DD161075A3 - METHOD FOR ABBEER USE FOR GENERATING MECHANICAL ENERGY WITH OPTIONAL CELL GENERATION - Google Patents

Abstract

The invention relates to a method for generating mechanical energy from Abwaerme as Nachschaltprozess Abwaerme producing thermodynamic processes and cycles, wherein the case usable heat transfer in the range of low temperature levels (<equal to 250 degrees) The aim of the invention is to make a thermodynamic cycle such that Abwaerme low levels can be used by cooling verwrachtlich by 100 degrees C for energy production. The essence of the invention is the fact that in a cyclic process a high-pressure working fluid is released by desorption at high pressure, superheated, expanded in a multi-stage extraction turbine work and dissolved by gradual absorption back into the solution, i.e., in the absorbent.

Description

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Title of the invention

Process for the utilization of waste heat for the production of mechanical energy with partly equal production of cold gases

Field of application of the invention

The invention relates to a method for generating mechanical energy and consequent electrical energy from waste heat with optionally simultaneous Etegen production, wherein the proportions of the generation of mechanical energy and refrigeration can follow strongly fluctuating demand ·

The process can be used as a downstream process (coupling process) of waste heat producing thermodynamic processes and cycle processes (chemical processes, combustion processes or other thermal energy processes), whereby the generation of mechanical energy is paramount and refrigeration can be assigned with a variable power component ». Waste heat is the primarily unusable portion of the heat conversion rate of thermodynamic processes that occurs in the range of low temperature levels of heat transfer media ( £ z 250 * ¹ G) and which is not or only occasionally or only to a minor extent for other process * external heat consumers can be used »

Characteristic of the known technical solutions

It is known that by evaporating and superheating a pure substance at high pressures and temperatures and then condensing the vapors in the vicinity of the ambient temperature, a thermal gradient for generating mechanical energy can be obtained (ζ «3» Olausius).

Rankine cycle). Furthermore, the use of pairs of working substances is known in which by heat from a solution a working fluid is released at high pressure (desorption) and at low pressure, low temperature and constant heat dissipation with low concentration of the solution is taken back from the solution (absorption) The heat gradient of the working fluid obtained in this way can be used to obtain mechanical energy, and this heat gradient can be increased by overheating the working fluid after desorption Contradictory reasons are that high heat gradients require a low absorption pressure, but on the other hand high deaeration of the solution is required to implement low absorption pressures. This results from the equilibrium conditions of the known working substance pairs solution of the desired desorption pressures can only be achieved by means of high desorption temperatures, this inevitably results in a limitation of the usable heat gradient and thus in waste heat quality, ie the heat transfer mediums used can not be cooled to the desired degree.

Ss are also known absorption refrigeration systems, the. are used exclusively for the production of cold from existing waste heat. The requirement for the Yerdampfungstemperatur of the refrigerant used, however, limits the amount of concentration of the rich solution and thus for the achievable cooling of the waste heat carrier, ie for the utilization of waste heat with low temperature level. The equilibrium concentration of the working medium vapor in working substance pairs with absorption liquids whose vapor pressure can not be neglected in the range of working temperature requires at low concentration of the rich solution next to the expeller column of the desorber an additional column with reflux generator (Dephlegmator) »Seasonal or short term

However, fluctuating demand for refrigeration restricts the uniform decrease of an existing waste heat demand.

According to DE-OS 940 466 and 942 515, multivolume processes for the conversion of heat into mechanical energy are known, which operate with a turbine in which the expansion of the working medium and its recompression takes place by absorption in a solution in a plurality of sintered stages the turbine is already removed from intermediate stages and introduced into the absorber with staggered pressure level. "In violation of the countercurrent principle, however, the poor solution (the absorbent) is completely released into the absorber with the highest pressure level, the rich solution thus produced from absorber stage to absorber stage further reduced in pressure, the working fluid thereby released to a large extent again and advantageously a larger loading width (Bntgasungsbreite) prevents it «occur in this multi-stage Yerfahren compared to a process with only one relaxation Gsund Absorptionsstufe Losses and Disadvantages to "The relaxation of the working fluid is only up to the removal parts of the highest pressure stage. The cost of further withdrawals is therefore disadvantageous and unjustifiable." In another method, the desorber by a heat exchanger with subsequent container for separation The contact between solution of medium concentration and working fluid, the Hess of the working medium vapor must be necessarily low, if the vapor pressure of the absorption liquid is not negligible "This leads to losses in the thermal gradient of the turbine and prevents the desired strong cooling of the heat carrier "In addition, the working fluid vapor can not be used for cooling without additional rectification."

A disadvantage of this method is also the renunciation of regenerative heat exchange zwischen.armer and rich solution. The rich solution is preheated by hot breath gases

The cycle thus receives too much heat, which must then dissipated from the poor solution back to the environment v / ground and instead of the heat exchange between the pure products, ie the rich and the poor solution, two heat transfer processes occur - each with a polluting medium (Zeitschrift Energie 26 (1974), 3 » ^p . 83« · 87) or * similar to: (DE-OS 2 $ T 42 263). - ''

Object of the invention

The aim of the invention is to develop a thermodynamic cycle in which at the same time mechanical energy and optionally cold, with flexible portions of the energy forms, are generated as waste heat of low temperature levels, whereby the heat carriers are cooled in a wide temperature.

Wide temperature range to considerably below 100 ° G

Explanation of the essence of the invention

The invention is based on the technical object of a method for the utilization of waste heat low temperature levels as Hachschalt sorption of thermal processes using a pair of working with well absorbable, low pressure at ambient pressure high pressure working fluid and a suitable absorbent for generating mechanical or electrical energy with wahlv / iron In this case, the high-pressure working fluid is released by desorption at high Brück thermally from the solution, superheated, in a removal turbine work performing relaxed and by stepwise absorption - according to the pressure levels of removal of the turbine with simultaneous heat dissipation again in the liquid solution, d * H # are bound in the absorbent, wherein high saturation of the rich solution and consequently low Desorptionsanfangstemperatur, a cooling of the heat transfer in the broad temperature range and the use of waste heat of low temperature levels is made possible *

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Brfindungsgeinäß this object is achieved in that the obtained at the lower end of the desorber poor solution their sensible heat first predominantly regenerative in a leilstromdesorber to a part of the solution to be degassed or in a Yorüberhitzer to those at the top of the desorber. then surrenders a further regenerative heat transfer in a heat exchanger to the Descrber zuzuführende rich solution and possibly further heat dissipation in Sihleinrichtungen with external heat dissipation and the poor solution is completely relaxed in a low-pressure absorber stage »This is the at the upper end of the desorber resulting vaporous working either completely overheater the multi-stage extraction turbine or to a part of the superheater multi-stage extraction turbine and the other Φeil condensed and fed via an absorption refrigeration directly the Hiederdruck absorber stage · The working fluid is expanded in the extraction turbine multi-stage work and the poor solution in the low-pressure Absorb erstufe takes from the first "(low pressure) stage of the extraction turbine unregulated and optionally from the Absorpt Thereafter, the solution (absorbent) is brought by a pump to the pressure of the next higher "absorber stage and takes there again as much working medium vapor from the second stage of the Entnähmeturbine up to the equilibrium concentration, whereupon a further stepwise saturation of the solution by gradually increasing the solution pressure with appropriate Arbeitsmitteldampfentnahme from the respective stages of the extraction turbine, so that after the last absorber stage (high-pressure absorber stage) a heavily loaded with working fluid rich solution with low Desorptionsanfangstemper and - by limiting the heat transfer from the poor solution to the rich solution in the heat exchanger close to the boiling "state, preferably with defined subcooling - enters the desorber" This is the counter-current to the degassing

Solution in the desorber guided heat transfer medium to considerably below 100 ° G cooled and at the same time a high purity of the working medium vapor in the desorber can be achieved. In a particular embodiment of the invention, it is provided that the amount of saturated solution is divided before the last (high pressure) absorber stage, of which one part of the high-pressure absorber stage and the other is fed to a parallel-connected medium pressure desorber operating at the same pressure , which is heated with waste heat even lower temperature levels »The working medium vapor of this medium pressure desorber is passed into the high-pressure ^ bsorberstufe, whereby the Arbeitsmitteldampfantnahme the high-pressure stage of the extraction turbine correspondingly reduced and thus the amount of relaxed to lower pressure levels in the extraction turbine working fluid is increased to the same extent The solution thereby degassed in the medium-pressure desorber is combined with the poor solution from the desorber after regenerative heat release in a partial flow desorber or a solution heat exchanger.

In a further embodiment of the invention. provided that the Bückverdichtung the working fluid in a two-stage. The saturated solution is fed from the high-pressure absorber stage via the heat exchanger to a medium-pressure desorber whose desorbierfcer working agent vapor in a Sesorptionsstufe absorbed by the poor solution from deseserber, the Hesorbat brought by a pump to higher pressure in the heat exchanger preheated, the working fluid released in the desorber again, overheated and expanded in the extraction turbine * Meanwhile, the accumulating in the medium pressure desorber poor solution after regenerative heat release in leilstromdesorber or preheater, further heat transfer in the heat exchanger and optionally in a cooling device of the low-pressure absorber tufe for relaxation and working fluid vapor supplied to it.

As a favorable embodiment of the invention by the combination

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the parallel and Seihe connected desorption is provided that the flow of the saturated solution after an absorber stage, preferably after the high-pressure absorber stage is divided, of which a Seilsbrom fed via the heat exchanger a Mitfceldruckdesorber and the desorbierbe Arbeibsmitbeldampf is fed to a Eesorpbionssbufe in the other part of the solution from the high-pressure Absorbersbufe is used as the absorbent and absorbs the working medium vapors of Mibteldesorbers »The Eesorbat is then fed through a solution heat exchanger to the desorber as rich solution« The poor solution from the medium pressure desorber is regenerative heat dissipation in a Teilstromdesorber and a heat exchanger and optionally an additional Suhleinrichtung relaxed in the Hiederdruck absorber stage for Arbeitsmitbeidampfaufnahme * The poor solution from the desorber is after regenerabiver heat release in the Lösungswärmebausc her and optionally supplied in a Kühlleininrichbung a Absorbersbufe with approximately the same concentration of the solution,

A preferred embodiment of the invention provides that the or in Mitteldruckdesorber and connected thereto absorber stage, Hesorptionssbufe prevailing system pressure in Gleitdruckbebrieb to compensate for fluctuating Kühlmibbelbemperaburen for influencing the Konzenbrabion rich, -in the desorber is controlled eintrebenden solution *

In an advantageous embodiment of the invention is provided for cooling water saving, that before the entry of the solution in the absorber stages an adiabafeer absorber is arranged and that the output of the Blederdruck absorber stage is followed by a further adiabatic absorber, in which emerging from the iTiederdruck Absorbersbufe solution nachgesätbigt with working fluid from the low-pressure stage of the extraction turbine and the exiting at the head of the adiababen absorber Arbeitsmibbeidampf then the Hiederdruck Absorbersbufe is forwarded »

Pur the entire invention is the use of the working substance pair ammonia-water of particular advantage. However, it is also possible to use another high-pressure working medium which boils at ambient pressure lower than ammonia, for example GO ₂ JP 13 P 23 or ethane in conjunction with a suitable absorption liquid.

embodiment

The invention will be explained in more detail below using an exemplary embodiment. In the accompanying drawing show:

: The schematic diagram of the invention

"Sorption process for recovering mechanical (electrical) energy from waste heat with first regenerative use of the sensible heat of the poor solution in a partial flow desorber.

: The block diagram of the sorption process according to the invention similar to Pig · 1 with a first regenerative heat utilization in a pre-superheater and the extension of the process by a condensation and cooling part.

Prinzip Sas schematic diagram of the sorption process according to the invention similar to Pig, 1 or 2 with medium-pressure desorber connected in parallel to the high-pressure absorber stage for displacement of the working medium in the direction of lower removal pressures in the take-off turbine «

Pig, 4 i The block diagram of the sorption process according to the invention similar to Pig. 1 or 2 for additional use of waste heat with a very low temperature level by two-stage thermal compression of the working medium,

Pig · 5 j The schematic diagram of a sorption process according to the invention with Heorhen- and parallel circuit of desorbers as a special combination of the processes according to Pig, 3 and Pig * 4,

g · 6: A section of the absorber part of the sorption process according to the invention, in which the absorber stages additionally adiabatic absorber upstream or downstream.

In a desorber 1 enters the top of the rich solution and passes through a distributor and a Stoffausfeauschteil in the heated Desorberteil 2, in which it flows on vertical drilling as a film down and emits working fluid, which flows in countercurrent to the degassing solution upwards. The same process also takes place in the partial flow desorber 22, the heat transfer medium for the heating of the Desorberteiles 2 occurs, if it gives off heat without phase change when Heizwär- ^ Sintritt 7 in, the Desorberteil 2 below and leaves this through the heating heat outlet When heated with steam, a subdivision of the heated Desorberteiles 2 is advantageous, being used in the upper rope saturated steam "lower pressure in the lower (Beil higher pressure · The resulting in the bottom of the desorber 1 poor solution gives their sensible heat either in a Seilstromdesorb he 22, flowing from bottom to top, to a leil of the rich solution (3 £ g '1) or in a superheater 10 to the vaporized, desorbed working fluid (Fig, 2) from «The further heat release of the poor solution takes place in one Heat exchanger 9 to the rich solution *

The poor solution arrives via an expansion device 13 "a cooling device 14 to the Hiederdruck absorber stage 5 · Ia Äes? Cooling device 14, the heat is transferred to a cooling medium *

The emerging at the top of the desorber 1 vaporous working fluid is optionally in the superheater 10, in any case, but in a externally heated superheater 3 »with a heat transfer inlet 11 and a heat exchanger outlet 12, further heated and then passes into a multi-stage extraction turbine. 4 In which it is gradually relaxed. From the individual stages of the Entnähmeturbine 4, the working fluid to the associated absorber stages 5, 5% 5 ^IJ , 5 ¹¹ * and is there from the poor solution or the stepwise

Enriched solution as a liquid absorbent (absorbent) under the heat of absorption to a cooling medium, sucked up "In the respective Absorbersfcufe 5j 5 ¹ » 5 ^lf > 5 ^tt! the poor solution or the previously enriched solution is loaded with working medium up to near the saturation state for this stage, the amount of absorbent (poor solution or solution) determining the amount of working fluid to be relieved of the associated stage of the removal turbine 4, However, the amount of the relaxed working fluid remains uncontrolled. "The solution saturated in the low-pressure absorber stage 5 is brought to a higher pressure by a pump 6 and is thus able to absorb working fluid again in the following pump inlet 5 * at this higher pressure Absorber stage 5 ^f assigned removal point of the extraction turbine 4 so much work equipment taken that the solution again almost reached the saturation state (equilibrium concentration) Thus, the Arbeitsmittelentnähme from the extraction turbine 4 is determined by the loading capacity of the solution in the associated absorber stage «The removal is unregulated; it is self-regulating, Yon stage to stage is brought reasonable 'enriched solution via pumps 6, 6 ^{f, if} 6, 6 ^tfi to a respective higher pressure and fed as rich solution at the end of the desorber. The solution is gradually enriched so strong with working fluid that it is recorded a very low Desorptionsanfangstemperatur for the rich solution on entering the desorber 1, which is at the heating heat inlet 7 i & Desorberteil 2 entering heat carrier for waste heat is cooled very far and the preheating of the rich solution for regenerative heat absorption in the heat exchanger 9 is only limitedly possible, so that in special cases the heat exchanger 9 can be dispensed with ·

The purity of the vaporous working fluid is so great ₉ that the working medium vapor can be sucked in at the same time for cooling (Pig, 2)

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Faucet 21 liquefied a partial flow of the working medium vapor in an air condenser, the condensate in a cooler 16 and stored in a container 17 The condensate is expanded in a decompression device 18 to the pressure of an evaporator 19 and thus withdrawn heat to a brine 20. The working medium vapor is removed from the evaporator 19 for heat absorption via the cooler 16 of the pressure in the next absorber stage, generally the Niederdruckabsorberstufe 5 and serves there in connection with the Arbeitsmitteldaiiipf removal from the last stage of the removal turbine 4 for enrichment of the poor solution in the described manner *

An extension of the basic method according to the invention is carried out by the parallel connection of a medium-pressure desorber 1 ^f to desorber 1, whereby the relaxation of the working fluid in the Entnähmeturbine 4- shifts to lower removal pressures, ie to a higher temperature gradient. In this case, the stream of the saturated solution before the last (high pressure) absorber stage 5 ^flf split «A partial stream of the solution is fed directly to the ^Hochdurck absorber stage 5 ^ftt » The other partial stream of the enriched solution is after heat absorption in a solution heat exchanger S ¹ to the desorber 1 parallel Htteldruckdesorber V abandoned, in which the working fluid is desorbed in a known manner »The working medium vapors accumulating at the top of the medium-pressure desorber 1 * are fed to the high pressure absorber stage 5 ^ttf « Thus, the Arbeitsmitteldampfentnahme from the extraction turbine 4 for this pressure level to the same extent In this way, the relaxation of the working fluid in the extraction turbine 4 is improved in favor of the lower removal pressures. The poor solution from the litteldruck desorber 1 * is, after heat dissipation in the solution heat exchanger 9 'to the medium pressure desorber 1 ¹ supplied rich solution, via a relaxation device 13 * merged with the poor solution from the desorber 1 Cig ₉ J5) ·

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Modifications of the method according to the invention are achieved by the use of a second medium-pressure desorber 1% of an additional solution heat exchanger 9 * and by additional arrangement of a further absorber, working as Eesorptionsstufe 26 «

By such modifications of the basic process, either the yield of mechanical energy can be increased or the process can be adapted to a plurality of available heat carriers, sometimes with a lower temperature level than necessary in the basic process. For the use of waste heat with a very low temperature level or to generate very high fluid pressures a two-stage thermal compression provided. The two stages of compression are: 1 # medium pressure desorption and medium pressure eesorption and 2 "desorption at high pressure". The rich solution coming from the high pressure absorber stage 3 ^ts and pump 6 ^{tr is} pressurized through the heat exchanger 9 via the medium-pressure Besor- 1 * supplied · Bas in Hitteldruck desorber 1 ^f desörbierfce working medium is "fed 26 of Eesorptionsstufe. When absorbent is the Eesorptionsstufe 26, coming from the bottom of the desorber 1 via the solution heat exchanger 9 ^f cooled and in the expansion device 13 ^f relaxed poor solution that · enriches with the working medium vapor from the medium pressure desorber 1 ^! ITach pressure increase by a pump 24 and heat absorption in the solution heat exchanger 9 * the enriched solution is fed to the desorber 1 · The poor solution from the medium pressure desorber 1 * is in a known manner on the Yorüberhitze r 10, the heat exchanger 9 »the expansion device 13 and the cooling device 14 of the low-pressure Ab sorb first ej? zugeleitefc (Pig.4),

In the expanded basic processes (parallel connection cdar two-stage thermal Eückverdichtung) of the desorber 1 operates as a high-pressure desorber,

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A further modification of this method results from the fact that at the highest Absorberdriick in the absorber stage 5 ^If exiting and brought by the pump 6 '* higher pressure rich solution is divided into two partial streams »A partial flow is after temperature increase in the heat exchanger 9 the medium pressure Desorber 1 * forwarded. The working medium vapor desorbed there is absorbed again in the Ee * sorption stage 26 by the other solution of the rich solution (absorbed). The rich solution (sorbate) thus produced is heated by the pump 24 and. Temperature increase in the solution heat exchanger 9 * abandoned on the desorber 1. The poor solution from the medium-pressure desorber 1 * is in a known manner via the heat exchanger 9 '<iie EntSpannungseinrichtung 13 and the cooling device 14 of the low-pressure absorber stage 5 supplied ^ while exiting the desorber 1 poor solution in an analogous manner via the solution heat exchanger. 9 %, the expansion device 13 'and the cooling means is passed 14 * · then this poor solution of a Absorbersbufe with approximately equal · concentration of the solution, for example, the absorber unit 5 ^lf is admixed.

Lifting the described processes, ie «basic process (Jig, 1 and 2)

- Process with parallel-connected medium-pressure desorber, cL.lu Terschängungsdesorber (S ¹ Ig ₉ 3)

- two-stage thermal recompression of the working fluid in a series of desorbers (Pig · 4)

various combinations and process expansions are possible with which special adaptations to the number and quality of the waste heat carriers can be realized * For example, if a heat transfer medium with a very low temperature level is available, an additional displacement desorber for the absorber stage is possible to use the medium-pressure level or parallel to the medium-pressure level, which then spans only one pressure level, but with it

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a further displacement of the working fluid in the unloading turbine 4 · in view of lower Entnähmedrücke and thus higher heat gradient is achieved. ₃

Claims (1)

Claim for invention 1 _# method for Hutzung of waste low temperature level for the generation of mechanical or "electrical energy with optional simultaneous cooling than Ifachschalt-Sorpbionsprozeß thermal process using a Arbeifesstoffpaares with well-absorbable high-pressure working medium and a liquid absorbent, in which the high-pressure working medium by desorption thermally released at high pressure, superheated and expanded in a multi-stage extraction turbine work, characterized in that the at the bottom of the desorber (1) resulting poor solution their sensible heat first predominantly regenerative in a Seilstromdesorber (22) "to an Ieil of degassing solution or in a pre-superheater (10) to the at the upper end of the desorber (1) resulting Arbeibsmitteldämpfe, which are the extraction turbine (4) zuzuleiten emits, and then another regenerative heat transfer in a heat exchanger (9) to the desorber (1) to be supplied rich solution and possibly further heat in Eühleinrichtungen (14) with external heat dissipation and the poor solution completely in a Hiederdruck Absorb erstufe (5) is relaxed, while that at the upper end of the desorber (1 ) accumulating vaporous working fluid either completely via superheater (10 j 3) of the multi-stage extraction turbine (4) or to a rope on the superheater (10j 3) of the multi-stage extraction turbine (4) and condensed on the other salvation and an absorption refrigeration system directly Uiederdruck- Absorber step (j?) Are fed, the working fluid in the extraction turbine (4) is relaxed in several stages occupationally and the poor solution in the Mederdruck- Absorbs sorbs (5) from the first (Hlederdruck) stage of the extraction turbine (4) unregulated and optionally from the absorption refrigeration plant absorbs Arbeibsmitteldampf up to the equilibrium concentration, then by e a pump (6) is brought to the pressure of a next higher absorber stage (5 ^f ) and there again absorbs so much working medium vapor from the second stage of the extraction turbine (4) up to the equilibrium concentration of this pressure stage and a further stepwise saturation of the solution by stepwise Increasing the solution pressure with appropriate work Mediumdampfentnähme from the respective stages of the extraction turbine (4), so that after the last (high pressure) absorber stage (5> ^lfI ) a heavily laden with working ^fluid , rich solution with low Desorptionsanfangstemper and - by limiting the heat exchange in the heat exchanger (9) near the Boiling state, but preferably with defined supercooling - in the desorber (1) re-enters and thus the in countercurrent to the degassing solution in the desorber (1) guided heat carrier to considerably below 100 ° Q cooled and simultaneously high purity of the working medium vapor in the desorber (1) is achievable » 2 »Procedure according to item 1 ,. characterized in that the amount of the saturated solution is divided before the last (high pressure) absorber stage (5 ^ttf ), of which one part of the high pressure absorber stage (5 ^{t! l} ) uid & ^e z other parts connected in parallel operating at the same pressure Medium pressure desorber (1 ^} ) fed and the working medium ^{vapor of} the medium pressure desorber (1 ¹ ) in the last (high pressure) absorber stage (5 ^lft ) is passed, whereby the Arbeitsmitteldampf removal of the high pressure stage of the removal turbine (4) correspondingly reduced and thus the amount of lower Pressure stages in the removal turbine (4) relaxed working fluid is increased to the same extent, while the medium pressure desorber (1 ¹ ) degassed solution after regenerative heat release in a Teilstromdesorber or a solution heat exchanger (9 ^f ) with the poor solution from the desorber (1 ) or fed into one of the absorber stages (5 ^f ; 5 ^fi ) * 3 »method according to item 1, characterized in that the Eückverdichtung of the working fluid is carried out by a zv / eistufigen thermal compressor, wherein the saturated solution of the high pressure absorber stage (5 ^JI ) via the heat exchanger (9) fed to a medium pressure desorber (1 ^f ), whose desorbed working medium vapor in an eesorption stage (26) is absorbed by the poor solution from the desorber (1), the hezorbate is absorbed by a pump (24 ×) to a higher level Pressure, in the heat exchanger (9 ¹ ) preheated, the working agent iia desorber (1) released again, overheated and in the removal turbine (4) is relaxed, while the medium pressure desorber (1 ^f ) resulting poor solution after regenerative heat dissipation in ieilstromdesorber ( 22) or in the pre-superheater (10) further heat dissipation in the heat exchanger (9) optionally in the cooling device (14) of the Hiederdruck Absorb erstufe (5) for relaxation and "Arbeitsmitteldampfaufnähme is fed. 4, process according to point 1 to 3 », characterized in that the stream of the saturated solution after a Absorberstufe (5> J 5 ¹ J 5 ¹ ')» preferably after the high-pressure Abs orb erstuf (5 ^tf ) is divided, of which a partial flow via the heat exchanger (9) to a medium-pressure desorber (1 ^! ) fed and the desorbed working medium vapor a. Besorptionsstufe (26) is supplied, in which the other part of the solution from the high-pressure absorber stage (p ^ir ) is used as the absorbent, and the working medium vapors of the medium pressure desorber (1 ¹ ) absorbed, the sesorbate then a solution heat exchanger (9 ^T ) the Desorber (1) is fed as a rich solution, while the poor solution from the medium pressure desorber (1 ^f ) after regenerative heat release in a leilstromdesorber and the heat exchanger (9) and optionally in the sniffer (14) in the low-pressure absorber stage (5) Arbeitsemitteldampfaufnahme relaxed and the poor solution from the desorber (1) after regener tiver heat dissipation in the solution heat exchanger (9 ¹ ) and optionally in a Eühleinrichtung (14 ') one of the absorber stage (5; 5' | 5 ^t! ) With approximately the same concentration of Solution is added « 5e method according to item 2 to 4, characterized in that in Mtteldruckdesorber (1 *) and associated with him absorber stage (5) or «Hesorptionsstufe (26) prevailing system pressure in Gleitdruckbetrieb to compensate - IS - fluctuating coolant temperatures are controlled to influence the concentration of the rich solution entering the desorber (1). 6 · Method according to items 1 to 5> characterized in that before the entry of the solution into the absorber stages (5 »5'J 5 ^ff 5 5 ^ftl ) ice adiabatic absorber (23) is arranged, and the output of the Hiederdruck absorber stage (5) a further adiabatic absorber (25) is connected downstream, in which the from the low-pressure absorber stage (5) emerging solution with working fluid from the Hiederdruckstufe the extraction turbine (4) and saturated at the head of the adiabatic absorber (25) emerging working fluid then the low-pressure absorber stage (5) is fed * 7 · The method of item 1 to 6, characterized in that as the working substance pair ammonia water or 'another high-pressure working fluid which boils at atmospheric pressure lower than ammonia, for example CQ ^, $ 13 »i ¹ 23 or ethane in conjunction with a suitable absorption liquid is used. For this purpose, _Jt_Seiten drawings.