DE1769768A1 - Multi-stage system for distillation - Google Patents

Description

Multi-stage system for distillation.

(The priority of the application in Israel Uo.28336 of July 17th, 1967 becomes

claimed,)

The present invention relates to a multi-stage distillation plant. The distillation plant is special, but not exclusively, for the desalination of salty water by the well-known evaporation process by relaxation under Reheating of the steam is provided and is therefore used in the following described in terms of a solohes procedure.

In the known evaporation process by expansion with reheating of the steam, the vapors from the steaming (or relaxation) chambers are brought into direct contact with the diluted water, which circulates through the binding chambers flows. The circulating distilled water is first fed cold into the condensation chamber of the last stage, and the temperature of the water increases to the extent that ea from each stage to the next, the one at

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higher temperature and higher pressure works, circulates, with the ctis temperature and dis volume of the water in the condensate chamber of the first stage being highest and greatest. The distillate is then passed through a heat exchanger in which it is heated by direct contact with an auxiliary liquid, for example with an "immiscible" oil heated by direct contact, part of the cooled distilled water is withdrawn as product and the residue is fed back in order to act again as a condensing agent for the vapor from the vaporization chambers Literature taken from, for example the book "Salt-Water Purification" by KS Spiegier, 1962, Srite 58 pp.

A major disadvantage of this method is the need to a pump at each stage for pumping the distillate from one condensation chamber to the next at which the temperature is set and the vapor pressure are higher. This need to place such a pump at each stage adds to the cost for the brush system and the entire energy requirement and limited experience has shown that the number of possible levels »Bine solution for The elimination of this disadvantage could evidently lie in the; the order of the stages as described in the above-mentioned Buöh Von * Spieglsr are described to reverse, so that calibrate the level with the lowest pressure and temperature is at the top. Indeed, the idea of making the distillate become the

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top level: to pump and then let it move downwards by gravity against the increasing pressure, the idea of using the energy of the lye that evaporates through expansion in order to increase it bv \ 7 <- _i ; < ? n, suggested by Te-ynliam Woodward in Chapter 4 of a recently published book (1966) entitled "Principles of Dosalination ¹¹ , edited by KS Spiegier, at page 130, but it is not an economically viable plant under realization such a system has heretofore been designed or developed.

A system for self-loving the lye has also been proposed (see pages 36-1 to 36-12 of the report on the "Second Suropean Symposium on Fresh Water from Il ^ erv / asstjr", Athens, 9th-12th Hai 1967), whereby the disa ^ s SyatJia ulc "'Jl. ^. ^ I:, .-" system is calibrated. According to this system, a riser pipe (a vertical roll, which has an enlarging cross-beam from the bottom upwards) connects two vertically arranged evaporator stages. The open bottom of the riser pipe extends slightly below the caustic level in the lower evaporator stage, and the open upper end of the riser pipe protrudes a little above the caustic potato in the upper stage. Bf? I this system, however, it is necessary that daa riser has a from untsn upwards widening cross-section, avoid an increase in the velocity of the steam-liquor mixture during the rapid movement diesas Geaieohß z \ x (pages 36 * 3 of the above reference) · Ba is also not possible to achieve substantial buoyancy, especially at low temperature stages. These disadvantages limit the applicability of the "Cl9mentine" system

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very, especially with regard to the desalination of sea water, the should be done on a large scale and at low cost.

According to one aim of the present invention, Bollen in the multi-stage · = Η distillation systems without considering the above Aspects improvements can be achieved.

According to the present invention, a multi-stage system for the distillation of alkalis in particular by means of a plurality of evaporators at different temperatures and steam pressures, both of which decrease from one stage to the other, has been developed, the old system for distillation being characterized in that the evaporators are arranged in increasing peaks, starting with the evaporator for the highest temperature and the highest vapor pressure at the lowest altitude, and that these stage evaporators are arranged in a vaporization circuit that uses the external vaporization energy of the feed liquid in order to drive sis' -ntgsg-n d «r gravity upwards through the successive V = rdenpfsrstufe by this circuit contains a Liituru connecting each pair of adjacent evaporators, and in which conduit a downward-flying column of feed liquid is formed and is maintained, as well as -Λώ.2 län _G -re , ascending cooking mixture column consisting of charge liquid and steam, which flows to the next higher evaporator below - to maintain a liquid level at the lower end of this set up ₆ eud'-ju dupping mixture column for the hydraulic closure ζ isch in the adjacent evaporators.

According to the below _: nb = aeliri ^ bcnsn preferred embodiment of the *. L, r induiV 3 :: .. ηΐϊ hl-. r. ocli den Vci'dh, training cycle in the form

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an ascending corrugated circuit with a vapor «r, which serves to separate the liquid from the vapor, at the apex imagine jader Wslla, each of which will flow downwards end column of feed liquid in one arm of the V / ^ 11 x- contains and the longer ascending Kochgemisclisäula out of liquid and vapor, in the hall every will emerges as that which has been mentioned hydraulic connection between the neighboring evaporators • is located.

As stated above, according to the invention, the boiling process and the external evaporation energy are used to induce the feed liquid (salty water or lye) to float upwards and to flow from one stage to the next at lower pressure but higher altitude . Due to the different vapor pressures in two successive evaporators, a flowing column of boiling mixture of base liquid and steam is formed and maintained in the processing line (sometimes called "cooking line"), the latter having a suitable shape and suitable cross-section to di ? desired height for the Kociisäuls to ^ i. The pressure ski 3dβ between two successive stages FTIR ungs- dia evaporator and Kondensationskanmi ^ rn approximately equal. However, the density of the water in the water line is greater than the density of Kochg ^<j premix in the Koclileitung. Correspondingly, in the state of equilibrium, the height of the column of kocli is greater than the height of the column of water in the same stage. For example, in a 103-stage plant (as beepkrieben sia below) corresponding to the equilibrium levels for

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three stages, d.ii. for the 1st, 52nd and last level, v / i: be foli-t; -

Step? Jr. 5 1 m 2 52 '■' '■' 3 »03 m. Cooking column 3 , 7 m 0 ,8th m 0 , 0 m m Water column 1 ,8th m 2 , 55 m 2 , 024 He’s now chi ede , 9 , 25 m , 976

In practice, the difference in height can be two consecutive Evaporation canisters equal to the height of the fiber column of the same level plus at least 2 straight.

Two forms an evaporating circulation system to be buoyant and evaporation by flashing the feed liquid are HISR described, wherein he ± one form U-Hohre be used and the other mold based on a Manometersystern from the Weil-Tyρ.

The individual objects, features, and advantages of the invention are elucidated from the description below.

The invention will now be made with reference to the associated Drawings described, the various distillation plants, according to the invention for use in the known Verdampfungsvarfahrsn erected by relaxation with reheating of the steam are somewhat graphical and only explain by way of example. In the drawings, the

Figures la and Ib, which when viewed together form Figure 1, a

such an arrangement is shown diagrammatically again, FIG. 2 is a section along the lines II-II of FIG. in which the structure of an evaporation chamber is explained,

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Figure 3 is a section along the lines III-III of Figure Ib, in which the structure of a condensation chimney is explained will,

Figure 4 explains a double chamber system, di ^ for each stage can be used, wobai a chamber as a vaporizer and the other ^ ammer is designed as a capacitor,

FIG. 5 explains an embodiment of a suitable evaporation cycle system with self-buoyancy.

In the drawings, the PlieB- and flow paths of the Plant flowing through and flowing through the following Wise marked: from salty water and lye by a line of alternating dots and lines, from fresh water through a continuous line, of water vapor through a line from points and from the immiscible auxiliary liquid (e.g. liquid hydrocarbon, hereinafter referred to as "oil") through a dashed line.

The system shown in Figures la and Ib contains a large number of "Sntspannungskammern (hereinafter referred to as" V = rdampfungskaünrarn "or" evaporator ") E1, E2, ... Sn, a large number of condensation channels C1, C2, ... Cn, a ~ n first VZaITi "= exchanger H1, in which the hoiäe is distilled? Water heats the oil, and a second v / era exchanger H2, in which that means: 3 oil heats the incoming salty water. The capacitors are arranged in increasing intervals, the capacitor C1 of the first stage mi '; the highest pressure and the hcclie ^ n -9Up era door t ^ i ^ of wrestle en lic'li ·} is UUED to d ^'3 r ^ Zond nsator Cn d "- r · η ultimately Stuf *.?]. i ^; , -l · ':: j sir * r .->"·λ' Si : uc !: u- ^r " dr .ri-

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lowest temperature is at the highest altitude. In the same ':'! - .: lae the evaporators are also arranged in increasing elevations, in that the evaporator E1 of the first stage with the highest temperature and the highest pressure is at the lowest altitude and the evaporator Sn is the last Stage mi ^; the lowest temperature and the lowest pressure at the highest altitude. The heat exchangers H1 and H2 work on the principle of direct contact. For example, it can be used in a heat exchanger which works according to the oil droplet method, according to which oil droplets flowing upwards in one heat exchanger are in direct contact with downflowers; salty water and in the other heat exchanger with fresh water. as it is described by Spipgl? r on pages 58/59 of the above-mentioned Eucii ^ s.

All evaporators belong to an evaporation cycle, the in all ^ enr.inen with ^ P, in which the evaporator by U-tubes 11, T2, ... Tn the B & ihe are connected. J-d ^ s U-Eohr has a short leg, in which one descends si let. ^ nde column of liquid from the salty water or the lye = trained and maintained #% rd, the or that flows out of each evaporator (from the first heat exchanger H1 in the first stage), with the longer ascending Kochgaiiiischsäule from the lye and the steam flows to the next higher evaporator. All capacitors belong in a curb Condenser circuit, which is generally referred to as CP, dir Wsss ^ rloitung ^ n WD1, WD2, ... WDn which contains the capacitors according to v <= rbind? n.

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The salty water is drawn from the B "haitor E1?: I and" through di- I "ump9 3? 1 through daa filter 2 and di i line 4 to jiriem open container R2 is pumped to a low level. The salty one

. V / ass-ir then flows through, the line 6 into the ob ~ r ~ Tiada das Heat exchanger H2, v / o ^ s through upward flow.nd-3 h-iißea Oil is heated and emerges at the lower end. That salty.? '7aseer

. then flows through line 8 (the short leg of the s ^ strm U-tube 11) to the szukrachten line under formation of the cooking line ED1 (which forms the long leg of the U-tube T1) for the evaporator E1 of the first stage . Λ

The evaporator E1 d: r first stage is located at ainar height iibär the outlet t ^ lls far the h, '? IJi5 - i salty what far from the ^! i7ary in3exchanger H2. The temperature and the vapor pressure are lower in E1, however, so that the Balzig-; Water itself iii Kocliaust? ^ ?. is located in the cooking line BD1. The ICochgemisch in Kochliitung BD1 is dall- ^ r of _ώ »ringerer density than the salty" aq-r in line 8 Di: 's-r ^Dichtpunt:. .Rsclii - db ^ v.irkt together with the pressure difference between the vacuum exchanger H2 and the evaporator tr E1 'fin rise-η of the co-ordination by di ■: ICoclization %

BD1 to the higher height 3 d ^ s V _{cr (} a.anpf ers E1.

Jed ^ r is the evaporator with ELNAT Z .. klonanlags (Pigur 2) .- equips £ which a spiral · -, L ^_f: itfläc: ..:, 10 for "jrl: ot separation ..rung .. Deatillationsdaupf of ea of d'n-L ^ ^ ug ntröpf CHSN erkraft by dl · Sohv / and di 'Δ -i-trifu_alkraft contains D ^<r vapor sweeps through άπη 3ctfeuclri; -. r 11 and enters du. ch dc-u; oLv-γλ Sade dsr chamber aua and wircj by L'ii ^H : uii ^ VI to the .zone ^1. (? ne & tor 01 of the first stage, while dis- L- ^ ujo ru ^ dsm un *: rnn

- lü -

1090ΛΑ / 1 362 bathroom original

End of the evaporator through, sine Leu _e .enauir.lsiIli.ituAj 31, 6.1 ζ n ± h d? R. vertical Kochi ^ itun ^ ED2 of the evaporator 12 of the second stage is connected, exits. The emerging from the second ^ rdampf .-, r E2 la el lower temperature and lower pressure is carried through line V2 to the condenser C2 of the second stage, while the remaining liquor from the evaporator E2 through the outlet B2, which is connected to the Cooking line BD3 of the evaporator is connected to the next stage at a higher altitude and at a lower pressure and lower temperature, exits. The process continues through the remaining stages · L represents evaporator, v? * Is maintained if i the salty water in the cooking line between each pair of steps in a Kociizustand and thereby aufstsigt each succeeding stage to the height. The liquor remaining in the evaporator in the final stage exits through line Bn into a tank KjJ and then flows downward through line "20" and the pin control generator IiH to the liquor outlet 22.

It can be seen that the liquor in the Aus 1ε. Γ line (ζ.E. B1 or B2) of a V-erdanpf. -Jrs and at the lower end of the cooking line (ζ.Ξ. 5D2 W. Or BD3), which leads to the next Verda, pfi-r, einsr_ hjrdraulisch? n forms a seal between d-sn two evaporators, so that the Dtn: pf with the higher pressure in one evaporator ^c r does not flow to the next evaporator with the lower pressure.

The evaporation cycle described above, the one Self-buoyancy and -rin & -lbstv3rdampft: 'n the i-iuge causes, can be viewed as if he were in the porm of an ascending undulating Circuit is present, which has a separator for Plüssig-

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kBit and steam (i.e. 'the Y ^ r stampf er) on d'-in climax, j ader V? 11 * contains, the pressure and the temperature from bottom to bottom Above with d? o anst.; ig'iid? n Kreiäkuf decrease - and every wave of the ascending circulation a descending column of liquid (i.e. through line 8 and the liquor outlet lines Bl, B2 etc. flowing lye.) and a longer ascending boiling mixture column (i.e. the I »b-uge and the steam» ', di's «bzvi» der through the Cooking lines BD1, BD2 etc. flow) and the liquid (dia ^ auge) in the valley of each wave a hydraulic lock forms between the -? 611 F-nhölispimkten. . ,

The Eiihlwasserdistillat in the condenser of the last Stage «" is ingested, flows through all by gravity Capacitors up to the first stage capacitor C1, γ / obei Y / annoyed; uiid water of deiii D ^ apf aufgenoi.iia * n to be taken from the Evaporator flows out and flows into the condensers. Of the Coidensator circuit CP, which is described in more detail below will, can be seen as if he were in the form of a sloping undulating circuit is present, which is a line contains, the k j-des pair of adjacent evaporators to each other ^ connects, and in v / elc'ner line a downward flowing column is formed and sustained out of plussiness and one shorter ascending column of! liquid- (or as below is described, the water flying out of the water in the water pipes e.g. WD1, and that flowing up to container 28 Water). Sin Sank "R4 is the last across the capacitor Stage provided, the part of the liquid distillate (the from the heat exchanger H1, as described below,

. - 12 -

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has been drawn), this part of the liquid, Distillate circulates through the condensers.

Each condenser contains a chamber 24, preferably with a cylindrical shape (see FIG. 3), which contains a * ⁶ plurality of perforated plates 26 which are arranged at different horizontal heights within the "chamber" and which with The vapor from the evaporator flows along this undulating path between the perforated plates, while the liquid distillate flows by gravity from one plate to the next, whereby it flows through the holes in the plates and also flows over the ends of the plates.

Each chamber also contains a vessel 28 which is closed at the bottom and open at the top and a conduit '30 which leads from the bottom of the chamber to the next chamber. The distillate flows from the £ & nk B4 through this line 30 into the vessel 28 of the condenser of the last stage and pours into the Koiid ^ -iieatorkammer, whereby v / arry and distillate, which -sich in the Ktrjn-r <? ing «blowing <? n steam has condensed. The liquid distillate leaves the condenser Cn through its line 30 and flows into the container of the next condenser (Cn-1), overflows the container 28 in the relevant condenser and removes the heat and the liquid distillate from the drain; condensing vapor from the evaporator of the relevant stage (3n-1), the process being continued in dirssr manner through cli ·· ^{1 :} n stages of the condenser. ·.

'..'-: il dii ΐ Mi -Ti, door and iUr Dfiupf pressure from inside condenser Cn to; ju - ... I ".o:>. -..-. ..t :. ^: ' cr O ¹ : ... ii: -1 · i ^ - <ii, ^^! Il ¹ "^ any d ^ r LrJ ^! ',; ng-? n 30

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BATH ORIGINAL

a column of liquid between the stages. The amount of each column of liquid is determined by the pressure difference between d-n- two capacitors fixed, and this throws a hydraulic one A seal between the capacitors is made, which prevents that the steam flows from the chamber at a higher pressure to the chamber at a lower pressure. The distillate runs from one level to the next by gravity, .where no special pump is necessary between each stage, wis 83 bai previously known systems was required.

The liquid distillate exits from d'-m Konda'ns a torstuf sn through line 32 at the bottom of the condenser 01 of the first stage, and is now at a very high temperature and a very high pressure, this Distillate is produced by the «Pump ·? P2 is pumped through an additional heater 34, in which the temperature of the distillate is further increased, and is then entered through line 36 into the upper end of the i / ämeaustauschers -Hl. The distillate flows down through this heat exchanger, heating the upward oil, and exits through line 38. Part of the liquid distillate, which is cold but is under high pressure, is supplied by a 1:12 generator. directed to the inlet 40 for the antsalzsne water. The other part is led through line 42 to pump P3, from where it is conducted up through line 44 to a tank H5 located at a higher altitude. This latter tank is open and therefore under atmospheric pressure. The tank H4 is kept at a very low pressure, which is lower than the pressure in the condenser Cn of the last stage, and therefore the distillate flows up from the tank H5 G-around the pressure difference between the two tanks to the tank E4, the flow through a regulator 46 (a known

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Sfasir

"te device) and -ins stand-iting 48 is passed. Yon dsm T ~ nk H4 the distillate is in turn passed through di-3 Eondensa ⁽ ; orstuf -in, whereby the heat and the distillate formed by condensation are absorbed, like 3 ea obsn is described wordo-n ..

In the heat exchanger H1 that is at the lower end Heat exchanger through line 50 and pump P4 a ^ -fliirte cold Oil heated by the downward flowing liquid distillate. The hot oil exits the heat exchanger 111 (as described below is) and is fed into the heat exchanger H2, where it is used to heat the salty water that has been fed in.

Since the jswailigo warm of the GIs changes with a change in temperature, three auxiliary circuits are provided for an oil flow between the heat exchangers H1 and H2 in order to equalize the heat capacity in each of the temperature ranges. For this' Z v / ack has ^ AL3o each of the heat exchanger IH and is H2 (di ?, v / ie set forth above, according to d ^a u vertical, working in direct contact {drip system where if? N 3rwähnten book by Spiegler is described, can be constructed) a different horizontal cross-section ricli f - '. r je ^ .en of the ge named oil circulations. In an auxiliary oil flow, a part of the oil exits through the outlet pipe 52 from the lower, larger end of the heat exchanger H1, flows through a surge generator M3 ¹ and then flows through line 54 into the upper, Larger dimensioned hide d - s heat exchangers 112 entered. In one-in the second oil circuit, another part of the oil emerges through al ν outlet fluid 56 from a higher ^: il of the heat exchanger B H1 with a smaller diameter, flows through a control generator MJ ¹¹ and is passed through line 58 to a lower part of the

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- 15 .— ". ■ - ■

Heat exchanger H2 entered with a smaller diameter. During the third oil circulation, the main mass of the oil passes from the upper part of the heat exchanger E1 with -d? N * smallest - · ΐΐ diameter, di; . Ausittsl ^ itun ^ 60, flows through '"the control generator -MJ ¹ "' and is then through line 62 in the lower part of the heat exchange cliers H2 with d * m smallest η diameter registered. The whole -.,; Cl leaves the heat exchanger through line 64 cold and scatters to the! Pump? P4, uiid v. ^! It is then re-entered in the "Inde." of the heat exchanger H1 through line 50.

The perforated plates 66, 68 and 70 are arranged in the heat exchanger H2 via the oil inlet lines 54, 58 and 62 in order to cause the oil to become part-or drip formed from it , immediately after it has been entered by this Siiila opening-sn - "ii is. line same perforated plate 71 is arranged over the 01-3inla £ l-: itui: ^ 50 in the ^ "heat exchanger H1 / The oil flows on dl-s? u ^r ; is3 in. b? id $: i" iära «from exchanger η in a v-rt-ilten odsr tropfch'onförniigen Sustä-id aufv / ärts, 7 / odurcli a? gro. ". '€ Ocnr- -TlcL *: f-i_" äi- "7ä: .- ;; ..- - -ab ^ r tr a gun =, ^ -sc ^ ii-n vird. ·.

üiiia ülwaschsäuls 0 "^ is on the upper: i Inde of the" »7ärmaausaus rather s H2

■ "■; ■ '■' ■" ^. '■. -r- ■ ■ '■

vor.g ^: 3. "-: ΐΐΐι *" iiri ^ kl'- ^s .i: ie- ll: nge. (s * E. stwa 5 ^) of the resulting distilled Ws-.BS-r from the tank H5 '"/ ird by L? ltu: ig 72 into the above.?r.::- -Snde d- · r ulwasclisiiul = OY / entered. This water runs through sin.I'iltrr 74 (s.3..-us glass fiber), -dss on sin-Bn Sisb 75 bef -: si; igt, u :: d &. 11.33 ■ o'd ^ r? In! 2 ^ iI d- ^ s ^ esa-rs becomes with the help of a l'ric.: T ^ re 7c with ϊΐιν-η Se ::. :: a? Lrolir 77 »das leads to an advantage, ^ saiiailt. The column contains "f -» r.-vr-üins pierced through flat? o2 ui-ΐ -groiT'i-n '^^^:.;. üj r ^; ι- 32 ', in di- L ■ i ^; "; u ._ ::;. 33 ^ injebaixt sinä, vo α ./ο -is SJ -'- i /.^'.-. ο ... u-lrcl.r 84 u .-: I 2- ;. i ^: -: .vv it: .. Y rt ilcr - 1 ii-t .vii-i. 109 8 4A / 1362

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The oil introduced into the heat exchanger H2 flows upwards in a dispersed or droplet-like state, as has been described above, and settles over the divider 86, but as soon as it rises further, the perforated plate 82 distributes it again. Ss joins again over the distributor ¹ 80 and then flows through the filter 74 to an outlet line 87 which is equipped with a reversed converter part 87 ^f at its lower end, the latter above the lower end of the funnel 76 is suitably arranged so that fc is above the level of the water it contains *

Dis Ölwaschsäuls OW to dm lower sin of the heat exchanger H2 washing the oil entrained salty water droplets and reduces the salinity of the water contained therein in the following · Wsise v / esentlichi First, the ^n> & sser forms of the manifold 86 üb an upper layer '-. R the fed-in salty water (which is introduced through the inlet line 6), so that the oil flowing upwards mixes with the washing water layer rather than with the originally fed salty water. The il with dem.öl during W Zusaoaenfließens over the V6rt <= r 86 entrained water is therefore considerably less salty, than it would be if. would premix the oil with dsm fed salty water. These entrained water droplets are carried with the oil to the heat exchanger H1, and because of its lower salt content the distilled water is less contaminated there than if the oil droplets could have been carried along by the fresh salty water. Is G-flrgf-ntlicli may be greater the entrained ^ Wasaermengft in the form of the "diluted" droplets, it ala 6 &] ohns the Wied ^ rholtfη washing processes würöf once ^ «äocli the oil in d ^ rn heat exchanger 111 is heated, it dissolves einön big part

109844 / 13.62. .. bath

These droplets and, accordingly, a smaller hatchet of the. Γ3ϊή-.3Π distilled water from the heat outlet cn · ".r E1 than it would otherwise be the ^ aIl. The salt content of the. '"' aseers entrained in the oil is " Passing on of the heat exchangers H2 in the i & aß- is further reduced, in that the oil (in dispersed form) in the tree between the perforated plate 82 and the Vsrtriler • because the Cl is washed by the "water that by di; Soliv / * r power of d ^ ia V _sr -part-sr flows downwards through this seam, the salt content of the water carried along is reduced still further by the Filtar 74, in which it was washed with the desalinated water introduced into the filter through the inlet 72 will.

In the following, a system according to the invention is exemplified Explanation of an embodiment of the invention with approximate values described. -

In disseiü ispiel B-103 levels (preferably at a slope) assembled vertically or on a Iiei ₆ ung. Dis • l'-HipÄ.ra ' ^! 'ur and the pressure of the salty water (Mesrwasaer) bein: Entry into di'-firsto pre-steaming stage S1 (ie at the lower end of the KociLUi-exercise BD1) is 180 ° C and 100.3 m Vfess? r. The temperature of the salty water falls after each level of dipping, and the temperature of the desalinated water increases by 1.5 ° C with each level of condensation Steam entering the condenser is 178.5 ° C, and the temperature of the cooling water flowing out of the first condenser is 177.5 ° C, and the last stage (ITr. 03) is below -. difference between the 2-mperatür of flowing into the vapor and the temperature Zondensator d ^ s aug d "m capacitor auBfliai - iid .-- n Ktüildeeifcillata 2 ° C" disser ¹ S * raperaturunterschied NIIM ^ t and by

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BAD0R1GINAL

after from the last to the first step, so dal; the difference in the first stage is 1 ° C ". Di-: T-.mpprature of the remaining, from Ä? .L · Hohr Bn after the last-n" evaporator flows out - ^ - nc !. The temperature of the cooling water flowing into the last condenser is 20.5 ° C.

The vapor pressure of the desalinated water leaving the condenser C1 (at 177.5 ° C) is 9.65 kg / cm ² or 96.5 m of water. Assuming that £ di; suitable height for each iond ^c .iisatorkammsr is 1.5 m and 50 m for pressure reduction in the d · 103) bsi ci-i -: r height of approximately 300 m above the first Koiidensationsksniisr b. The last evaporation chamber Sn (Ur.103) will advantageously also be at a height of about 300 m, provided that the height difference of z "* of successive evaporators is equal to the height of the water column of the same stage plus 2 m is, wi-c it further ob.n has become bischx-i-'ten for the Zondfinsatorfn In this example the salty Vfess ^ r ara unt: r ^: -n 5n.de of the first Eochsäule (BD1) 180 ° C and a pressure of 100.3 m of water. The temperature and pressure v; ürd-i, up to the last V? rdanpferstufe En (lir. 103) by about 25.5 ° and un? ir.:; .. pressure from «-tv / a 0.32 m of water fall.

In the present example, 1000 kg of salt water (from 20.5 ° C) would pass through the outflow 40 for tfüotilliert a «Yasser and about 3000 kg of Hestlauge (from 24 ° C) ) duich d.-n Ls.ug '- nausflul: 22 (where di =. lye contains 4.7 £ SkIz;) from 4000 lig Ii. ^ r water (which contains 3.5 S * salt), which in cLU system with 17.5 ° C

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109844 / 136.2

sp-fis-t can be obtained. About 3870 kg of distilled water (with 177> 5 ° G) would pass the condenser CI of the first stage and would pass through. Fuel heat (common fuel or nuclear fuel) "can be heated to 183 ° C at the heater 34. The enthalpies of pure water of 177.5 ° C and 183 ° C are 179» 65 Ecal / kg and 165.4.0 Keal / fcg. Consequently the theoretical heat requirement (Q) per 1000 kg of desalinated water product would be 3870 · (185.40 179.65) or 22.25 Kcal ". The degree of concentration (E) would correspond to 45 kg of washer product per 1000 Kcal. The through-miss ratio (salty water / water product) would be 4. The relaxation temperature would be ISO ⁰ C - 24 ° C or 156 ° C.

The 3870 kg of salted water at 183 ° C were "used around the oil in a heat exchanger Ht from sthE. 18, -5 ° C to 181 ° C to heat, and the hot oil would be used in the heat exchanger H2 " up to 4000 kg of fresh salty water at 17.5 ° C To be heated to 180 ° C. -

entire. Work output "in the water and oil circuits per 1000 kg of distilled water produced would, as expected, assuming that the pumps and the control generators are working with 85j6iger output, after a preliminary calculation? Those for pumps P1, P2, P3 and P4 required power is expected to be 470600, 508100 and 588000 kg «m. The drive power" of the control generators MI, 112 and (M3 ⁴ , M3 ^lf , HJ " ¹ ) is expected to be 739500, 118200 and 469800 kg» m. The total work output is according to these Calculations therefore as expected ■. * ■ "■ ■ ■ ■

764200 kg «m or 1.4 Kwh.

- 20 -

109844/1362 BAD «« BW.

For comparison, table I below shows comparison data for the anticipated working conditions and the values for Q (theoretical heat demand) and R (degree of efficiency) indicated,? / ie sis according to your example discussed above (referred to as attachment no.1) and after three examples based on known flash evaporation systems (referred to as Annexes ITr.2,3 and 4) are. Appendix Mr. 2 is a multi-stage stress evaporation layer with a device for heating the eyes to 143 C and 121 ° C (see page 152, Mg. 164 of "1965 Saline Water 'Conversion Bepört "published by the U.S. Office of Saline Water). Annex Mr. 3 is a multi-stage satellite voltage evaporation system with lye circulation, which was established in HLiat, Israel (cf. the article by L. Steinfeld and A. KLkinis, published in the "Journal of the Association of Engineers and Architects in Israel ", May / June 1965). Plant No. 4 uses steam reheating and liquid-liquid heat exchange, which was developed by PMC Corporation, Santa Clara, California (see. Office of Saline Water Report, No. 78, September 1963).

In table I dis is due to the condensation of relaxed water vapor heated liquid with "SW" for incoming seawater and circulating lye in systems no. 2 and 3 and with "W" for circulating and flowing desalinated water in the systems No. 1 and 4 designated. The lye that evaporates through relaxation is labeled "B". .

- 21 -

109 844 / 136Ϊ bad original

Table I. Comparison of the working conditions and the values for Q and

into) Attachment 1 system Last stage Pressure m First stage 5.55 CVJ system 5 ,.O system 4th I. 2 • in) -B (out) 105 72 Temp. ⁰ C water 95.17 50 20th Pay the levels into) 0.292 6th 2 beyond) 24 O..52O 1.5 . Temp . ° C < D ^ mi 56 C Temp ⁰ C 2 out) -W (in) 25.5 0.028 176 Q. 70 96 SY / (in) 1.5 0.246 96.50 21st .1 54. 52 B (out) SWi out) 20.5 0.270 5.40 22nd .95 56. 57 B. SW (out) -SW (in) 22nd 0.024 1 96.90 1 .85 1. 5 B. B (out) -W (out) 1.5 177.5 100.50 8th 22nd W. B (out; -SW (out) 1.5 76 27 W. 178.5 96 5 W. SW (out) -SW (in) 0.022 180 15th .6 27 SW (in) 2 17th .45 29 84 W (out) -W (in) 1 .85 1. W (in; 96 5 B (out) -SW (out) 5 .67 4th 64 SW (out) B (out) -W (out) 1 .7 ■ 1. Y / (out) 156 .5 84. 96 B (in) -B (out) 6th 5 B (out) B (in) 5 .6 4th 158 86. 96 54 5 5 122. 1 .7 1. 5 141, , 6 91. 127. 145, , 5 95. 152. .2 .2 .2 .2

22.5 kcal ■ 1 kg of product

45 kg product 1000 Kcal

50.6 52.7

70

14.5

73

15.5

Flow ratio

5.8

10.5

5.5

Relaxation

Evaporation area

Temperature increase through additional heating provision

156 ° C

5.5 ⁰ C

122 ° C 59 ° C 100 ° C

5.5 ° C 6.7 °

15.5 ⁰ C

1O98A4 / 1302

- 22 -

Has been connected in the "Clementine" -Auftriebsverfehren, it wii above briefly discussed, a riser (a standpipe mi ¹ - from the bottom to whether ^ n widening cross-section) in two s-inkrr. elitist Lg ₁ ^ - = - subordinate levels. These levels are called KaruEggs 1 and 2 and the saturation pressure and temperature with P ₁ , P _? and T ₁ and T ″ denotes. The open bottom of the riser pipe is slightly immersed in the lye below the surface in the lowest chamber (1), and the open upper part of the riser pipe is arranged a little above the ocular mirror in the upper chamber (2). The following data are given in a sample on pages 36-9 of the aforementioned reference:

= 1.033 ρ
kg / cm σ C. 2 = Ο; 935 kg / cm = 100 ° / Dd = 97.2 °

Under these conditions 5 kg of water vapor are converted from 1000 kg salty water with a salinity of 3.5? ° through relaxation evaporation frsi.

The volume of the relaxing mixture or the cooking mixture of lye and steam is at P ₂ = 0.935 kg / cm ² and T ' ₂ = 97.7 ° C (T'p is the saturation temperature of the salty water at i " while T ₂ ^dis Sättigungstamperstür of pure water at P ₂₎ is about 10,000 1 and outer dia evaporation energy of 5 kg V / ater about 84500 kg-m (approximately 40kcal / kg evaporated water). Theoretically, this ürj.ir _{s is} amount can raise the tensing mixture or cooking mixture to a level of 64.5 π. In practice, however, the "Cl« mautine "system achieves a lift height of only 0.91 to 0.95 m.

1098U / 1362 - ₂₃ - bad or.ginau

'- 23 -' .. ■■■■. ' ::

iei df-m erf i: aduiigsgriaä £ ~ n system are, as has been explained above, the outlet or lye solutions (B) and the cooking line (3D) also connected to each other in their lower uide and form U- Pipe e. These are used to connect the lower end of each evaporation chamber (1) with the subsequent upper chamber (chamber 2) at a point which is above the ocular level of the latter. As the lye flows through the lower ΐ ~ ϋ of chamber 1 into the shorter leg of the U-shaped tube, it forms a Lgug ^ n column with a height of h .. in this leg. The overpressure P is = hd, v.snn d dit; Is the density of the lye, for which 1 Λ is used. This pressure, together with the pressure difference in the two ammers (P. - Pp), corresponds to the pressure Pg ¹ = hpd ^{1 of} the boiling mixture column in the longer leg of the U-tube, which leads to the interior of the% mmer 2, plus the pressure drop A. p »which can be traced back to the flowing of the lye and the cooking mixture through the U-ear.

The condition for the height of lift of the eye of level . 1 to level 2 are determined by the inequality:

h ^> ^ e ₁ - P ₂ ) >> ₂ d »+ 6ϊ ^

The lift height is (P- - P ") - +. A (both in m water). The symbol "ä · ¹ is the height of the steam-filled space in the Eonaensator, in which the condensation between the steam and the cooling liquid is brought about directly, plus the pressure drop in m water, which is due to the flow of the liquid for larger plants is a ^m "equal to or greater than 2 m, preferably 3 m _# The Auftrisbshöhe for large installations is 3m 'where h = h + P. -. P ₂ is in m of water. In the example above, h = 0.98 m of water, under

1789768

assuming that 50 $ of the evaporation takes place in the cooking limb (of the U-tube) and 50 $ in chamber 2, the mean density is d. ^{1 of} the cooking column for the conditions of the example above:

d ¹ = Ϊ000 / (2.5 χ 1780 + 997.5) - 0.18 kg / l and_ the above inequality results

'ü 4 + 0.98- ^ (Il, + 0.98 + 3) 0.18 + AP orer

0.82 Ji ₁ + 0.26> ΔΡ

If Yes ... = 2 then * & P <^ 1.90 m of water for a length of the U-Eohr of about 12 m.

It is easy to see that for a large diameter of the U-Hohrs, and especially for a large diameter of the Kochschen- ' kels, reached a very high speed for the cooking mixture can be if the ^ eye limb of the U-Hohrs dift required Having height.

The present invention therefore makes it possible to produce a? substantial To maintain lift height even at steps with lower temperature, which is not possible with the "Clementine" system. Also requires the present invention does not use risers that widen from bottom to top, which is what the "clementine" system does is necessary to avoid an increase in the speed of the steam-Leu ^ en mixture during its relaxation.

FIG. 4 illustrates a modified system in which each evaporator-condenser stage consists of double-chamber devices SC1, SC2. Each of these devices is in the form of a cylindrical vessel with a transverse wall 150, where the vessel is in a? Ver

. 1098U / 1362 _ _ßAD

- 25 ~: -.; ■ .- ■

Steam chamber B and a condenser chamber 0 separate »The U-tubes ITt, IT2, ΪΪ3 connect all evaporator chambers in sequence, and the inclined tube CCP connects all of the condenser chambers

. Sequentially. The lye from which the steam is released by relaxation forms, moves against the force of gravity upwards through the U-tubes and evaporators in the following order: The pure cooling water,

, through which the relaxed steam is condensed, moves see through the force of gravity downwards through the inclined tube CCB and, in accordance with the sequence, through the condensers.

In the system EC2 of Figure 4, this occurs through the inclined pipe CCP downward flowing cooling water through inlet 152 into the Condenser chamber and flows through a through line. 154, which forms a basin above the perforated plate 156, upwards * The pure cooling water then flows according to gravity in the form of thin rays or drops through the latter Pl & ttε through and flows through outlet 158 in dis inclined Tube CCP back, where it goes to the system of the next lower level, in this Pail EC1, flows. The inclined pipe CCP is with a ÜLilinklDlech 160, through the daa mixture of pure Water and oil are directed in such a way that they are at the desired level Moving paths.

The ^ & uge in the Vf-rdanipfungs circuit system ', ϊ3 £ moves en ¹ ^; - ig'? Η of the force of gravity through the U-tubes TT1, TT2 etc. from the evaporator E of one stage to the closest stage upwards. This mixture is lifted from one stage to the next by the external energy of the water evaporation. For this purpose, each of the U-tubes (e.g. U-tube TT2, which contains the

1098U71362

" ²⁶ "

A short leg Ts (comparable to the eye outlet line B1, B2, etc. in Figure 1), which is connected to the outlet of an evaporator, and a long leg Tg (the cooking lines BD1, BD2, etc. in Figure 1. Comparable), which is connected to inlet 162 of the evaporator of the next higher elevation. The vapor pressure in the evaporator of the plant from the lower stage (301) is such that the liquor in the short leg Ts is in liquid form, whereby a Q downward flowing liquid column Ii is formed in the short leg Ta. The vapor pressure in the evaporator of the higher-stage system (EC2) is somewhat lower, so that the eye that flows up through the long limb Tg is in the Eoohg state, whereby an upwardly flowing column of mixture BM 'comes out and water vapor is formed T The lower end of the Eoch mixture column is denoted by BM * and is located at a level which is below the upper Sn.de of the downward flowing liquid column L in the short leg Ts. The tsil of the downward-flowing liquid column L in the short leg Ts above the level EII'br sits at a sufficient height so that the overpressure of this liquid column together with the pressure difference from the two stages equals the overpressure of the upward-flowing cooking mixture column BM in your long limb Tg and the pressure loss · - · compensated by the S ^ rciun d ^ r fluid. Thus the liocli ^ uiscii vos dfu evaporation of the "rine stage" is raised to that of the next stage, while the liquid is in the ^; The liquid column L as well as in the connecting piece between di ·. s \ ru ^ id of the upward-flowing coconut mixture column BM (that is, the liquid up to the level BlI ') creates a hydraulic seal between the neighboring evaporators.

10 9.8 A 4/13 62 - 27 -

BATH ORIGINAL

• Ia Pigur 4 represents "h ^M the difference in vapor pressure, in m water, '■ ...: between the systems EC1 and 202, ^M b1 ^tt represents the height of the '& liquid column L in the short leg Ts above the mirror BM, and% 2 "represents the height of the cooking mixture column BM in the long leg Tg. In large systems, an effective condenser should also contain condensation and flow areas. a height of 'about 1.5 m and an additional height of 1.5 m should be provided for a pressure drop that is caused by the downward flow of the circulating pure water from step to step'. The TJ-Eohr should therefore be constructed in such a way that the height (h2) of the cooking mixture column BIi is greater than h1. + h + 2 m, preferably equal to h1 + h + 3 m, in order to "cause the lye-oil-mixture to rise" from one evaporator to the evaporator of the next stage.

The 'Kochgf'misch flows through the 3inlai 162 into the evaporator, where the evaporation takes place through relaxation. The liquid phase (ie di-3! ”Eye) drips down and flows through the short leg Ts of the U-tube to the next evaporator, as described above . 164 down through a line 166 .and. upwards through eia ·? perforated plate 168 with a large lociidurchiaessirr -in di ° .Konde; isatorkanm «r. C, where it condenses on the jets and droplets of pure water lying upwards and flows through the condenser due to its gravity. The li'-ng'i 'and the temperature of the water are increased at the rate in which the water flows downward through the condensation circuit from one condenser to the next. The pressure difference of dvsn two stages is v / by one

1098A4 / 1 3 62 - 28

_B AD

Vacuum control device 170 maintained at each stage, the device 170 being designed to be a tube with openings contains - which has a line to the condenser chamber both over as well as under the basin placed on the perforated plate. The liquid between the baffles 160 of zv / ei successive stages form between the steps a hydraulic lock.

Bs can be seen that the same type, according to which the liquor lifting system works, with other circulatory devices than the U-Sohre TT1, TT2 etc. can be equipped and that the evaporator each stage in a separate plant from the condenser

♦ may be present.

One such modification is shown in FIG. 5, in which the j-Tdsr evaporator .LiI ¹ , 52 'is located in a separate plant. AUj- ~ rd-Ei v / ird-. · 11 -.- from U-üolir-ni -sin ·? i'ianom? teinrichtung from "» 7.- .. 11-Tyρ used. J-.d-.r evaporator is in the form -.iinss horizontal- ^ n cylinder and is with nin; -r dedicated line odsr -in ^ m s-rikr 3 hurried Sei: -nk ^ l 172 v? rbund? n, d-: r und? n is closed. That under ---: Isnde d = r Itoiirl-'itung 174 i & t near ά-. ΐη Bod-n des Schenk ^ -lö 172 ang-. oi'dnet, while the upper. ::, Sude mi ', the Sinla ·? · des or ^ aclibartsn höh-; r fii V ^.; rdaL.pf-rs "i2 'via dsn Spi.'rj ^r l which is connected in it b ^: Ί ΐΐιά1ΐθίΐ..η liquid kit. The steam flows through -iinan iaitf euchtir 176 to an outlet from the ³ line 178, which is connected to the condenser at the stage.

It can be seen that the Hoho (h1) -the liquid in the evaporator and its legs 172 from the lower level to the level of the under-311 3nd & 8 174 'dor formed therein Eocii, -; iiiisciiöäule dtr liquid column L iu the short handle Ϊ «

1098 44/1362

SAD ORIGINAL

corresponds to the system described in FIG. 4, and that the height (h2) of the cooking mixture column in the pipeline 174 corresponds to the height of the cooking mixture column BIi in the long leg of FIG. The liquid in the evaporator and the lower end of the tube 172 together with the liquid form the lower part of the pipeline 174 up to the level 174 ^f the. hydraulic lock between the evaporator stages.

'Desirably a can one. A number of cylinders or legs 172 with its pipeline 174 can be provided for each cylinder or leg between the evaporators, if an adaptation to the flow rate of a larger amount of the Koohmixture is to take place. An equal number of U-tubes (eg TH -— £ Tn) can be provided according to the embodiments of FIGS. 1 a, 1 b. ^:

It may also be necessary to move the mixture during its flow from one evaporator to the next. This is preferably done by blowing in steam or by mechanical means Move the liquid fragrance at the bottom of the longer leg of the U-Hohr in Figures 1-4 or on at the end of the contact line 174 in FIG.

To reduce the G-vSeed height required for a system with a If a large number of stages is required, the evaporators and condensers can be arranged in a large number of windings with the first step of each turn "starting at the same bottom level and the last step of each turn ends at the same highest altitude, for example on

- 30 -

1 0 9 8 A k 1 1 3 6 2 bad

Salts 130 of the book "Principles of Sesalination" published in ^ ahre 1966, edited by E.S. Spiegier, is described.

It is to be understood that the above values are based on preliminary calculations and are only given to illustrate the principles of the invention and that these values are not necessarily accurate and do not need to be adhered to for the various features disclosed to be successful. It is also self-evident that the embodiments described represent only examples and that many other changes, modifications and transfers of the invention or some features of the invention are possible,

BATH ORIGINAL

1098U / 1362

Claims (11)

Patentan's claims 1} Multi-stage system for the distillation "especially of eyes" by means of a plurality of evaporators at different temperatures and vapor pressures, both of which decrease from one stage to the other, characterized in that these evaporators are arranged in peaks to be increased, starting with λ the evaporator for the highest temperature and the highest vapor pressure d-.sr lowest height, and that ^di;? se stage evaporator angeorel in an evaporation cycle · - are nrt, the rdampfungsenergie the outer Vr = uses the Bsschickungsfllissigkeit to them against gravity through the V-? rdanpf -rstuf en to drive upwards by di-s -.τ ICr.vislauf «? a line that contains the j- ^ des i ^J aar b -ixaclibärt ^ r evaporator raitc-inandsr connects, and in a v / elcher .line trine a downward-flowing column of 3: schiQkun ^ siquid-k-'it is formed and maintained, which flows out of its evaporator, eo'.vie ^ ine longer, ascending Eocheemi sciisäulf :: from Seschickuii ^ sf 1 bite and steam, the next higher "placed ^ -iien evaporator together uiit-r preservation eiii-s I? l ^; issi _: -: k? its3piegel at the lower end of this rising steam g ^ miscli column for the hydraulic closure between the neighboring evaporators. "■■■ -. ■ ■ - - 2 - BATH 1098A4 / 1362 2) Plant for distillation after. Claim 1, characterized in that that the evaporator cycle system in the form of an increasing undulating circuit with an as,! Drenn-. device for liquid and vapor serving evaporators is formed at the apex of each shaft, each of these shafts having the downward flowing column of feed liquid in its one arm and the longer upward flowing Cooking mixture column of feed liquid and steam in its other arm and the feed liquid in the ^ aI of each shaft contains the hydraulic lock mentioned forms between the neighboring evaporators. 3) Plant for distallation according to claim 1, characterized in that the line which connects each pair of adjacent evaporators with one another is in the form of a U-tube with a short leg in which the downward-flowing liquid column is formed and maintained, and with a long leg in which the upward flowing cooking mixture column is formed and maintained. 4) Plant for distillation not required. 1, characterized in that that the conduit connecting each pair of adjacent evaporators has a leg leading from the lower part The end of each vaporizer and contains a pipe, connecting each evaporator to the evaporator of the adjacent higher stage, the lower end of each tube in the called leg of the evaporator in question is arranged and the upper volume in the adjacent higher evaporator is arranged above the liquid level present therein, - 3 109844/1362 1769763 by placing the thigh and the pipeline a manoiueterayatem • from the WeIl-Tyρ, where in this manometer system in the called Hohrleitung the upward-flowing cooking mixture column is trained and maintained and the compliance in the lower evaporator and leg above the lower end of said cooking mixture column said one downward flowing liquid column forms. ■ · 5) Plant for distillation'nach one of claims 1-4 for use in a system with capacitors through which a Cooling liquid flows - and at which liquid the vapor • is condensed directly, characterized in that the. Height of said Kochgemisohsäule at least the same h ₁ + h ■ + a where "hl" di-3 is the height of the liquid column, "h" is the difference in vapor pressure in the two evaporators in meters of water urid "a ^{11 is the} height of the steam that fills the edge of the condenser, in d * m -di * direct condensation of the vapor and sr cooling liquid is effected, plus the pressure drop in meters that results from the flow of the feet. 6) Plant for distillation according to a dar.Ansprüche 1-5 »thereby characterized in that it contains a Koxidenaationakrsislaufayatem with -then multiplicity of in h? ine interconnected Capacitors, one for each stage, with different temperatures and pressures, both of which decrease from one level to the next, being the plurality "of capacitors also with : increasing Ub3-rhöhüngen-with the capacitor with the highest Temperature and the highest vapor pressure at the lowest altitude 109844/1362 -V- BATH are arranged, further comprising a pump for pumping the Coolant to the condenser with the highest height and the lowest pressure is available, the so-called cold cracking. by gravity flows from one condenser to the next, while it flows through the condensate taking place on it tion of the vapor from the evaporator of its corresponding Stage is heated, said condensate circulation system includes a conduit connecting each pair of adjacent condensers connects with each other, in that in the line a downward flowing coolant column and a shorter upward flowing coolant column are formed and maintained. 7) plant for distillation according to claim 6, characterized in that that said capacitor line includes a line extending from the lower end of the capacitor of each Step into the interior of a container that goes into the condenser the next lower level is arranged, leads. 8) Plant for distillation according to one of the claims 6 or 7, characterized in that the evaporators and condensers from each stage consist of a single device, which is separated into two chambers, r / obei the one K & coer as Evaporator and the other - ^ aminer designed as a condenser is. 9) Plant for the Festillation according to one of Anspritzer'6-8, thereby characterized in that it has a first heat exchanger for heating an auxiliary means for heat exchange that hot *? liquid leaving the condenser system 109844/1382 " ⁵ " • ORIGINAL BATHROOM ■ t distillate and a second heat exchanger for heating of the feed liquid by the hot auxiliary for Ή ■ · ■ ■ ■ ■ ■ ■ ■ ^ * contains the heat exchange. · 10) plant for distillation according to claim 9, characterized geksnnzeich- ' • 'net, the said tool for heat exchange a is liquid immiscible with the feed liquid and the liquid distillate, the plant is also means for diverting a small portion of the cold liquid distillate to the second heat exchanger at its end, through which the immiscible auxiliary liquid for the ' Heat exchange emerges, with a separating layer consisting of * - " liquid distillate between the feed liquid and of the emerging immiscible auxiliary liquid for the Y / arm exchange, - with which separating layer the latter Liquid flows together, whereby the feed liquid, those with the immiscible auxiliary liquid for the Heat exchange has been entrained, is diluted before the latter is fed into the first heat exchanger. 11) plant for distillation according to one of claims 9 or 10, characterized in that the two said heat exchangers work according to the vertical principle with direct contact, whereby in the heat exchangers. Means are provided, the one Variety of flow circuits from the auxiliary liquid for the heat exchange between the named heat exchangers enable and every cycle within a temperature range works that depends on the temperature of the other circuit 109844/1362 is different in that there are cliings in the two exchanges of heat separate heat exchange sub-areas for each cycle are provided with a different horizontal cross-sectional area than that of the other sub-areas. 1 09 844/1362 bad original