WO2008094057A2

WO2008094057A2 - Coabsorbent cycles heat pumping and mechanical work producing procedure and applying installation

Info

Publication number: WO2008094057A2
Application number: PCT/RO2007/000018
Authority: WO
Inventors: Mihail Dan Staicovici
Original assignee: Mihail Dan Staicovici
Priority date: 2006-09-26
Filing date: 2007-09-24
Publication date: 2008-08-07
Also published as: WO2008094057A3

Abstract

Procedure of producing combined heating, cooling and electrical power with high global efficiency, using coabsorbent truncated heat pumping cycles of much higher thermal efficiency than those known so far in coupling with a known thermodynamic Rankine power cycle, thermally connected with two fluids of low temperature potential, e.g. (5-75) °C, but with sensible different temperatures, AT = (10 - 50) °C, identified as heat pumping coabsorbent truncated cycles sink and heat sources, the hottest one at least or both coming of the thermal coupling with the power cycle, the first fluid of higher temperature, e.g. 40 °C during the cold season and (50-80) °C during the warm season, being a fraction of that which extracted the heat from the power cycle exothermic condensing or low cogeneration processes and the second one, of lower temperature, e.g. (5-35) °C, being a fraction of that which was cooled by the power cycle sink source.

Description

COABSORBENT CYCLES HEAT PUMPING AND MECHANICAL WORK PRODUCING PROCEDURE AND APPLYING INSTALLATION

The invention is referring to a procedure of increasing the coabsorbent cycles heat pumping and mechanical work producing efficiency and feasibility and to an applying installation, destined to industrial and domestic, city and rural applications of combined heating, cooling and electricity production with classic and renewable energy sources use.

The city combined heating, cooling and electricity production is based on coupling, in an unitary globally optimized system, with minimum primary energy consumption, the thermal power stations with the heat pumping coabsorbent thermodynamic cycles, taking place in installations including generation and desorption devices on one side and resorption and absorption devices on the other side, being in heat exchange with two low temperature fluids, e.g. (5-75) ⁰C, but with sensible different temperatures, e.g. AT = (IOSOfC, the hottest one at least or both coming of the thermal power station provided by a condensing turbine, in such a way that the first fluid of higher temperature is a fraction of that which cooled before the power station condenser or it comes of a heating process resulted from a low temperature power station cogeneration, e.g. (50-8O)⁰C, and the second one, of lower temperature, is a fraction of that which was cooled before in the power station cooling tower, or it has a different origin, cooled in a different way, respectively, a resorption device and a desorption one, where useful heating and cooling effects are produced, respectively, solution pumps and optionally a compressor.

The rural combined heating, cooling and electricity production is based on the trigeneration coabsorbent cycles, taking place in installations which include for example a desorber, externally heated, and an absorber, externally cooled, both operating at a low pressure, e.g. (0.1-2) bar, a resorber, externally cooled, operating at an intermediate pressure, e.g. (2-6) bar, a high pressure generator, e.g. (30-60) bar, externally heated, a turbo-generator group, solution to solution and vapor to solution heat exchangers, pumps and regulating and expansion valves.

Referring to city heating, there are already known solutions based on heat pumps operated by single-fluid mechanical vapor compression and using for heat production the condensing heat of a power station as one heat source. The main disadvantage of this method and application plant is that in most cases the primary energy use effectiveness is close to that of a warm water gas fired boiler having COPf_jeatj_ng ai_ofr_aι ~ 0.8—0.9, especially when power stations have poor efficiency, and this favors applying local direct fossil fuel burning based heating solutions when district heating is not available, with environmentally very harmful consequences.

Referring to city cooling, there are already known solutions based on mechanical vapor compression (mvc) use. Globally, this technology consumes today about 40% of the total electrical power produced worldwide. More often then not, it is characterized quantitatively by the coefficient of performance, COP_jnV0== useful delivered cooling power / electrical power introduced in system. For three main cooling applications, industrial, at -45 ⁰C, medium, -22.5 ⁰C and air conditioning, at 0 ⁰C, the COP's have practical values of 1.26, 1.96 and 3.63, respectively. The main disadvantage of this method and applying plant is that thermodynamically, qualitatively, the mechanical vapor compression destroys much of the system exergy input, that is it has low exergetic efficiency, similarly defined as COP, η_ex_)taax = 0.31 - 0.36 , canceling in heat pumping applications to a good extent the endeavor of power station electrical efficiency increase. Referring to rural heating and cooling, there are already known solutions based on fossil fuel burning for heating and on the mechanical vapor compression for cooling. Theirs disadvantages were already emphasized above. There are also methods for separate heating, cooling and electrical power producing by by means of of renewable energies. Their main disadvantage is that these methods and applying plants are confronted with poor exergy efficiencies, η_ex < 0.1. Referring to the coabsorbent cycle, it is already known the coabsorbent cooling cycle, further named also nontruncated of cooling, which includes a high pressure generator, e.g. p=(5-50) bar, externally heated, generating refrigerant vapour of a mean concentration YQ,_W resorbed subsequently in a high pressure resorber externally cooled and having maximum outlet absorbent concentration y%g , named threshold concentration of the generated vapour, y^o < YQ_>W . A first disadvantage of this procedure and applying installation, coming mainly of the nontruncated cooling cycle rigid configuration, is that in many volatile absorbent and high temperature lift applications concentration threshold problems appear, that is more often then not it happens that yjlO ≥ YG,_IΠ znά f°^{r tfl}i^s reason cycle is not working. A second disadvantage of this procedure and applying plant is that in certain applications available heat source temperature is less than that actually needed and again the coabsorbent cycle cannot be used.

Referring to the coabsorbent cycle, it is already known the coabsorbent heating cycle, or coabsorbent heat transformer cycle, further named also nontruncated of heating, which includes a low pressure desorber, e.g. p=(0.1-2) bar, externally heated, generating refrigerant vapor of a mean concentration YD,m absorbed subsequently in a low pressure absorber, externally cooled, having y^Q as concentration threshold, so that yAO ≤^D,m - A ^^rst disadvantage of this procedure and applying installation, coming mainly of the nontruncated heating cycle rigid configuration, is that in many volatile absorbent applications concentration threshold problems appear in this case as well, that is more often then not it happens that y/^o ≥ Y∑) m and cycle is not useful. A second disadvantage of this procedure and applying plant is that in certain applications available cooling source temperature is too high as compared to that actually required and again the coabsorbent cycle cannot be used. A first technical problem consists in finding a procedure of increasing the coabsorbent cycle effciency and feasibility, capable to enable working in the cooling mode with generation temperatures reduced enough in order to benefit of low thermal potential heat sources supply on one side, and working in the heating mode with cooling temperatures higher than those corresponding to the nontruncated cycle of origin on the other side, without concentration threshold problems. A second technical problem consists in finding a procedure of combined heating, cooling and electricity producing with high global efficiency, COP_trigeneration > ^⁹ » applicable mainly in geographical zones with high energy demand such as cities and which is consuming a reduced amount of primary energy first because it enables to transform in useful heat and cooling the low thermal potential sources resulted from the electrical power producing process, available in sufficient quantity and with quasiconstant parameters during the whole year.

A third technical problem consists in finding a procedure of combined heating, cooling and electricity producing with high global effectiveness and exergy efficiency COPfrig_enerati_on » 1.0 -1.5 and fj_eχ = 0.40 -0.50, respectively, applicable mainly in rural geographical zones. The procedure, according to the invention, solves the first technical problem in that, for fluid cooling it is using a coabsorbent truncated cooling cycle connected to heat sources with practically ittimited availability, of renewable, waste or classic origin, capable of heating to a maximum temperature for generation processes, e.g. (40-70) ⁰C and of cooling to a

minimum temperature or resorption and absorption processes, e.g. (10-40) ⁰C, in such a

way that ΔTfø = Ttø -TM ≥ (8 -1O)³C, coming of a nontruncated cooling cycle,

including a low pressure desorption process p\ , e.g. (0.1-2) bar, where useful cooling effect occurs, e.g. Tp/ = (213,15 - 273,15)K , a truncation column used as nontruncated cycle truncation process, having pressure between the low one a and a high pressure p_n, e.g. (10-50) bar and is made up by a low pressure absorption process coupled on vapor side with the low pressure desorption process, a low pressure mixing process of the absorbents coming of the low pressure absorption and desorption processes in order to generate the one mean concentration absorbent y^ and temperature TM^PU VM) - ^M , a series of i stages, i=l, ..., n, « e iV, of isobar opposite intermediary generation and resorption processes, having increasing pressures between the low pressure and the high one of the last stage,

and temperatures between and , being coupled on vapor side having essentially

increasing mean concentrations

fiilfilύαg the concentration threshold condition

•••_» n and being supplied in pre-established proportions by uniform absorbents coming, for the first stage of the mixture of the one mean concentration absorbent with that coming of the second generation stage, for each of the following next stages of the mixture of the absorbent coming of the first inferior resorption stage with that coming of the first superior generation stage, and for the high pressure stage of the resorption process of the last but one resorption process, and processes between successive stages of the truncation column inside and outside of it, of absorbent pressure increasing and reduction and of heat recovery.

The procedure, according to the invention, solves the first technical problem in that, for fluid cooling also it is using a coabsorbent truncated cooling hybrid cycle connected to heat sources with limited availability, of renewable, waste or classic origin, capable of heating to a maximum temperature Tj^ for generation and desorption processes, e.g. (40-70) ⁰C and of cooling to a

minimum temperature Tj^ for resorption and absorption processes, e.g. (10-40) °C, in such a

way that

, coming of a nontruncated cooling hybrid cycle,

including a low pressure desorption process p\ , e.g. (0.1-2) bar, where useful cooling effect occurs, e.g.

, a high pressure resorption process Pf₁, e.g. (10-50) bar, a truncation hybrid column used as nontruncated hybrid cycle truncation process, having pressures between the low one a and an intermediary pressure p_m^ , pfr > p_mχ > p\ , and is made up by a low pressure absorption process coupled on vapor side with the low pressure desorption process, a low pressure mixing process of the absorbents coming of the low pressure absorption and desorption processes in order to generate the one mean concentration absorbent yjrf and temperature _> ^a series of i-1 stages, i<n, i,ne N of isobar

opposite intermediary generation and resorption processes, and an i stage with an intermediary pressure generation process p_mι = pj, with stages pressure increasing from the low pressure to the inermediary one Pint>Pi+l >Pi ^≥Pl and temperatures between T^ and T]^ , being

coupled on vapor side having essentially increasing mean concentrations k≤i-1 , k e N, fulfiling the concentration threshold condition yRθ,k ^{≤ γ}G,m,k_> k≤ i-l , yRO,n ^{≤ Y}G,m,i ^m& being supplied in pre-established proportions by uniform absorbents coming, for the first stage of the mixture of the one mean concentration absorbent with that coming of the second generation stage, for each of the following next stages of the mixture of the absorbent coming of the first inferior resorption stage with that coming of the first superior generation stage, and for the last i stage at p_mι and resorption process at pf, by the absorbent coming of the resorption process of the last but one resorption process, a process of increasing generated vapor pressure from the inermediary pressure to the high one, and processes between successive stages of the truncation column inside and outside of it, of absorbent pressure increasing and reduction and of heat recovery.

The procedure, according to the invention, solves the first technical problem in that, for fluid heating it is using a coabsorbent truncated heating cycle connected to heat sources with practically illimited availability, of renewable, waste or classic origin, capable of heating to a maximum temperature T^ for generation and desorption processes, e.g. (40-70) ⁰C and of

cooling to a minimum temperature Tu for resorption and absorption processes, e.g. (10-40)

⁰C, in such a way that ATj^ =Ttø -TM ≥ (8-10)⁰C, coming of a nontruncated heating

cycle, including a high pressure resorption process Pf₁, e.g. (10-50) bar, where useful heating effect occurs, e.g. TRj _n = (353,15- 453,15)κ , a truncation column used as nontruncated cycle truncation process, having pressures between the high value and a low pressure value pj, e.g. (0.1-2) bar and is made up by a high pressure generation process coupled on vapor side with the high pressure resorption process, a high pressure mixing process of absorbents coming of the high pressure generation and resorption processes in order to generate the one mean concentration absorbent yjtf and temperature

Ttø _> ^{a sta}8^e of low pressure absorption and desorption processes, a series of i stages, i=l, ..., n, n e N, of isobar opposite intermediary generation and resorption processes, with stages pressures decreasing from the high pressure to the low one p\ < pj+\ <p\ < Pf₁ and temperatures between Ttø and T^f , being coupled on vapor side having essentially decreasing mean concentrations ^γG,m,i+k-l ^{≥ γ}G,m,i+k ^{≥ γ}D,m fulfϊling the concentration threshold condition yRO,i+k ^{≤ γ}G,m,i+k> k≤n -i , i,k,n & N , y^O ^{≤ γ}D,m » ³^ being supplied in pre- established proportions by uniform absorbents coming, for the first stage of the mixture of the one mean concentration absorbent with that coming of the second stage of resorption, for each of the following i=2, ..., n-1 next stages of the mixture of the absorbent coming of the first superior resorption stage with that coming of the first inferior generation stage, for the i=n stage by the mixture of the absorbent coming of the i=n-l generation process with that of the low pressure absortion process, and for the low pressure processes stage of the absorbent coming of the n generation process, and processes between successive stages of the truncation column inside and outside of it, of absorbent pressure increasing and reduction and of heat recovery.

The procedure, according to the invention, solves the first technical problem in that, for fluid heating also it is using a coabsorbent truncated heating hybrid cycle connected to heat sources with limited availability, of renewable, waste or classic origin, capable of heating to a maximum temperature T^ for generation and desorption processes, e.g. (40-70) ⁰C and of cooling to a

way that AT^ = Ttø - Ttø ≥ (8 - lOfC , coming of a nontruncated heating hybrid cycle,

including a high pressure resorption process Pf₁, e.g. (10-50) bar, where useful heating effect occurs, e.g. T^ _n = (353,15 - 453,15)^ , a truncation hybrid column used as nontruncated hybrid cycle truncation process, having pressures between an intermediary value Pfat, joint < Pf₁ , and a low pressure value /?/, e.g. (0.1-2) bar and is made up by an intermediary pressure generation process coupled on vapor side with the high pressure resorption process, an intermediary pressure mixing process of absorbents coming of the high pressure resorption and intermediary pressure generation processes in order to generate the one mean concentration absorbent ytø and temperature Tfof (pj^ , yj^ ) < TJM , a stage of low pressure absorption and desorption processes, a series of n-i stages of isobar opposite intermediary generation and resorption processes, noted by i+1, i+2, ..., n, i, n e N , with stages pressures decreasing from the intermediary pressure to the low one p_m^ ≥Pi+k >Pi+k+l >Pl_> k e N and temperatures between TM and TM , being coupled on vapor side having essentially decreasing mean

concentrations YG,m,i+k-l ≥ ^YG,m,i+k ^{≥ Y}D,m _> fulfϊling the concentration threshold condition yRO,i+k ^{≤ γ}G,m,i+k> ^≤n-i, i,k,n <= N, yAO ^{≤ γ}D,m , and being supplied in pre- established proportions by uniform absorbents coming, for the second stage of the mixture of the one mean concentration absorbent with that coming of the third stage of resorption, for each of the following next stages of the mixture of the absorbent coming of the first superior resorption stage with that coming of the first inferior generation stage, for the n stage by the mixture of the absorbent coming of the i=n-l generation process with that of the low pressure absortion process, and for the low pressure processes stage of the absorbent coming of the n generation process, a process of increasing the pressure of the generated vapor from the intermediary value to the high value and processes between successive stages of the truncation column inside and outside of it, of absorbent pressure increasing and reduction and of heat recovery. The procedure, according to the invention, solves the second technical problem in that, for combined heating, cooling and electrical power production with high global efficiency COPfrig_enerafi_on > 0.9 , there are used heat pumping coabsorbent truncated cycles, according to the invention and the procedures described above, which have a much higher thermal efficiency than those known so far , e.g. COP = 10-200, depending on sources temperature and availability and applications working parameters, where the COP is defined by the ratio between the useful energy output and the mechanical work input consumed for mechanical vapor compression and pumping, in coupling with a known thermodynamic Rankine power cycle, including an endothermic high temperature and pressure vapor generation process, e.g. I/_j = 550°C and ph ^llObar , low temperature and pressure vapor condensing exothermic processes, e.g. T\ = (28,6 -39,5)°C and />/ = (θ,04-0,07)før, a low temperature cogeneration 2/ = (39,5 - 8θ)PC and p\ - (θ,O7 - 0,48)δαr , a vapor expansion process from the high pressure to the low one producing useful mechanical work, a process of transforming the mechanical work in useful electrical energy, processes of increasing the working fluid pressure and transport and of heat recovery, thermally connected with two fluids of low temperature potential, e.g. (5- 75)°C, but with sensible different temperatures, Ar = (IO-SO)⁰C, identified as heat pumping coabsorbent truncated cycles sink and heat sources, the hottest one at least or both coming of the thermal coupling with the power cycle, the first fluid of higher temperature, e.g. 40⁰C during the cold season and (50-80)°C during the warm season, being a fraction of that which extracted the heat from the exothermic condensing or low cogeneration processes and the second one, of lower temperature, e.g. (5-35)°C, being a fraction of that which was cooled by the power cycle sink source, or it has a different origin, cooled in a different way, respectively, in such a way that a fraction of the heat rejected by the power cycle during the condensing or cogeneration processes mentioned above is recovered by the coabsorbent heat pumping cycle and transformed in amount of (23-48)% and (24-33)% in useful cooling, e.g. (213,15- 273,15)K and useful heat, e.g. (353,15- 453,15)£, respectively, supplementary supplying the consumer of heat, cooling and electrical power, besides the electrical and thermal power supply produced by the Rankine power cycle partially working in counterpressure mode.

The procedure, according to the invention, solves the third technical problem in that, for combined heating, cooling and electrical power production, it is used a coabsorbent truncated cycle resembling the cooling one, according to the inventon and procedure described above, connected to heat sources with limited availability, of renewable, waste or classic origin, capable of heating to a maximum temperature T^ for the i=l, ...,n-l generation processes,

e.g. (40-70) ⁰C and of cooling to a minimum temperature Ttø coding for the i=l, ...,n-l resorption

processes and an absorption process, e.g. (10-40) ⁰C, in such a way that and to a high temperature source capable to achieve

maximum generation temperatures coming of a

nontruncated non-isobar cooling cycle, including a low pressure desorptiott process p\ , e.g. (0.1-2) bar, where first useful cooling effect occurs, e.g.

, a high pressure generation process /tø, e.g. (30-60) bar, reaching the maximum temperature TQQ , an intermediary pressure resorption process />int _> Pl < Pint ^KPh_> ^e S- (2-6) bar, resorbing the vapor generated by the high pressure generation process with concentration threshold condition fulfilment yRO,mt < ^G, m h ⁸^ when heat is produced by a temperature sensibly equal to that of resorption process end, e.g. (50-120) ⁰C, as second useful effect, a

mechanical work producing process achieved through generated vapor expansion from the high pressure to the intermediary one, a process of transforming the mechanical work into electrical power, as third useful process, a truncation column used as nontruncated cycle truncation process when cooling process temperature decrease is necessary, having pressures between the low pressure and the intermediary one and is made up by a low pressure absorption process coupled on vapor side with the low pressure desorption process, a low pressure mixing process of the absorbents coming of the low pressure absorption and desorption processes in order to generate the one mean concentration absorbent yjrf and temperature , a series of i

stages, i=l, ..., n-1, n e N, of isobar opposite intermediary generation and resorption processes having increasing pressures between the low pressure and the intermediary one, , and temperatures between Ttø and Tj^ , being

coupled on vapor side having essentially increasing mean concentrations fulfϊling the concentration threshold condition

» •••_> ⁿ"l» and being supplied in pre-established proportions by uniform

absorbents coming, for the first stage of the mixture of the one mean concentration absorbent with that coming of the second generation stage, for each of the following next stages of the mixture of the absorbent coming of the first inferior resorption stage with that coming of the first superior generation stage, and for the last stage of the mixture of the absorbent coming of the high generation process with the absorbent coming of the last but one resorption process and processes between successive stages of the truncation column inside and outside of it, of absorbent pressure increasing and reduction and of heat recovery.

The installation, according to the invention, solves the first technical problem in that, for fluids cooling it includes a low pressure desorber, a truncation column with pressures between the low pressure and a high one and temperatures within Ty and Ty + ATtø , e.g. 30 and (30

+max. 40 ) ⁰C, made up by a low pressure stage with an absorber, coupled on vapor side with the desorber of low pressure, a low pressure mixer for the one mean concentration absorbent generation, a series of i isobar stages, i-1, ..., n, of generators and resorbers coupled on vapor side, with pressures increasing from the low pressure to the high one, n-1 intermediary mixers of mean concentration supplying in pre-established quantities the series of isobar stages of generators and resorbers, by means of of increasing and reducing absorbent pressure and transport and heat recovery of gax and absorbent/absorbent type and a connection between the high pressure resorber of the truncation column and the low pressure desorber.

The installation, according to the invention, solves the first technical problem in that, for fluids cooling also it includes a low pressure desorber, a truncation column with pressures between the low pressure and an intermediary one and temperatures within Ty and Ty + ATy , e.g. 30 and (30 +max. 40 ) ⁰C, made up by a low pressure stage with an absorber, coupled on vapor side with the desorber of low pressure, a low pressure mixer for the one mean concentration absorbent generation, a series of i-1, i<n, i,ne N isobar stages of generators and resorbers coupled on vapor side, with pressures increasing from the low pressure to the intermediary one, a last i stage with an intermediary pressure generator, i-1 intermediary mixers of mean concentration supplying in pre-established quantities the series of the isobar stages of generators and resorbers, by means of of increasing and reducing absorbent pressure and transport and heat recovery of gax and absorbent/absorbent type, a resorber working at a high pressure, higher than the intermediary one, coupled on vapor side with the intermediary pressure generator, a compressor increasing the pressure of the generated vapor from the intermediary pressure to the high one and a connection between the n high pressure resorber of the truncation column and the low pressure desorber.

The installation, according to the invention, solves the first technical problem in that, for fluids heating it includes a high pressure resorber, a truncation column with pressures between the high value and a low one and temperatures within Ty and Ty + ATy , e.g. 30 and (30 +max. 40 ) ⁰C, made up by a high pressure generator coupled on vapor side with the resorber of high pressure, a high pressure mixer for the one mean concentration absorbent generation, a series of i isobar stages of generators and resorbers, i=l, ..., n, coupled on vapor side, with pressures decreasing from the high value to the low one, and a low pressure stage with an absorber and a desorber coupled on vapor side, n-1 intermediary mixers of mean concentration supplying in pre-established quantities the series of isobar generators and resorbers, by means of of increasing and reducing absorbent pressure and transport and heat recovery of gax and absorbent/absorbent type, and a connection between the low pressure desorber of the truncation column and the high pressure resorber. The installation, according to the invention, solves the first technical problem in that, for fluids heating also it includes a high pressure resorber, a truncation hybrid column with pressures between an intermediary value and a low one and temperatures within Ttø and

Ttø + Δ?A/ , e.g. 30 and (30 +max. 40 ) ⁰C, made up by an intermediary pressure generator

coupled on vapor side with the resorber of high pressure, an intermediary pressure mixer for the one mean concentration absorbent generation, a series of n-i isobar stages of generators and resorbers, noted by i+1, i+2, ..., n, i,ne N, coupled on vapor side, with pressures decreasing from the intermediary value to the low one, and a low pressure stage with an absorber and a desorber coupled on vapor side, n-i-1 intermediary mixers of mean concentration supplying in pre-established quantities the series of isobar generators and resorbers, by means of of increasing and reducing absorbent pressure and transport and heat recovery of gax and absorbent/absorbent type, a compressor for increasing generated vapor pressure from the i stage intermediary value till the high pressure value and a connection between the low pressure desorber of the truncation column and the high pressure resorber.

The installation, according to the invention, solves the second technical problem in that, for combined heating, cooling and electrical power production with high global efficiency

COPtrig_eneratj_on > 0.9 , it is used a heat pumping coabsorbent truncated machine, according to the invention and the procedures described above, which has a much higher thermal efficiency than those known so far , e.g. COP = 10-200, depending on sources temperature and availability and applications working parameters, in coupling with a known Rankine cycle power plant provided with a condensing turbine with cogeneration steam bleedings, thermally connected with two fluids of low temperature potential, e.g. (5-75)°C, but with sensible different temperatures, AT = (IO-SO)⁰C, and playing the role of coabsorbent machine sink and heat sources, namely the first fluid of higher temperature is a fraction of that which extracted the heat from the condenser during, the cold season, at e.g. 4O⁰C, or it comes of a power plant low cogeneration heating process during the warm season, at e.g. (50-8O)⁰C, and the second one, of lower temperature, e.g. (5-35)°C, is a fraction of that which was cooled by the power station cooling tower, or it is of a different origin, cooled in a different way, respectively, in such a way that a fraction of the heat rejected by the power station during the condensing or cogeneration processes mentioned above is recovered by the heat pumping coabsorbent truncated machine and transformed in amount of (23-48)% and (24-33)% in useful cooling, e.g. (213,15- 273,15)/r and useful heat, e.g. (353,15- 453,15)K, respectively, supplementary supplying the consumer of heat, cooling and electrical power, besides the electrical and thermal power supply produced by the Rankine power station partially working in counterpressure mode. The installation, according to the invention, solves the third technical problem in that, for combined heat, cooling and electrical energy producing it includes as a first example, a low pressure desorber, where a first useful cooling effect is produced, a high temperature and pressure generator, an intermediary presure and temperature resorber which is resorbing the vapor generated by the high pressure generator producing heat as second useful effect, a turbo- generator activated by the refrigerent vapor expanding from the high pressure to the intermediary one with producing electrical power as third useful effect, a truncation column with pressures between the low value and the intermediary one and temperatures within and

Ttø +MM , e.g. 30 and (30 +max. 40 ) ⁰C, made up by a low pressure stage absorber

coupled on vapor side with the desorber, a low pressure mixer for the one mean concentration absorbent generation, a series of i stages, i=l, ..., n-1, n e N, of generators and resorbers coupled on vapor side, with pressures increasing between the low value and the intermediary one, i-1 intermediary mixers of mean concentration which supply in pre-established quantities the series of generators and resorbers isobar stages, by means of of increasing and decreasing absorbent pressure and transport and of heat recovery, of gax and solution to solution type, a connection between the intermediary pressure resorber and the low pressure desorber. The advantages offered by the invention are as follows:

1. By its application, it is possible to obtain a city and rural combined heat, cooling and electrical energy producing system, globally energetically optimized, with minimum primary energy consumption; 2. It enables and broadens the application of nontruncated coabsorbent cycles practically to all globe geographical zones, enjoying of an advanced degree of versatility; 3. It capitalizes on qualities of working combinations having volatile absorbents or limited solubility field, otherwise difficultly to turn to good account; Next, it will be given an example of invention achievement, in connection with Figs. 1 to 16, which are representing:

• Fig. 1 - Cooling procedure with truncated coabsorbent cycle, plotted in the log p

- 1/T diagram; • Fig. 2 - Example of applying installation of the cooling procedure with truncated coabsorbent cycle, plotted in the log p - 1/T diagram;

• Fig. 3 - Cooling procedure with truncated coabsorbent hybrid cycle, plotted in the log p - 1/T diagram;

• Fig. 4 - Example of applying installation of the cooling procedure with truncated coabsorbent hybrid cycle, plotted in the log p - 1/T diagram;

• Fig. 5 - Another example of applying installation of the cooling procedure with truncated coabsorbent cycle, plotted in the log p - 1/T diagram;

• Fig. 6 - Heating procedure with truncated coabsorbent cycle, plotted in the log p

- 1/T diagram; • Fig. 7 - Example of applying installation of the heating procedure with truncated coabsorbent cycle, plotted in the log p - 1/T diagram;

• Fig. 8 - Heating procedure with truncated coabsorbent hybrid cycle, plotted in the log p - 1/T diagram;

• Fig. 9 - Example of applying installation of the heating procedure with truncated coabsorbent hybrid cycle, plotted in the log p - 1/T diagram;

• Fig. 10 - Another example of applying installation of the heating procedure with truncated coabsorbent hybrid cycle, plotted in the log p - 1/T diagram;

• Fig. 11 - Example of applying installation of thermal power station - coabsorbent heat pumping installation coupling for high global efficiency combined heat, cooling and electrical power producing;

• Fig. 12 - Another example of applying installation of thermal power station - coabsorbent heat pumping installation coupling for high global efficiency combined heat, cooling and electrical power producing;

• Fig. 13 - Another example of applying installation of thermal power station - Coabsorbent heat pumping installation coupling for high global efficiency combined heat, cooling and electrical power producing;

• Fig. 14 - Non-isobar truncated coabsorbent cycle trigeneration procedure, plotted in the log p - 1/T diagram; • Fig. 15 - Example of applying installation of the non-isobar truncated coabsorbent cycle trigeneration procedure, plotted in the log p - 1/T diagram;

• Fig. 16 - Another example of applying installation of the non-isobar truncated coabsorbent cycle trigeneration procedure, plotted in the log p - 1/T diagram.

The procedure, according to the invention, solves the first technical problem in that, for fluid cooling it is using a coabsorbent truncated cooling cycle connected to heat sources with practically illimited availability, of renewable, waste or classic origin, capable of heating to a maximum temperature Tfof for generation processes, e.g. (40-70) ⁰C and of cooling to a

minimum temperature Tj^ for resorption and absorption processes, e.g. (10-40) ⁰C, in such a

coming of a nontruncated cooling cycle,

including a low pressure desorption process p\ , e.g. (0.1-2) bar, where useful cooling effect occurs, e.g. Tj)J = (213,15 - 273,15)^ , a truncation column used as nontruncated cycle truncation process, having pressure between the low one a and a high pressure p_n , e.g. (10-50) bar and is made up by a low pressure absorption process coupled on vapor side with the low pressure desorption process, a low pressure mixing process of the absorbents coming of the low pressure absorption and desorption processes in order to generate the one mean concentration absorbent yjtf and temperature i=l, ..., n, n e JV, of

isobar opposite intermediary generation and resorption processes, having increasing pressures between the low pressure and the high one of the last stage, Pn≥Pi+l > Pi > Pl ³^ temperatures between Tfrf and Ttø , being coupled on vapor side having essentially

increasing mean concentrations YG,m,i ≤ ^G,m,i+\ — ^G,m,n-l _> fiilfiling the concentration threshold condition yRO,i ^{≤ γ}G,m,i = ^l~^_> •••» ^{n an}^ being supplied in pre-established proportions by uniform absorbents coming, for the first stage of the mixture of the one mean concentration absorbent with that coming of the second generation stage, for each of the following next stages of the mixture of the absorbent coming of the first inferior resorption stage with that coming of the first superior generation stage, and for the high pressure stage of the resorption process of the last but one resorption process, and processes between successive stages of the truncation column inside and outside of it, of absorbent pressure increasing and reduction and of heat recovery, in such a way that the rich absorbent leaves the resorption process of the truncation column last stage at p_n , it is subcooled in a recovering way in the desorption process at pi , from TRQ _n ≥ Ttø to a temperature approaching 7m , it is expanded till /?/, it suffers the desorption process where it extracts the heat from the medium which must be cooled and that of subcooling and reaches the state parameters Tj)Q ≤ Ty si XDO ^≥yM_> ^d the absorbent coming of the generation process of the first truncation column stage is subcooled in a recovering way, it is expanded untill the low pressure, it suffers the absorption process of the desorbed refiigerent vapor, it is mixing at the low pressure with the absorbent coining of the desorption process and it generates the one mean concentration absorbent which is covering the truncation column in the way described above untill the last stage, in order to close the cycle.

From the functional point of view, the procedure solving the first technical problem of fluids cooling it is using a truncated cooling cycle plotted by solid line in Fig. 1 in the log p - 1/T diagram of the known refrigerent-absorbent working combination, connected to heat sources capable of heating to a maximum temperature Ty for generation processes, e.g. (40-70) ⁰C and of

cooling to a minimum temperature Ty for resorption and absorption processes, e.g. (10-40)

°C, in such a way that ATy - Ty - Ty ≥

coming of a nontruncated cooling cycle, represented in same very diagram by the external contour with solid line in the left side and with dashed line in the right side, including a low pressure desorption process (1-2), pi , e.g.

(0.1-2) bar, where useful cooling effect occurs, e.g. Jp/ = (213,15 - 273,15)K , a truncation column used as nontruncated cycle truncation process, having pressure between the low value a and a high pressure p_n , e.g. (10-50) bar and is made up by a low pressure absorption process (3- 4) coupled on vapor side with the low pressure desorption process (1-2), a low pressure mixing process of the absorbents coming of the low pressure absorption and desorption processes in order to generate the one mean concentration absorbent yy and temperature Ty(pι,yy)≥Ty , point M, a series of i stages, i=l, ..., n, w e iV, of isobar opposite

intermediary generation ψj -5(joj) and resorption {pj -SROj/ processes, having increasing pressures between the low pressure and the high one of the last stage, p_n≥Pi+\ > Pi > Pl ^and temperatures between Ty and Ty , being coupled on vapor side having essentially

increasing mean concentrations YG,m,i ^{≤ γ}G,m,i+l ^≤^G,m,n-l_^ fulfiling the concentration threshold condition }>RO,i ^≤YG,m,i _> i"¹ _* •••» ⁿ _. ^and being supplied in pre-established proportions by uniform absorbents coming, for the first stage of the mixture of the one mean concentration absorbent with that coming of the second generation stage, point 5j , for each of the following next i stages of the mixture of the absorbent coming of the first inferior resorption stage i-1 with that coming of the first superior generation stage i+1, points 5j , i=2, ...,n-l, and for the high pressure stage of the resorption process of the last but one resorption process n-1, point 5_n and processes between successive stages of the truncation column, of the one mean concentration absorbent y^ pressure increasing from pj to p\ and of the absorbent coming of resorption processes, pf-.\ to pj , i=2, ..., n, of pressure reduction of absorbent coming of generation processes, from p\ to pj and from p\ to p\~\, i-2, ..., n, and of heat recovery between opposite processes of absorption-generation and of resorption-generation, of gax and of absorbent-absorbent type, in such a way that the rich absorbent leaves the truncation column last stage resorption process ψn ~^RO,n) ^at Pn ■_» ** is subcooled in a recovering way in the desorption process (1-2) at p\ from TRQ _n ≥ T^f till a temperature approaching Tj)J ,

portion \$RO n ~^)_> & is expanded till p\, it suffers the desorption process (1-2) where it extracts the heat from the medium which must be cooled and that of subcooling and reaches the state parameters Tj)Q ≤ T^f si yj)Q ≥ yj^ , and the absorbent coming of the generation process vl ~^GO,l) °f ^tne first truncation column stage is subcooled in a recovering way, it is expanded untill the low pressure, it suffers the absorption process (3-4) of the desorbed refrigerent vapor, it is mixing at the low pressure with the absorbent coming of the desorption process and it generates the one mean concentration absorbent which is covering the truncation column in the way described above untill the last stage at p_n , in order to close the cycle.

The applying installation, according to the invention, is described here for the sake of clarity for a double truncated coabsorbent cycle, Fig. 2. The desorber 1 receives the rich absorbent 2, a fraction of it evaporates at the low pressure producing refrigerent vapor 3 through heating by the external source 4 which is being cooled in order to get the plant useful effect, and the rest exits the desorber 1 as absorbent 5. The vapor 3 are superheated in the superheater 6, where is subcooling in a recovering way the absorbent 7 coming from the high pressure resorber 8, then is absorbed in the absorber 9 at a pressure sensibly equal to the low one, and the subcooled absorbent 7 is expanded from the high pressure till the low one by means of of the expansion valve 10, in order to enter the desorber 1. The poor absorbent 11 enters the absorber 9, it absorbes vapor 3 and leaves the device as richer absorbent 12. Prior to enter the absorber 9, the poor absorbent 11 is first subcooled in a recovering way in the heat exchanger 13, providing the intermediary pressure generator 14, where it comes of, a fraction of its necessary generation heat, then it is expanded from the intermediary pressure to the low one, by means of of the expanding valve 15. A fraction of absorber 9 absorption heat is transfered in a gax way as generation heat to generator 14, by means of of the intermediary heat exchange loop 16, provided with a pump of circulation 17. The rest of generation heat is provided to generator 14 by the external heat source 18. The absorbents 5 and 12, of sensibly equal pressures, are mixed in the low pressure mixer 19, cyclic forming the plant one mean concentration absorbent 20, which, subsequently is pumped with pump 21 from the low pressure to the intermediary one, is preheated in a recovering way in the heat exchanger 22 receiving a fraction of the absorber 9 absorption heat and then is introduced in the inermediary pressure mixer 23. The rest of the not recovered absorber 9 absorption heat is eliminated finally by means of of the plant cooling source 24. In the intermediary pressure mixer 23, the one mean concentration absorbent it is mixing with the absorbent 25, which priority has been suffering successively a first subcooling process in a recovering way in the heat exchanger 26, providing the high pressure generator 27 which it is coming of a fraction of its generation heat, then a second sucooling process in a recovering way in the heat exchanger 28 and an expansion from the high pressure till the intermediary one in the throttling valve 29, forming a mean concentration absorbent 30, which is supplying in pre- established quantities through the regulating valves 31 and 32, the intermediary pressure generator 14 and resorber 33, respectively. The refrigerant vapor 34, generated by the generator 14 is resorbed in the resorber 33, cooled mainly by the plant sink source 24. The absorbent 35, coming of the resorber 33 is pumped by the pump 36 from the intermediary pressure till the high one in the high pressure vessel 37, priority being preheated in a recovering way successively in the heat exchanger 38, receiving a fraction of the intermediary pressure resorber 33 resorption heat, and in the heat exchanger 28. The absorbent 39 coming of the high pressure vessel 37 is supplying in pre-established quantities through the regulating valves 40 and 41, the high pressure generator 27 and resorber 8, respectively. A fraction of the high generator 27 generation heat is supplyed by the external heat source 42. The vapor of refrigerent 43, generated by the high pressure generator 27 is absorbed by the high pressure resorber 8, cooled by the plant sink source 24, in order to close the cycle. For cycles having the temperature lift of max. 35 ⁰C, the applying installation can be provided by two pressure stages with gax heat exchange, for very high COP. The procedure, according to the invention, solves the first technical problem in that, for fluid cooling also it is using a coabsorbent truncated cooling hybrid cycle connected to heat sources with limited availability, of renewable, waste or classic origin, capable of heating to a maximum temperature Ttø for generation and desorption processes, e.g. (40-70) ⁰C and of cooling to a

minimum temperature TΆA for resorption and absorption processes, e.g. (10-40) ⁰C, in such a way that Δ2 I1Yi/. = 21 M ^*-/¹ heating - T cooling ≥ (8 - lOfC , coming of a nontruncated cooling hybrid cycle,

including a low pressure desorption process p\ , e.g. (0.1-2) bar, where useful cooling effect occurs, e.g. T_j}j = (213,15 - 273,15)£ , a high pressure resorption process Pf₁, e.g. (10-50) bar, a truncation hybrid column used as nontruncated hybrid cycle truncation process, having pressures between the low one a and an intermediary pressure p\_nι , Pf₁ > p_m- ι > pi , and is made up by a low pressure absorption process coupled on vapor side with the low pressure desorption process, a low pressure mixing process of the absorbents coming of the low pressure absorption and desorption processes in order to generate the one mean concentration absorbent yjy[ and temperature a series of i-1 stages, Kn, i,ne N of isobar

opposite intermediary generation and resorption processes, and an i stage with an intermediary pressure generation process py^ = pj, with stages pressure increasing from the low pressure to the inermediary one p_mt>Pi+i >Pi ≥Pl and temperatures between TM and Tj^ , being

coupled on vapor side having essentially increasing mean concentrations YG,m,k - ^G,m,k+1 _> k≤i—1 , k e N, fulfiling the concentration threshold condition yRO k -YG,m,k_> k≤i~\ , yRO,n ^≤ ^G,m,i ³^ being supplied in pre-established proportions by uniform absorbents coming, for the first stage of the mixture of the one mean concentration absorbent with that coming of the second generation stage, for each of the following next stages of the mixture of the absorbent coming of the first inferior resorption stage with that coming of the first superior generation stage, and for the last i stage at /?j_nt and resorption process at Pf₁ by the absorbent coming of the resorption process of the last but one resorption process, a process of increasing generated vapor pressure from the inermediary pressure to the high one, and processes between successive stages of the truncation column inside and outside of it, of absorbent pressure increasing and reduction and of heat recovery, in such a way that, the absorbent coming of the i- 1 stage resorption process is supplying in pre-established quantities the generation process at pfa and of resorption at Pf₁, the vapor generated at /r_mt is suffering first a process of pressure increasing from p\_nχ to Pf₁ and a resorption one at Pf₁, with useful heat elimination e.g. (50- 120) ⁰C, the rich absorbent leaves the resorption process at Pf₁, it is subcooled in a recovering way in the desorption process at pi , from TRQ

? _n ≥ Ttø cooling to a temperature approaching Tpj ,

it is expanded till p\, it suffers the desorption process where it extracts the heat from the medium which must be cooled and that of subcooling and reaches the state parameters

TOO ^≤ ^M si yDO - yi_/l ₅ ^md the absorbent coming of the generation process of the first truncation column stage is subcooled in a recovering way, it is expanded untill the low pressure, it suffers the absorption process of the desorbed refiigerent vapor, it is mixing at the low pressure with the absorbent coming of the desorption process and it generates the one mean concentration absorbent which is covering the truncation column in the way described above untill the last stage, in order to close the cycle.

From the functional point of view, the procedure solving the first technical problem of fluids cooling also it is using a coabsorbent truncated cooling hybrid cycle represented by solid line in Fig. 3 in the log p - 1/T diagram of the known refrigerent-absorbent working combination diagram, connected to heat sources capable of heating to a maximum temperature Tj^ for

generation and desorption processes, e.g. (40-70) ⁰C and of cooling to a minimum temperature Ttø for resorption and absorption processes, e.g. (10-40) ⁰C, in such a way that

coming of a nontruncated cooling hybrid cycle,

represented in the same very diagram by the outside solid line contour on the left side and by dashed line on the right side, including a low pressure desorption process (1-2) p\ , e.g. (0.1-2) bar, where useful cooling effect occurs, e.g.

, a high pressure resorption process yju,n ~~5RO,n)_> Ph_> ^e §- (10-50) bar, a truncation hybrid column used as nontruncated hybrid cycle truncation process, having pressures between the low one and an intermediary pressure p\_nt , Pf₁ > p[_nt > p[ , and is made up by a low pressure absorption process (3-4) coupled on vapor side with the low pressure desorption process (1-2), a low pressure mixing process of the absorbents coming of the low pressure absorption and desorption processes in order to generate the one mean concentration absorbent yj^f and temperature , point M, a series of i-1 stages, i<n, i,ne N of isobar opposite

intermediary generation (5# - 5QQ ft) and resorption processes, and

an i stage with an intermediary pressure generation process p_m' t =Pi, with stages pressure increasing from the low to the inermediary one pjnt>P_/+l ^>Pi ~Pl ^an(^ temperatures between

Tfrf and TW , being coupled on vapor side having essentially increasing mean

concentrations

fulfiling the concentration threshold condition

^d being supplied in pre-established proportions by uniform absorbents coming, for the first stage of the mixture of the one mean concentration absorbent with that coming of the second generation stage, point 5i, for each of the following next k , k=2, ..., i-1 stages of the mixture of the absorbent coming of the first inferior resorption k-1 stage with that coming of the first superior generation stage k+1, points 5# , k=2, ..., i-1, and for the last i stage at ρ_mt and resorption process at pfr by the absorbent coming of the resorption process of the last but one resorption process, i-1, point 5j , a process of increasing generated vapor pressure from the intermediary pressure to the high one, and processes between successive stages of the truncation column, of pumping the one mean concentration absorbent yj^ from p\ to p\ and of the absorbent coming of the resorption processes ..., i-1, and of pressure reduction of the absorbent coming of

generation processes p\ to p\ and from

..., i-1, and of heat recovery between opposite processes of absorption-generation and resorption-generation, of gax and absorbent to absorbent type, in such a way that, the absorbent coming of the i-1 stage resorption process *^s supplying in pre-established quantities the generation process at

Fint '

and of resorption at pfr,

^tfle vapor generated at p_mχ is suffering first a process of pressure increasing from p_mχ to Pf₁ and then a resorption one at pfj, with useful heat elimination, e.g. (50-120) ⁰C, the rich absorbent leaves the resorption process

^at Ph' & *^s subcooled in a recovering way in the desorption process (1-2) at

Pl, from ^{to a} temperature approaching Tjyj , portion (5/rø _Λ -6), it is

expanded till pj, it suffers the desorption process (1-2) where it extracts the heat from the medium which must be cooled and that of subcooling and reaches the state parameters

∞d the absorbent coming of the generation process of the first truncation column stage

is subcooled in a recovering way, it is expanded untill the low pressure, it suffers the absorption process (3-4) of the desorbed refrigerent vapor, it is mixing at the low pressure with the absorbent coming of the desorption process and it generates the one mean concentration absorbent which is covering the truncation column in the way described above untill the last i stage, in order to close the cycle. The installation applying the procedure of solving the first technical problem of fluids cooling also, according to the invention, represented in a first variant in Fig. 4, in the log p - 1/T diagram, connected to an external heat source 1 of low temperature potential for a generation process and to an external sink source 2 for cooling an absorption process, including a truncation column with a low pressure absorber 3 />/ externally cooled by the source 2 and a generator 4 at pressure p\, externally heated by the source 1, a low pressure pj desorber S connected by the absorber 3 on refrigerent vapor side 6 desorbed from the desorber 5, a high pressure resorber 7, Ph' Ph ^> Pl - Ph connected with the generator 4 on vapor side 8 generated by the generator 4, via a compressor 9 of vapor 8 pressure increase from p\ to Pf₁, a mixing of absorbents 10 and 11 coming of the desorber 5 and absorber 3 respectively in order to generate the one mean concentration absorbent 12 in a mixer 13 at pressure p\ , a supply with absorbent 12 in pre- established quantities 14 and 15 of the generator 4 and resorber 7 respectively by means of the regulating valves 16 and 17 respectively, a heat exchanger 18 recovering the heat of the absorbent 19 coming of the generator 4 by the absorbent 12, a valve 20 for reducing the pressure of the absorbent 19 from p\ to pi, a pump 21 for increasing the pressure of the absorbent 12 from pi to Pf₁, and connections between devices, in such a way that, the rich absorbent 22 coming of the resorber 7 is subcooled in a recovering way in the desorber 5 through the connection 23, it is expanded from Pf₁ to p\ by means of the throttling valve 24, it is suffering the desorption process in the desorber 5 where it is extracting the heat of the medium 25 which must be cooled as a first useful effect and the subcooling heat of the absorbent 22, the absorbent 19 is subcooled in a recovering way in the heat exchanger 18, it is expanded from p\ till p\ in the expansion valve 20, it is entering the absorber 3 where it suffers the absorption process of the vapors 6, the absorbents 10 and 11 coming from desorber 5 and absorber 3 respectively are mixing in the mixer 13 at p\ generating the absorbent 12 of one mean concentration, the absorbent 12 is pumped by the pump 21 from pi to Pf₁, it is preheated in the heat exchanger 18, it is distributed to generator 4 and resorber 7 in the way described above, and the vapor 8 generated in the generator 4 is compressed by the compressor 9 from p\ till Pf₁ and it is resorbed in the resorber 7 transfering the resorption heat to an external source 26, as second useful effect, in order to close the cycle.

The installation applying the procedure of solving the first technical problem of fluids cooling also, according to the invention, represented in a second variant in Fig. 5, in the log p - 1/T diagram, connected to an external heat source 1 of low temperature potential for a generation processes and to an external sink source 2 for cooling absorption and resorption processes, including a low pressure desorber 3 at /?/, a high pressure resorber 4 at Pf₁, a hybrid truncation column with pressures between the low value and an intermediary one p[_nι , made up by an absorber 5 at pj, externally cooled by source 2, coupled with the desorber 3 on vapor side 6 desorbed by the desorber 3, a mixer at pi for mixing the absorbents 8 and 9 coming of the desorber 3 and absorber 5 respectively in order to generate the one mean concentration absorbent 10, a stage of pressure p\ , p\ > pi with a generator 11 externally heated and a resorber 12, externally cooled, coupled on vapor side 13 generated by the generator 11 and resorbed by the resorber 12, an intermediary pressure p_mi stage Ph >Pm' t >Pl ^≥Pl ^w^^{tn a} generator 14 externally heated, a supply for the generator 11 and resorber 12 in pre-establshed quantities respectively by uniform absorbents 15 and 16 respectively, regulated by the valves 17 and 18 respectively coming of the mixture 19 at p\ of the absorbent 10 with the absorbent 20 coming of the generator 14, a pump 21 for pumping the absorbent 10 from p\ to p\, a pump 22 for pumping the absorbent 23 coming of the resorber 12 from p\ to pfo, a valve 24 for reducing the pressure of the absorbant 25 from p\ to pi , a valve 26 for reducing the pressure of the absorbant 20 from p_mι to p\, a recovering heat exchanger 27 between absorbents 25 and 10, a recovering heat exchanger 28 between absorbents 20 and 23, and connections between devices, in such a way that, the absorbent 23 after being pumped and preheated it is supplying in pre- established quantities the generator 14 by the absorbent 29 regulated by the valve 30 and the resorber 4 by the absorbent 31 regulated by the valve 32, the vapor 33 generated by the generator 14 is compressed from JPj_n^ Ia Ph by ^tne compressor 34 and are resorbed in the resorber 4 with heat producing transferred to the external source 35 as a first useful effect, the rich absorbent 36 coming from the resorber 4 is subcooled in a recovering way in the desorber 3 through the connection 37, it is expanded from Pf₁ to p\ by means of the expanding valve 38, it is suffering the desorption process in the desorber 3 where it is extacting the heat of the medium 39 which must be cooled as a second useful effect and the subcooling heat of the absorbent 36, the absorbent 25 is subcooled in a recovering way in the heat exchanger 27, it is expanded from p\ ^t0 Pl by means of the valve 24, it is suffering the absorption process of the vapor 6 in the absorber 5 becoming absorbent 9, it is mixed up in the mixer 7 with the absorbent 8, is is forming the absorbent 10 of the one mean concentration and it is pumped in the truncation column which is covered in the way mentioned above, in order to close the cycle. The plant described above has been modeled with the ammonia/water working combination for trigeneration of heat, cooling and electrical power in coupling with a thermal power station, obtaining the following results:

• Heat source temperature: a) (40-45) ⁰C, winter, condensing turbine with steam bleedings for cogeneration of power and district heating; (70-80) ⁰C, summer, condensing turbine with steam bleedings for cogeneration of power and heating of low temperature;

• The installation transforms in useful cooling (48 - 23)% out of the heat source supply for desorber inlet temperatures of 0 to -45 ⁰C, and the electrical power consumption is (3.1-. 27.1)% out of the cooling capacity; • Calculated COP for: a) industrial cooling at -45°C; b) medium cooling at -22.5 ⁰C and c) air conditioning cooling at O⁰C are: a) COP=3.69; b) COP=11.56 and c) COP=33.2, respectively;

• Same installation has at the same time for the high pressure resorption inlet temperatures of (50- 130) ⁰C, (24-33)% heating useful capacity out of the heat source supply;

• Bearing in mind that mechanical vapor compression cooling consumes solely about 40 percent out of the total electrical power produced today, the estimation shows that introducing thermal power station-coabsorbent technology coupling trigeneration, it would be possible to reduce the primary energy consumption worldwide by (8-27)%; this figure could reach values of (15-35)%, if same type coabsorbent heating applications were included here.

The procedure, according to the invention, solves the first technical problem in that, for fluid heating it is using a coabsorbent truncated heating cycle connected to heat sources with practically illimited availability, of renewable, waste or classic origin, capable of heating to a maximum temperature fyf for generation and desorption processes, e.g. (40-70) °C and of

cooling to a minimum temperature T^f for resorption and absorption processes, e.g. (10-40)

⁰C, in such a way that ATAS ≥ (8- lθ)°C , coming of a nontruncated heating

cycle, including a high pressure resorption process pfr, e.g. (10-50) bar, where useful heating effect occurs, e.g. Tjtf _n = (353,15- 453,15)K^" , a truncation column used as nontruncated cycle truncation process, having pressures between the high value and a low pressure value pi , e.g.

(0.1-2) bar and is made up by a high pressure generation process coupled on vapor side with the high pressure resorption process, a high pressure mixing process of absorbents coming of the high pressure generation and resorption processes in order to generate the one mean concentration absorbent yj^ and temperature TM^Ph-_>yM)~ ^M _> ^{a sta}S^e of low pressure absorption and desorption processes, a series of i stages, i=l, ..., n, n e N , of isobar opposite intermediary generation and resorption processes, with stages pressures decreasing from the high pressure to the low one p\ ≤Pi+\ <Pi < Ph ^d temperatures between Tj^ and Tj^ , being coupled on vapor side having essentially decreasing mean concentrations YG,m,i+k-ϊ ^{≥ Y}G,m,i+k ^≥ ?D, m fulfiling the concentration threshold condition yROJ+k ^{≤ Y}G,m,i+k » k≤n-i, i,k,n& N , y^O ^{≤ r}D,m _> and being supplied in pre- established proportions by uniform absorbents coming, for the first stage of the mixture of the one mean concentration absorbent with that coming of the second stage of resorption, for each of the following i=2, ..., n-1 next stages of the mixture of the absorbent coming of the first superior resorption stage with that coming of the first inferior generation stage, for the V=Ti stage by the mixture of the absorbent coming of the i=n-l generation process with that of the low pressure absortion process, and for the low pressure processes stage of the absorbent coming of the n generation process, and processes between successive stages of the truncation column inside and outside of it, of absorbent pressure increasing and reduction and of heat recovery, in such a way that, the poor absorbent leaves the desorption process at p\ , it is pumped till pfo, it is preheated in a recovering way in the resorption process at Pf₁ from TJJQ < Ttø till a

temperature close to TRJ , it is suffering the resorption process where it rejects the resorption heat to the medium which must be heated up and that of preheating and reaches the state parameters TΏQ ≥ TM si ynn ≤ yj^ , and the absorbent coming of the resorption process of

the truncation column first stage is pumped from p\ to Pf₁, it is preheated in a recovering way, it suffers the refrigerent vapor generation process at Pf₁, it is mixing at the high pressure with the absorbent coming of the high pressure resorption process and it generates the one mean concentration aabsorbent which is covering the truncation column downstairs until the last stage and finally the stage at pf in the way descibed above, in order to close the cycle.

From the functional point of view, the procedure solving the first technical problem of fluid heating it is using a coabsorbent truncated heating cycle represented by solid line in Fig. 6, in the log p - 1/T diagram of the known refrigerent-absorbent working combination, connected to heat sources capable of heating to a maximum temperature for generation and desorption

processes, e.g. (40-70) ⁰C and of cooling to a minimum temperature 2_jy for resorption and

absorption processes, e.g. (10-40) °C, in such a way that ATM = Ttø - TM > (8- lθ)PC ,

coming of a nontruncated heating cycle, represented in the same very diagram by the external solid line contour on the right side and by dashed line on the left side, including a high pressure resorption process (1-2), Pf₁, e.g. (10-50) bar, where useful heating effect occurs, e.g.

TRI,H - (353,15 - 453,15)^T , a truncation column used as nontruncated cycle truncation process, having pressures between the high value and a low pressure value pi, e.g. (0.1-2) bar and is made up by a high pressure generation process (3-4) coupled on vapor side with the high pressure resorption process (1-2) , a high pressure mixing process of absorbents coming of the high pressure generation and resorption processes in order to generate the one mean concentration absorbent y^ and temperature Ttøipfr, JM) ^{≤ 2}M ■_> poύrt M, a stage of low pressure absorption ^m^ Resorption processes , a series

of i stages, i~l, ..., n, ti e N, of isobar opposite intermediary generation

^ resorption processes ^w^h stages pressures decreasing from the high pressure to the

low one ^m^ temperatures between and , being coupled on

vapor side having essentially decreasing mean concentrations

fulfiling the concentration threshold condition

, and being supplied in pre-established quantities by uniform absorbents coming,

for the first stage of the mixture of the one mean concentration absorbent with that coming of the second stage of resorption, point 5j, for each of the following i=2, ..., n-1 next stages of the mixture of the absorbent coming of the first superior resorption stage i+1 with that coming of the first inferior generation stage i-1, points

for the i=n stage by the mixture of the absorbent coming of the i=n-l generation process with that of the low pressure absortion process

³^ f°^{r tne} l°^w pressure processes stage of the absorbent coming of the n generation process

P^oult ^AI ^≡ ^D/ » ⁸^ processes between successive stages of the truncation column, of reducing the pressure of the one mean concentration absorbent ytø from pf_j to pi , of the absorbent coming of the generation processes from

and from p_n to p\, of incresing the absorbent pressure coming of the absorption process from Pl to p_n, and of the resorption processes from pj to Pi~\, i=2, ..., n and from ρ\ to pjj, and of heat recovery between opposite processes of absorption-generation and of resorption- generation, of gax and absorbent to absorbent type, in such a way that, the poor absorbent leaves the desorption proces

at p\, it is pumped till Pf₁, it is preheated in a recovering way in the resorption process (1-2) at Ph from Tjyn < Tj^ till a temperature close

to Tjtf, portion 5jrχ) -6, it is suffering the resorption process where it is rejecting the resorption heat to the medium which must be heated up and that of preheating, reaching state parameters and yjig ≤ y^ , and the absorbent coming of the resorption process

of the truncation column first stage it is pumped from p\ till Pf₁, it is preheated in a recovering way, it is suffering the generation process (3-4) of the refrigerent vapor at Pf₁, it is mixed up at the high pressure with the absorbent coming of the high pressure resorption process and generates the one mean concentration absorbent which is covering the truncation column downstairs until the last stage and finally the stage at pj, in the way described above, in order to close the cycle.

The installation of applying the procedure which solves the first technical problem of fluids heating, represented in a first variant in the log p - 1/T in Fig. 7, connected to a sink source 1 of external cooling for absorption and resorption processes and to a heat source 2 of low thermal potential for generation and desorption processes supply, having a truncation column including a low pressure absorber 3 at p\ externally cooled by source 1, a low pressure desorber 4 at p\ externally heated by the source 2 and connected with the absorber 3 on refrigerant vapor side 5 desorbed by the desorber 4, an intermediary pressure stage p\^ with a generator 6 externally heated by the source 2 and a resorber 7 externally cooled with the source 1 coupled with the generator 6 on refrigerent vapor side 8 generated by the generator 6 and a high pressure Pf₁ generator 9 Ph > /?_mt > Pl , externally heated by the source 2, a resorber 10 of high pressure Pf₁ connected with the generator 9 on refrigerent vapor side 11 generated by the truncated column generator 9, a mixing in the mixer 12 at Pf₁ of the absorbents 13 and 14 coming of the generator 9 and the resorber 10 respectively in order to generate the one mean concentration absorbent IS, a mixing in the mixer 16 at p_mι of the absorbents 15 and 17 coming of the absorber 3 in order to get a mean concentration absorbent which is supplying in pre-established quantities 18 and 19 the resorber 7 and the generator 6 respectively by means of the regulating valves 20 and 21 respectively, a supply with absorbent 22 coming of the generator 6 of the absorber 3 and of the desorber 4 in pre-established quantities 23 and 24 respectively by means of the regulating valves 25 and 26 respectively, a heat exchanger 27 for subcooling the absorbent 15 by preheating in a recovering way the rich absorbent 28 coming of the resorber 7, a heat exchanger 29 of subcooling the absorbent 22 through preheating in a recovering way the absorbent 17, a valve 30 for reducing the pressure of the absorbent 15 from Pf₁ to /%t , a valve 31 for reducing the pressure of the absorbent 22 from p_m- χ to /?/, a pump 32 for increasing the pressure of the absorbent 17 from p\ to p_mt , a pump 34 for increasing the pressure of the poor absorbent 35 coming of the desorber 4 from p\ to Pf₁, and connections between devices, in such a way that, the absorbents 13 and 14 are mixing up in the mixer 12 at Pf₁, are generating the one mean concentration absorbent 15 which is subcooled in the heat exchanger 27, it is expanded in the valve 30, it is mixing up in the mixer 16 at p_mι with the absorbent 3 which priorily was pumped from p\ to ρ_mι with the pump 32 and preheated in a recovering way in the heat exchanger 29 and it is supplying with the absorbents 18 and 19 the resorber 7 and the generator 6 respectively in the way already shown, the vapor 8 generated in the generator 6 is resorbed in the resorber 7, the absorbent 22 is subcooled in the heat exchanger 29, it is expanded from p_mχ to

Pl in the valve 31, it is supplying the absorber 3 and the desorber 4 with the absorbents 23 and

24 respectively in the way already shown, the vapor 5 desorbed in the desorber 4 is absorbed in the absorber 3, the absorbent 35 coming of the desorber 4 is pumped by the pump 34 from the low pressure till the high one, it is preheated in the resorber 10 through connection 36, it enters the resorber 10 where it is suffering the resorption process of the vapor 11, the resorption heat is eliminated by means of the external source 37 heating it up as the useful effect and preheating the absorbent 35, and the absorbent 28 coming of the resorber 7 is pumped by the pump 33 from pι_nt till Pf₁, it is preheated in a recovering way in the heat exchanger 27, it enters the generator

9 where it is suffering the generation process in order that finally the resulting absorbent 13 be mixed up in the mixer 12 with the absorbent 15 and close the cycle.

The procedure, according to the invention, solves the first technical problem in that, for fluid heating also it is using a coabsorbent truncated heating hybrid cycle connected to heat sources with limited availability, of renewable, waste or classic origin, capable of heating to a maximum temperature Ty hmltns for generation and desorption processes, e.g. (40-70) ⁰C and of cooling to a

minimum temperature Ty for resorption and absorption processes, e.g. (10-40) ⁰C, in such a

way that ATy - Ty - Ty ≥ (8 - 10)⁵C , coming of a nontruncated heating hybrid cycle,

including a high pressure resorption process Pf₁, e.g. (10-50) bar, where useful heating effect occurs, e.g. T^j _n = (353,15 -453,15)κ , a truncation hybrid column used as nontruncated hybrid cycle truncation process, having pressures between an intermediary value p_mχ , p_m- t < ph, and a low pressure value pi, e.g. (0.1-2) bar, and is made up by an intermediary pressure generation process coupled on vapor side with the high pressure resorption process, an intermediary pressure mixing process of absorbents coming of the high pressure resorption and intermediary pressure generation processes in order to generate the one mean concentration absorbent yy and temperature Ty (p\_nt , yy ) < TM , a stage of low pressure absorption and desorption processes, a series of n-i stages of isobar opposite intermediary generation and resorption processes, noted by i+1, i+2, ..., n, i,n e N , with stages pressures decreasing from the intermediary pressure to the low one p_mχ > pj₊fc > Pi+fc+i >Pl, k e N and temperatures between Ty and Ty , being coupled on vapor side having essentially decreasing mean

concentrations YG,m,i+k-\ - ^G m,i+k ^≥ ^D,m _> fulfiling the concentration threshold condition yROj+k ^{≤ γ}G_jnj+k> k≤n-i, i,k,neN, yAO ≤^γD,m > »^nd being supplied in pre- established proportions by uniform absorbents coming, for the second stage of the mixture of the one mean concentration absorbent with that coming of the third stage of resorption, for each of the following next stages of the mixture of the absorbent coming of the first superior resorption stage with that coming of the first inferior generation stage, for the n stage by the mixture of the absorbent coming of the i=n-l generation process with that of the low pressure absortion process, and for the low pressure processes stage of the absorbent coming of the n generation process, a process of increasing the pressure of the generated vapor from the intermediary value to the high value and processes between successive stages of the truncation column inside and outside of it, of absorbent pressure increasing and reduction and of heat recovery, in such a way that, the absorbent coming of the resorption process at pj+\ is pumped to /%t _» ft *^s preheated in a recovering way, it is supplying the generation process at /?_mt , the generated vapor of refrigerent is compressed from p_mt to Py₁ where it is suffering the resorption process, the poor absorbent leaves the desorption process al pi , it is pumped till Py₁, it is preheated in a recovering way by subcooling the absorbent coming of the high pressure resorption process, it is suffering the resorption process producing the resorption heat taken over by the medium which must be heated up as useful effect, and the absorbent coming of the high pressure resorption process is subcooled in a recovering way untill it is reaching saturation parameters at

ft ^ιs mixing with the absorbent coming of the generation process at p_mι in order to generate the one mean concentration absorbent, which is covering the truncation column downstairs until the last stage and then the stage at pi in the way described above, closing the cycle.

From the functional point of view, the procedure solving the first technical problem of fluids heating too it is using a coabsorbent truncated heating hybrid cycle represented by solid line in

Fig. 8, in the log p - 1/T diagram ot the known refrigerent-absorbent working combination, connected to heat sources capable of heating to a maximum temperature 7X/ for generation

and desorption processes, e.g. (40-70) ⁰C and of cooling to a minimum temperature Ttø for

resorption and absorption processes, e.g. (10-40) ⁰C, in such a way that ^TM - TM ~?M ≥ (8-lθ)°C, coming of a nontruncated heating hybrid cycle, represented in the same very diagram by the external solid line contour to the right side and by dashed line to the left side, including a high pressure resorption process (1-2), pj_j, e.g. (10-50) bar, where useful heating effect occurs, e.g. Tβj _n = (353,15 - 453,15)ΛT , a truncation hybrid column μsed as nontruncated hybrid cycle truncation process, having pressures between an intermediary value p_mι , p_m- χ < p_n , and a low pressure value /?/, e.g. (0.1-2) bar, and it is made up by an intermediary pressure generation process coupled on vapor side with the high pressure resorption process, an intermediary pressure mixing process of absorbents coming of the high pressure resorption and intermediary pressure generation processes in order to generate the one mean concentration absorbent >%/ and temperature

» point M,

a stage of low pressure absorption

and desorption processes

^a series of n-i stages of isobar opposite intermediary generation

³^ resorption processes

^{noted bv i+1}> ⁱ⁺²> •••> ⁰ _^ i,» eJV, with stages pressures decreasing from the intermediary pressure to the low one Pmt

and temperatures between and , being

coupled on vapor side having essentially decreasing mean concentrations

Mfiling the concentration threshold condition

m > ^md being supplied in pre- established proportions by uniform absorbents coming, for the second stage of the mixture of the one mean concentration absorbent with that coming of the third stage of resorption i+2, point 5 j₊i , for each of the following next stages i+k, 2≤k≤n-i~l, of the mixture of the absorbent coming of the first superior resorption stage

^wft^ft th^at coming of the first inferior generation stage

points 5/₊#, for the n stage by the mixture of the absorbent coming of the i=n-l generation process with that of the low pressure absortion process, point 5_n, and for the low pressure processes stage of the absorbent coming of the n generation process, a process of increasing the pressure of the stage i generated vapor from the intermediary value to the high value and processes between successive stages of the truncation column, of increasing the pressure of the absorbent coming of the absorption process from p\ to

P_n and of the absorbent coming of the resorption processes from

, of reducing the pressure of the absorbent coming of the high pressure resorption process from Pf₁ to j^int _? of the one mean concentration absorbent from pj to pi+\ and of the absorbents coming of the generation processes from

and from ρ_n to pi and of heat recovery between opposite processes, of absorption-generation and of resorption-generation, of gax and of absorbent to absorbent type, in such a way that, the absorbent coming of the resorption process at is pumped till pf = p^ ,

it is preheated in a recovering way, it is supplying the generation process (3-4) at pfa , the refiigerent vapor generated is compressed from /?_mt to Ph where it is suffering the resorption process (1-2), the poor absorbent leaves the desorption process (5 ^j ≡ $DI ~$Dθ) ^at Ph ^{liL m} pumped till pf,, it is preheated in a recovering way subcooling the absorbent coming of the resorption process (1-2) at Pf₁, it is suffering the resorption process where it is yielding the resorption heat to the medium which must be heated up as useful effect, and the absorbent coming of the resorption process at Pf₁ is subcooled in a recovering way till the saturation parameters at syno n_>P_\'n\)_> ft *^s fluxing at Pint ^w^ⁿ &^e absorbent coming of the generation process at p_mχ generating the one mean concentration absorbent which is covering the trauncation column untill the last atage and then the stage at p\ , in the way described above, closing the cycle.

The installation applying the procedure solving the first technical problem of fluids heating also, according to the invention, represented in a first variant in Fig. 9, in the log p - 1/T diagram, connected to an external sink source 1 of cooling for an absorption process and to an external heat source 2 of low thermal potential of heating for generation and desorption processes, having a truncation column with a desorber 3 of low pressure p\ externally heated by the source 2, an absorber 4 of low pressure p\ externally cooled by the source 1 and connected by the desorber 3 on vapor 5 desorbed in the desorber 3 and a generator 6 of intermediary pressure p_mt externally heated by source 2, a high pressure resorber 7, Pf₁, Pf₁

^> Pl coupled with the generator 6 on vapor side 8 generated by the generator 6 via a compressor 9 for increasing the vapor 8 pressure from _jp_mt till Pf₁, an absorbent of the one mean concentration

10 coming of a mixing process in the mixer 11 at Pj_n^ of the absorbent 12 coming of the resorber 7 at Pf₁ with the absorbent 13 coming of the generator 6, a heat exchanger 14 enabling absorbent 12 heat recovery by the absorbent 15 coming of the desorber 3, a heat exchanger 16 enabling absorbent 12 heat recovery by the absorbent 17 coming of the absorber 4, a supply with absorbents 10 of the one mean concentration in preestablished quantities 18 and 19 of the absorber 4 and desorber 3 respectively by means of the regulating and expansion valves 20 and

21 respectively, reducing the pressure from /?_mt to pi, a pump 22 of increasing the pressure of the poor absorbent 15 from p\ to Pf₁, a pump 23 of increasing the pressure of the rich absorbent 17 coming of the absorber 4 from p\ to />_mt , and a valve 24 reducing the absorbent

12 pressure from Pf₁ to p_m- _i , and connections between devices, in such a way that, the absorbent 12 coming of the resorber 7 at Pf₁ is subcooled in a recovering way in the heat exchangers 14 and 16, it is expanded from Pf₁ to p_m- ι in the valve 24, it is mixed up in the mixer 11 at jt>_mt with the absorbent 13 forming the absorbent 10 of the one mean concentration, the absorbent 10 is distributed to the absorber 4 and desorber 3 in the way already shown, the vapor of refiigerent 5 desorbed in the desorber 3 are absorbed in the absorber 4, the absorbent 15 is pumped from the pressure p\ to Pf₁ by means of the pump 22, it is preheated in the heat exchanger 14 and it enters the resorber 7 at Pf₁, the absorbent 17 coming of the absorber 4 is pumped from pi to p\_nχ by means of the pump 23, it is preheated in a recovering way in the heat exchanger 16, it enters the generator 6 at j?_mt , it is heated up to a low temperature level by the source 2 generating refrigerent vapor 8 which finally is compressed by the compressor 9, it is resorbed in the resorber 7 at Pf₁ by the absorbent 15 producing useful heat extracted by the external source 25 , for closing the cycle.

The installation applying the procedure solving the first technical problem of fluids heating also, according to the invention, represented in a second variant in Fig. 10, in the log p - 1/T diagram, connected to an external sink source 1 of cooling for an absorption process and to an external heat source 2 of low thermal potential of heating for generation and desorption processes, having a low pressure absorber 3 at p/ externally cooled by the source 1, a high pressure resorber 4 at Pf₁, a truncation column including besides the absorber 3, a desorber 5 of low pressure pi externally heated by the source 2 and connected with the absorber 3 on refrigerent vapor side 6 desorbed in the desorber 5, a p\ pressure stage having a generator 7 externally heated by the siurce 2 and a resorber 8 externally cooled by source 1 coupled with the generator 7 on refrigerent vapor side 9 generated by the generator 7, a stage at an intermediary pressure with a generator 10 externally heated by source 2, Pf₁ > p\_nι >p\ >pf connected with the resorber at Pf₁ on vapor side generated by the generator via a compressor 12 which increases vapor 11 pressure from p_mχ till Pf₁, a supply with the absorbent 13 coming of the generator 7 at

Pl in pre-established quantities 14 and 15 of the absorber 3 and desorber 5 respectively by means of the regulating and throttling valves 16 and 17 respectively, a mixing process at p_mι in the mixer 18 of the absorbent 19 coming of the generator 10 with the absorbent 20 coming of the resorber 4 in order to generate the one mean concentration absorbent 21, a supply in pre- established quantities of the resorber 8 and of the generator 7 with the absorbents 22 and 23 respectively, obtained through a mixing process in the mixer 24 of the absorbent 21 with the absorbent 25 coming of the absorber 3 by means of the regulating and throttling valves 26 and 27, a heat exchanger 28 for subcooling the absorbent 13 by heating in a recovering way the absorbent 25, a heat exchanger 29 for subcooling the absorbent 20 by heating in a recovering way the poor absorbent 30 coming of the desorber 5, a heat exchanger 31 of further subcooling the absorbent 20 by heating in a recovering way the rich absorbent 32 coming of the resorber 8, a valve 33 for reducing absorbent 20 pressure from Pf₁ till p\_nχ , a valve 34 for reducing absorbent

21 pressure from p_mχ till p\, a pump 35 of increasing absorbent 25 pressure from pi till p\, a pump 36 of increasing absorbent 32 pressure from p\ till p_mt , a pump 37 of increasing absorbent 30 pressure from p\ till Pf₁, and connections between devices, in such a way that, the absorbent 20 coming of resorber 4 at Pf₁ is subcooled in a recovering way successively in the heat exchangers 29 and 31, it is expanded from Pf₁ to /%t ^{m tne} valve 33, it is mixing in the mixer 18 at /»_mt with the absorbent 19 in order to generate the one mean concentration absorbent 21, the absorbent 21 is expanded in the valve 34 till a pressure sensibly equal to p\, at this pressure it is mixing in the mixer 24 with the absorbent 25 pumped from pi to p\ with pump 35 and pre-heated in the heat exchanger 28, the resulted mixture is supplying the resorber 8 and the generator 7 in the way already shown, the absorbent 23 is supplying the generator 7, the vapor 9 generated in the generator 7 are resorbed in the resorber 8, the absorbent 13 is subcooled in the heat exchanger 28, it is expanded from p\ till p\ supplying the absorber 3 and the desorber 5 in the way already shown, the vapor 6 is absorbed in the absorber 3, the absorbent 30 is pumped from p\ till Pf₁, it is subcooled in the heat exchanger 29 supplying the resorber 4 at Pf₁, the absorbent 32 is pumped from p\ to p\^ , it is preheated in the heat exchanger 31, it is supplying the generator 10, and the vapor 11 is compressed by means of the compressor 12 from

Pl_nI till Pf₁ and is resorbed in the resorber 4 in order to produce heat transferred as useful heat to the external source 38 and to close the cycle.

The procedure, according to the invention, solves the second technical problem in that, for combined heating, cooling and electrical power production with high global efficiency COP_trig_eneratj_on > 0.9 , there are used heat pumping coabsorbent truncated cycles, according to the invention and the procedures described above, which have a much higher thermal efficiency than those known so far , e.g. COP = 10-200, depending on sources temperature and availability and applications working parameters, in coupling with a known thermodynamic Rankine power cycle, including an endothermic high temperature and pressure vapor generation process, e.g. Tf₁ = 550⁰C and pj_j =l70bar , low temperature and pressure vapor condensing exothermic processes, e.g. 7/ = (28,6-39,5)PC and />/ =(θ,O4-O,O7)&αr, a low temperature, cogeneration 7/ = (39,5 -8O)³C and pi = (p,07-0,4S)bar, a vapor expansion process from the high pressure to the low one producing useful mechanical work, a process of transforming the mechanical work in useful electrical energy, and processes of increasing the working fluid pressure and transport and of heat recovery, thermally connected with two fluids of low temperature potential, e.g. (5-75)°C, but with sensible different temperatures, AT = (lθ- 5O)⁰C , identified as heat pumping coabsorbent truncated cycles sink and heat sources, the hottest one at least or both coming of the thermal coupling with the power cycle, the first fluid of higher temperature, e.g. 40⁰C during the cold season and (5O-8O)°C during the warm season, being a fraction of that which extracted the heat from the exothermic condensing or low cogeneration processes and the second one, of lower temperature, e.g. (5-35)°C, being a fraction of that which was cooled by the power cycle sink source, or it has a different origin, cooled in a different way, respectively, in such a way that a fraction of the heat rejected by the power cycle during the condensing or cogeneration processes mentioned above is recovered by the eoabsorbent heat pumping cycle and transformed in amount of (23-48)% and (24-33)% in useful cooling, e.g. (213,15- 273,15)K and useful heat, e.g. (353,15- 453,15)K, respectively, supplementary supplying the consumer of heat, cooling and electrical power, besides the electrical and thermal power supply produced by the Rankine power cycle partially working in counterpressure mode.

The installation applying the procedure solving the second technical problem of combined heat, cooling and electrical power producing with high global efficiency, according to the invention, presented in a first variant in Fig. 11, is receiving on one side in the refrigerent vapor generation and desorption devices compartment 1 of the heat pumping installation 2, a fraction of the heat released by the condenser of the thermal power station supplyed by a non-renewable or renewable heat source, at a temperature sensibly equal to the condensing temperature by means of an intermediary heat transfer fluid with state 3, which, next, is sent with state 4 to the power station cooling tower in order to be cooled, and on the other side, it is yielding the heat produced in the refrigerent vapor resorption and absorption devices compartment 5 of the heat pumping installation 2 to an intermediary heat transfer fluid having state 6, at a temperature sensibly equal to the power station sink source temperature, or sensibly lower than that of condensation mentioned above characterizing another source colder than that, which subsequently is sent with state 7 to the power station cooling tower, or to another similar cooling source or colder in order to be cooled, in such a way that it enables the operation of the refrigerent vapor resorption compartment 8 and/or that of desorption 9 of the heat pumping installation 2, in order to produce useful effects of heating and/or cooling respectively, available to the heat and/or cooling consumer by means of the intermediary heat transfer fluids 10 and 11 and / or 12 and 13, respectively.

The installation applying the procedure solving the second technical problem of combined heat, cooling and electrical power producing with high global efficiency, according to the invention, presented in a second variant in Fig. 12, in order to avoid the contamination of the thermal power station referred to in the first variant of applying procedure by fluids of a different nature, it is transferring the intermediary heat transfer fluid heat of state 3 to the refrigerent vapor generation and desorption devices compartment 1 and it is yielding the heat produced in the refrigerent vapor resorption and absorption devices compartment 5 to the intermediary heat transfer fluid of state 6 by means of the heat exchangers 14 and 15 respectively and of the closed loops 16 and 17 respectively, where an intermediary heat transfer fluid is circulated by means of the pumps 18 and 19 respectively.

The installation applying the procedure solving the second technical problem of combined heat, cooling and electrical power producing with high global efficiency, according to the invention, presented in a third variant in Fig. 13, connected to a sink source with a cooling tower 1 and an intermediary heat transfer fluid 2 and a heat source 3 of renewable or non-renewable origin, including a thermal power station for electrical power producing, having a steam boiler 4, extermally heated with the source 3 at a high pressure and temperature, e.g. Tj_n = 550⁰C si Pi_n = 170bar, an electrical condensation steam turbine-generator group 5 provided with steam bleedings, a condenser 6 externally cooled with the source 1 at low pressure and temperature of condensation, e.g. Tj = (28,6-39,5)°C si pj =(θ,O4~O,θi)bar , communicating with the turbine through the connection 7, a turbine steam bleeding 8 with temperatures and pressures Tj =(39,5-80^ and pj = (θ,O7-O,48)&αr respectively for a power station power and low temperature heat cogeneration, a turbine steam bleeding 9 with temperatures and pressures Tj - (120-14O)³C and pj » (2-4)&αr respectively for a power station power and medium temperature heat cogeneration, a pump 10 for increasing the condensate 11 pressure from the condenser 6 pressure till that of the steam boiler 4, a coabsorbent heat pumping installation provided with truncation column 12 including a compartment 13 for generation processes, heated up in function of the sink source 1 temperature either from the condenser 6 or from the steam bleeding 8 via a heat exchanger 14 in order to provide perpetually a temperature difference of at least Δ7 ^Xa^V/^X = 7 ^tX^V/^X tncaktn -7¹λ^V1/ rod* > ( ^V8-lθ) '^pC between truncation column extreme working ° temperatures, a compartment 15 for resorption and absorption processes cooled by the source 1, a compartment 16 for a resorption process producing the useful heating effect e.g. (353,15 - 453,15)/;: and a compartment 17 for⁴a desorption process producing the useful cooling effect e.g. (213,15- 273,15}K, a heat exchanger 18 named also of thermofication or of district heating which first compartment of is thermally coupled with the steam bleeding 9, a heat exchanger 19 named also district heating point exchanger which first compartment of is thermally coupled either with the second compartment of the heat exchanger 18 or with the compartment 16 of the installation 12, or simultaneousy with both, a heat exchanger 20 named also district cooling point exchanger which first compartment of is thermally coupled with the compartment 17, a connection 21 supplying with steam the turbine 5 from the steam boiler 4, a low temperature heating loop made up of the steam bleeding 8, a regulating-closing valve 22, heat exchanger 14 first compartment via a connection 23, a pressure reducing valve 24 and a connection 25 with condensate 11 evacuation and pump 10 suction line, a medium temperature heating loop made up of the steam bleeding 9, a regulating-closing valve 26, first compartment of the heat exchanger 18, a pressure reducing valve 27 and a connection 28 to the connection 25, a loop with an intermediary fluid transferring the heat from the heat exchanger 18 second compartment to the heat exchanger 19 first compartment made up by the tour 29 via a regulating-closing valve 30 and the return 31 via the circulation pump 32, a loop with intermediary fluid transferring the heat from the compartment 16 of the installation 12 to the heat exchanger 19 first compartment made up by the tour 29 via a regulating-closing valve 33 and the return 34 via the pump 32, a ditrict herating loop 35 through the heat exchanger 19 second compartment, a loop with intermediary fluid transferring the coolness from compartment 17 of the installation 12 to the heat exchanger 20 first compartment made up by the tour 36 via a regulating-closing valve 37 and the return 38 via the circulation pump 39, a district cooling loop 40 by the heat exchanger 20 second compartment, a main loop for cooling the power station condenser second compartment by mens of the intermediary cooling fluid 2 having a tour 41 via a circulation pump 42 and a return 1 via a regulating valve 43 and a connection 44, a complementary loop for cooling the power station condenser second compartment by mens of the intermediary cooling fluid 2 having the tour 41 via the circulation pump 42 and the return 1 via a regulating valve 45, a serial connection of the heat exchanger 14 second compartment with the compartment 13 and with the tour 1 by means of connections 46, 47 and 48 and a compartment 15 cooling loop by means of a tour 49 via a pump of circulation 50 and the return 48 and the tour 1, in such a way that, the thermal power station coupled with the heat pumpimg installation is producing on one side during year cold period first electrical power by means of the working agent generated with the heat source 3 in the steam boiler 4, expanded in the turbine-generator group 5 via connection 21 condensed in the condenser 6 by source 1 in the way already shown above, second thermal energy for district heating and domestic water preparing using steam bleeding 9 and the medium temperature heating loop described above and third thermal energy used similarly and cooling supplied to the district by means of installation 12 through heat exchangers 19 and 20 and district heating and cooling loops respectively described above and supplied by the heat source from the condenser 6 via the valve 45, connection 46, heat exchanger 14 first side without heat supply in its second compartment from the bleeding 8, connection 47, compartment 13, connection 48, cooling tower 1, pump 42, connection 41, and the other side during year warm period first also electrical power in the way described above, second optionally thermal energy for preparing district domestic warm water using the bleeding 9 and the medium temperature loop described above and third thermal energy used similarly and cooling supplied to the district by means of the installation 12 through heat exchangers 19 and 20 and the district heating and cooling loops respectively mentioned above, cooled also by the cooling loop described above and supplied by the heat source from the condenser 6 via the valve 45, connection 46, heat exchanger 14 first compartment with heat supply from the bleeding 8 through the heating low temperature heating loop mentioned above, connection 47, compartment 13, connection 48, cooling tower 1, pump 42 and connection 41.

The procedure, according to the invention, solves the third technical problem in that, for combined heating, cooling and electrical power production, it is used a coabsorbent truncated cooling non-isobar cycle, according to the inventon and procedure described above, connected to heat sources of renewable, waste or classic origin, capable of heating to a maximum temperature Ttø for the i=l, ...,n-l generation processes, e.g. (40-70) ⁰C and of cooling to a

minimum temperature Ty[ for the i=l, ...,n-l resorption processes and an absorption process,

e.g. (10-40) ⁰C, in such a way that MM ^ TM ~TM ≥ (8-lθVC, and to a high

temperature source capable to achieve maximum generation temperatures TQQ » Ttø , e.g.

TQQ = (l8O-25θ)°C, coming of a nontruncated cooling cycle, with non-isobar generation and resorption processes, including a low pressure desorption process pi , e.g. (0.1-2) bar, where first useful cooling effect occurs, e.g. Tβj = (213,15 - 273,15)£ , a high pressure generation process ph, e.g. (30-60) bar, reaching the maximum temperature TQQ , an intermediary pressure resorption process p_mi, Pl < p\_nt < Ph_> ^e & (2-6) bar, resorbing the vapor generated by the high pressure generation process with concentration threshold condition fulfilment yRO,mX < ^G,m,h ^anc* when heat is produced by a temperature sensibly equal to that of resorption process end, TΏJ _m - χ > , e.g. (50-120) ⁰C, as second useful effect, a

mechanical work producing process achieved through, generated vapor expansion from the high pressure to the intermediary one, a process of transforming the mechanical work into electrical power, as third useful process, a truncation column used as nontruncated cycle truncation process mostly when cooling process temperature decrease is necessary, having pressures between the low pressure and the intermediary one and it is made up by a low pressure absorption process coupled on vapor side with the low pressure desorption process, a low pressure mixing process of the absorbents coming of the low pressure absorption and desorption processes in order to generate the one mean concentration absorbent y\{ and temperature 2M(P/₃.FM) ^≥ ^M •> ^a series of i stages, i-1, ..., n-1, n <= N, of isobar opposite intermediary generation and resorption processes having increasing pressures between the low pressure and the intermediary one, Pint≥Pi > Pi-X > Pl _> ^l~^ ■ • • _> n-1, n e N, and temperatures between Ttø and TJM , being coupled on vapor side having essentially increasing mean concentrations YG,m,i ^≤YG,_tn,i+\ ^≤YG,m,n-l_> fulfiling the concentration threshold condition yRO,i ^{≤ γ}G,m,i _> ^_* •••» ⁿ~*» ^ being supplied in pre-established proportions by uniform absorbents coming, for the first stage of the mixture of the one mean concentration absorbent with that coming of the second generation stage, for each of the following next stages of the mixture of the absorbent coming of the first inferior resorption stage with that coming of the first superior generation stage, and for the last stage of the mixture of the absorbent coming of the high generation process with the absorbent coming of the last but one resorption process and processes between successive stages of the truncation column inside and outside of it, of absorbent pressure increasing and reduction and of heat recovery, in such a way that, the rich absorbent leaves the resorption process at j%t , it is subcooled in a recovering way in the desorption process at /?/ from Tj^ till a temperature approaching Tj)J , it is expanded till

Pl , it is suffering the desorption process where is taking over the heat from the medium which must be cooled as useful effect and that of subcooling and it reaches the state parameters Tj)Q ≤ Tj^ and yjyo - ^M _> ^tne absorbent coming of truncation column first stage generation process is subcoolet in a recovering way, it is expanded till the low pressure, it is suffering the absorption process of the desorbed refrigerent vapor, it is mixing at the low pressure with the absorbent coming of the desorption process and it is generating the one mean concentration absorbent which is covering the truncation column till the last stage in the way described above, the absorbent coming of resorption process of the n-1 stage is pumped from P_n-I to Pf₁, it is supplying in pre-established quantities the resorption process at /?_mt , on one side, and the generation process at Pf₁, not before to be preheated in a recovering way by the absorbent coming of the generation at Pj₁, on the other side, the vapor generated at Pf₁ is expanded with producing of useful mechanical work and is resorbed at pfa producing useful heat, and the absorbent coming of the Pf₁ generation process is subcooled in a recovering way, it is expanded till p_n~\ and is participating to the n-1 stage supply, in the way described above, in order to close the cycle.

From the functional point of view the procedure solving the third technical problem of combined heating, cooling and electrical power production, it is using a coabsorbent truncated cooling non-isobar cycle, represented by solid line in Fig. 14 in the log p - 1/T diagram of the known refrigerent-absorbent working combination, connected to heat sources capable of heating to a maximum temperature Tj^ for the i=l, ...,n-l generation processes, e.g. (40-70) ⁰C and

of cooling to a minimum temperature TM for the i=l, ...,n-l resorption processes and an

absorption process, e.g. (10-40) ⁰C, in such a way that ΔJQV/ - TM_K - TM ≥ φ-lOjfC,

and to a high temperature source capable to achieve maximum generation temperatures TGO ^>> ?M _> ^G-S- T(JO = (l 80 - 25θ)° C , coming of a nontruncated cooling cycle, with non- isobar generation and resorption processes, represented in the same very diagram by dashed line, including a low pressure desorption process (1-2), p\ , e.g. (0.1-2) bar, where first useful cooling effect occurs, e.g. TQJ = (213,15- 273,15)ΛT, a high pressure generation process (3-4), Pf₁, e.g. (30-60) bar, reaching the maximum temperature TQQ , an intermediary pressure resorption process (5-6), p_mχ , pj <jø_mt < Ph, e g- (2-6) bar, resorbing the vapor generated by the high pressure generation process (3-4) with concentration threshold condition fulfilment >7tø,int ^{< Y}G,m,h ^an^ when heat is produced by a temperature sensibly equal to that of resorption process end, TRJ _mt > TM , e.g. (50-120) ⁰C, as second useful effect, a

mechanical work producing process achieved through generated vapor expansion from the high pressure to the intermediary one, a process of transforming the mechanical work into electrical power, as third useful process, a truncation column used as nontruncated cycle truncation process mostly when cooling process temperature decrease is necessary and low grade sources are available, having pressures between the low pressure and the intermediary one and it is made up by a low pressure absorption process (7-8) coupled on vapor side with the low pressure desorption process (1-2), a low pressure mixing process of the absorbents coming of the low pressure absorption and desorption processes in order to generate the one mean concentration absorbent ytø and temperature TM(PI, JM ) - ^M = ^a series of i stages, I=I, ..., n-1, n e N , of isobar opposite intermediary generation

and resorption

processes having increasing pressures between the low pressure and the intermediary one,

, and temperatures between , being

coupled on vapor side having essentially increasing mean concentrations

fulfiling the concentration threshold condition

⁹^ being supplied in pre-established proportions by uniform absorbents coming, for the first stage of the mixture of the one mean concentration absorbent with that coming of the second generation stage, point 9j , for each of the following next i stages of the mixture of the absorbent coming of the first inferior resorption stage i-1 with that coming of the first superior generation stage i+1, points 9/, i=2, ..., n-2, and for the n-1 stage of the mixture of the absorbent coming of the high pressure generation process with the absorbent coming of the last but one resorption process n-2, punctul 9_w_i , and processes between successive stages of the truncation column, of pumping the one mean concentration ytø absorbent from p/ to p\, and of the absorbent coming of the resorption processes from pf-\ to pj , i=2, ..., n-1, of reducing the pressure of the absorbent coming of the generation processes from pi to pi and from pj to p/-i, \~2, ..., n-1, and processes of heat recovery between opposite processes of absorption-generation and of resorption-generation, of gax and absorbent to absorbent type, in such a way that, the rich absorbent leaves the resorption process (5-6) at

Pint? ft *^s subcooled in a recovering way in the desorption process (1-2) at p\ from TRO int≥^M till a temperature approaching Tj)j , it is expanded till pi , it is suffering the desorption process where is taking over the heat from the medium which must be cooled as useful effect and that of subcooling and it reaches the state parameters %**&

the absorbent coming of truncation column first stage generation process Vl ~^GO,\) is subcooled in a recovering way, it is expanded till the low pressure, it is suffering the absorption process of the desorbed refrigerent vapor, it is mixing at the low pressure with the absorbent coming of the desorption process and it is generating the one mean concentration absorbent which is covering the truncation column till the last stage n-1 in the way described above, the absorbent coming of resorption process (9_n_i -9RO,_Π-\) of the n-1 stage is pumped from p_n-\ to pfi, it is supplying in pre-established quantities the resorption process (5-6) at Pint ' ^{on one s}^^e' ^an£^ ^tne generation process (3-4) at Pf₁, not before to be preheated in a recovering way by the absorbent coming of the generation process at Pf₁, point 10, by the poor absorbent coming of the generation processon (3-4) Pf₁, on the other side, the vapor generated at PIi is expanded with producing of useful mechanical work and is resorbed at p_mι producing useful heat, and the absorbent coming of the pj_j generation process (3-4) is subcooled in a recovering way until it reaches saturation parameters at p_n~\ , it is expanded till Pn-Λ &ⁿd is participating to the n-1 stage supply, in the way described above, in order to close the cycle.

The applying installation of the procedure solving the third technical problem of producing combined heat, cooling and electrical power, according to the invention, represented in a first variant in Fig. 15 in the log p - 1/T diagram is connected to an external sink source 1 of cooling for an absorption process and to external heat source 2 for a generation process and it is including a low pressure desorber 3 at /?/ , a low pressure absorber 4 at p\ , externally cooled by source 1 and connected with the desorber 3 on refrigerent vapor side 5 desorbed by the desorber 3, a generator 6 of high pressure Pf₁ externally heated, a resorber 7 of intermediary pressure

Pint » Ph > Fmt ^> Pl ■_> connected with the generator 6 on refrigerent vapor side 8 generated by the generator 6 via a turbogenerator group 9, a one mean concentration absorbent 10 obtained in a mixer 11 by mixing up at p\ of the absorbents 12 and 13 coming of the desorber 3 and absorber 4 respectively, a supply with the absorbent of the one mean concentration of the resorber 7 at p_m^ by the absorbent 14 via the regulating valve 15 and of the generator 6 at Pf₁ with the absorbent 16 via the regulating valve 17 in pre-established quantities, a heat exchanger 18 recovering the heat of the poor absorbent 19 coming of the generator 6 at Pf₁ by the one mean concentration absorbent, a valve 20 for reducing the pressure of the absorbent 19 from Pf₁ to pi, a valve 21 for reducing the pressure of the rich absorbent 22 coming of the resorber 7 from pi_nt to pi and a pump 23 for pumping the one mean concentration absorbent 10 from pi to Pf₁, in such a way that , the absorbent 22 is leaving the resorber 7, is subcooled in a recovering way in the desorber 3 through the connection 24, it is expanded with the valve 21 from /?_mt to pi , it is suffering the desorption process in the desorber 3 where it is taking over the heat of an external fluid 25 which must be cooled as first useful effect and that of the absorbent 22 subcooling, the absorbent 19 is subcooled in a recovering way in the heat exchanger 18, it is expanded till /?/, it enters the absorber 4 where it is suffering the absorption process of the desorbed refrigerent vapor 5 producing supplementary useful thermal effect besides that produced in the resorber 7 when absorption interval and sink source temperature are enough high, it is mixing at the low pressure as absorbent 13 with the absorbent 12 forming the one mean concentration absorbent 10 which is pumped from pi to Pf₁, it is preheatred in a recovering way, it is distributed to the generator 6 and resorber 7 and the generated refrigerent vapor 8 are expanded from Pf₁ to Pj_x^ producing mechanical work and electrical power by means of the turbogenerator 9 as second useful effect and heat as third useful effect heating up the external fluid 26 when resorbed in the resorber 7, in order to close the cycle.

The installation described above was modeled with the ammonia/water working combination for trigeneration of heat, cooling and electrical power working mode. Some results follow:

• End generation temperature: 200⁰C;

• Sink source temperature: a) (20-30) ⁰C si b) 40⁰C; • Beginning desorption temperature: -22 pana Ia -12⁰C;

• Beginning resorption temperature: (60-90) ⁰C;

• Electrical efficiency : (8-11)%;

• Cooling efficiency: (25-27)%;

• Heating efficiency: (72-74)% for the a) sink source and 117% the b) sink source; • Global efficiency, equal to partial efficiencies addition: (105-112)% for sink source a) and 150% for sink source b); efficiency=(useful energy output)/(generation energy input).

The applying installation of the procedure solving the third technical problem of producing combined heat, cooling and electrical power, according to the invention, represented in a second variant in Fig. 16 in the log p - 1/T diagram is connected to an external sink source 1 of cooling for absorption and resorption processes, to an external heat source 2 of low thermal potential for a generation process and to an external heat source 3 of high thermal potential for a second generation process and it is including a low pressure desorber 4 at pi , a low pressure absorber 5 at pi , externally cooled by source 1 and connected with the desorber 4 on refrigerent vapor side 6 desorbed by the desorber 4, a generator 7 of high pressure pfo externally heated by source 3, a resorber 8 of intermediary pressure Pj_x^ , Pf₁ > p^ > p\ connected with the generator 7 on refrigerent vapor 9 generated by the generator 7 via a turbogenerator group 10, an absorbent 11 of the one mean concentration generated in a mixer 12 by mixing up at p\ of absorbents 13 and 14 coming of the desorber 4 and absorber 5 respectively, a truncation column with a stage at a pressure p\ , Pf₁ > Pm' t≥Pl ^> Pl ^w*^{tn a} generator 15 externally heated by the low grade source 2 and a resorber 16 externally cooled coupled with the generator 15 on refrigerent vapor 17 generated by the generator 15, a supply in pre-established quantities of the resorber 16 at p\ with the absorbent 18 via the regulating valve 19 and of the generator 15 at p\ with the absorbent 20 via the regulating valve 21 coming of the mixing up in the mixer 22 at a pressure sensibly equal to p\ of the absorbent of the one mean concentration 11 with the absorbent 23 coining of the generator 7 at pfr, on one side, and of resorber 8 at p_m' χ with the absorbent 24 via the regulating valve 25 and of the generator 7 at Pf₁ with the absorbent 26 via the regulating valve

27, on the other side, a heat exchanger 28 recovering the absorbent 23 heat by the absorbent 29 coming of the resorber 16, a heat exchanger 30 recovering the absorbent 31 heat coming of the generator 15 at p\ by the one mean concentration absorbent 11, a valve 32 reducing the pressure of absorbent 23 from pfr to p\, a valve 33 reducing the pressure of absorbent 31 from

Pl to pi, a valve 34 reducing the pressure of absorbent 35 from /r_mt to p\, a pump 36 for pumping the one mean concentration absorbent 11 from pi to p\, a pump 37 for pumping the absorbent 29 from p\ to Pf₁, in such a way that the absorbent 35 leaves the resorber 8, it is subcooled in a recovering way in the desorber 4 through connection 38, it is expanded by means of valve 34 from p_mi to pi , it is suffering the desorption process in the desorber 4 where is taking over the heat of an external fluid 39 to be cooled as first useful effect and that of absorbent 35 subcooling, the absorbent 23 is subcooled in a recovering way in the heat exchanger 28, is expanded till pressure p\ in the expansion valve 32, the absorbent 31 is subcooled in a recovering way in the heat exchanger 30, is expanded in the valve 33 till pi , it is entering the absorber 5 where is absorbing vapor 6, the resulting absorbent 14 is mixing up in the mixer 12 with the absorbent 13, the resulting one mean concentration absorbent 11 is pumped with pump 36, it is mixing up in the mixer 22 with the subcooled absorbent 23, the resulting absorbent supplies the generator 15 and the resorber 16 in the way shown before, the vapor 17 generated in the generator 15 is resorbed in the resorber 16, the resulting absorbent 29 is pumped by the pump 37, it is preheated in a recovering way in the heat exchanger 28, it is distributed to the resorber 8 and generator 7 in the way shown above, the vapor 9 generated in the generator 7 is expanded in the turbogenerator 10 producing electrical energy, as second useful effect, is resorbed in the resorber 8 producing heat in order to heat up the external fluid 40, as third useful effect, for closing the cycle.

Claims

1. Procedure of a coabsorbent cycle efficiency and feasibility increase, Fig. 1, enabling its working with generation temperatures enough reduced in order to benefit of a supply of heat sources of low thermal potential and to avoid concentration threshold problems, destined to industrial and domestic, city and rural applications of cooling production with the help of classic or renewable energy sources and consisting of operating a coabsorbent truncated cooling cycle coming of a coabsorbent nontruncated cooling cycle, characterized in that, it is connected to sources capable of heating to a maximum temperature for generation processes, e.g. (40-70) ⁰C and of cooling to a

minimum temperature TM for resorption and absorption processes, e.g. (10-40) ⁰C, in

such a way that ΔTfø = Ttø - T^f > (8 - 1O)^C , including a low pressure desorption

process p\ where useful cooling effect occurs, a truncation column used as nontruncated cycle truncation process, having pressure between the low value a and a high pressure p_n and is made up of a low pressure absorption process coupled on vapor side with the low pressure desorption process, a low pressure mixing process of the absorbents coming of the low pressure absorption and desorption processes in order to generate a one mean concentration absorbent_* a series of i stages, i=l, ..., n, n e N , of isobar opposite intermediary generation and resorption processes, having increasing pressures between the low pressure and the high one of the last stage, p_n>Pi+l > Pi > Pl and temperatures between Tj^ and Tj^ , being coupled on vapor side having essentially increasing

mean concentrations YG,m,i ^{≤ γ}G,m,i+l ^{≤ γ}G,m,n-l_> &lfiling the concentration threshold condition yRO,i ^≤ ^G,m,i _> ^_> • • •_> ⁿ and being supplied in pre-established proportions by uniform absorbents coming, for the first stage of the mixture of the one mean concentration absorbent with that coming of the second generation stage, for each of the following next i stages of the mixture of the absorbent coming of the first inferior resorption stage i-1 with that coming of the first superior generation stage i+1, i=2, ...,n-l, and for the high pressure stage of the resorption process of the last but one resorption process n-1, and processes between successive stages of the truncation column, of the one mean concentration absorbent pressure increasing from pi to p\ and of the absorbent coming of resorption processes from p,__j to p\ , i=2, ..., n, of pressure reduction of absorbent coming of generation processes, from p\ to pi and from pf to pj_i, i=2, ..., n, and of heat recovery between opposite processes of absorption-generation and of resorption-generation, of gax and of absorbent-absorbent type, in such a way that the rich absorbent leaves the truncation column last stage resorption process at p_n, it is subcooled in a recovering way in the desorption process at p\ from Tpn _n ≥ TM till a temperature approaching 7/)/ , it is

expanded till p\, it suffers the desorption process where it extracts the heat from the medium which must be cooled and that of subcooling and reaches the state parameters TOO ^≤ ?M ^md yDO ^≥ yM » ³^ ^tne absorbent coming of the generation process of the first truncation column stage is subcooled in a recovering way, it is expanded untill the low pressure, it suffers the absorption process of the desorbed refrigerent vapor, it is mixing at the low pressure with the absorbent coming of the desorption process and it generates the one mean concentration absorbent which is covering the truncation column in the way described above untill the last stage at p_n , closing cycle.

2. Applying installation according to the claim 1, describing a double truncated coabsorbent cycle, Fig. 2, including a desorber 1 receiving the rich absorbent 2, a fraction of it evaporates at the low pressure producing refrigerent vapor 3 through heating by the external source 4 which is being cooled in order to get the plant useful effect and the rest exits the desorber 1 as absorbent 5, the vapor 3 are superheated in the superheater 6 where is subcooling in a recovering way the absorbent 7 coming from the high pressure resorber 8 then is absorbed in the absorber 9 at a pressure sensibly equal to the low one, and the subcooled absorbent 7 is expanded from the high pressure till the low one by means of of the expansion valve 10 in order to enter the desorber 1 and the poor absorbent 11 enters the absorber 9, it absorbes vapor 3 and leaves the device as richer absorbent 12, characterized in that, prior to enter the absorber 9 the poor absorbent 11 is first subcooled in a recovering way in the heat exchanger 13 providing the intermediary pressure generator 14 where it comes of a fraction of its necessary generation heat, then it is expanded from the intermediary pressure to the low one by means of the expanding valve 15, a fraction of absorber 9 absorption heat is transfered in a gax way as generation heat to generator 14 by means of of the intermediary heat exchange loop 16 provided with a pump of circulation 17 and the rest of generation heat is provided to generator 14 by the external heat source 18, the absorbents 5 and 12 of sensibly equal pressures are mixed in the low pressure mixer 19 cyclic forming the plant one mean concentration absorbent 20 which subsequently is pumped with pump 21 from the low pressure to the intermediary one, is preheated in a recovering way in the heat exchanger 22 receiving a fraction of the absorber 9 absorption heat and then is introduced in the inermediary pressure mixer 23, the rest of the not recovered absorber 9 absorption heat is eliminated finally by means of the plant cooling source 24 in the intermediary pressure mixer 23, the one mean concentration absorbent it is mixing with the absorbent 25 which priorily has been suffering successively a first subcooling process in a recovering way in the heat exchanger 26 providing the high pressure generator 27 which it is coming of a fraction of its generation heat, then a second sucooling process in a recovering way in the heat exchanger 28 and an expansion from the high pressure till the intermediary one in the throttling valve 29 forming a mean concentration absorbent 30 which is supplying in pre-established quantities through the regulating valves 31 and 32 the intermediary pressure generator 14 and resorber 33 respectively, the refrigerant vapor 34 generated by the generator 14 is resorbed in the resorber 33, cooled mainly by the plant sink source 24, the absorbent 35 coming of the resorber 33 is pumped by the pump 36 from the intermediary pressure till the high one in the high pressure vessel 37, priorily being preheated in a recovering way successively in the heat exchanger 38, receiving a fraction of the intermediary pressure resorber 33 resorption heat and in the heat exchanger 28, the absorbent 39 coming of the high pressure vessel 37 is supplying in pre-established quantities through the regulating valves 40 and 41 the high pressure generator 27 and resorber 8 respectively, a fraction of the high generator 27 generation heat is supplyed by the external heat source 42, and the vapor of refrigerent 43 generated by the high pressure generator 27 is absorbed by the high pressure resorber 8, cooled by the plant sink source 24, closing cycle.

3. Procedure of a coabsorbent cycle efficiency and feasibility increase according to claims 1 and 2 and Fig. 3, enabling its working with generation temperatures enough reduced in order to benefit of a supply of heat sources of low thermal potential and to avoid concentration threshold problems, destined to industrial and domestic, city and rural applications also of cooling production with the help of classic or renewable energy sources and consisting of operating a coabsorbent truncated hybrid cooling cycle coming of a coabsorbent nontruncated cooling hybrid cycle, characterized in that, it is connected to sources capable of heating to a maximum temperature Tj^ for generation and

desorption processes, e.g. (40-70) ⁰C and of cooling to a minimum temperature Ttø for

resorption and absorption processes, e.g. (10-40) ⁰C, in such a way that

ΔTfcf - TM "^■ keatus ~TM ^■"^■' raolMs ≥ (8 -1O)³C, including a low pressure desorption process pi

where useful cooling effect occurs, a high pressure resorption process Pf₁, a truncation hybrid column used as nontruncated hybrid cycle truncation process, having pressures between the low one and an intermediary pressure p_m- i , pfj > p_m% > pi and is made up by a low pressure absorption process coupled on vapor side with the low pressure desorption process, a low pressure mixing process of the absorbents coming of the low pressure absorption and desorption processes in order to generate the one mean concentration absorbent, a series of i-1 stages, i<n, i,n e N of isobar opposite intermediary generation and resorption processes, and an i stage with an intermediary pressure generation process PuA ~ Pi) w^k stages pressure increasing from the low to the inermediary one j%it>jPr+i > Pi ^≥ Pl ²^ temperatures between TJM and Ttø , being coupled on vapor side having essentially increasing mean concentrations

fulfϊling the concentration threshold condition a«^d being supplied in pre-established

proportions by uniform absorbents coming, for the first stage of the mixture of the one mean concentration absorbent with that coming of the second generation stage, for each of the following next k , k=2, ..., i-1 stages of the mixture of the absorbent coming of the first inferior resorption k-1 stage with that coming of the first superior generation stage k+1, and for the last i stage at jp_mt and resorption process at pfr by the absorbent coming of the resorption process of the last but one resorption process i-1, a process of increasing generated vapor pressure from the intermediary pressure to the high one, and processes between successive stages of the truncation column, of pumping the one mean concentration absorbent from p\ to p\ and of the absorbent coming of the resorption processes pjc~\ to pfc , k=2, ..., i-1, and of pressure reduction of the absorbent coming of generation processes p\ to pj and from and of heat recovery

between opposite processes of absorption-generation and resorption-generation, of gax and absorbent to absorbent type, in such a way that, the absorbent coming of the i-1 stage resorption process is supplying in pre-established quantities the generation process at p_mχ and of resorption at Pf₁, the vapor generated at p^ is suffering first a process of pressure increasing from p_mt to ph and then a resorption one at Pf₁ with useful heat elimination, the rich absorbent leaves the resorption process at /%, is subcooled in a recovering way in the desorption process at p\ , from to a temperature approaching Tnj , is

expanded till p\, it suffers the desorption process where it extracts the heat from the medium which must be cooled and that of subcooling and reaches the state parameters TOO - TM ^d yDO ^≥yM-_> ^m& ^tne absorbent coming of the generation process of the first truncation column stage is subcooled in a recovering way, it is expanded untill the low pressure, it suffers the absorption process of the desorbed refrigerent vapor, it is mixing at the low pressure with the absorbent coming of the desorption process and it generates the one mean concentration absorbent which is covering the truncation column in the way described above untill the last i stage, closing cycle.

4. Installation applying the procedure according to claims 1, 2 and 3 and Fig. 4, connected to an external heat source 1 of low temperature potential for a generation process and to an external sink source 2 for cooling an absorption process, characterized in that, it is including a truncation column with a low pressure absorber 3 p\ externally cooled by the source 2 and a generator 4 at pressure p\ , externally heated by the source 1, a low pressure Pl desorber 5 connected by the absorber 3 on refrigerent vapor side 6 desorbed from the desorber 5, a high pressure resorber 7, Pf₁, Ph > p\ ≥ Pl, connected with the generator 4 on vapor side 8 generated by the generator 4, via a compressor 9 of vapor 8 pressure increase from p\ to Pf₁, a mixing of absorbents 10 and 11 coming of the desorber 5 and absorber 3 respectively in order to generate the one mean concentration absorbent 12 in a mixer 13 at pressure pj, a supply with absorbent 12 in pre-established quantities 14 and 15 of the generator 4 and resorber 7 respectively by means of the regulating valves 16 and 17 respectively, a heat exchanger 18 recovering the heat of the absorbent 19 coming of the generator 4 by the absorbent 12, a valve 20 for reducing the pressure of the absorbent 19 from pi to pi, a pump 21 for increasing the pressure of the absorbent 12 from p\ to Pf₁, and connections between devices, in such a way that, the rich absorbent 22 coming of the resorber 7 is subcooled in a recovering way in the desorber 5 through the connection 23, it is expanded from Pf₁ to p\ by means of the throttling valve 24, is suffering the desorption process in the desorber S where it is extracting the heat of the medium 25 which must be cooled as a first useful effect and the subcooling heat of the absorbent 22, the absorbent 19 is subcooled in a recovering way in the heat exchanger 18, it is expanded from p\ till p\ in the expansion valve 20, is entering the absorber 3 where it suffers the absorption process of the vapors 6, the absorbents 10 and 11 coming from desorber 5 and absorber 3 respectively are mixing in the mixer 13 at pi generating the absorbent 12 of one mean concentration, the absorbent 12 is pumped by the pump 21 from p\ to Pf₁, is preheated in the heat exchanger 18, it is distributed to generator 4 and resorber 7 in the way described above, and the vapor 8 generated in the generator.4 is compressed by the compressor 9 from pi till Ph and is resorbed in the resorber 7 transfering the resorption heat to an external source 26, as second useful effect, closing cycle.

5. Installation applying the procedure according to claims 1, 2, 3 and 4 and Fig. 5, connected to an external heat source 1 of low temperature potential for generation processes and to an external sink source 2 for cooling absorption and resorption processes, characterized in that, it is including a low pressure desorber 3 at pi, a high pressure resorber 4 at Ph, a hybrid truncation column with pressures between the low value and an intermediary one Pint , made up by an absorber 5 at p\, externally cooled by source 2, coupled with the desorber 3 on vapor side 6 desorbed by the desorber 3, a mixer at p\ for mixing the absorbents 8 and 9 coming of the desorber 3 and absorber 5 respectively in order to generate the one mean concentration absorbent 10, a stage of pressure p\, p\ > Pi with a generator 11 externally heated and a resorber 12, externally cooled, coupled on vapor side 13 generated by the generator 11 and resorbed by the resorber 12, an intermediary pressure Pint stage Pf₁ > /?_mt > p\ ≥pι with a generator 14 externally heated, a supply for the generator 11 and resorber 12 in pre-establshed quantities respectively by uniform absorbents 15 and 16 respectively, regulated by the valves 17 and 18 respectively coming of the mixture 19 at p\ of the absorbent 10 with the absorbent 20 coming of the generator 14, a pump 21 for pumping the absorbent 10 from pi to p\, a pump 22 for pumping the absorbent 23 coming of the resorber 12 from p\ to /fø, a valve 24 for reducing the pressure of the absorbant 25 from p\ to p\, a valve 26 for reducing the pressure of the absorbant 20 from p_mi to p\, a recovering heat exchanger 27 between absorbents 25 and 10, a recovering heat exchanger 28 between absorbents 20 and 23, and connections between devices, in such a way that, the absorbent 23 after being pumped and preheated it is supplying in pre-established quantities the generator 14 by the absorbent 29 regulated by the valve 30 and the resorber 4 by the absorbent 31 regulated by the valve 32, the vapor 33 generated by the generator 14 is compressed from /?_mt Ia Pf₁ by the compressor 34 and are resorbed in the resorber 4 with heat producing transferred to the external source 35 as a first useful effect, the rich absorbent 36 coming from the resorber 4 is subcooled in a recovering way in the desorber 3 through the connection 37, it is expanded from Pf₁ to p\ by means of the expanding valve 38, it is suffering the desorption process in the desorber 3 where it is extacting the heat of the medium 39 which must be cooled as a second useful effect and the subcooling heat of the absorbent 36, the absorbent 25 is subcooled in a recovering way in the heat exchanger 27, it is expanded from p\ to p\ by means of the valve 24, it is suffering the absorption process of the vapor 6 in the absorber 5 becoming absorbent 9, it is mixed up in the mixer 7 with the absorbent 8, is is forming the absorbent 10 of the one mean concentration and it is pumped in the truncation column which is covered in the way mentioned above, closing cycle.

6. Procedure of efficiency and feasibility increase of a coabsorbent cycle, Fig. 6, enabling its working with cooling temperatures higher than those corresponding to nontruncated cycles of origin and to avoid concentration threshold problems, destined to industrial and domestic, city and rural applications of heating production with the help of classic or renewable energy sources and consisting of operating a coabsorbent truncated heating cycle coming of a coabsorbent nontruncated heating cycle, characterized in that, it is connected to heat sources capable of heating to a maximum temperature Ttø for

generation and desorption processes, e.g. (40-70) ⁰C and of cooling to a minimum temperature Ttø for resorption and absorption processes, e.g. (10-40) °C, in such a way

that ΔTtø = Ttø -Ttø > (8~lθ)°C , including a high pressure resorption process

Pf₁ where useful heating effect occurs, a truncation column used as nontruncated cycle truncation process, having pressures between the high value and a low pressure value pj and is made up by a high pressure generation process coupled on vapor side with the high pressure resorption process, a high pressure mixing process of absorbents coming of the high pressure generation and resorption processes in order to generate the one mean concentration absorbent, a stage of low pressure absorption and desorption processes, a series of i stages, i=l, ..., n, n e N, of isobar opposite intermediary generation and resorption processes, with stages pressures decreasing from the high pressure to the low one pi ≤ Pf₊I <Pj <Ph and temperatures between Ttø and Ttø , being coupled on vapor side having essentially decreasing mean concentrations

^G m,i+k-A -^G,m,i+k -^D,m fulfiling the concentration threshold condition yRO,i+lc ^{≤ γ}G,m,i+k> k ≤ n-i , i,k,n<≡N , y^o ≤ Yo,m > ^{mά bein}S supplied in pre- established quantities by uniform absorbents coming, for the first stage of the mixture of the one mean concentration absorbent with that coming of the second stage of resorption, for each of the following i=2, ..., n-1 next stages of the mixture of the absorbent coming of the first superior resorption stage i+1 with that coming of the first inferior generation stage i-1, i=2, ...,n-l, for the i=n stage by the mixture of the absorbent coming of the i=n-l generation process with that of the low pressure absortion process, and for the low pressure processes stage of the absorbent coming of the n generation process, and processes between successive stages of the truncation column, of reducing the pressure of the one mean concentration absorbent from Pf₁ to p\ and of the absorbent coming of the generation processes from /?/_j to p\ , i=2, ..., n and from p_n to pi, of incresing the absorbent pressure coming of the absorption process from pf to p_n , and of the resorption processes from pi to P_j~\, i=2, ..., n and from ρ\ to Pf₁, and of heat recovery between opposite processes of absorption-generation and of resorption-generation, of gax and absorbent to absorbent type, in such a way that, the poor absorbent leaves the desorption process at p\, it is pumped till Pf₁, it is preheated in a recovering way in the resorption process at pfr from Tβo ≤Ttø till a temperature close to TRJ, it is suffering the

resorption process where it is rejecting the resorption heat to the medium which must be heated up and that of preheating, reaching state parameters TJRQ ≥ Tj^ and

yRO ^≤yM _> ^md the absorbent coming of the resorption process of the truncation column first stage it is pumped from p\ till Pf₁, it is preheated in a recovering way, it is suffering the generation process of the refrigerent vapor at pf_j, it is mixed up at the high pressure with the absorbent coming of the high pressure resorption process and generates the one mean concentration absorbent which is covering the truncation coluπtti downstairs until the last stage and finally the stage at /?/, in the way described above, closing cycle. Procedure applying installation according to claims 1, 2, 3 , 4, 5 and 6 and Fig.

7, connected to a sink source 1 of external cooling for absorption and resorption processes and to a heat source 2 of low thermal potential for generation and desorption processes supply, characterized in that, it has a truncation column including a low pressure absorber 3 at pi externally cooled by source 1, a low pressure desorber 4 at p\ externally heated by the source 2 and connected with the absorber 3 on refrigerant vapor side 5 desorbed by the desorber 4, an intermediary pressure stage p_m- χ with a generator 6 externally heated by the source 2 and a resorber 7 externally cooled with the source 1 coupled with the generator 6 on refrigerent vapor side 8 generated by the generator 6 and a high pressure Pf₁ generator 9 pf, > pfa > pi , externally heated by the source 2, a resorber 10 of high pressure Pf₁ connected with the generator 9 on refrigerent vapor side 11 generated by the truncated column generator 9, a mixing in the mixer 12 at Pf₁ of the absorbents 13 and 14 coming of the generator 9 and the resorber 10 respectively in order to generate the one mean concentration absorbent 15, a mixing in the mixer 16 at P]_n^ of the absorbents 15 and 17 coming of the absorber 3 in order to get a mean concentration absorbent which is supplying in pre-established quantities 18 and 19 the resorber 7 and the generator 6 respectively by means of the regulating valves 20 and 21 respectively, a supply with absorbent 22 coming of the generator 6 of the absorber 3 and of the desorber 4 in pre- established quantities 23 and 24 respectively by means of the regulating valves 25 and 26 respectively, a heat exchanger 27 for subcooling the absorbent 15 by preheating in a recovering way the rich absorbent 28 coming of the resorber 7, a heat exchanger 29 of subcooling the absorbent 22 through preheating in a recovering way the absorbent 17, a valve 30 for reducing the pressure of the absorbent 15 from Pf₁ to p_mχ , a valve 31 for reducing the pressure of the absorbent 22 from ρ_mι to p[, a pump 32 for increasing the pressure of the absorbent 17 from pi to p^ , a pump 34 for increasing the pressure of the poor absorbent 35 coming of the desorber 4 from /?/ to Pf₁, and connections between devices, in such a way that, the absorbents 13 and 14 are mixing up in the mixer 12 at Pf₁, are generating the one mean concentration absorbent 15 which is subcooled in the heat exchanger 27, it is expanded in the valve 30, it is mixing up in the mixer 16 at /%t with the absorbent 3 which priorily was pumped from ρ\ to ρ_mι with the pump 32 and preheated in a recovering way in the heat exchanger 29 and it is supplying with the absorbents 18 and 19 the resorber 7 and the generator 6 respectively in the way already shown, the vapor 8 generated in the generator 6 is resorbed in the resorber 7, the absorbent

22 is subcooled in the heat exchanger 29, it is expanded from Pj₁^ to /?/ in the valve 31, it is supplying the absorber 3 and the desorber 4 with the absorbents 23 and 24 respectively in the way already shown, the vapor 5 desorbed in the desorber 4 is absorbed in the absorber 3, the absorbent 35 coming of the desorber 4 is pumped by the pump 34 from the low pressure till the high one, it is preheated in the resorber 10 through connection 36, it enters the resorber 10 where it is suffering the resorption process of the vapor 11, the resorption heat is eliminated by means of the external source 37 heating it up as the useful effect and preheating the absorbent 35, and the absorbent 28 coming of the resorber 7 is pumped by the pump 33 from p_mi till Pf₁, it is preheated in a recovering way in the heat exchanger 27, it enters the generator 9 where it is suffering the generation process in order that finally the resulting absorbent 13 be mixed up in the mixer 12 with the absorbent 15 and close cycle.

8. Procedure of increasing the efficiency and feasibility of a coabsorbent cycle according to claims 1, 2, 3, 4, 5, 6 and 7 and Fig. 8, enabling its working with cooling temperatures higher than those corresponding to nontruncated cycles of origin and to avoid concentration threshold problems, destined to industrial and domestic, city and rural applications also of heating production with the help of classic or renewable energy sources and consisting of operating a coabsorbent truncated heating hybrid cycle coming of a coabsorbent nontruncated heating hybrid cycle, characterized in that, it is connected to heat sources with limited availability capable of heating to a maximum temperature TM for generation and desorption processes, e.g. (40-70) and of cooling to a minimum

temperature TM for resorption and absorption processes, e.g. (10-40) °C, in such a way

that ATM = TM -TM ≥(8-lθ)PC, including a high pressure resorption process

Ph where useful heating effect occurs, a truncation hybrid column used as nontruncated hybrid cycle truncation process, having pressures between an intermediary value Pw' fc , FuA < Ph_> ^an& ^a *^ow pressure value pi, and it is made up by an intermediary pressure generation process coupled on vapor side with the high pressure resorption process, an intermediary pressure mixing process of absorbents coming of the high pressure resorption and intermediary pressure generation processes in order to generate the one mean concentration absorbent, a stage of low pressure absorption and desorption processes, a series of n-i stages of isobar opposite intermediary generation and resorption processes, noted by i+1, i+2, ..., n, i,neN, with stages pressures decreasing from the intermediary pressure to the low one p_ιxA ≥ pj₊fc > Pj+k+i > pj, k e N and temperatures between iM_∞α] ^m& TM ^' » being coupled on vapor side having essentially decreasing mean

concentrations YG,mJ+k--l ^≥YG,m,i+k ^≥YD,m _> folfiling the concentration threshold condition yRO,i+k ≤ ΫG,m,i+k , k≤n-i, i,k,n& N , y^O ^≤^D₎m _> ^d being supplied in pre-established proportions by uniform absorbents coming, for the second stage of the mixture of the one mean concentration absorbent with that coming of the third stage of resorption i+2, for each of the following next stages i+k, 2 < k ≤ n - i ^:-l , of the mixture of the absorbent coming of the first superior resorption stage with that coming of the first inferior generation stage, for the n stage by the mixture of the absorbent coming of the i=n- 1 generation process with that of the low pressure absortion process, and for the low pressure processes stage of the absorbent coming of the n generation process, a process of increasing the pressure of the stage i generated vapor from the intermediary value to the high value and processes between successive stages of the truncation column, of increasing the pressure of the absorbent coming of the absorption process from p\ to p_n and of the absorbent coming of the resorption processes from p_n-fc+i to /?_w_£_+/_i , i ≤ k ≤ n - 1 , of reducing the pressure of the absorbent coming of the high pressure resorption process from Py₁ to p_mi , of the one mean concentration absorbent from pf to />/+l and of the absorbents coming of the generation processes from Pf+fc to pj₊fc₊ι , l ≤ k ≤ n i - 1 and from p_n to p\ and of heat recovery between opposite processes, of absorption- generation and of resorption-generation, of gax and of absorbent to absorbent type, in such a way that, the absorbent coming of the resorption process at pj₊\ is pumped till pj = /r_mt , it is preheated in a recovering way, it is supplying the generation process at

Pint _» the refrigerent vapor generated is compressed from p_m- χ to pfr where it is suffering the resorption process, the poor absorbent leaves the desorption process at pi, it is pumped till /%, it is preheated in a recovering way subcooling the absorbent coming of the resorption process at pf_j, it is suffering the resorption process where it is yielding the resorption heat to the medium which must be heated up as useful effect, and the absorbent coming of the resorption process at pjj is subcooled in a recovering way till the saturation parameters at (vjRO,»_>.Pint)_> ^{li ιs} mixing at p_mχ with the absorbent coming of the generation process at p_m^ generating the one mean concentration absorbent which is covering the trauncation column untill the last atage and then the stage at /?/ , in the way described above, closing cycle.

9. Installation applying the procedure according to claims 1, 2, 3, 4, 5, 6, 7 and 8 and Fig. 9, connected to an external sink source 1 of cooling for an absorption process and to an external heat source 2 of low thermal potential of heating for generation and desorption processes, characterized in that, it is including a truncation column with a desorber 3 of low pressure p\ externally heated by the source 2, an absorber 4 of low pressure /y externally cooled by the source 1 and connected by the desorber 3 on vapor 5 desorbed in the desorber 3 and a generator 6 of intermediary pressure p_ιv^ externally heated by source

2, a high pressure resorber 7, p/_j, Pf₁ >_Jpj_nt > pi coupled with the generator 6 on vapor side 8 generated by the generator 6 via a compressor 9 for increasing the vapor 8 pressure from /?_mt till Pj₁, an absorbent of the one mean concentration 10 coming of a mixing process in the mixer 11 at p_m- ι of the absorbent 12 coming of the resorber 7 at p^ with the absorbent 13 coming of the generator 6, a heat exchanger 14 enabling absorbent 12 heat recovery by the absorbent 15 coming of the desorber 3, a heat exchanger 16 enabling absorbent 12 heat recovery by the absorbent 17 coming of the absorber 4, a supply with absorbents 10 of the one mean concentration in preestablished quantities 18 and 19 of the absorber 4 and desorber 3 respectively by means of the regulating and expansion valves

20 and 21 respectively, reducing the pressure from /?_mt to /y, a pump 22 of increasing the pressure of the poor absorbent IS from pi to p/j, a pump 23 of increasing the pressure of the rich absorbent 17 coming of the absorber 4 from p\ to /r_mt , and a valve 24 reducing the absorbent 12 pressure from Pf₁ to p_mt , and connections between devices, in such a way that, the absorbent 12 coming of the resorber 7 at Pi₁ is subcooled in a recovering way in the heat exchangers 14 and 16, it is expanded from Pf₁ to p\^ in the valve 24, it is mixed up in the mixer 11 at p\_nι with the absorbent 13 forming the absorbent 10 of the one mean concentration, the absorbent 10 is distributed to the absorber 4 and desorber 3 in the way already shown, the vapor of refrigerent 5 desorbed in the desorber 3 are absorbed in the absorber 4, the absorbent 15 is pumped from the pressure

Pl to Ph by means of the pump 22, it is preheated in the heat exchanger 14 and it enters the resorber 7 at Pf₁, the absorbent 17 coming of the absorber 4 is pumped from pi to Pj_nI by means of the pump 23, it is preheated in a recovering way in the heat exchanger 16, it enters the generator 6 at p_m- χ , it is heated up to a low temperature level by the source 2 generating refrigerent vapor 8 which finally is compressed by the compressor 9, it is resorbed in the resorber 7 at Pf₁ by the absorbent 15 producing useful heat extracted by the external source 25 , for closing cycle.

10. Installation applying the procedure according to claims 1, 2, 3, 4, 5, 6, 7, 8 and 9 and Fig.

10, connected to an external sink source 1 of cooling for an absorption process and to an external heat source 2 of low thermal potential of heating for generation and desorption processes, characterized in that, it is including a low pressure absorber 3 at pi externally cooled by the source 1, a high pressure resorber 4 at Pf₁, a truncation column including besides the absorber 3, a desorber 5 of low pressure p\ externally heated by the source 2 and connected with the absorber 3 on refrigerent vapor side 6 desorbed in the desorber 5, a p\ pressure stage having a generator 7 externally heated by the siurce 2 and a resorber 8 externally cooled by source 1 coupled with the generator 7 on refrigerent vapor side 9 generated by the generator 7, a stage at an intermediary pressure with a generator 10 externally heated by source 2, Pf₁ > p_mi > p\ > pi connected with the resorber 4 at Pf₁ on vapor side 11 generated by the generator via a compressor 12 which increases vapor 11 pressure from p_mχ till Pf₁, a supply with the absorbent 13 coming of the generator 7 at p\ in pre-established quantities 14 and 15 of the absorber 3 and desorber 5 respectively by means of the regulating and throttling valves 16 and 17 respectively, a mixing process at

/?_mt in the mixer 18 of the absorbent 19 coming of the generator 10 with the absorbent 20 coming of the resorber 4 in order to generate the one mean concentration absorbent 21, a supply in pre-established quantities of the resorber 8 and of the generator 7 with the absorbents 22 and 23 respectively, obtained through a mixing process in the mixer 24 of the absorbent 21 with the absorbent 25 coming of the absorber 3 by means of the regulating and throttling valves 26 and 27, a heat exchanger 28 for subcooling the absorbent 13 by heating in a recovering way the absorbent 25, a heat exchanger 29 for subcooling the absorbent 20 by heating in a recovering way the poor absorbent 30 coming of the desorber 5, a heat exchanger 31 of further subcooling the absorbent 20 by heating in a recovering way the rich absorbent 32 coming of the resorber 8, a valve 33 for reducing absorbent 20 pressure from Pf₁ till p_mι , a valve 34 for reducing absorbent 21 pressure from jPi_βt till pi, a pump 35 of increasing absorbent 25 pressure from pi till p\, a pump 36 of increasing absorbent 32 pressure from p\ till ρ_mι , a pump 37 of increasing absorbent 30 pressure from p\ till Pf₁, and connections between devices, in such a way that, the absorbent 20 coming of resorber 4 at Pf₁ is subcooled in a recovering way successively in the heat exchangers 29 and 31, it is expanded from Pf₁ to p_mi in the valve 33, it is mixing in the mixer 18 at p_m- ι with the absorbent 19 in order to generate the one mean concentration absorbent 21, the absorbent 21 is expanded in the valve 34 till a pressure sensibly equal to p\, at this pressure it is mixing in the mixer 24 with the absorbent 25 pumped from pi to p\ with pump 35 and pre-heated in the heat exchanger

28, the resulted mixture is supplying the resorber 8 and the generator 7 in the way already shown, the absorbent 23 is supplying the generator 7, the vapor 9 generated in the generator 7 are resorbed in the resorber 8, the absorbent 13 is subcooled in the heat exchanger 28, it is expanded from p\ till pj supplying the absorber 3 and the desorber 5 in the way already shown, the vapor 6 is absorbed in the absorber 3, the absorbent 30 is pumped from pi till Pf₁, it is subcooled in the heat exchanger 29 supplying the resorber 4 at Pf₁, the absorbent 32 is pumped from p\ to p\^ , it is preheated in the heat exchanger 31, it is supplying the generator 10, and the vapor 11 is compressed by means of the compressor 12 from /?_mt till Pf₁ and is resorbed in the resorber 4 in order to produce heat transferred as useful heat to the external source 38 and to close cycle.

11. Procedure of producing combined heating, cooling and electrical power with high global efficiency C0P#^g_eMg_røftow > 0.9 , feasible in geographical zones with high energy demand, such as towns, and needing a reduced primary energy consumption because for heating and cooling it is taking advantage of the low temperature potential energy, of satisfactory availability and quasi-constant parameters the whole year, resulted from the electrical power producing process, characterized in that, there are used coabsorbent truncated heat pumping cycles, according to claims 1, 2, 3, 4, 5, 6, 7, 8, 9 and 10, which have a much higher thermal efficiency than those known so far, e.g. COP = 10- 200, depending on sources temperature and availability and applications working parameters, in coupling with a known thermodynamic Rankine power cycle, including an endothermic high temperature and pressure vapor generation process, e.g. Tf₁ = 55O⁰C and pf_j -HObar , low temperature and pressure vapor condensing exothermic processes, e.g.

7/ =(28,6-39,5)°C and p[ -(θ,04-0,07)bar, a low temperature cogeneration 7/ = (39,5-8θ)°C and /?/ =(θ,07-0,48)δαr, a vapor expansion process from the high pressure to the low one producing useful mechanical work, a process of transforming the mechanical work in useful electrical energy, and processes of increasing the working fluid pressure and transport and of heat recovery, thermally connected with two fluids of low temperature potential, e.g. (5-75)°C, but with sensible different temperatures, AT = (IO-SOfC, identified as heat pumping coabsorbent truncated cycles sink and heat sources, the hottest one at least or both coming of the thermal coupling with the power cycle, the first fluid of higher temperature, e.g. 40⁰C during the cold season and (50-8O)⁰C during the warm season, being a fraction of that which extracted the heat from the exothermic condensing or low cogeneration processes and the second one, of lower temperature, e.g. (5-35)°C, being a fraction of that which was cooled by the power cycle sink source, or it has a different origin, cooled in a different way, respectively, in such a way that a fraction of the heat rejected by the power cycle during the condensing or cogeneration processes mentioned above is recovered by the coabsorbent heat pumping cycle and transformed in amount of (23-48)% and (24-33)% in useful cooling, e.g. (213,15- 273,15)K and useful heat, e.g. (353_S15- 453,15)K , respectively, supplementary supplying the consumer of heat, cooling and electrical power, besides the electrical and thermal power supply produced by⁵ the Rankine power cycle partially working in counterpressure mode.

12. Installation applying the procedure according to claim 11 and Fig. 11, characterized in that, it is receiving on one side in the refiigerent vapor generation and desorption devices compartment 1 of the heat pumping installation 2, a fraction of the heat released by the condenser of the thermal power station supplyed by a non-renewable or renewable heat source, at a temperature sensibly equal to the condensing temperature by means of an intermediary heat transfer fluid with state 3, which, next, is sent with state 4 to the power station cooling tower in order to be cooled, and on the other side, it is yielding the heat produced in the refrigerent vapor resorption and absorption devices compartment 5 of the heat pumping installation 2 to an intermediary heat transfer fluid having state 6, at a temperature sensibly equal to the power station sink source temperature, or sensibly lower than that of condensation mentioned above characterizing another source colder than that, which subsequently is sent with state 7 to the power station cooling tower, or to another similar cooling source or colder in order to be cooled, in such a way that it enables the operation of the refrigerent vapor resorption compartment 8 and/or that of desorption 9 of the heat pumping installation 2, in order to produce useful effects of heating and/or cooling respectively, available to the heat and/or cooling consumer by means of the intermediary heat transfer fluids 10 and 11 and / or 12 and 13, respectively.

13. Installation applying the procedure according to claims 11 and 12 and Fig. 12, characterized in that, in order to avoid the contamination of the thermal power station referred to in the first variant of applying procedure by fluids of a different nature, it is transferring the intermediary heat transfer fluid heat of state 3 to the refiigerent vapor generation and desorption devices compartment 1 and it is yielding the heat produced in the refiigerent vapor resorption and absorption devices compartment 5 to the intermediary heat transfer fluid of state 6 by means of the heat exchangers 14 and 15 respectively and of the closed loops 16 and 17 respectively, where an intermediary heat transfer fluid is circulated by means of the pumps 18 and 19 respectively.

14. Installation applying the procedure according to claims 11, 12 and 13 and Fig. 13, connected to a sink source with a cooling tower 1 and an intermediary heat transfer fluid 2 and a heat source 3 of renewable or non-renewable origin, characterized in that, it is including a thermal power station for electrical power producing, having a steam boiler 4, extermally heated with the source 3 at a high pressure and temperature, e.g. T_jn = 55O⁰C si

Pin ~ i70bar , an electrical condensation steam turbine-generator group 5 provided with steam bleedings, a condenser 6 externally, cooled with the source 1_. at low pressure and temperature of condensation, e.g. Tj = (28,6~39,5)°C si />y =(θ,O4-O,O7)før, communicating with the turbine through the connection 7, a turbine steam bleeding 8 with temperatures and pressures Tj = (39,5-8θ)°C and pj = (θ,07-0,48)&αr respectively for a power station power and low temperature heat cogeneration, a turbine steam bleeding 9 with temperatures and pressures Tj = (l2O-14θ)°C and pj « (2-4)bar respectively for a power station power and medium temperature heat cogeneration, a pump 10 for increasing the condensate H pressure from the condenser 6 pressure till that of the steam boiler 4, a coabsorbent heat pumping installation provided with truncation column 12 including a compartment 13 for generation processes, heated up in function of the sink source 1 temperature either from the condenser 6 or from the steam bleeding 8 via a heat exchanger 14 in order to provide perpetually a temperature difference of at least ATIU - TM -TU ≥ iS-lOΨC between truncation column extreme working temperatures, a compartment 15 for resorption and absorption processes cooled by the source 1, a compartment 16 for a resorption process producing the useful heating effect e.g. (353,15- 453,15)K and a compartment 17 for a desorption process producing the useful cooling effect e.g. (213,15- 273,15)j£, a heat exchanger 18 named also of theπnofication or of district heating which first compartment of is thermally coupled with the steam bleeding 9, a heat exchanger 19 named also district heating point exchanger which first compartment of is thermally coupled either with the second compartment of the heat exchanger 18 or with the compartment 16 of the installation 12, or simultaneousy with both, a heat exchanger 20 named also district cooling point exchanger which first compartment of is thermally coupled with the compartment 17, a connection 21 supplying with steam the turbine S from the steam boiler 4, a low temperature heating loop made up of the steam bleeding 8, a regulating-closing valve 22, heat exchanger 14 first compartment via a connection 23, a pressure reducing valve 24 and a connection 25 with condensate 11 evacuation and pump 10 suction line, a medium temperature heating loop made up of the steam bleeding 9, a regulating-closing valve 26, first compartment of the heat exchanger 18, a pressure reducing valve 27 and a connection 28 to the connection 25, a loop with an intermediary fluid transferring the heat from the heat exchanger 18 second compartment to the heat exchanger 19 first compartment made up by the tour 29 via a regulating-closing valve 30 and the return 31 via the circulation pump 32, a loop with intermediary fluid transferring the heat from the compartment 16 of the installation 12 to the heat exchanger 19 first compartment made up by the tour 29 via a regulating-closing valve 33 and the return 34 via the pump 32, a ditrict herating loop 35 through the heat exchanger 19 second compartment, a loop with intermediary fluid transferring the coolness from compartment 17 of the installation 12 to the heat exchanger 20 first compartment made up by the tour 36 via a regulating-closing valve 37 and the return 38 via the circulation pump 39, a district cooling loop 40 by the heat exchanger 20 second compartment, a main loop for cooling the power station condenser second compartment by mens of the intermediary cooling fluid 2 having a tour 41 via a circulation pump 42 and a return 1 via a regulating valve 43 and a connection 44, a complementary loop for cooling the power station condenser second compartment by mens of the intermediary cooling fluid 2 having the tour 41 via the circulation pump 42 and the return 1 via a regulating valve 45, a serial connection of the heat exchanger 14 second compartment with the compartment 13 and with the tour 1 by means of connections 46, 47 and 48 and a compartment 15 cooling loop by means of a tour 49 via a pump of circulation 50 and the return 48 and the tour 1, in such a way that, the thermal power station coupled with the heat pumpimg installation is producing on one side during year cold period first electrical power by means of the working agent generated with the heat source 3 in the steam boiler 4, expanded in the turbine-generator group 5 via connection 21 condensed in the condenser 6 by source 1 in the way already shown above, second thermal energy for district heating and domestic water preparing using steam bleeding 9 and the medium temperature heating loop described above and third thermal energy used similarly and cooling supplied to the district by means of installation 12 through heat exchangers 19 and 20 and district heating and cooling loops respectively described above and supplied by the heat source from the condenser 6 via the valve 45, connection 46, heat exchanger 14 first side without heat supply in its second compartment from the bleeding 8, connection 47, compartment 13, connection 48, cooling tower 1, pump 42, connection 41, and the other side during year warm period first also electrical power in the way described above, second optionally thermal energy for preparing district domestic warm water using the bleeding 9 and the medium temperature loop described above and third thermal energy used similarly and cooling supplied to the district by means of the installation 12 through heat exchangers 19 and 20 and the district heating and cooling loops respectively mentioned above, cooled also by the cooling loop described above and supplied by the heat source from the condenser 6 via the valve 45, connection 46, heat exchanger 14 first compartment with heat supply from the bleeding 8 through the heating low temperature heating loop mentioned above, connection 47, compartment 13, connection 48, cooling tower 1, pump 42 and connection 41.

15. Procedure of trigeneration of hign global efficiency and exergy effectiveness yCOPfyigenerare « 1.0-1.5 , Fig. 14, destined to combined heat, cooling and electrical power producing with the help of classic or renewable energy sources in towns but especially rural zones and consisting in achieving a coabsorbent truncated cooling cycle with non-isobar generation and resorption processes, characterized in that, it is connected to heat sources capable of heating to a maximum temperature Ttø for the F=I, ...,n-l

generation processes, e.g. (40-70) ⁰C and of cooling to a minimum temperature Tj^ for

the i-1, ...,n-l resorption processes and an absorption process, e.g. (10-40) ⁰C, in such a way that ΔTtø = Tfrf -^M ^≥ (8-lθ)PC , and to a high temperature source capable

to achieve maximum generation temperatures TQQ » T^ , e.g.

TQQ = (l80-25θ)°C, including a low pressure desorption process p\ where first useful cooling effect occurs, e.g. Tj)j = (213,15 - 273,15)K , a high pressure generation process Pf₁ reaching the maximum temperature TQQ , an intermediary pressure resorption process Pint » Pl < Pint < Ph resorbing the vapor generated by the high pressure generation process with concentration threshold condition fulfilment yRO,m ^{< Y}G,m,h ^d when heat is produced by a temperature sensibly equal to that of resorption process end, TM int ^> ^M _> ^e §- (50-120) ⁰C, as second useful effect, a mechanical work producing process achieved through generated vapor expansion from the high pressure to the intermediary one, a process of transforming the mechanical work into electrical power, as third useful process, a truncation column used as nontruncated cycle truncation process mostly when cooling process temperature decrease is necessary and low grade sources are available, having pressures between the low pressure and the intermediary one and it is made up by a low pressure absorption process coupled on vapor side with the low pressure desorption process, a low pressure mixing process of the absorbents coming of the low pressure absorption and desorption processes in order to generate the one mean concentration absorbent, a series of i stages, i=l, ..., n-1, n e N , of isobar opposite intermediary generation and resorption processes having increasing pressures between the low pressure and the intermediary one, p\x&>pi >Pi-\ >Pl, i-1, •••, n~l, « e JV, and temperatures between TM and Ttø , being coupled on vapor side having essentially

increasing mean concentrations YG,m,i ^{≤ γ}G,m,i+ϊ ^{≤ Y}G,m,n~\ _> fulfiling the concentration threshold condition yjioj ≤YG,m,i _> ⁱ⁼¹» •••» ^n-1» ⁸^ being supplied in pre-established proportions by uniform absorbents coming, for the first stage of the mixture of the one mean concentration absorbent with that coming of the second generation stage, for each of the following next i stages of the mixture of the absorbent coming of the first inferior resorption stage i-1 with that coming of the first superior generation stage i+1, i=2, ..., n-2, and for the n-1 stage of the mixture of the absorbent coming of the high pressure generation process with the absorbent coming of the last but one resorption process n-2, and processes between successive stages of the truncation column, of pumping the one mean concentration absorbent from p\ to p\, and of the absorbent coming of the resorption processes from /;/__j to pf , i=2, ..., n-1, of reducing the pressure of the absorbent coming of the generation processes from pi ^'to pi and from p\ to pi~\, i-2, ..., n-1, and processes of heat recovery between opposite processes of absorption- generation and of resorption-generation, of gax and absorbent to absorbent type, in such a way that, the rich absorbent leaves the resorption process at p_mι , it is subcooled in a recovering way in the desorption process at p\ from TRQ _mt>?M ^tu^ ^a temperature

approaching Tβj , it is expanded till p\, it is suffering the desorption process where is taking over the heat from the medium which must be cooled as useful effect and that of subcooling and it reaches the state parameters Tβo ≤Ttø and JDO ≥ JKM _> ^tfte absorbent coming of truncation column first stage generation process is subcooled in a recovering way, it is expanded till the low pressure, it is suffering the absorption process of the desorbed refrigerent vapor, it is mixing at the low pressure with the absorbent coming of the desorption process and it is generating the one mean concentration absorbent which is covering the truncation column till the last stage n-1 in the way described above, the absorbent coming of resorption process of the n-1 stage is pumped from p_n-\ to Pf₁, it is supplying in pre-established quantities the resorption process at /?_mt , on one side, and the generation process at Pf₁, not before to be preheated in a recovering way by the absorbent coming of the generation process at Pf₁ by the poor absorbent coming of the generation processon Pf₁, on the other side, the vapor generated at Pf₁ is expanded with producing of useful mechanical work and is resorbed at p_mι producing useful heat, and the absorbent coming of the Pf₁ generation process is subcooled in a recovering way until it reaches saturation parameters at p_n-\ , it is expanded till ρ_n-\ and is participating to the n-1 stage supply, in the way described above, closing cycle.

16. Installation applying the procedure according to claim 15, Fig. 15, for producing combined heat cooling and electrical power, connected to an external sink source 1 of cooling for an absorption process and to external heat source 2 for a generation process, characterized in that, it is including a low pressure desorber 3 at pi , a low pressure absorber 4 at pj , externally cooled by source 1 and connected with the desorber 3 on refrigerent vapor side 5 desorbed by the desorber 3, a generator 6 of high pressure Pf₁ externally heated by source

2, a resorber 7 of intermediary pressure p_m^ , Pf₁ > p_m- ι > p\ , connected with the generator 6 on refrigerent vapor side 8 generated by the generator 6 via a turbogenerator group 9, a one mean concentration absorbent 10 obtained in a mixer 11 by mixing up at pi of the absorbents 12 and 13 coming of the desorber 3 and absorber 4 respectively, a supply with the absorbent of the one mean concentration of the resorber 7 at p\^ by the absorbent 14 via the regulating valve 15 and of the generator 6 at Pf₁ with the absorbent 16 via the regulating valve 17 in pre-established quantities, a heat exchanger 18 recovering the heat of the poor absorbent 19 coming of the generator 6 at Pf₁ by the one mean concentration absorbent, a valve 20 for reducing the pressure of the absorbent 19 from Pf₁ to pi , a valve 21 for reducing the pressure of the rich absorbent 22 coming of the resorber 7 from jPjut to pi and a pump 23 for pumping the one mean concentration absorbent 10 from pi to Pf₁, in such a way that , the absorbent 22 is leaving the resorber 7, is subcooled in a recovering way in the desorber 3 through the connection 24, it is expanded with the valve 21 from /%t to pi , it is suffering the desorption process in the desorber 3 where it is taking over the heat of an external fluid 25 which must be cooled as first useful effect and that of the absorbent 22 subcooling, the absorbent 19 is subcooled in a recovering way in the heat exchanger 18, is expanded till pi , it enters the absorber 4 where it is suffering the absorption process of the desorbed refrigerent vapor 5 producing supplementary useful thermal effect besides that produced in the resorber 7 when absorption interval and sink source temperature are enough high, it is mixing at the low pressure as absorbent 13 with the absorbent 12 forming the one mean concentration absorbent 10 which is pumped from pi to Pf₁, is preheatred in a recovering way, is distributed to the generator 6 and resorber

7 as already shown and the generated refrigerent vapor 8 is expanded from Pf₁ to /?j_nt producing mechanical work and electrical power by means of the turbogenerator 9 as second useful effect and heat as third useful effect heating up the external fluid 26 when resorbed in the resorber 7, closing cycle.

17. Installation applying the procedure according to claim 15, Fig. 16, for producing combined heat, cooling and electrical power, connected to an external sink source 1 of cooling for absorption and resorption processes, to an external heat source 2 of low thermal potential for a generation process and to an external heat source 3 of high thermal potential for a second generation process, characterized in that, it is including a low pressure desorber 4 at Pi, a low pressure absorber 5 at p\ , externally cooled by source 1 and connected with the desorber 4 on refrigerent vapor side 6 desorbed by the desorber 4, a generator 7 of high pressure Pf₁ externally heated by source 3, a resorber 8 of intermediary pressure /?_mt ,

Ph > Pint > Pl connected with the generator 7 on refπgerent vapor 9 generated by the generator 7 via a turbogenerator group 10, an absorbent 11 of the one mean concentration generated in a mixer 12 by mixing up at pf of absorbents 13 and 14 coming of the desorber 4 and absorber 5 respectively, a truncation column with a stage at a pressure p\, Pf₁ > Pim≥Pi > pi with a generator 15 externally heated by the low grade source 2 and a resorber 16 externally cooled coupled with the generator 15 on refπgerent vapor 17 generated by the generator 15, a supply in pre-established quantities of the resorber 16 at Pl with the absorbent 18 via the regulating valve 19 and of the generator 15 at p\ with the absorbent 20 via the regulating valve 21 coming of the mixing up in the mixer 22 at a pressure sensibly equal to p\ of the absorbent of the one mean concentration 11 with the absorbent 23 coming of the generator 7 at pfr, on one side, and of resorber 8 at pfa& with the absorbent 24 via the regulating valve 25 and of the generator 7 at Pf₁ with the absorbent 26 via the regulating valve 27, on the other side, a heat exchanger 28 recovering the absorbent 23 heat by the absorbent 29 coming of the resorber 16, a heat exchanger 30 recovering the absorbent 31 heat coming of the generator 15 at p\ by the one mean concentration absorbent 11, a valve 32 reducing the pressure of absorbent 23 from Pf₁ to Pl , a valve 33 reducing the pressure of absorbent 31 from pi to pi , a valve 34 reducing the pressure of absorbent 35 from pfa to pj, & pump 36 for pumping the one mean concentration absorbent 11 from jo/ to pi, a pump 37 for pumping the absorbent 29 from pi to ph, in such a way that the absorbent 35 leaves the resorber 8, it is subcooled in a recovering way in the desorber 4 through connection 38, it is expanded by means of valve 34 from p\_nι to pi , it is suffering the desorptϊon process in the desorber 4 where is talcing over the heat of an external fluid 39 to be cooled as first useful effect and that of absorbent 35 subcooling, the absorbent 23 is subcooled in a recovering way in the heat exchanger 28, is expanded till pressure p\ in the expansion valve 32, the absorbent 31 is subcooled in a recovering way in the heat exchanger 30, is expanded in the valve 33 till pj , it is entering the absorber 5 where is absorbing vapor 6, the resulting absorbent 14 is mixing up in the mixer 12 with the absorbent 13, the resulting one mean concentration absorbent 11 is pumped with pump 36, it is mixing up in the mixer 22 with the subcooled absorbent 23, the resulting absorbent supplies the generator 15 and the resorber 16 in the way shown before, the vapor 17 generated in the generator 15 is resorbed in the resorber 16, the resulting absorbent 29 is pumped by the pump 37, it is preheated in a recovering way in the heat exchanger 28, it is distributed to the resorber 8 and generator 7 in the way shown above, the vapor 9 generated in the generator 7 is expanded in the turbogenerator 10 producing electrical energy, as second useful effect, is resorbed in the resorber 8 producing heat in order to heat up the external fluid 40, as third useful effect, closing cycle.