology
Conventional solution separating technology is widely used in concentrating or the fields such as desalination of seawater of general distillation, soup, and this technology belongs to the separation of solution.
When a large amount of soln using heating method being separated, will consume suitable energy for achieving the above object, and uneconomical.For example, in the water desalination, direct heating makes the moisture in the solution become steam, extracting steam out with vacuum pump, need like this to consume very big energy, and salinity will constantly improve in the moisture separating process, need continuous energy input moisture could be separated, this kind mode is very uneconomical.
Again, the various salt crystallizations that produced in high-temperature heating process will produce scale problems in processing procedure, cause the efficient of distiller greatly to descend, and cause the isolated moisture of energy limited, do not meet the demand of a large amount of uses.
This shows that above-mentioned ordinary method still has many defectives, demand urgently being improved.
Summary of the invention
The objective of the invention is to solute concentrates.Do not expending the too much energy and using under the principle of lower temperature range, utilize the multilevel vacuum distilling device, implement liquid-discharge vacuumizing method with de-gas liq, make container for evaporation produce vacuum, because of the temperature of vacuum distilling and the use range increase of pressure, so the progression of vacuum distilling is increased, cooperate the constant temperature distillation method, the transmission of solution, and the regeneration of thermal cycle solution, solution is separated and reclaim certain energy and do to use repeatedly, set the temperature of vacuum distillings at different levels according to the thermograde of thermal cycle solution, make the multilevel vacuum distilling that is separated into of de-gassed solution, then the isolating solution of unit energy is improved, and the cryogenic strong solution of its discharge is made further solute with vacuum freeze-drying method and concentrated.
An of the present invention order is to reduce Cost of seawater desalination.Use range increase because of temperature and pressure, help to increase the progression of vacuum distilling, and then the quantum of output of increase water, on the other hand, because evaporation of water heat is about 7 times of heat of solidification, so the method for freezing consumes less energy and produces identical finished product water, the ice crystal of icing low temperature concentrated seawater that produces of multi-stage vacuum and thawing can effectively reduce the temperature of the thermal cycle solution of multilevel vacuum distilling last step discharge, the progression of vacuum distilling is increased, increase the quantum of output of water, at last, cryogenic thermal cycle solution reclaims vaporization heat according to the mode that progression successively decreases, make certain energy do to use repeatedly, the icing required low temperature seawater of multi-stage vacuum is from multi-stage vacuum refrigerative last step, and the icing ice crystal that produces of multi-stage vacuum is to be melted by the steam that multilevel vacuum distilling and multi-stage vacuum cooling produce, therefore in conjunction with multilevel vacuum distilling, the multi-stage vacuum cooling, and multi-stage vacuum freezes and can effectively reduce Cost of seawater desalination.
Another object of the present invention is at the soil cost that reduction is founded the factory.Multilevel vacuum distilling, the multi-stage vacuum cooling, and the icing de-gassed solution of multi-stage vacuum, steam, the conduit of flowing through with condensation water, container for evaporation, distiller, and the container that freezes is to utilize liquid-discharge vacuumizing method to make it produce vacuum, liquid-discharge vacuumizing method is a vacuum principle of utilizing the pressure support liquid height that drags Li Qieli, therefore the container for evaporation or the icing container of the first step are folded on the second stage, fold on the third stage second stage, be stacked into a tower shape mutually with this, to increase the difference of altitude of low level container and annex and container for evaporation or icing container, therefore reduce the land area of founding the factory and using, and reduce the required energy of generation vacuum.The cooling of the multilevel vacuum distilling of tower shape, multi-stage vacuum, and multi-stage vacuum freeze make thermal cycle solution, solution (seawater), and agglomerative finished product water all constantly flow, can reduce the usage quantity of pump, and reduce fouling and corrosion.
For achieving the above object, the present invention adopts a kind of constant temperature distillation and equipment thereof, and wherein, the constant temperature distillation utilizes constant temperature distillation unit to realize that described constant temperature distillation method comprises:
Implement liquid-discharge vacuumizing method with de-gas liq, set described constant temperature and distill unitary original state, the described constant temperature that described de-gassed solution, steam and condensation water are flowed through distills unitary conduit, container for evaporation and distiller and produces vacuum and airtight;
Close the flow control valve of described container for evaporation, in the container for evaporation of this vacuum, inject described de-gassed solution and reach suitable height;
Set the temperature of the vacuum distilling of described container for evaporation, make described de-gassed solution carry out explosive evaporatoin under the temperature of this vacuum distilling, the setting of described temperature should be lower than described de-gassed solution and flow into the temperature that described container for evaporation and thermal cycle solution flow into the liquid gas interface in the described container for evaporation;
Described de-gassed solution and described thermal cycle solution continue to flow into and flow out described container for evaporation and described liquid gas interface respectively, when described container for evaporation continue to produce steam and reach the saturated vapour pressure of temperature of this vacuum distilling, beat and to rise the steam that described flow control valve produces described container for evaporation and enter in the distiller, make the pressure in the described container for evaporation keep stable;
If the effusive temperature of described de-gassed solution or described thermal cycle solution is lower than the temperature of vacuum distillation, adjust described flow control valve, reduce the output of steam, if its temperature is higher than the temperature of vacuum distilling, adjust described flow control valve, increase the output of steam;
Described thermal cycle solution flows through described distiller, reclaim vaporization heat and elevate the temperature, therefore, when described thermal cycle solution provides vaporization heat at the described liquid gas interface of inflow, its temperature is higher than the temperature when flowing through described distiller and reclaiming vaporization heat, so that provide vaporization heat to described container for evaporation, make the working temperature of described container for evaporation be higher than the working temperature of described distiller, cause evaporation and agglomerative thermal cycling to keep balance;
Entering the condensation water that the steam in the described distiller produces after condensing is recovered.
In the air that remains in described de-gassed solution continues to be accumulated in conduit that de-gassed solution, steam and condensation water flow through, container for evaporation, distiller, and during the temperature of the vacuum distilling of the described de-gassed solution of its pressure influence, implement liquid-discharge vacuumizing method with de-gassed solution once more, make described constant temperature distill unitary conduit, container for evaporation and distiller and recover vacuum tightness, reach this constant temperature distillation and lead the original state that the unit is set.
The equipment of realizing above-mentioned constant temperature distillation is the constant temperature distillation unit of constant temperature distillation method, and described constant temperature distillation unit comprises:
One container for evaporation, described container for evaporation is connected with distiller with the conduit that condenses, and the steam of generation is imported in the distiller;
One flow control valve is located at the appropriate location of the described conduit that condenses, and depresses at the saturation steam of the temperature of the vacuum distilling of described setting when described container for evaporation, controls the output of the steam of described container for evaporation, and keeps the pressure in the described container for evaporation;
One liquid gas interface, described liquid gas interface is located in the described container for evaporation, and the thermal cycle solution that vaporization heat is provided flows into and the outflow liquid gas interface with same traffic via described conduit and by-pass valve control thereof, and see through the caloic conduction of liquid gas interface, make the de-gassed solution evaporation in the described container for evaporation;
One distiller, described distiller is to reclaim the thermal cycle solution of vaporization heat, through described conduit and by-pass valve control, in same traffic inflow and outflow distiller, absorb the vaporization heat of the steam of described container for evaporation generation, improving its temperature, and condensing vapour is condensation water, and permanent set liquid enters in the vacuum vessel and reclaims;
One low level container and annex thereof, it utilizes a plurality of conduits and by-pass valve control under suitable difference of altitude, make de-gassed solution, steam, and the condensation water described conduit of flowing through, container for evaporation, and distiller produce vacuum;
Wherein, each flows into certain flow and flows out described container for evaporation the de-gassed solution of certain temperature through described conduit and by-pass valve control thereof.
Implement the multilevel vacuum distilling device of described constant temperature distillation method, it comprises:
One pre-process equipment is the well heater that de-gassed solution and thermal cycle solution is heated to a design temperature respectively;
One multilevel vacuum distilling tower, be to be formed with the mutual storehouse of the mode of tower shape by the constant temperature of a plurality of above-mentioned vacuum distillings distillation unit, the first step is folded on the second stage, and fold on the third stage second stage, be stacked into a tower shape mutually with this, the inflow of its correspondence and effusive conduit interconnect;
One rearmounted treatment facility, comprise the vacuum vessel, the heat exchanger that reduces the temperature of the effusive thermal cycle solution of last step that reclaim condensation water and strong solution, keep reclaiming the constant temperature distillation unit of heat exchanger, a plurality of vacuum distillings of temperature of the vacuum vessel of condensation water shares a low level container and annex thereof, so that the recycle pump of generation vacuum and thermal cycle solution.
The multilevel vacuum distilling device is being set under the original state, cooperate the constant temperature distillation method, the transmission of solution, and the regeneration of thermal cycle solution, and with solution separating, set the temperature of vacuum distillings at different levels according to the thermograde of thermal cycle solution, make the multilevel vacuum distilling that is separated into of solution, after the temperature that reduces the effusive thermal cycle solution of last step, the mode of successively decreasing again according to progression, continuously flow into and flow out distiller at different levels, to reclaim vaporization heat, make its temperature successively decrease with progression and increase progressively, do to use to reclaim certain energy repeatedly, for the progression that makes vacuum distilling increases, and then the isolating solution of unit energy is improved, then increase the use range of the temperature of thermal cycle solution, just the temperature of the effusive thermal cycle solution of last step of multilevel vacuum distilling is lower, then the progression of multilevel vacuum distilling the more, therefore must reduce the temperature of the effusive thermal cycle solution of last step with more cryogenic solution, just can make evaporation and agglomerative thermal cycling keep balance, therefore utilize icing the assisting of multi-stage vacuum cooling and multi-stage vacuum as multilevel vacuum distilling, when multi-stage vacuum refrigerating unit and the multi-stage vacuum device that freezes is being set under the original state, cooperate the constant temperature distillation method, the transmission of solution and the discharge opeing vacuum method of freezing, and solution is done icing the separation, the multi-stage vacuum cooling is vacuum transpiration cooling effect, the temperature of solution is reduced, with the cryogenic fluid that freezes as multi-stage vacuum, and the cost of saving precooling, the freeze heat of solidification of required melted ice crystal of multi-stage vacuum is the steam that produces from multilevel vacuum distilling and multi-stage vacuum cooling, or the heat energy of condenser discharge, and the ice crystal of low temperature strong solution that multi-stage vacuum freeze to produce and thawing can be used to reduce the temperature of the effusive thermal cycle solution of last step of multilevel vacuum distilling, therefore the cooling of multilevel vacuum distilling and multi-stage vacuum can be combined into the method for a solution separating with multi-stage vacuum, with as sea water desaltination and the spissated method of solute.
Implement liquid-discharge vacuumizing method with de-gas liq, make de-gassed solution, steam, reach the conduit that condensation water is flowed through, container for evaporation, container freezes, and distiller produces vacuum, its pressure for the saturated vapor pressure of the temperature of using this liquid and very small amount of air pressure with, the constant temperature distillation method of utilizing boiling point of liquid to increase with pressure, the thermograde of gradable use thermal cycle solution, make it become multilevel vacuum distilling, its distillation temperature and pressure increase progressively with progression and successively decrease, therefore increase heat transfer area and condensation water, the thermal cycle solution of certain temperature, according to the progression incremental manner, continuously flow into and flow out the liquid gas interface of container for evaporation at different levels, provide vaporization heat to make the de-gassed solution evaporation, after the temperature of the thermal cycle solution that reduces its last step discharge, according to the progression mode of successively decreasing, continuously flow into and flow out distiller at different levels, to reclaim vaporization heat, and be liquid with devaporation, its temperature is successively decreased with progression and is increased progressively, make certain energy do to use repeatedly, flow at last in the well heater of thermal cycle solution, be heated to the temperature of setting, finish cycling program one time, because the temperature head build-up of pressure of container for evaporation of each grade and distiller is poor, the steam that container for evaporation is produced flows toward distiller, continue to be lower than the temperature of container for evaporation when the temperature of distiller, what then distiller continued is liquid with devaporation, its condensation water and steam compile the lower temperature that flows into next stage, the distiller of low pressure continues to do cooling and condense, permanent set liquid is collected to keep cryogenic vacuum vessel, so evaporation and agglomerative thermal cycling can be kept balance, de-gassed solution is according to the progression incremental manner, continuously flow into and flow out container for evaporation at different levels, the strong solution that its last step is discharged can be utilized vacuum freeze-drying method to make further solute and concentrate.
The multi-stage vacuum cooling is the temperature that vacuum transpiration cooling principle reduces solution, with the cryogenic fluid that freezes as multi-stage vacuum, cooperate the constant temperature distillation method, the de-gassed solution of normal temperature is according to the progression incremental manner, continuously flow into and flow out container for evaporation at different levels, therefore its temperature increases progressively with progression and successively decreases, and the steam that the multi-stage vacuum cooling produces can be used to melt the ice crystal that multi-stage vacuum freezes and produces.Wherein, the liquid that de-gassed solution can obtain after the degassing for general mixing solutions such as lean solution, soup etc., or the liquid that after the degassing, obtains for seawater.
The icing required cryogenic fluid of multi-stage vacuum is to cool off from multi-stage vacuum, the transmission of conjugate solutions, the discharge opeing vacuum method of freezing, and the heat extraction of condenser, make the container that freezes produce ice crystal, and the icing cryogenic strong solution of being discharged of multi-stage vacuum and the ice crystal of thawing, can be used to reduce the temperature of the effusive thermal cycle solution of last step of multilevel vacuum distilling, and can be used to the stable temperature that reclaims the vacuum vessel of condensation water, make evaporation and agglomerative thermal cycling keep balance, and the steam that multilevel vacuum distilling and multi-stage vacuum cooling are produced, can import in the icing container that multi-stage vacuum freezes with melted ice crystal, its cryogenic strong solution and melted ice crystal reclaim with vacuum vessel.
In order to improve the output of thermo-efficiency and condensation water, multi-stage vacuum freezes as follows with multilevel vacuum distilling and multi-stage vacuum cooling bonded advantage:
1. because the icing low temperature strong solution that produces of multi-stage vacuum and the ice crystal of thawing, can be used to reduce the effusive thermal cycle solution of multilevel vacuum distilling last step temperature, and keep to reclaim the temperature of the vacuum vessel of condensation water, increase the scope of thermal cycle solution use temperature, so improve the progression of multilevel vacuum distilling, and then improve the output of condensation water;
2. the icing required cryogenic de-gassed solution of multi-stage vacuum is from the effusive solution of multi-stage vacuum cooling last step, reduces the cost of precooling;
3. the multi-stage vacuum heat of solidification of required melted ice crystal of freezing is the steam that produces from multilevel vacuum distilling and multi-stage vacuum cooling;
4. multilevel vacuum distilling, multi-stage vacuum cooling, and multi-stage vacuum freeze and can share vacuum low level container and annex thereof;
Therefore the cooling of multilevel vacuum distilling and multi-stage vacuum can be combined into the method for a solution separating with multi-stage vacuum, with as sea water desaltination and the spissated method of solute.
The invention provides a kind of multi-stage vacuum cooling, the solution separating of freezing and multi-stage vacuum refrigerating unit of sea water desalination method implemented, described multi-stage vacuum refrigerating unit is to form with the mutual storehouse of the mode of tower shape with the constant temperature of a plurality of vacuum cooling distillation unit, the first step is folded on the second stage, fold on the third stage second stage, be stacked into a tower shape mutually with this, the inflow of its correspondence and effusive conduit interconnect, a low level container and annex thereof are shared in the constant temperature distillation unit of a plurality of vacuum cooling, to produce vacuum.
The present invention also provides a kind of icing device of multi-stage vacuum of implementing multi-stage vacuum cooling, the solution separating of freezing and sea water desalination method, the icing device of described multi-stage vacuum is with the mutual storehouse of the mode of tower shape by a plurality of icing containers, the first step is folded on the second stage, fold on the third stage second stage, is stacked into a tower shape mutually with this; The icing device of described multi-stage vacuum also comprises: transmission is arranged at a liquid-solid interface in the container that freezes as caloic, with condenser the heat of solidification of solution and vaporization heat discharge-a plurality of conduits and by-pass valve control thereof are connected with the multilevel vacuum distilling device with the multi-stage vacuum refrigerating unit, the steam of generation is flowed in the icing container of each grade; Cooperate low level container and annex thereof, make de-gassed solution, steam, reach conduit, the icing vacuum a plurality of conduits of container and by-pass valve control that condensation water is flowed through; Reclaim the ice crystal of thawing and the vacuum vessel of low temperature strong solution.
Multilevel vacuum distilling provided by the present invention, cooling, icing solution separating and the method and the equipment thereof of sea water desaltination with other routine techniques mutually relatively the time, have following advantage:
One, the thermal source of well heater used in the present invention can be cryogenic useless waste heat or sun power;
Two, implement liquid-discharge vacuumizing method by de-gas liq, make container for evaporation produce vacuum, its pressure for the saturation vapour pressure that uses this liquid and very small amount of air pressure and, therefore can improve the progression of vacuum distilling;
Three, according to the vacuum principle of liquid-discharge vacuumizing method, therefore first step container for evaporation is folded on the container for evaporation of the second stage, and fold on the third stage second stage, is stacked into a tower shape mutually with this, become a multilevel vacuum distilling or multi-stage vacuum refrigerative device, therefore reduce the area that uses the soil;
Four, a plurality of container for evaporation that are stacked into the tower shape all constantly flow de-gassed solution, thermal cycle solution and agglomerative distilled water, and working temperature increases progressively according to progression and successively decrease, and can reduce the usage quantity of pump, and reduce fouling and corrosion;
Five, thermal cycle solution provides the vaporization heat of de-gassed solution and reclaims vaporization heat, certain energy can be reused;
Six, the multi-stage vacuum refrigerating unit provides discharge opeing vacuum-junction ice production apparatus employed cryogenic de-gassed solution, can save the cost of precooling;
Seven, the discharge opeing vacuum-junction ice production apparatus cryogenic strong solution of being discharged and the ice crystal of thawing can reduce the temperature of the effusive thermal cycle solution of multilevel vacuum distilling last step, improve the progression of multilevel vacuum distilling.
Description of drawings
Consult the detailed description and the accompanying drawing thereof of the following relevant preferred embodiment of the present invention, can further understand technology contents of the present invention and purpose effect thereof; Relevant accompanying drawing is:
Fig. 1 is the synoptic diagram that the constant temperature distillation method is implemented in the constant temperature distillation unit of vacuum distilling of the present invention;
Fig. 2 is that multilevel vacuum distilling device of the present invention is implemented the solution separating of multilevel vacuum distilling and the configuration schematic diagram of sea water desalination method;
Fig. 3 is that the icing device of multi-stage vacuum refrigerating unit of the present invention and multi-stage vacuum is implemented multi-stage vacuum cooling, the solution separating of freezing and the configuration schematic diagram of sea water desalination method.
Embodiment
See also Fig. 1, Fig. 1 is the synoptic diagram that the constant temperature distillation method is implemented in the unit, constant temperature teahouse of vacuum distilling of the present invention, the constant temperature distillation method is to utilize boiling point of liquid to increase with pressure, and the temperature head of vacuum causes the principle of the pressure difference of saturated vapo(u)r, utilize the constant temperature distillation unit of vacuum distilling, make de-gassed solution in the container for evaporation of vacuum, constantly boiling evaporation under a temperature of setting and do not change the pressure of container for evaporation makes evaporation and agglomerative thermal cycling keep the equilibrated method.Wherein, de-gassed solution can hold the liquid that liquid, soup etc. obtain as useless for general mixing solutions after the degassing, or is the liquid that seawater obtains after the degassing.
As shown in Figure 1, the constant temperature distillation unit of vacuum distilling is by a container for evaporation 21, a flow control valve 22, a distiller 4, a liquid gas interface 211, the conduit a that condenses, and a plurality of conduit b, c, e, f, g, h, i, j, k, l and by- pass valve control 23,24,25,26,27,28,29,30 combine, container for evaporation 21 is connected with distiller 4 with the conduit a that condenses, the steam of its generation is imported in the distiller 4, flow control valve 22 is located at the appropriate location of condensing conduit a, when container for evaporation 21 is depressed at the saturated vapo(u)r of the temperature of the vacuum distilling of this setting, the steam that control container for evaporation 21 produces, enter in the distiller 4 via the conduit a that condenses, and keep pressure in the container for evaporation 21; Distiller 4, flows into and outflow distiller 4 with same traffic through conduit g, h to reclaim the thermal cycle solution of vaporization heat, absorb the vaporization heat of the steam of container for evaporation 21 generations, improving its temperature, and condensed vapor is condensation water, and permanent set liquid enters in the vacuum vessel 8 and reclaims; De-gassed solution with certain temperature, via conduit i, j and by-pass valve control 23 thereof, 24, each flows into certain flow and outflow container for evaporation 21, liquid gas interface 211 is located in the container for evaporation 21, the thermal cycle solution that vaporization heat is provided is via conduit b, c, flow into and outflow liquid gas interface 211 with same traffic, and the caloic that sees through liquid gas interface 211 is conducted, make the de-gassed solution evaporation in the container for evaporation 21, provide the temperature of the thermal cycle solution of vaporization heat to be higher than the temperature of the thermal cycle solution that reclaims vaporization heat, therefore the working temperature of container for evaporation 21 is higher than the working temperature of distiller 4, its temperature head causes the pressure difference of saturated vapo(u)r, the steam that orders about container for evaporation 21 generations flows toward distiller 4, make evaporation and agglomerative thermal cycling keep balance, the constant temperature distillation unit of the vacuum distilling of conduit i and by-pass valve control 23 connection upper levels thereof or the well heater of de-gassed solution, conduit j and by-pass valve control 24 thereof connect the constant temperature distillation unit or the vacuum vessel 9 of the vacuum distilling of next stage, its function is as conduit i and by-pass valve control 23 thereof, make de-gassed solution flow into the constant temperature distillation unit of the vacuum distilling of next stage, conduit e and control gate 25 thereof connect the constant temperature distillation unit of the vacuum steaming anchor of upper level, if do not have the constant temperature distillation unit of the vacuum distilling of upper level, then when implementing liquid-discharge vacuumizing method, use as exhaust, conduit f and by-pass valve control 26 thereof connect the constant temperature distillation unit or the vacuum vessel 8 of the vacuum distilling of next stage, its function is as conduit e and by-pass valve control 25 thereof, make steam and condensation water flow into the constant temperature distillation unit of next stage vacuum distilling, conduit b, the constant temperature distillation unit of the vacuum distilling of h connection upper level or the well heater of thermal cycle solution, conduit c, the constant temperature distillation unit of the vacuum distilling of g connection next stage or heat exchanger are to reduce its temperature, by-pass valve control 27, when the 30 constant temperature distillation unit for the vacuum distilling that prevents other grade produce vacuum, after causing de-gas liq to produce vacuum, closed control valve doorway 27,30 make it airtight.
As shown in Figure 1, it is to implement liquid-discharge vacuumizing method with de-gas liq (to please refer to No. the 02106683.3rd, China that the constant temperature of vacuum distilling distills unitary original state, the patent that is entitled as " having vacuum drying method of multi-usage closed type cleaning and device thereof " is applied for deeply), make de-gassed solution, steam, the conduit a that flows through with condensation water, e, f, i, j, container for evaporation 21, distiller 4 produces vacuum, low level container 3 and annex thereof are with conduit k, 1 and by- pass valve control 27,28,29,30 each and conduit j, f links to each other, under suitable difference of altitude, implement liquid-discharge vacuumizing method and produce vacuum, when by- pass valve control 24,26 close after, de-gas liq is filled with container for evaporation 21, distiller 4, and conduit a, e, f, i, j, k, l, closing control valve 23,25, adjust the pressure in the low level container 3, come into effect liquid-discharge vacuumizing method, at last, flow control valve 22 cuts out, by- pass valve control 27,30 close, and the injection de-gassed solution reaches suitable height in the container for evaporation 21 of vacuum, and the temperature of the vacuum distilling of setting container for evaporation 21, its temperature is lower than de-gassed solution and thermal cycle solution flows into the temperature of evaporating appearance 2521 and liquid gas interface 211, if de-gassed solution is identical solution with de-gas liq, when then implementing liquid-discharge vacuumizing method, the part volume generation vacuum of container for evaporation 21 is got final product.
The constant temperature distillation method is under the condition of suitable liquid gas interface 211, its steam output is according to the flow of de-gassed solution and thermal cycle solution, and inflow is decided with effusive temperature head, as shown in the figure, when de-gassed solution and the lasting inflow of thermal cycle solution and outflow container for evaporation 21 and liquid gas interface 211 thereof, container for evaporation 21 continues to produce steam, and when reaching the saturation vapour pressure of temperature of vacuum distilling of this setting, beating up-flow adjustable valve 22 enters in the distiller 4 steam of container for evaporation 21 generations, what continue when distiller 4 is liquid with devaporation, flow control valve 22 must be kept the stable of container for evaporation 21 internal pressures, adjust flow control valve 22 according to de-gassed solution or the effusive temperature of thermal cycle solution simultaneously, be lower than the temperature of vacuum distilling when effusive temperature, adjust Flow-rate adjustment and read 22, reduce the output of steam, when effusive temperature is higher than the temperature of vacuum distilling, adjust flow control valve 22, increase the discharge of steam.
If liquid gas interface 211 and conduit b, the c of the thermal cycle solution that vaporization heat is provided are removed in the constant temperature of vacuum distilling distillation unit, then become the constant temperature distillation unit of vacuum cooling; As thermal source, when de-gassed solution evaporated, the temperature of de-gassed solution reduced its de-gassed solution, formed the vacuum cooling effect with self temperature, and the constant temperature of vacuum cooling distills unitary original state and distills unitary original state as the constant temperature of vacuum distilling.
In the process of vacuum distilling or vacuum cooling, the air that remains in de-gassed solution can continue to be accumulated in conduit a, e that de-gassed solution, steam and condensation water flow through, f, i, j, container for evaporation 21, the distiller 4, if during the temperature of the vacuum distilling of its pressure influence de-gassed solution, the constant temperature of should be once more implementing vacuum distilling or vacuum cooling with de-gassed solution distills unitary original state, make it recover vacuum tightness, so the solution more completely that outgases, can reduce the number of times of implementing original state.
See also Fig. 2, Fig. 2 is that multilevel vacuum distilling device of the present invention is implemented the solution separating of multilevel vacuum distilling and the configuration schematic diagram of sea water desalination method, and as shown in Figure 2, multilevel vacuum distilling device 1 of the present invention comprises:
One pre-process equipment, be the solution that will remove the impurity and the degassing, and thermal cycle solution be heated to the well heater 12,13 of a design temperature respectively;
The constant temperature distillation unit 2 of a plurality of vacuum distillings, the constant temperature distillation unit 2 of described a plurality of vacuum distillings is stacked into a multilevel vacuum distilling device 1 mutually in the mode of tower shape, the first step is folded on the second stage, fold on the third stage second stage, be stacked into a tower shape mutually with this, the inflow of its correspondence and effusive conduit c interconnect, and a low level container 3 and annex thereof are shared in the constant temperature distillation unit 2 of a plurality of vacuum distillings, to produce vacuum;
One rearmounted treatment facility, comprise the vacuum vessel 8,9 that reclaims condensation water and strong solution, reduce the temperature of the thermal cycle solution that last step discharges heat exchanger 51, keep reclaiming a low level container 3 and an annex thereof of being shared the constant temperature distillation unit 2 of heat exchanger 52, a plurality of vacuum distillings of temperature of the vacuum vessel 8 of condensation water, the recycle pump 53 that reaches thermal cycle solution.
As shown in Figure 2, the original state of multilevel vacuum distilling device 1 is the mode of successively decreasing according to progression, implement the original state of the constant temperature distillation unit 2 of vacuum distilling step by step, the liquid gas profile of equilibrium according to the tax gasoloid, set the thermograde of thermal cycle solution,, set the temperature of each grade vacuum distilling again according to the thermograde of thermal cycle solution, its temperature increases progressively with progression and successively decreases, so the saturation vapour pressure of the temperature of vacuum distilling is passed and will be successively decreased with progression.Wherein, the liquid that de-gassed solution can obtain after the degassing for general mixing solutions such as lean solution, soup etc., or the liquid that after the degassing, obtains for seawater.
As shown in Figure 2, the transmission of its solution is to be heated to the de-gassed solution of design temperature, the mode that increases progressively according to progression, each is with certain flow, continuously flow into and flow out container for evaporation at different levels 21, evaporation along with de-gassed solution, its concentration increases progressively with progression and increases, or separate out crystallization, the strong solution that last step is discharged, reclaim with vacuum vessel 9, its strong solution can be utilized vacuum freeze-drying method to make further solute and concentrate, when if container for evaporation 21 has crystallization to separate out, then before the container for evaporation 21 that flows into next stage, leach crystallisate earlier, its crystallisate reclaims with vacuum vessel, and the residual air that is dissolved in de-gassed solution can continue to be accumulated in the constant temperature distillation unit 2 of vacuum distilling, and when influencing the temperature of vacuum distilling of de-gassed solution, especially first, the constant temperature distillation unit 2 of the vacuum distilling of secondary, should implement the original state of the constant temperature distillation unit 2 of vacuum distilling once more with de-gassed solution, make it recover vacuum tightness, therefore near the solution that outgases fully, can reduce the constant temperature of implementing vacuum distilling steam pin unit 2 from original state, make it recover vacuum tightness, therefore near the solution that outgases fully, the constant temperature that can reduce the vacuum distilling of enforcement steams the number of times of the original state of pin unit 2.
As shown in Figure 2, the regeneration of thermal cycle solution is to be heated to the thermal cycle solution of design temperature ' mode that increases progressively according to progression, with same traffic, continuously flow into and flow out liquid gas interface at different levels 211, the vaporization heat of de-gassed solution is provided, its temperature increases progressively with progression and successively decreases, the thermal cycle solution that last step is discharged reduces its temperature with heat exchanger 51, again with recycle pump 53 actings, the mode of successively decreasing according to progression, it is continuously flowed into and flowing out distiller at different levels 4, absorbing vaporization heat, and is condensation water with devaporation, its temperature is successively decreased with progression and is increased progressively, and passes back at last in the well heater 13 of thermal cycle solution; In order to reclaim certain energy, do to use repeatedly, so the Recycle design of thermal cycle solution is: A. is heated to a design temperature; B., vaporization heat is provided, and its temperature increases progressively according to progression and successively decreases; C. reduce temperature; D. reclaim vaporization heat, its temperature is successively decreased according to progression and is increased progressively; If the effusive temperature of last step is lower than normal temperature, multilevel vacuum distilling can cool off with multi-stage vacuum, combine, and thermal cycle solution reduces its temperature with multi-stage vacuum cooling, the cryogenic strong solution of generation of freezing and the ice crystal of thawing; If the effusive temperature of last step is higher than normal temperature, then reduce the temperature of thermal cycle solution with normal temperature liquid.
Provide the thermograde of the thermal cycle solution of vaporization heat to set according to the liquid gas profile of equilibrium of de-gassed solution, set the temperature that each grade vacuum distilling is used according to this, because of the temperature range of using not overlapping, the formed temperature curve of each grade vacuum distilling is the ladder type curve so thermal cycle solution is flowed through, the thermograde of Here it is thermal cycle solution.
See also Fig. 3, Fig. 3 is that the icing device of multi-stage vacuum refrigerating unit of the present invention and multi-stage vacuum is implemented, the multi-stage vacuum cooling, the solution separating of freezing and the configuration schematic diagram of sea water desalination method, described multi-stage vacuum cooling, the solution separating method of freezing, be to utilize the method for freezing and melting, produce condensation water, and can be used to auxiliary multilevel vacuum distilling, make it increase the use range of the temperature of thermal cycle solution, and then increase progression, and the output and the thermo-efficiency of increase condensation water, make whole condensation water output more simultaneously, the effusive cryogenic fluid of the last step of multi-stage vacuum refrigerating unit imports in the icing device of primary multi-stage vacuum, can save the energy of precooling, the transmission of conjugate solutions, the constant temperature distillation method, the discharge opeing vacuum method of freezing makes de-gassed solution produce ice crystal, the progression that the concentration of its de-gassed solution is frozen with vacuum increases progressively and increases progressively, so its temperature increases progressively with progression and successively decreases.Wherein, the liquid that de-gassed solution can obtain after the degassing for general mixing solutions such as lean solution, soup etc., or the liquid that after the degassing, obtains for seawater.
As shown in Figure 3, multi-stage vacuum refrigerating unit 6, be to form a multistage vacuum cooling unit 6 with the mutual storehouse of the mode of tower shape by the constant temperature of a plurality of vacuum cooling distillation unit 61, the inflow of its correspondence and effusive conduit interconnect, do the transpiration cooling of vacuum with the temperature of de-gassed solution self, the mode that the de-gassed solution of normal temperature increases progressively according to progression, continuously flow into and flow out container for evaporation 611 at different levels, cooperate the constant temperature distillation method, the temperature of de-gassed solution increases progressively with progression and successively decreases, but its concentration does not significantly change, the temperature of the effusive de-gassed solution of last step is near the temperature of freezing, a low level container 3a and annex thereof are shared in the constant temperature distillation unit 61 of a plurality of vacuum cooling, after icing container 71 produces ice crystal, its temperature is lower than the temperature of container for evaporation 611, so the steam that container for evaporation 611 produces can import in the container 71 that freezes smoothly, and melted ice crystal.
As shown in Figure 3, the multi-stage vacuum device 7 that freezes, be to form with the mutual storehouse of the mode of tower shape by a plurality of icing containers 71, establish a liquid-solid interface 711 in the icing container 71, utilize condenser 72 to see through the caloic transmission of liquid-solid interface 711, the heat of solidification of de-gassed solution is discharged, utilizing conduit 5 and multi-stage vacuum to steam the scholar device is connected, the steam that the cooling of multilevel vacuum distilling and multi-stage vacuum is produced flows into respectively in the icing container 71 of each grade, share a low level with multi-stage vacuum refrigerating unit 6 and hold different 3a and annex thereof, make de-gassed solution, steam, and the condensation water mobile conduit and the container 71 generation vacuum of freezing, the ice crystal of the thawing that the discharge opeing vacuum method of freezing produces and cryogenic strong solution are with vacuum vessel 10,11 reclaim, and can be used to reduce the temperature of the thermal cycle solution that the multilevel vacuum distilling last step discharges, and keep its reclaim condensation water temperature.
As shown in Figure 3, the original state of the icing device 7 of multi-stage vacuum is the modes of successively decreasing according to progression, implement liquid-discharge vacuumizing method with de-gas liq step by step, make de-gassed solution, steam, reach the conduit that condensation water is flowed through, and the container 71 that freezes produces vacuum, and avoid de-gas liq to reflux, the original state of multi-stage vacuum refrigerating unit 6 is the modes of successively decreasing according to progression, implement the original state of the constant temperature distillation unit 61 of vacuum cooling step by step, set the distillation temperature of each grade vacuum cooling then, its temperature increases progressively with progression and successively decreases, so the distillation pressure of vacuum cooling increases progressively with progression and successively decreases.
The discharge opeing vacuum method of freezing is that the icing mode with the falling liquid film of condenser 72 heat extractions and discharge opeing vacuum makes de-gassed solution form in liquid-solid interface 711 to form ice crystal uniformly, as shown in Figure 3, it is the icing container 71 of filling with the vacuum of the first step with the effusive cryogenic de-gassed solution of multi-stage vacuum cooling last step, provide liquid-solid interface 711 to form in the icing container 71 for ice crystal, utilize the caloic transmission of condenser 72 and liquid-solid interface 711, heat of solidification in the container 71 that freezes and vaporization heat are discharged, and gradually de-gassed solution is discharged with liquid-discharge vacuumizing method, its de-gassed solution flows into the second stage, the second stage flows into the third stage, then the de-gassed solution of last step flows into vacuum vessel 11, the liquid level of icing container 71 reduces gradually with the discharge of de-gassed solution, therefore the vacuum volume of its generation increases gradually, because the heat extraction of condenser 72, make the de-gassed solution of liquid phase form composition ice crystal uniformly in liquid-solid interface 711 as the falling liquid film mode of freezing, the container 71 interior vacuum volumes that freeze simultaneously increase gradually, because the heat extraction that condenser 72 continues, make the pressure ratio equilibrium vapor pressure ratio equilibrium vapour pressure of volume of vacuum low, then the de-gassed solution surface can rise the beginning evaporation, because the result of evaporation heat absorption can cause remaining mother liquor to turn cold, will reduce temperature because of transpiration-cooled effect, its water vapour (equilibrium vapor pressure) is by the surface adsorption of liquid-solid interface 711, condenser 72 is taken away the heat of water vapour, make water vapour transfer the ice crystal of solid phase to, impel de-gassed solution to continue evaporation, to keep the balance of its vapour pressure, and produce more Ice, after the mother liquor that thickens gradually is discharged from lentamente, the volume of vacuum increases gradually, impelling more, the water vapour of multimass produces, quicken the generation of ice crystal, more and more dense mother liquor is discharged, and has only ice crystal at last in icing container 71.
As shown in Figure 3, the mode that the transmission of solution increases progressively according to progression, each icing container 71 of flowing through, when the container 71 that freezes will not condense after the de-gassed solution of ice crystal enters the icing container 71 of time one-level fully, the icing container 71 of inferior one-level just rises the icing method of beginning enforcement discharge opeing vacuum, and the steam that multilevel vacuum distilling and multi-stage vacuum cooling produce just rises in the icing container 71 of beginning importing, ice crystal is melted, permanent set liquid reclaims with vacuum vessel 10, therefore the ice crystal that freezes of multi-stage vacuum condense and thawing is discrete, when container 71 has crystallization to separate out if freeze, then de-gassed solution is before the icing container 71 that flows into next stage, leach crystallisate earlier, its crystallisate is dissolved in de-gassed solution with the vacuum vessel recovery residual air can continue to be accumulated in the constant temperature distillation unit of vacuum cooling, and when influencing the temperature of vacuum distilling of de-gassed solution, especially first, the constant temperature distillation unit of the vacuum cooling of secondary, the original state of should be once more implementing the constant temperature distillation unit 61 of vacuum cooling with de-gassed solution makes it recover vacuum tightness, therefore near the solution that outgases fully, can reduce the constant temperature of implementing vacuum cooling and distill the number of times of unitary original state.
Claims (8)
Priority Applications (3)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNA2006100018481A CN1935676A (en) | 2002-12-12 | 2002-12-12 | Method and equipment for solution separation and seawater desalination |
| CNB021567174A CN1297491C (en) | 2002-12-12 | 2002-12-12 | Method and equipment for solution separation and seawater desalination |
| CNB2006100018496A CN100371044C (en) | 2002-12-12 | 2002-12-12 | Solution separation and seawater desalination method |
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| CNB021567174A CN1297491C (en) | 2002-12-12 | 2002-12-12 | Method and equipment for solution separation and seawater desalination |
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| CNA2006100018481A Division CN1935676A (en) | 2002-12-12 | 2002-12-12 | Method and equipment for solution separation and seawater desalination |
| CNB2006100018496A Division CN100371044C (en) | 2002-12-12 | 2002-12-12 | Solution separation and seawater desalination method |
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| CNA2006100018481A Pending CN1935676A (en) | 2002-12-12 | 2002-12-12 | Method and equipment for solution separation and seawater desalination |
| CNB2006100018496A Expired - Fee Related CN100371044C (en) | 2002-12-12 | 2002-12-12 | Solution separation and seawater desalination method |
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| CNB2006100018496A Expired - Fee Related CN100371044C (en) | 2002-12-12 | 2002-12-12 | Solution separation and seawater desalination method |
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| CN1778693B (en) * | 2005-01-27 | 2012-05-02 | 蔡梅初 | Through-flow vacuum seawater desalination plant and method thereof |
| CN101671059B (en) * | 2009-10-06 | 2011-03-30 | 冯静 | Method and device structure for preparing ice and desalinating seawater by vehicles and natural energy resources |
| CN101671058B (en) * | 2009-10-06 | 2011-01-26 | 冯静 | Semi-automatic production method and equipment for preparing ice and desalinating seawater by natural energy resources |
| ES2786498T3 (en) * | 2010-02-23 | 2020-10-13 | Aquamill Five Star Pty Ltd | Device for heating a liquid comprising a solvent and a solute and for separating the solvent and the solution |
| CN109489133A (en) * | 2018-09-29 | 2019-03-19 | 东南大学 | A kind of solar energy solution regeneration system based on passive vacuum |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4880504A (en) * | 1987-02-24 | 1989-11-14 | Cellini John V | Vacumm distillation system with spiralled cold coil |
| CN1205647A (en) * | 1996-09-20 | 1999-01-20 | 美国技术集团有限公司 | Small compact vacuum distillation appts. |
| CN2399372Y (en) * | 1999-09-20 | 2000-10-04 | 丁成玉 | Low pressure distillation and evaporation seawater desalting appts. |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| JP3394815B2 (en) * | 1993-08-30 | 2003-04-07 | 東静電気株式会社 | Vacuum distillation method and vacuum distillation apparatus |
| US5853549A (en) * | 1995-03-14 | 1998-12-29 | Sephton; Hugo H. | Desalination of seawater by evaporation in a multi-stack array of vertical tube bundles, with waste heat. |
| CN1220633C (en) * | 1997-12-25 | 2005-09-28 | 株式会社荏原制作所 | Desalination method and desalination apparatus |
-
2002
- 2002-12-12 CN CNB021567174A patent/CN1297491C/en not_active Expired - Fee Related
- 2002-12-12 CN CNA2006100018481A patent/CN1935676A/en active Pending
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Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4880504A (en) * | 1987-02-24 | 1989-11-14 | Cellini John V | Vacumm distillation system with spiralled cold coil |
| CN1205647A (en) * | 1996-09-20 | 1999-01-20 | 美国技术集团有限公司 | Small compact vacuum distillation appts. |
| CN2399372Y (en) * | 1999-09-20 | 2000-10-04 | 丁成玉 | Low pressure distillation and evaporation seawater desalting appts. |
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| CN1935676A (en) | 2007-03-28 |
| CN100371044C (en) | 2008-02-27 |
| CN1827200A (en) | 2006-09-06 |
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