CN1158220C - Integrated multistage and multieffect desalination method and its equipment - Google Patents
Integrated multistage and multieffect desalination method and its equipment Download PDFInfo
- Publication number
- CN1158220C CN1158220C CNB011106530A CN01110653A CN1158220C CN 1158220 C CN1158220 C CN 1158220C CN B011106530 A CNB011106530 A CN B011106530A CN 01110653 A CN01110653 A CN 01110653A CN 1158220 C CN1158220 C CN 1158220C
- Authority
- CN
- China
- Prior art keywords
- effect
- seawater
- level
- water
- desalination
- Prior art date
- Legal status (The legal status 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 status listed.)
- Expired - Fee Related
Links
Images
Classifications
-
- 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
Landscapes
- Heat Treatment Of Water, Waste Water Or Sewage (AREA)
- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
Abstract
The present invention provides a method by utilizing a distillation method to desalt water. The method comprises a multistage flash evaporation process and a multiple-effect distillation process which are simultaneously completed in each stage-effect. In each stage-effect, the seawater is simultaneously evaporated by the stage-effect in a flash way, and is heated by the steam of the previous stage-effect. The present invention especially provides an integral desalting technology for executing the method and a desalting and a device for realizing the technology.
Description
Technical field
The present invention relates to the sea water desaltination field, particularly a kind of distillating method that utilizes, the integrated desalination process that multistage flash evaporation and multi-effect distilling process are organically combined and realize improving water generation ratio, reduce heat energy consumption.The present invention relates to desalination system and the device of realizing this technology simultaneously.
Background technology
For many years, distillation method is the topmost method of sea water desaltination all the time, about 2700 ten thousand steres of present global fresh water day output, and wherein about 70% is to produce with distillation method.In the used distillation method the most extensive employing have two kinds, a kind of is multistage flash evaporation (MSF), another kind is multi-effect distilling (MED), their essential characteristic is only to finish single physical process in each level or in imitating, so water generation ratio (Gais-Out put Ratio of whole desalination process, or GOR) all lower, generally be less than or equal to 16.7 and 21 respectively.So-called water generation ratio is meant the desalination water yield that steam obtained that consumes unit mass, with formulate is:
Water generation ratio (the GOR)=acquisition desalination water yield (kg)/consumption quantity of steam (kg)
Water generation ratio is that the index of water process heat energy consumption is made in an expression intuitively, and water generation ratio is higher, and consumption of heat energy is fewer, thereby also reduces the power consumption that drives sea-water pump, can effectively improve the economic benefit of seawater (comprising salty misery) desalination plant.
The principle of work of flash distillation is known, is provided with pressure and is respectively P
I-1And P
iAdjacent two chambers, when seawater from corresponding pressure P
I-1Down, temperature of saturation is T
I-1(P
I-1) chamber to enter pressure be P
iChamber after, the temperature of seawater will be changed into temperature of saturation T
i(P
i), remaining heat content disengages by vaporizing rapidly, and flash distillation promptly takes place, and condensation and this part steam of collection are exactly desalination water.The water production rate of flash distillation is to be determined by the heat content on the seawater saturation curve and the latent heat of vaporization, because the product desalination water yield of the seawater of unit mass in the MSF process is certain, common way is to adopt multistage flash evaporation to improve to make water efficient, so can cause the volume of MSF device very huge, the raw materials consumption of the unit's of making desalination water output is huge.
Multi-effect distilling MED is different with multistage flash evaporation MSF, driving medium in multistage flash evaporation and the thermal source seawater of working exactly itself, and multi-effect distilling is the heating evaporation of steam to seawater, and the steam of evaporation is used as the thermal source of next effect, in the seawater of heating evaporation next stage, self obtains condensation, form desalination water through collecting, therefore, the multi-effect distilling process is exactly the process that repeatedly produces steam and vapor condensation formation desalination water, as each effect, come down to a condenser/evaporator.Imitate number the more, desalination water output the more, but the heat interchanging area that requires also increases thereupon.
In multistage flash evaporation, the quantity of steam of productions at different levels is by the overheated temperature difference (T of place level seawater
I-1-T
i) heat content and seawater amount long-pending remove the decision of vaporization latent heat.Because the heat content difference between the final stage of top only is about 1/5th of the latent heat of vaporization, so the desalination water productive rate of series system only is about 1/5 of string maritime interior waters flow.The seawater degree of enrichment of final stage is still very low, can not significantly improve the degree of enrichment of discharging seawater.And improve progression only is a kind of improvement, basic improvement can not be arranged, so normally make the recirculation of part concentrated seawater.But the seawater circular flow of multistage flash evaporation is than much higher times of desalination water productive rate, and power consumption is also very big.In multi-effect distilling, there is not this strict corresponding relationship, any one desalination water productive rate of imitating only depends on by last one imitates the quantity of steam of input as thermal source.In theory, the desalination water productive rate of every effect is the restriction that is not subjected to the work seawater flow, can increase to any level, therefore can improve the desalination water productive rate by the total effect number that strengthens top effect steam input and increase in the string, the while also can reduce the current consumption that drives marine stream by improving the degree of enrichment of discharging seawater.In theory, it is unconfined that this benefit increases, but cost is unrestrictedly to increase heat interchanging area.Consider from the angle of material, seawater has extremely strong corrodibility, carbon steel material can not be applied to the contact surface with seawater, must adopt the material of anti-seawater corrosion, and the price of this class material is high more a lot of than steel, and therefore, the increase of imitating number has the restriction of a degree, the increase that is heat interchanging area must limit within the acceptable range, and the increase of producing the water benefit is actually and is restricted.
In multistage flash evaporation, top pressure can make seawater gravity flow in the whole process fully, supercharging in the middle of not only not needing, and also inter-stage also will add inter-stage damping step-down.But in multi-effect distilling, each pressure reduction of imitating of front end is bigger, might guarantee that seawater flows with the speed of design, and the effect of the overwhelming majority afterwards can not guarantee all gravity flow must outer portion provide pressure head.
Summary of the invention
The object of the present invention is to provide the multistage multi-effect sea water desalting technology of a kind of realization (MSFMED), flash distillation and distillation in each level-effect, have been used simultaneously, and the design by many steps flow process, realize the integrated desalinating process of multistage multi-purpose, reach and significantly improve water generation ratio, the purpose of reduction heat energy consumption.
Another object of the present invention has been to provide desalting equipment and the system that is used to realize above-mentioned integrated multistage multiple-effect desalinating process, be designed to many many parallel oblique of step groove liquid streaming structures, improve water generation ratio, when cutting down the consumption of energy, also reducing the whole height of device.
At first, the invention provides a kind of method of utilizing the desalination by distillation seawater, comprise multistage flash evaporation and multi-effect distilling process, and flash distillation and still-process are all finished in each level-effect simultaneously, in each level-effect, seawater is simultaneously by the flash distillation of the corresponding levels-effect with from the steam heating of previous level-effect.The present invention especially provides the integrated desalinating process of implementing this method.
Need to prove that be " level " and " effect " of multi-effect distilling of difference multistage flash evaporation process, the present invention represents to finish simultaneously flash distillation and assembled unit of distillatory with " level-effect ".
According to desalination method of the present invention, what adopt is single flow desalination flow process, keep certain potential energy difference that the seawater potential energy of each grade-effect ingress is provided between two successive stages-effect by making, and making concentrated seawater in each level-effect chamber, all realize gravity flow, the concentrated seawater after this desalination flow process is drained from final stage-effect.Test-results proves, adopts integrated desalinating process of the present invention, and the utilization ratio of seawater is higher, so adopt single flow.Single flow is that the concentration of seawater of high temperature section is lower, is of value to the influence of alleviating fouling than the additional benefit of recirculation type.Preferably utilize the scarp to improve the seawater potential energy of each grade-effect ingress in the present invention, also utilize the difference of altitude between adjacent level-effect further to improve potential energy simultaneously.Change kinetic energy into by potential energy and guarantee the gravity flow of concentrated seawater in each grade-effect chamber, and guarantee certain velocity of flow, realize stable heat exchange.
The present invention with the concentrated seawater reversed flow of being desalinated after handling, realizes the preheating of self with the water coolant of new seawater as the desalination process simultaneously at the heat of absorption evaporative process.Specifically, new seawater from seawater water intaking field enters desalting equipment from final stage-effect, be divided into two strands and carry out preheating, wherein, one is as the water of condensation of multistage flash evaporation process, another strand reclaims the water of condensation of the desalination water of having desalinated as multistage-effect still-process, when new seawater when some levels is preheating to 39-49 ℃, two strands of new seawater are drawn simultaneously, carry out degasification, add the processing of scale inhibitor, chemical treatment and control pH value, again in the pump-back system, continue afterwards by previous stages-effect process preheating.Final preheating temperature should be high as much as possible, is heated to≤during 135 ℃ of left and right sides, can through the desalinating process flow process, discharges until last concentrated seawater from the top chamber of sending into through thermal source again.
According to the present invention, in the level and effect of each correspondence, the concentrated seawater of MED effect and the concentrated seawater of MSF level are merged into one concentrated seawater, keep every grade of pressure-controlling that chamber is interior in the MSF process fully.So, when concentrated seawater when the higher relatively chamber of adjacent upper level pressure flows into the next stage chamber that pressure is lower comparatively speaking, just finished flash vaporization process, produced the steam of MSF process, after carbonated drink is separated, be used for the new seawater of preheating at the top of chamber, the saturated desalination water of condensation is collected the back by the condensate collector on top and is flowed out chamber, is utilized to the new seawater of preheating outside chamber again.
According to processing method of the present invention, when concentrated seawater is finished flash distillation by pressure-controlling in each chamber when,, produce the steam of MED process by the steam heating of MED chamber, this part steam is also introduced the MED chamber of next effect again behind steam separator, as the vapour source of heating.Saturated desalination water after being condensed flows out from the bottom, is pooled to the external heat exchanger ingress of upper level flash distillation desalination water, and both pressure is identical.In this course, except that concentrated seawater and flash vaporization process are share, as broad as long with the technological process of tower MED.
Multistage flash evaporation is to keep chamber by the corresponding saturation pressure of temperature of saturation control with the common ground of multi-effect distilling, to keep the water layer of concentrated seawater thin as far as possible simultaneously, it is very little promptly to form between the levels concentrated seawater pressure reduction by water colunm height, makes the fully evaporation of also having an opportunity of the concentrated seawater of lower floor.In fact, the concentrated seawater water layer always has certain thickness, and the influence that brings thus can remedy in design calculation in the correction by necessity.
In the multiple-effect technical process, in order to obtain enough big coefficient of heat emission, the flow velocity of concentrated seawater just can not be low excessively, but flow velocity is big, and drag losses is also big.Thus, theoretically, this flow velocity can be high as much as possible, but also need consider various engineering factors in the actually operating.As a rule, particularly imitating under a lot of condition of number, pressure reduction between effect can not guarantee the concentrated seawater gravity flow, outer polishing head must be arranged, according to the preferred embodiment of the invention, multistage-effect process that whole desalination process is designed to many steps, each step is made up of a plurality of level-effects, the relative position of at different levels-effect is inclined to set from high to low, makes the seawater of each grade-effect ingress that certain potential energy all be arranged.Between adjacent two steps, seawater and desalination water water pump lifting potential energy.According to principle of conservation of momentum, the relative potential energy that has when entering the evaporation chamber when concentrated seawater is big more, and velocity of flow is also big more.So technical scheme of the present invention also comprises the potential energy that improves concentrated seawater, for example make concentrated seawater flow into the evaporation chamber with a bigger angle of inclination, like this, both guaranteed the completely stable gravity flow of seawater in the evaporative process, made full use of potential difference again, and made the step total height controlled.As for the potential energy between the step, except that first step, remaining all obtains by booster water pump.For example, when the loop of nuclear reactor heat supply water that adopts and confession steam is positioned at factory building basal plane 15m eminence, provide the pressure head of 15m water column naturally, first step starting point that Here it is.After treating that this natural pressure head exhausts, utilize water pump respectively concentrated seawater and desalination water to be brought up to required height again, make it to finish the gravity flow of whole process.
The method according to this invention, in the division of step, almost completely let nature take its course, the new seawater that enters from final stage just is preheating to 39-49 ℃ when reaching the division of latter two step, can help seawater degasification, add the processing operation of scale inhibitor and control pH value etc.The preferred scheme according to the present invention, these many steps are multistage-and the effect process can design three steps, first step utilizes section for the nuclear reactor potential difference, the second and the 3rd step then relies on water pump and improves potential energy and form gravity flow, and to make the division points of the 2nd and the 3rd step be the flow process section of new seawater when being preheating to 39-49 ℃ just.
According to another aspect of the present invention, on the basis that proposes the technical process of above-mentioned integrated multistage multiple-effect, also design has proposed effectively to realize many many parallel oblique of step groove liquid streaming desalination systems of this desalination process, concentrated seawater flows in inclined groove, guarantee the gravity flow speed that the MED process is required by the relative potential energy difference, simultaneously in chamber, keep constant pressure, to finish flash vaporization process.The potential energy of concentrated seawater is provided jointly by many steps of device and the pressure difference between level-effect, pressure difference is bigger between the level-effect of high temperature section, can be used to the potential energy that provides more, pressure difference is very little between the level-effect of low-temperature zone, can only consume on resistance gauge, potential energy relies on the phase contraposition senior middle school that is assigned at different levels-effect from step to obtain fully.
Seawater desalination system according to realization seawater desalinization process provided by the invention, comprise a plurality of level-effect molectrons that form by flash distillation and water distilling apparatus combination, these level-effect molectrons are connected mutually, and be configured to many stepped form, each step comprises a plurality of described level-effect molectrons, the relative position of their longshore current journey directions is provided with the U-shaped pipe as the concentrated seawater runner from high to low between each grade-effect molectron, and on this U-shaped pipe pressure-losses device is set.When adjacent level-effect just was the step division points, this U-shaped Guan Zewei was used to promote the import and export water pipe of the topping-up pump of concentrated seawater potential energy.
According to multistage multiple-effect system of the present invention, each level-effect molectron wherein is a casing, comprise two chambers up and down, from top to bottom, top is flash distillation plant, and the middle and upper part is divided into steam separator, and is provided with the desalination water outlet of leading to outside the chamber, the middle part is for being provided with the waved plate of Baltimore groove, groove upper opening; The bottom is the moving sweating room in the source of multi-effect distilling process, and the bottom is the desalination water collector, and described molectron be configured to before the low heeling condition in high back, the relative height of scarp front end just forms potential energy.
Just begin in the MSFMED process, be in the first step-effect, the vapour space that the source steam that is come by vapour source enters the bottom, enter Baltimore groove through the new seawater behind the heat exchanger of heat source reheat by water-in simultaneously, on the one hand because the corresponding saturation pressure Psctl of the first step flashing chamber temperature T s (1) that pressure drop is extremely controlled, new seawater in the Baltimore groove discharges its superheated heat immediately by steam, realize the flash process process.This part steam is through the steam separator of middle and upper part, seawater drip isolate after, by the condensation of top flash distillation plant tube bank condensation, form desalination water, splash in the desalination water collector of top.MED process desalination water in the last bottom water collector with next stage-effect of this part water compiles, and together flows to the new seawater preheating of external heat exchanger confession.On the other hand owing to enter concentrated seawater in steam (a little higher than Psctl of pressure is the saturation pressure of steam) the heating Baltimore groove of lower space, the latent heat of vaporization is passed to concentrated seawater in the groove, make it the part vaporization, form the multi-effect distilling process, self becomes water of condensation, splashes in the water collector of bottom.Steam by this part generation is also drawn by the steam outlet on top behind the steam separator of middle and upper part, enters in the bottom steam chest of next stage-effect through the bottom of next stage-effect steam inlet, finishes the effect still-process in the effect of the second stage-effect.The seawater working condition is identical substantially in later at different levels-effect.
In general, concentrated seawater in I level-effect, by the flash distillation in the corresponding levels-effect with by the next steam heating of I-1 level-effect, finish MSF and MED process, the steam of generation belongs to the MSF procedure division, by the new cooled with seawater that is preheated in the beam tube at top, form water of condensation, be collected in the temporary transient collector in top, the desalination water with the bottom of I+1 level-effect compiles then; Belong to the steam of MED procedure division, draw, flow into I+1 level-effect as vapour source by steam outlet.The steam here is idle most in the corresponding levels-effect and I+1 level-effect internal consumption, by the time next stage-live steam that the effect chamber produces, but the desalination water of condensation step by step-imitate accumulative total, up to final stage-effect.Part steam that the steam that final stage-effect produces produces except that the MSF process by new seawater condensation, unnecessary steam is wanted the outer end that put to imitate condenser to come condensation, the similar process of the turbine exhaust vapour condensation in it and power station.
According to design provided by the invention, the basic assurance of concentrated seawater gravity flow is the runner in the inclination Baltimore groove in each MSFMED level-effect, is designed to the ingress height, the exit is low, drive the concentrated seawater gravity flow by potential energy, and guarantee flow velocity, and normally the most stable the flowing of flowing that potential energy drives.At the front end of MSFMED process, the pressure reduction between adjacent level-effect is bigger, can utilize the raise concentrated seawater potential energy of each grade-effect ingress of this pressure reduction, allows concentrated seawater stably flow to the exit along the inclination runner then, finishes the MSF-MED process in this grade-effect.Along with the increase of level-effect numbering, the concentrated seawater temperature reduces, and the pressure reduction between adjacent level-effect descends, be not enough to form natural head, this moment must the beginning second step, and to utilize potential difference to form basically at different levels-concentrated seawater gravity flow driving head in imitating, up to the final stage-effect of whole process.
In the design according to many many parallel oblique of step groove liquid streamings of the present invention, the connection design between adjacent level-effect is very important, relates to concentrated seawater and steam connecting passage and resistance pressure drop.In the integral system of the present invention, the mechanism of MSF process is identical, also adopts the U-shaped pipe concentrated seawater connecting passage design of MSF process, but distinct with it: 1, the long-pending weak point than single MSF process of cross section of fluid channel.Because half of the interior many parallel grooves of chamber is the vapour space, increase according to level-effect ordinal number, the concentrated seawater flow successively decreases and designs at different levels-area in the transverse section of connecting passage between imitating, promptly, the length of section and bending radius wide and the U-shaped pipe, for example width is 15cm, and bending radius is 25cm, resistance gauge just is placed near the nearly bottom of U-shaped pipe, and the length of passage is determined by the flow of concentrated seawater; 2, a terminal bottom of not installing of U-shaped passage, and the concentrated seawater of level-effect confluxes and distribution trough before and after being, conflux and distribution trough also to make the flow velocity of concentrated seawater in connecting passage very low, keep resistance pressure drop very little, simultaneously to the breathing redeeming of many parallel oblique concave-board in the chamber to temperature; 3, integrated MSFMED's is at different levels-and effect all is in different heights, thereby two common upright arms of U-shaped pipe are not isometric.When adjacent level-effect just was the step division points, then the U-shaped pipe connecting just changed into the import and export design of topping-up pump.
Draw thus, the invention provides a kind of efficient, the desalination process of low consumption also provides a design of overlapping desalting equipment, its main feature just is traditional multistage flash evaporation process and multi-effect distilling process are combined, wherein each item parameter and operation control are all calculated according to the theory that those skilled in the art grasped and are determined, but this combination is not simple technology stack, its effect but is to make us unexpected in production application, bring increase substantially (having brought up to about 40) of water generation ratio thus from present 16.7-21, energy consumption but reduces significantly, and this will embody from the following aspects:
At first, two single operating process are combined dexterously, flash distillation and distillation are all taken place in the chamber of each grade-effect simultaneously, made full use of thermal energy source;
The second, adopt the single flow flow process, reason is that the present invention desalinates seawater enrichment factor after the processing up to about 6.75-7.0, promptly salts contg was about for 20% (salinity in China coastal waters is about 3%) from the effusive strong brine of final stage, and it is than the concentration much higher (enrichment factor of present most desalting equipments generally is about 2) of the concentrated seawater of general sea water desaltination discharge.Under highly enriched rate, the recirculation flow process of concentrated seawater has lost meaning, but such saltiness is also far below the saturated salinity of seawater, thereby can not stop up runner because of separating out crystal salt, the seawater after the work drained fully (can realize the comprehensive utilization of seawater better).Compare with present most recirculation flow processs that adopt, greatly reduce the watt consumption of seawater driving pump;
Three, adopt the design of many steps, under the prerequisite that guarantees potential energy, the total height of desalting equipment is lowered, and is reduced to from common 160m tower height and generally is no more than 35m, has not only reduced the energy consumption of carrying seawater, makes the maintenance of device more convenient;
Four, improved the structure of each grade-effect dexterously, changed chamber into inclined design, seawater relies on stable gravity flow by each level-effect chamber, and the consumption of transmitting power is descended;
Five, in each level-effect, the seawater runner is the waved plate with Baltimore groove, and seawater is passed through in the turbulent flow mode, has increased the coefficient of heat transfer, also helps the evaporation of lower floor's seawater,, obtains higher heat exchanger effectiveness that is;
Six, the contriver is improved present flash distillation plant after the calculating of many examples and test relatively, make the desalination water of condensation in each grade-effect all be drawn outdoor, be utilized to the new seawater of preheating again, this improvement has overcome in each grade condensation desalination water will repeatedly be flashed shortcoming with condensation with flow process, thereby significantly reduce heat interchanging area, simultaneously, heat exchanger effectiveness between water and the water is higher than water and vapour, so, to same brine disposal amount, heat interchanging area required for the present invention is little, helps improving water production rate;
Seven, the consumption of electric energy of the present invention unexpectedly is lower than 1 degree/ton water especially, and present minimum current consumption is at about 2.25 degree/ton water.
In sum, promotion and implementation of the present invention are the development to for many years desalination technology, will bring considerable economic, particularly in water resources deficient day by day today, immeasurable value are arranged more.
Description of drawings
Fig. 1 is the integrated MSFMED process flow sheets of three many parallel oblique of step chutes of the present invention.
Fig. 2 is the associated plant structural representation of each grade-effect in the flow process of the present invention.
Fig. 3 is an A-A schematic cross-section among Fig. 2.
Embodiment
Describe enforcement of the present invention and characteristics in detail below in conjunction with accompanying drawing.
As shown in Figure 1, the present invention can realize by such integrated design and technology, whole process is a single flow, be divided into three steps, relative level with respect to the ground factory building, about 15 meters of first step (concordant with nuclear reactor supplying heat source height), the relative level of second step be about 35 meters, about 25 meters of the 3rd step.In the desalination process, new seawater flows into the laggard flow process of going into from final stage, and new seawater needs enter earlier flow process again in the winter job after the preheater preheating.Every grade new seawater all flows into from the device right upper portion, through the MSF process, by self obtaining preheating behind the steam of new seawater preheating pipework condensation flash section, flows out from the device left upper portion then.After preheating step by step,, further be heated to the temperature of requirement again by outer thermal source, send into the evaporation chamber from the 1st grade of outflow.The flow direction of the concentrated seawater after the heating is what to be intersected with new seawater, and is concentrated through step by step flash vaporization and multi-effect distilling from the inlet inflow of the 1st grade-effect, discharges from final stage.
In conjunction with Fig. 2 and Fig. 3, water distilling apparatus of the present invention is combined in multistage flash evaporation and multi-effect distilling in the casing, the low heeling condition in high back before whole box body is arranged to, parallel series connection is (for the engineering design factor between each casing, under the situation of design and engineering specifications permission, the angle of inclination between each casing can be inequality).Casing is made up of two chambers, and top is the flashing chamber 1 of MSF process, comprises arranging good condensation tube bank 2, as the preheater of new seawater; The middle and upper part is a steam separator 3, can be filter screen; The middle part is the waved plate with Baltimore groove 4, the groove open topped, and these grooves 4 are set in parallel on the scarp of casing, and concentrated seawater flows out with turbulence form from groove; The bottom is the sweating room 5 of MED process, i.e. MED chamber, and desalination water collector 6 is established in its bottom.Referring to Fig. 2, be provided with desalination water outlet 21 in MSF chamber bottom, external in order to the water of condensation outlet box that flash distillation is obtained, merge with the water of condensation of MED process and to collect in the outside new seawater preheating device (referring to schema 1).
Just begin in the MSFMED process, be in the first step-effect, enter the sweating room 5 of bottom by the next source steam of vapour generator, new seawater through preheating enters Baltimore groove 4 by water-in 7 simultaneously, on the one hand because the corresponding saturation pressure Psctl (1) of the first step flashing chamber 1 temperature T s (1) that pressure drop is extremely controlled, new seawater in the Baltimore groove 4 discharges its superheated heat immediately by steam, realize the flash process process.This part steam is through the steam separator 3 of middle and upper part, seawater drip isolate after, restrained 2 condensations by the condensation of top flash distillation plant, form desalination water, splash in the desalination water collector of top, this part water is drawn from desalination water outlet 21, compiles with MED process desalination water in the bottom water collector of next stage-effects, together flows to the new seawater preheating of external heat exchanger (new seawater preheating device) confession (can referring to Fig. 1).On the other hand owing to enter concentrated seawater in the steam heating Baltimore groove 4 of sweating room 5 of bottom, the latent heat of vaporization is passed to concentrated seawater in the groove, make it the part vaporization, form and imitate still-process, self becomes water of condensation, splashes in the water collector 6 of bottom.Steam by this part generation is also drawn by the steam outlet 22 on top behind the steam separator 3 of middle and upper part, goes into steam ports 8 through the bottom of next stage-effect and enters in the sweating room 5 of next stage-effect, finishes the effect still-process in the effect of the second stage-effect.The seawater working condition is identical substantially in later at different levels-effect.
The division principle of three steps is among Fig. 1, difference of altitude is bigger between several level-effects of front end, can utilize the raise concentrated seawater potential energy of each grade-effect ingress of this difference of altitude, make seawater stably flow to the exit along the inclination runner, finish the MSF-MED process in this grade-effect, increase along with level-effect, the concentrated seawater temperature reduces, pressure reduction between adjacent level-effect descends, available pressure reduction is very little, must begin second step this moment, promptly by topping-up pump seawater risen to new height, regains potential energy.Division between second and third step then is raised to 39-49 ℃ with the temperature of the new seawater that is preheated, generally can be about 45 ℃, carry out new seawater extraction system degasification, add processing such as scale inhibitor, chemical treatment and control pH value this moment, returned by water pump more afterwards and continue in the system to be preheated.
Between adjacent level-effect, designed the concentrated seawater inter-stage passage 9 of U-shaped tubular construction,, made flashing chambers at different levels keep the pressure of being controlled, and can provide enough spaces to lay pressure-losses mechanism in order to enough water seals to be provided.This U-shaped pipe runner then changes into the import and export design of topping-up pump at two step boundarys.
Claims (13)
1, a kind of method of utilizing the desalination by distillation seawater, comprise multistage flash evaporation and multi-effect distilling process, in each level-effect, seawater generation single flash, also distill simultaneously, and, the new seawater of the flash-off steam of generation preheating in the corresponding levels-effect and being condensed, except that the first step-effect, seawater distills by the steam heating from previous level-effect.
2, the described method of claim 1, it adopts single flow desalination flow process, new seawater as the water coolant of desalination process with handle after the concentrated seawater reversed flow, absorb the heat of flash distillation and still-process and realize self preheating; The difference of keeping certain height between two successive stages-effect provides the concentrated seawater potential energy of each grade-effect ingress, and makes concentrated seawater all realize gravity flow in each level-effect chamber.
3, claim 1 or 2 described methods, wherein, multistage-effect process that whole desalination process is designed to many steps, each step is made up of a plurality of level-effects, the relative position of these grades-effect is setting from high to low, and the seawater potential energy of poor each grade-effect ingress that raises of keeping certain height between adjacent level-effect is between adjacent two steps, with the potential energy of water pump lifting seawater, and when reaching last step, the new seawater that final stage enters just is preheating to 39-49 ℃.
4, the described method of claim 3, wherein, through flash distillation and distillation, drawn chamber respectively and compiled, and is used for the new seawater of preheating by the saturated desalination water that is condensed in each level-effect for concentrated seawater.
5, the described method of claim 3, wherein, these many steps are multistage-and the effect process comprises three steps, and new seawater enters from the final stage of the 3rd step, and the division points of the 2nd and the 3rd step is that new seawater is preheating to 39-49 ℃ just.
6, the described method of claim 3 wherein, when the new seawater that is preheated arrives latter two step division points, is drawn earlier and is imposed necessity processing that comprises the degassing, adds scale inhibitor and control pH value, is sent back to and continues preheating in the flow process.
7, realize the sea water desalinating plant of the described seawater desalinization process of aforementioned arbitrary claim, comprise a plurality of level-effect molectrons that form by flash distillation and water distilling apparatus combination, these level-effect molectrons are connected mutually, and be configured to many stepped form, each step comprises a plurality of described level-effect molectrons, the relative position of their longshore current journey directions from high to low, be provided with U-shaped pipe between each grade-effect molectron as the concentrated seawater runner, when just be the step division points between adjacent level-effect, this U-shaped pipe runner then is the import and export that are used to promote the topping-up pump of concentrated seawater potential energy.
8, the described sea water desalinating plant of claim 7, wherein, these level-effect molectron longshore current journey directions are inclined to certain angle, and relative position from high to low.
9, the described sea water desalinating plant of claim 8, wherein, at different levels-as to imitate molectron longshore current journey direction to be inclined to the parallel series connection of certain angle.
10, the described sea water desalinating plant of claim 8, wherein, each level-effect molectron is a casing, comprise two chambers up and down, from top to bottom, top is flash distillation plant, the middle and upper part is divided into steam separator, and being provided with the desalination water outlet of leading to outside the chamber, the middle part is the waved plate that is provided with Baltimore groove, the groove upper opening; The bottom is the sweating room of still-process, and the bottom is the desalination water collector, and described molectron is configured to the low heeling condition in preceding high back.
11, the described sea water desalinating plant of claim 10, wherein, the flash distillation plant on each casing top is provided with steam outlet, and the sweating room of bottom is provided with into steam ports, and from the second stage-effect, the steam outlet of previous stage-effect communicates with the steam ports of going into of back one-level-effect.
12, each described sea water desalinating plant of claim 7-11, it is made up of three steps, and the division points of the 2nd and the 3rd step is located between the level-effect molectron of the new seawater that enters from final stage when being preheating to 39-49 ℃.
13, a kind of device that can be used for the sea water desaltination processing, molectron for flash distillation and water distilling apparatus, comprise two chambers up and down, from top to bottom, top is flash distillation plant, is provided with to be arranged with the condensation tube bank, the middle and upper part is divided into steam separator, and being provided with the desalination water outlet of leading to outside the chamber, the middle part is the waved plate that is provided with Baltimore groove, the groove upper opening; The bottom is the sweating room of still-process, and the bottom is the desalination water collector, and described molectron is configured to the low heeling condition in preceding high back.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB011106530A CN1158220C (en) | 2001-04-13 | 2001-04-13 | Integrated multistage and multieffect desalination method and its equipment |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB011106530A CN1158220C (en) | 2001-04-13 | 2001-04-13 | Integrated multistage and multieffect desalination method and its equipment |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1380257A CN1380257A (en) | 2002-11-20 |
| CN1158220C true CN1158220C (en) | 2004-07-21 |
Family
ID=4658732
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CNB011106530A Expired - Fee Related CN1158220C (en) | 2001-04-13 | 2001-04-13 | Integrated multistage and multieffect desalination method and its equipment |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN1158220C (en) |
Families Citing this family (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1302828C (en) * | 2005-06-23 | 2007-03-07 | 西安交通大学 | Apparatus for heat recoverin multigrade flash desalting of sea water |
| CN102603104A (en) * | 2011-01-20 | 2012-07-25 | 四川仁智石化科技有限责任公司 | Innocent treatment method for high chlorine wastewater in oil and gas fields |
| CN110713219A (en) * | 2019-10-12 | 2020-01-21 | 申杰涛 | Multistage flash evaporation technology and device for flash evaporation of flow flash evaporation surface |
-
2001
- 2001-04-13 CN CNB011106530A patent/CN1158220C/en not_active Expired - Fee Related
Also Published As
| Publication number | Publication date |
|---|---|
| CN1380257A (en) | 2002-11-20 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| Saidur et al. | An overview of different distillation methods for small scale applications | |
| CN102531256B (en) | Low-temperature seawater desalination process method and device | |
| CN103880232B (en) | A kind of organic brine waste treatment system and method | |
| CN101489937A (en) | Multi stage column distillation (MSCD) method for osmotic solute recovery | |
| CN104402079A (en) | Industrial waste heat type low-temperature multi-effect sea water desaltation system and sea water desaltation method thereof | |
| WO2006094437A1 (en) | A method and an multi-effect evaporation for waste water of alkylene oxides | |
| CN204298090U (en) | Industrial exhaust heat type low temperature multi-effect seawater desalting system | |
| CN108147608A (en) | It is a kind of to utilize compressed air and the multiple-effect evaporation crystal system and method for heat pump treatment of Power brine waste | |
| CN103613155B (en) | Heat pipe-type low temperature two sea water desalting equipment | |
| CN1171799C (en) | Multi-effect distilling process and equipment for desalinating seawater | |
| CN201587871U (en) | Multi-stage vacuum distillation sea water desalinating device | |
| CN101880068A (en) | Water treatment device and method | |
| CN1760136A (en) | A kind of industrial water system clean preparation method that comprises recirculated cooling water and boiler water supply | |
| CN103663589A (en) | Seawater desalinization method and seawater desalinization device | |
| CN203295308U (en) | Organic salt-containing waste water treating system | |
| CN202849193U (en) | Multistage vacuum distillation seawater desalting device | |
| CN201660457U (en) | Novel multiple-effect distilled sea water desalination device | |
| CN1158220C (en) | Integrated multistage and multieffect desalination method and its equipment | |
| CN106698564A (en) | Sea water desalinization method by waste heat recovery | |
| Al-Mutaz | Msf challenges and survivals | |
| CN112919718A (en) | Low-temperature normal-pressure double-effect high-salinity wastewater evaporation device and treatment method | |
| WO2001072638A1 (en) | Desalination device | |
| CN106966462A (en) | A kind of multistage seawater desalting coupled system | |
| CN1864783A (en) | A multi-effect distilling method for desalt and condensation and device | |
| CN214654253U (en) | Low-temperature normal-pressure double-effect high-salinity wastewater evaporation device |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| C19 | Lapse of patent right due to non-payment of the annual fee | ||
| CF01 | Termination of patent right due to non-payment of annual fee |