DE102021002893B3 - Absorption power cooling cycle of a sorption system based on ammonia and water for utilizing thermal energy to generate electricity and cooling - Google Patents

Abstract

The invention relates to an absorption power cooling cycle of a sorption system for a two-component mixture of ammonia and water for utilizing a heat input from an external thermal energy source to generate electricity and cooling. Based on the method and system described in DE 10 2011 106 423 B4, the compression work of a gas turbine is not used as an alternative to pre-cooling before compression or to generate electricity, but is used in combination to increase performance. The almost linear temperature gradient of the waste heat from a gas turbine is used in circuits with a temperature gradient and the heat is used in two parts: namely in the upper temperature range for power generation and in the lower temperature range for pre-cooling. An absorption cycle is arranged to generate electricity, and a compression and resorption cycle and a turbine system comprising a gas turbine (6a, 6d) are arranged to generate refrigeration. The poor solution of the absorption (16a, 16b) and the compression circuit (36) are fed to a low-pressure absorber (1), their rich solutions (28) are combined and discharged from the low-pressure absorber (2). The low-pressure vapor of the resorption circuit (39) generated in the resorption circuit is only fed to the low-pressure absorber (2). The heat input to the absorption power-refrigeration cycle takes place in a waste heat boiler (5) from the exhaust gas (9) of a gas turbine (6a, 6d). The efficiency of the gas turbine with a regenerative heat exchanger (6c) is increased by the cooling capacity generated in the degasser (43), since the supply air (9a) of the gas turbine is cooled in the degasser (43).

Description

The invention relates to an absorption power cooling cycle of a sorption system for a two-component mixture of ammonia and water for utilizing a heat input from an external thermal energy source to generate electricity and cooling.

The main elements for generating electricity and cooling in the absorption power-cooling cycle are a compression cycle and a turbine system that includes a gas turbine. The efficiency of gas turbines can be increased if gas turbine pre-cooling is carried out. An interconnection of the compression and resorption circuits with a deaerator providing cooling (cold production) is ideally suited for the pre-cooling process.

Gas turbines are operated with closed and open circuit. In the last few decades, almost only open gas turbines have been built because their efficiency could be significantly increased by means of increased combustion chamber temperatures (up to 1400 °C) and in combination with the downstream steam turbine process an overall efficiency of approx. 61% is achieved. For a climate-neutral energy supply, however, there is the disadvantage that the fuels first have to be produced with conversion stages (and the associated efficiency losses) on a regenerative basis.

The performance of gas turbines depends to a large extent on the inlet temperature of the circulating medium used - air in most applications - in the power turbine and on the inlet temperature in the compressor. Its inlet temperature has a significant effect on the efficiency of the system if the gas turbine is also equipped with a regenerative counterflow heat exchanger.

A significant part of the relaxation work of a gas turbine is required for compression work. It is known to obtain an electricity credit by supplying cold to a gas turbine. There are three fundamentally different process steps to reduce the compression work: intermediate cooling of the compression, pre-cooling before the compression and use of the waste heat from the compression through coupled Carnot cycle processes. Ideally, these process steps are equivalent (U. Reiter: Use of refrigeration processes for better energy utilization of compressor and gas turbine systems. Diss. Uni. Hanover; 1981). However, only one of the three process steps was used in each case - mostly intermediate cooling. In the case of open gas turbines, the drop in inlet temperature into the compressor is limited to approx. 6 ℃.

With the combination of closed gas turbines and steam circuits, higher efficiencies can be achieved if suitable process designs are observed. (H. Bormann: Investigations for combined power plant processes with closed gas turbine and steam turbine Diss. Hanover; 1980). Depending on the system design, there is a greater bandwidth for the overall efficiency. The share of the gas process in the total useful output must be 20 to 30%. Certain circuit variants increase efficiency in the individual processes, but have the opposite effect in the combined process. This includes intercooling during compression. In order to increase efficiency, it is necessary to supply additional heat to the steam cycle in addition to the waste heat from the gas turbine. If the water vapor circuit is additionally designed with intermediate heating, there is an increase of approx. 2 efficiency points. However, this requires very large power plants.

Such a concept is described for a solar thermal tower system (M. Za, M. Mehos, G. Glatzmaier, B. Sakadjian: Development of a concentrating solar power system using fluidized bed technology for thermal energy conversion and solid particles for thermal energy storage; Energy Procedia 69 (2015) pp.1349-1359). On the basis of coal-fired systems, heat is transferred to a gas turbine and steam circuit (with reheating) in an overpressure boiler, and also to a waste heat boiler. The compression in the gas turbine cycle is carried out with intercooling. Heat carriers are small, inexpensive particles that are temporarily stored in a hot and a cold storage tank. It is stated that such a concept is suitable for other circuit configurations and that heat losses in the storage tank are low. The system should achieve a cycle efficiency of 44 to 50%.

Cold can be generated by both compression and absorption systems, which can be powered by a low-temperature source. Gas turbines provide such as waste heat so that a compression refrigeration system is not practical.

Gas turbines with a regenerative counterflow heat exchanger in particular produce more waste heat than is required for the operation of an absorption chiller for pre-cooling. In US20020069665A1 and in DE 10 2011 106 423 B4 refrigeration and power generation with the same two-component mixture of ammonia and water is presented, whereby this is only used for gas turbine pre-cooling in the first case. The disadvantage is that for power generation, the pressure gradient is coupled to that of the sorption refrigeration system and is therefore limited. In DE 10 2011 106 423 B4 Alternatively, a coupling with a resorption chiller is shown. In contrast to the absorption refrigeration system, this has a second so-called resorption solution cycle between an absorber and a degasser in the refrigeration part. This is where the cold is generated. In both apparatuses, heat input or cold generation takes place with a sliding temperature change, which can be used thermodynamically advantageously for the sliding temperature change during compression and waste heat utilization of a gas turbine. The generation of cold is closely linked to the generation of electricity arranged there in such a way that the temperature rise and thus the lowest degassing temperature is limited.

A key feature of the system design in DE 10 2011 106 423 B4 is to generate ammonia vapor with a defined water content (optimally 6%) and to superheat it and expand it into the wet-steam area. The water content is predominantly condensed here, with its heat of condensation being almost twice as high as that of ammonia. In order to generate electricity with the same or approximately the same pressure gradient, steam is expelled first with a single and then twice heat supply at different temperature ranges and three expellers are arranged for this purpose. Two pressure levels are combined in the solution circuit for power generation and one pressure level in the solution circuit for driving the refrigeration (by means of deaerators).

In refrigeration, the temperature rise increases as the difference between the ammonia content of the rich solution in the deaerator and the rich solution in the absorber, to which the deaeration steam is fed, increases. This temperature range is in DE 10 2011 106 423 B4 limited insofar as only two absorbers can be arranged for combined power and cooling generation, but not - as for power generation - three absorbers connected in series can be arranged. The refrigeration circuit consists of two partial circuits with two absorbers that work at different temperature levels. The degassing steam is fed to the absorber with the higher water content. There is no degree of freedom for supplying expanded steam.

With a large degassing width of a solution circuit, there is the possibility of heat recovery in the first absorption section of a single absorber. In US20020069665A1 a corresponding heat transfer to a desorber column is arranged. In DE 10 2005 005 409 B4 a lower absorption temperature is established by placing a second absorber operating at lower pressure. It can be supplied with steam that has been expanded with a larger pressure drop compared to a single absorber. During expulsion, in DE 10 2005 005 409 B4 the poor solution is recycled through the high pressure generator.

In order to keep the pressure loss in the exhaust gas of a gas turbine during heat dissipation low, in US20020069665A1 arranged to introduce a two-component mixture of ammonia and water into a waste heat boiler and discharge it as a two-phase mixture after heat input. The phases are then separated in a desorber; Expelled steam, producing almost pure ammonia vapor. This is used to generate electricity and cooling. The disadvantage is that in this process, the amounts of material and heat to be exchanged in the desorber are very high, that the temperature level for refrigeration is set at over 100 ℃ and that electricity and refrigeration are coupled to one another via a common absorber. In proceedings after DE 10 2011 106 423 B4 high-pressure steam is not rectified.

In high-temperature electrolysis, heat is supplied as superheated steam. Here, the heat for the water vaporization replaces an equal amount of electricity. Generating this water vapor with low overpressure and waste heat temperatures of 150 to 200 ℃ has been successfully tested.

task

Starting from in DE 10 2011 106 423 B4 The problem to be solved is to use the compression work of a gas turbine not as an alternative to pre-cooling before compression or to generate electricity, but rather in combination to increase performance.

The solution to the problem can be found in a main claim and in other associated subclaims. Further preferred developments of the invention are formulated in the dependent claims.

• • das nahezu lineare Temperaturgefälle der Abwärme einer Gasturbine in Kreisläufen mit Temperaturgefälle zu nutzen,
• • den Wärmeeintrag zweigeteilt zu nutzen: im oberen Temperaturbereich zur Stromerzeugung, im unteren Temperaturbereich grundsätzlich zur Vorkühlung.

The solution to the task is based on two basic ideas:

• • to use the almost linear temperature gradient of the waste heat from a gas turbine in circuits with a temperature gradient,
• • to use the heat input in two ways: in the upper temperature range to generate electricity, in the lower temperature range basically for pre-cooling.

The basis of the implementation is that circuits with the two-component mixture of ammonia and water are characterized by a sliding - albeit non-linear - temperature gradient during heat input and internal heat transfer.

In absorption systems with the two-component mixture of ammonia and water, cold can be generated at the same temperature level by evaporating almost pure ammonia solution. This use case runs frequently. The required expulsion pressure of such systems requires temperatures of over 100 ℃ for expulsion, which means that the goal of using a heat source in stages would be missed. Such high temperatures are not required to generate the greatest temperature rise of a maximum of 30 Kelvin with a sliding temperature reduction using a deaerator, whereby a temperature rise of up to 20 Kelvin is sufficient in combination with power generation.

Arranging steam generators by means of a deaerator instead of an evaporator also has energy advantages. The enthalpy in evaporating ammonia/water solutions is usually around 300 kJ/kg lower than in almost pure ammonia solution, with the consequence that this alone requires around 25% less heat input. Their rectification loss is eliminated in the process described; the loss variable expansion throttling decreases as a result of the reduced pressure ratio between expulsion and refrigeration.

In DE 10 2011 106 423 B4 a three-stage use of heat is planned, whereby external heat input in the temperature range above approx. 100 ℃ is successively fed to two high-pressure expellers, below approx. 100 ℃ to a medium-pressure expeller in order to be able to expand the high-pressure steam generated in this way to low pressure. Since heat input in the temperature range below 100 ℃ is only used to generate cold in the process described, the second high-pressure expeller and its solution feed line are advantageously dispensed with. Although the power generation falls, the efficiency with reduced heat input increases. The use of refrigeration in a gas turbine circuit is advantageous in terms of construction costs insofar as additional power generation can be attributed to a smaller gas turbine compressor. The method can advantageously be used both for gas turbines with an open process and with a closed process. If the gas turbines are provided with a regenerative counterflow heat exchanger, the relative increase in output due to the coupling described is particularly large. With regard to closed gas turbines, the point of the greatest total power shifts to a higher pressure ratio of the gas turbine and drops only slightly when the pressure ratio is increased beyond this. The associated increase in performance is economically more attractive than in gas turbines without the coupling described.

A significant reduction in construction costs is compared to US20020069665A1 expected. The temperature ranges of the desorber and absorber overlap there, so that heat can be transferred from the absorber to the desorber. This construction effort is not necessary because the necessary high absorption temperature for this process step is not reached due to the arrangement of a second absorption pressure stage. Its arrangement is the core of the method described. In addition, the construction cost of a medium-pressure trickle ejector is lower than that of a desorber.

The efficiency advantage to be achieved with the method is discussed using the following example of a closed gas turbine. It is assumed that this is equipped with a regenerative counterflow heat exchanger as usual. The values refer to 1 kg of air in the gas turbine cycle. The pressure loss in the circuit is of greater importance for the efficiency. This is set at 9.5% and is therefore lower than was previously recorded as a result of heat generation using coal firing.

The calculation example is based on the fact that the degassing steam - as in 2 , 3 , 4 , 5 , 7 shown - is fed to the low absorber. The compression temperature is reduced from 25 to 6 ℃. This maximum temperature can be reached with open gas turbines. With a lowest absorption temperature of 20 ℃ set according to ISO conditions, a pinch point of 23 K results in the medium-pressure expeller. This is usually designed with 5 to 10 K, so that there is a reserve at tropical ambient temperatures before the efficiency of the gas turbine process drops. Such reserves do not exist in gas turbines without absorption, power and cooling coupling.

• * ohne Generatorverlust
• * ohne möglicherweise notwendige Wasserstoffverdichtung

In principle, the additional effort for the compression of the circuit medium - in the example air - would be reduced by additional electricity generation by means of compression heat. A pressure loss of 0.5% is assumed for the pre-cooling process step. An efficiency of 86% is assumed for the gas turbine compressor, 90% for the power turbine and 85% for the absorption power turbine. closed gas turbine pressure ratio compressor power turbine supply of heat electrical output* [kJ/kg] Efficiency** [%] GGT 3.5 25℃ ► 174.25°C 850°C ► 594.06°C 574.96°C ► 850℃ 315.6kJ/kg 143.24 45.4 GGT 3.66 25℃ ► 180.55℃ 850°C ► 585.68°C 585.68℃ ► 850℃ 325.4kJ/kg 146:17 44.9 Closed gas turbine + absorption power-refrigeration cycle pressure ratio compressor power turbine supply of heat electrical output* [kJ/kg] Efficiency** [%] GGT 3.5 6℃ ► 146.21℃ 850°C ► 594.96°C 574.96°C ► 850℃ 315.1kJ/kg 151.94 48.2 AK 165.56° ► approx. 105.5℃ 60.79kJ/kg 11.72 19.3 GGT+ acc 315.1kJ/kg 163.66 51.9 acc 165.56° ► 70.82°C 96.99kJ/kg 20.42 21:1 Closed gas turbine + absorption power refrigeration.+ WD electrolyser pressure ratio compressor power turbine supply of heat electrical output* [kJ/kg] Efficiency** [%] GGT 4.5 6℃ ► 180.37°C 850° ► 547.44°C 527.44℃ ► 850℃ 368.33kJ/kg 169.92 46.20 AK 165.56°C ► approx. 105.5℃ 60.79kJ/kg 11.72 19.3 WD electrolyser 200.75°C ► 165.56°C Thermal material 36.39 kJ/kg 36.39*0.7= 25.47 70.00 GGT+ AKKE 367.73kJ/kg 207:11 56.3 AKKE 200.73°C ► 70.82°C 137.78kJ/kg 66.66 48.4

• * without generator loss
• * without possibly necessary hydrogen compression

In the example, the internal heat transfer through the poor solution of the medium-pressure expeller is not calculated in the efficiency calculation for the absorption circuit (AK).

With the present invention, the efficiency of the absorption power cooling cycle (AKK) significantly exceeds that of alternative power generation processes - up to double the value. From the efficiency of approx. 52% of a closed gas turbine with AKK it can be concluded that the alternative of coupling a closed gas turbine with a downstream steam circuit will lead to lower efficiencies.

The electrical output of the closed gas turbine also increases with the pressure ratio, while the amount of waste heat and its maximum temperature increase at the same time. If the pressure ratio of the closed gas turbine is increased from 3.5 to 4.5, for example, the quantity and temperature of the waste heat increases. In 7 shows how this waste heat is used by generating steam in a steam electrolysis. This heat is converted into hydrogen with the same efficiency as the resulting reduced electrical power requirement. An efficiency of 0.7 is assumed for both. This increases the overall efficiency, and the partial efficiency of the absorption power-cooling cycle increases significantly.

The pressure ratio of a closed gas turbine could be meaningfully increased up to a pressure ratio of about 6.5. Compared to the pressure ratio of 4.5, the electrical output would be increased by 15.39 kJ/kg and the additional usable amount of waste heat by 71.06 kJ/kg. Alternatively, additional waste heat could also be achieved through a larger temperature difference in regenerative heat recovery in the gas turbine cycle, with the additional electrical power being correspondingly lower or omitted entirely.

Four different methods of heat input from an external heat source are described. They differ only in terms of transmission to power generation. In the following table, the results are related to the method according to claim 8 - keyword "water flow". The comparison shows that the processes differ minimally in terms of performance, but significantly in terms of the effort required for internal heat transfer - mainly in the high-pressure trickle expeller. Method in claim # with "keyword" Representation in figure(s) Max. temperature in external heat source Use of heat to generate electricity perfomance external heat input internal heat transfer 8 "heat carrier" 4, 6 180℃ 100% 103% 100.00% 7 "Two-phase with enriched solution" 2, 7 180℃ 107% 35% 99.2%

In the following the invention is explained with reference to drawings.

• 1: Strom- und Kälteerzeugung nach 8 aus Stand der Technik ( DE 10 2011 106 423 B4 );
• 2: Kälteerzeugung und -übertragung an das Kreislaufmedium einer Offenen Gasturbine und Wärmeübertragung an reiche und angereicherte Lösung des Absorptionskreislaufs;
• 3: Kälteerzeugung und -übertragung an das Niederdruckgas einer Geschlossenen Gasturbine und Wärmeübertragung an reiche Lösung des Absorptionskreislaufs;
• 4: Kälteerzeugung und -übertragung an das Kreislaufmedium einer Offenen Gasturbine und Wärmeübertragung an einen umlaufenden Wasserstrom;
• 5: Kälteerzeugung und -übertragung an das Niederdruckgas einer Geschlossenen Gasturbine und Wärmeübertragung an reiche und arme Lösung des Absorptionskreislaufs;
• 6: Kälteerzeugung und -übertragung an das Niederdruckgas einer Geschlossenen Gasturbine und Wärmeübertragung an einen umlaufenden Wasserstrom und an einen Wasserdampferhitzer;
• 7: Kälteerzeugung und -übertragung an das Niederdruckgas einer Geschlossenen Gasturbine und Wärmeübertragung an reiche und angereicherte Lösung des Absorptionskreislaufs und zur Hochtemperaturelektrolyse und
• 8: solarthermische Wärmenutzung und Betrieb in Grundlastfahrweise.

The figures show the process and system for generating electricity and cooling with the two-component mixture of ammonia and water in detail:

• 1 : Electricity and cooling generation after 8th from the state of the art ( DE 10 2011 106 423 B4 );
• 2 : Cold production and transfer to the cycle medium of an open gas turbine and heat transfer to rich and enriched solution of the absorption cycle;
• 3 : Cold production and transfer to the low pressure gas of a closed gas turbine and heat transfer to rich solution of the absorption cycle;
• 4 : Cold generation and transfer to the circulating medium of an open gas turbine and heat transfer to a circulating water stream;
• 5 : Cold production and transfer to the low pressure gas of a closed gas turbine and heat transfer to rich and lean solution of the absorption cycle;
• 6 : refrigeration generation and transfer to the low pressure gas of a closed gas turbine and heat transfer to a circulating water stream and to a steam heater;
• 7 : Cold production and transfer to the low pressure gas of a closed gas turbine and heat transfer to rich and enriched solution of the absorption cycle and for high temperature electrolysis and
• 8th : Solar thermal heat utilization and operation in base load mode.

In the figures, essential reference numbers for the absorption circuit are numbered 11 to 19; for the absorption circuit and compression circuit with the numbers 21 to 29, for the compression circuit with the numbers 31 to 39 and for the absorption circuit with the numbers 41 to 49.

the 1 from the prior art shows an additional and resorption cycle for refrigeration by means of a degasser. The reference numbers of the figure are retained as in the prior art.

In the 1 will the joint generation of electricity and cooling with the 8th the DE 10 2011 106 423 B4 shown in . The core of the design there is the generation and expansion of ammonia vapor with a water content of optimally 6%. This steam composition is defined in this figure by the equilibrium line of solution and steam when exiting the steam generator, using the fact that this differs from pressure and temperature on the one hand and from the steam exit at the hot or cold end of the expeller on the other. With this approach, a gradual utilization of a heat source with a temperature gradient with one heat input of the upper temperature range and two heat input in the medium temperature range at high pressure level and in the lower temperature range at the lower temperature range is arranged for power generation. In the 1 deviating from this, the heat input in the lower temperature range is used in the expeller <25> both to generate electricity and to generate cold. Due to this competitive situation, with increasing refrigeration only an increasing partial expansion <32> of the high-pressure steam is provided only to medium pressure instead of to low pressure. In the arrangement of two absorbers with two pressure levels, the temperature rise of the refrigeration is fixed and low. The poor solutions <8e, 22> formed during the high-pressure and medium-pressure expulsion are fed to a very low-pressure absorber <13a>. Enriched solution <20> is fed from this absorber to the medium-pressure expeller <25>, enriched solution <4a> to a high-pressure expeller <9> and enriched solution <4> to a low-pressure absorber <14b>. Rich solution <2> formed there is conducted to a high-pressure generator <3b>.

In the DE10 2011 106 423 B4 The cycle design shown is rearranged in the following in different process steps. In particular, a heat source with a sliding temperature gradient is only divided into two, arranged at the upper temperature level for generating electricity and at the lower temperature level for generating cold. The principle of a double temperature-graded heat input for power generation is no longer used.

the 2 shows cold generation and transfer to the cycle medium of an open gas turbine with regenerative counterflow heat exchanger and heat input from its exhaust gas to rich and enriched solution of an absorption cycle.

In the 2 an absorption cycle for power generation and a thermal compression cycle and a resorption cycle for refrigeration are shown. According to the invention, the absorption circuit and thermal compression circuit are linked in shared absorbers (1) and (2). In the following, the thermal compression cycle is simply referred to as the compression cycle.

Among other things, enriched solution (29) of the absorption circuit and the compression circuit is removed from a low-pressure absorber (1). This common flow is raised to low pressure by means of the first solution pump (21) and is introduced into the low pressure absorber (2) for absorption. In both absorbers (1, 2) absorption heat is transferred to a coolant.

Rich solutions (28) of the absorption cycle and the compression cycle are taken from the low-pressure absorber (2). This (28) is raised to medium pressure by means of the second solution pump (21a) and then passed through a first solution heat exchanger (22) for heat transfer. Thereafter, the rich solutions (28) of the absorption cycle and the compression cycle are separated into rich compression cycle solution (38) and rich absorption cycle solution (18). This stream (18) is raised to high pressure by means of the third solution pump (11a). The rich absorption cycle solution (18) is then routed to a waste heat boiler (5) through which the exhaust gas stream (9) from a gas turbine (6a) with a regenerative countercurrent heat exchanger (6c) flows and first heated to boiling temperature, then converted by partial evaporation into a two-phase mixture (18p) of the absorption cycle. This two-phase mixture (18p) is removed from the waste heat boiler (5) and introduced into a desorber (13). There, the two-phase mixture (18p) is separated into water-rich ammonia vapor and a poor solution.

The first partial flow (18a) of enriched absorption cycle solution is raised to high pressure by a fourth solution pump (11b) and heated in a second solution heat exchanger (12). It is then divided into a second (18b) and a third partial flow (18c) of enriched absorption cycle solution. The second partial stream (18b) of enriched absorption circuit solution is introduced into the top of the desorber (13). The third partial stream (18c) of enriched absorption circuit solution is introduced into the two-phase mixture (18p) that has already partially formed. With this measure, the ratio of expelled vapor to the remaining solution is kept so low that the increasing vapor expulsion remains in the range of bubble evaporation. This is characterized by very high heat transfer.

Two process steps take place simultaneously in the desorber (13). Firstly, the rising water-rich ammonia vapor is reduced to water-containing ammonia vapor by heat and mass exchange with the second partial stream (18b) trickling down, enriched absorption circuit solution and lean solution is formed. For the purpose of heat and mass exchange, several trough-like surfaces are arranged at different heights in a known manner. Secondly, water-rich ammonia vapor (19) is expelled from the second partial flow (18b) of enriched absorption circuit solution by means of indirectly heat-transferring poor absorption circuit solution (16) and additional poor solution is formed. The poor solutions formed during rectification and expulsion run into the sump of the desorber (13). There they are combined with the liquid phase of the phase separation to form the lean absorption cycle solution (16). This poor solution is passed through the trough-like surfaces from bottom to top. The water-rich ammonia vapor (19) exits the top of the desorber (13), the water content of which is determined at least approximately via an equilibrium line of the introduced second partial flow (18b) of enriched absorption cycle solution to a water content of 6%

After heat transfer, the lean absorption cycle solution (16) is removed from the top of the high-pressure trickle separator (13a) and a first partial stream of the lean absorption cycle solution (16a) is separated off. The remaining main stream (16b) of lean absorption circuit solution is passed through the second solution heat exchanger (12) for heat transfer, the amount of the main stream (16b) being dimensioned so large that the first partial stream of enriched absorption circuit solution (18a) is heated to boiling temperature by it. The main stream (16b) of poor absorption circuit solution is then lowered to the lowest pressure level by means of a first throttle (17) and introduced into the lowest pressure absorber (1) for absorption.

The water-rich ammonia vapor (19) is routed to the waste heat boiler (5). There, the heat is transferred in succession to a steam superheater (5a), to the two-phase mixture that forms (18p) and finally in parallel to the stream of rich absorption circuit solution (18) to be heated or to a water stream (7).

The superheated, water-rich ammonia vapor (19a) is routed to a turbine (14) and expanded in it down to the wet-steam range. The mechanical work is converted into electricity by a generator (15). Ultra-low-pressure steam (19b), expanded to ultra-low pressure, is removed from the turbine (14) and fed to the ultra-low-pressure absorber (1) for absorption. In the event that the refrigeration requirement drops disproportionately or completely during operation outside of the system design, only low-pressure steam (19c) expanded to low pressure is removed from the turbine (14) and fed to the low-pressure absorber (2) for absorption. A valve (19e) is arranged for this purpose.

The rich compression circuit solution (38) is fed to a medium-pressure operated medium-pressure trickle expeller (33) and introduced into its head for ejection. The expulsion process step takes place in the medium-pressure trickle expeller (33): By means of an indirect heat-transferring water flow (7), almost pure medium-pressure ammonia vapor (39) is expelled from the rich compression circuit solution (38) and lean compression circuit solution (36) is formed: lean collects at the bottom of the medium-pressure trickle expeller (33). Compression circuit solution (36) and is taken from the medium-pressure trickle expeller (33). The almost pure medium-pressure ammonia vapor (39) emerges from the head of the medium-pressure trickle expeller (33) and is conducted to a medium-pressure absorber (3) at the same pressure for absorption. Poor resorption circuit solution (46) is introduced into this medium-pressure absorber (3). After absorption is enough Resorption cycle solution (48) removed and lowered to low pressure by means of a fourth throttle (47) and then introduced into a degasser (43).

Air (9a) sucked in from the environment is passed through the degasser (43) for supercooling (cold generation) and fed to a compressor (6b) of an open gas turbine (6a). The cold transfer then takes place to the circulating medium of the open gas turbine (6a).

The low-pressure steam (49) of the resorption circuit is introduced into the low-pressure absorber (2) for absorption.

In the waste heat boiler (5), heat is introduced into a water flow (7) in parallel to heat up the rich absorption circuit solution (18). The water flow (7) is directed to the medium-pressure trickle expeller (33) for heat transfer. After the heat transfer has taken place, the water flow (7), supported by a circulation pump (11c), is routed back to the waste heat boiler (5).

The separated first partial flow of poor solution (16a) of the absorption circuit is lowered to medium pressure by means of a second throttle (17a) and combined with the poor compression cycle solution (36) for heat transfer through the first solution heat exchanger (22).

The mixed stream (26) of poor solutions from the absorption and compression circuit is lowered to the lowest pressure by means of a third throttle (27) and introduced into the lowest-pressure absorber (1) for absorption.

A resorption cycle is arranged for cooling, which is also operated with the two-component mixture of ammonia and water. The resorption circuit is driven by the medium-pressure steam, which is fed from the medium-pressure trickle ejector (33) to a medium-pressure absorber (3) of the resorption circuit and absorbed there. The heat of absorption is given off to the environment. The rich resorption cycle solution (48) drawn off from the medium-pressure absorber (3) of the resorption cycle is lowered to the pressure of a degasser (43) by means of a fourth throttle (47) and introduced into it. The expulsion process step is arranged in the degasser (43), with cold being generated.

The rich resorption cycle solution (48) is converted into a two-phase mixture of the resorption cycle by means of external heat input at a temperature level below the ambient temperature.

The two-phase mixture of the resorption circuit is then fed to a vapor separator (44) and separated into low-pressure vapor (49) from the resorption circuit and poor resorption circuit solution (46). The almost pure ammonia vapor is led to an absorber (1 or 2) under the same pressure for absorption. The poor resorption circuit solution (46) is raised to medium pressure by means of a fifth solution pump (41) and conducted to the medium-pressure absorber (3) for absorption.

In the descriptions of the following figures, only changes to the description are made 2 received.

the 3 shows refrigeration generation and transfer to the low pressure gas of a closed gas turbine and heat transfer to rich solution of the absorption cycle.

In contrast to the open gas turbine 2 the closed gas turbine is used with a regenerative heat exchanger. Optimum efficiencies are achieved with lower pressure ratios during compression and a lower maximum temperature in the waste heat boiler. The waste heat boiler with successively arranged heat transfer to the steam superheater (5b), formation of a two-phase mixture (18p) and in parallel connection to the solution heating (18d) and to the circulating water flow (7) is expanded with a gas turbine cooler (7b) and a deaerator (43) as the temperature falls . The heat from the gas turbine cooler is dissipated to the environment. The temperature of the cycle medium (9c) of the closed gas turbine (e.g. air) can be reduced to below 0 ℃. In contrast to the representation of 2 the feeding of enriched absorption circuit solution (18c) into the two-phase mixture (18p) that forms is eliminated. In contrast to the representation of 2 a second partial stream of rich absorption circuit solution (18f) is introduced into the head of the desorber (13). A first partial stream (18e) of rich absorption circuit solution is separated from the common stream of rich solution (28) of the first absorption circuit and the compression circuit and the main stream of rich solutions (28a) of the absorption circuit and the compression circuit is thus formed.

Analogous to 2 this partial flow (18e) of rich absorption circuit solution is raised to high pressure level by means of a fourth solution pump (11b) and heated in a second solution heat exchanger (12). It is then divided into a second (18f) and a third partial flow (18g) of rich absorption circuit solution. Analogous to the representation of 2 is in 3 described, in the desorber (13) to carry out rectification and expulsion by means of a trickling down second partial flow (18f) of rich absorption cycle solution.

Due to the lower water content and the lower boiling temperature, the solution is richer (18f) instead of enriched (18a) - as in 2 shown - the thermodynamic equilibrium for the exiting water-containing ammonia vapor (19d) results in a suboptimal water content. To correct this, a quantitatively small third partial flow of rich absorption circuit solution (18g) is added, so that the water weight fraction after the steam superheater (5a) in the superheated water-rich ammonia vapor (19a) is increased to the optimum fraction according to the invention - usually 6%.

Thereafter, the main stream (28a) is separated into a rich compression cycle liquor stream (38) and a main rich absorption cycle liquor stream (18d). Analogous to 2 the main stream (18d) is raised to high pressure by means of the third solution pump (11a). The main flow of rich absorption circuit solution (18d) is then passed to a waste heat boiler (5) through which the low-pressure gas (9c) of the closed gas turbine with regenerative countercurrent heat exchanger (6c) flows and in contrast to 2 heated in a third (12a) solution heat exchanger. The heat is transferred from the first partial flow of the poor absorption circuit solution (16a) and the poor compression circuit solution (36).

A fourth solution heat exchanger (42) is inserted in the resorption cycle, with poor resorption cycle solution (46) heating up rich resorption cycle solution (48).

In the degasser (43) the refrigeration takes place. Cold transfer then takes place to the low pressure gas of the closed gas turbine (6b).

the 4 shows cold production and transfer to the cycle medium of an open gas turbine and heat transfer to a circulating water stream.

In the 4 will in contrast to 2 arranged to drive the absorption power refrigeration cycle, a circulating flow of water (7). Heat is introduced into this in the waste heat boiler (5), through which the exhaust gas flow (9) from an open gas turbine (6a) flows. First, the heat is introduced to the steam superheater (5a). The water stream (7) is successively a high-pressure trickle expeller (13a), an additionally arranged fifth solution heat exchanger (12b) and then as in 2 and 3 shown to the medium-pressure operated medium-pressure trickle expeller (33). Then it is returned to the waste heat boiler (5), supported by a circulation pump (11c).

In contrast to 2 and 3 the absorption circuit is not routed via the waste heat boiler. The rich absorption circuit solution (18) is raised to high pressure by means of the fourth solution pump (11b). This rich solution (18) is largely heated to the boiling point in the first (22) and completely in the fifth (12b) solution heat exchanger. Almost the entire amount of the rich absorption cycle solution (18) is introduced into the head of a high-pressure trickle expeller (13a) with the second partial flow (18f) of the absorption cycle. When it was previously separated into a second (18f) and a third partial flow (18g) of rich absorption circuit solution solution, only a small amount is allocated to the third partial flow (18g). Expulsion is carried out in the high-pressure trickle expeller (13a) by means of a trickling down second partial flow (18e) of rich absorption circuit solution. The heat transfer takes place in countercurrent to the trickling down third partial flow (18f) of rich absorption cycle solution through the water flow (7) and in parallel through poor absorption cycle solution (16). This poor solution (16) is previously discharged from the sump of the high-pressure trickle expeller (13a).

The water content of the steam (19a) after the steam superheater (5a) is increased, as already 3 described

The poor absorption circuit solution (16) is first lowered to medium pressure by means of a second throttle (17a), the poor solutions (26a) of the absorption and compression circuit are routed via the second solution heat exchanger (12) to the ultra-low-pressure absorber (1).

The rich compression circuit solution (38) is raised to medium pressure by means of the sixth solution pump (31) and fed into the head of the medium-pressure trickle expeller in supercooled form.

In the degasser (43) the refrigeration takes place. Cold transfer then takes place to the supply air (9a) of the open gas turbine (6a).

the 5 shows refrigeration generation and transfer to the low pressure gas of a closed gas turbine and heat transfer to rich and lean solution of the absorption cycle.

In contrast to 2 the heat input to the forming two-phase mixture (18p) and the steam superheating (5a) of the absorption circuit is shown in parallel with an economizer (5eco) of a steam turbine. In the waste heat boiler, this heat input is preceded by the one for water evaporation and overheating. It is shown that the exhaust gas from an open gas turbine (6a) flows through the waste heat boiler.

In contrast to the representation of 2 a second partial stream of poor solution (16c) is introduced into the two-phase mixture (18p), which has already partially formed. This second partial flow (16c) is for the most part only heated in the waste heat boiler and releases the absorbed heat in the desorber (13) again. In comparison to 2 the Quantity of a poor solution in a desorber sump increases. This second partial stream (16c) of poor absorption circuit solution is separated from the stream of poor solution (16) after the desorber (13) and fed to the waste heat boiler (5). The process steps that are linked to the supply of rich solution to the desorber are closed 3 described.

In the degasser (43) the refrigeration takes place. Cold transfer then takes place to the low pressure gas (9c) of the closed gas turbine (6b).

the 6 shows refrigeration generation and transfer to the low pressure gas of a closed gas turbine and heat transfer to a circulating water stream and to a steam heater.

Analogous to 4 a circulating flow of water (7) is arranged to drive the absorption power refrigeration cycle. Analogous to 5 shows the heat input connected in parallel to the economizer of a steam turbine. Deviating from the in 5 described waste heat boiler, a device for generating steam (8a) is arranged in the low overpressure range. This steam generator (8) is arranged in the waste heat boiler (5) before the steam superheater (5a). The inlet temperature of the heat input to the steam generator is designed for at least 220 ℃, in particular by arranging a high pressure ratio of the closed gas turbine - at least 4.5. The steam (8a) generated in the steam generator (8) is exported to a heat consumer (20) outside the overall system.

In contrast to the representations of the previous figures, steam is not fed from the steam separator (44) to the low-pressure absorber (2), but as low-pressure steam (49a) of the resorption cycle to the low-pressure absorber (1). Low-pressure steam (19c) is fed from the turbine (14) to the low-pressure absorber (2). The low-pressure gas (9c) of the closed gas turbine is cooled down to below 0 ℃ by the refrigeration transfer.

In the degasser (43) the refrigeration takes place. Cold transfer then takes place to the low pressure gas (9c) of the closed gas turbine (6b).

the 7 shows refrigeration generation and transfer to the low pressure gas of a closed gas turbine and heat transfer to rich and enriched solution of the absorption cycle and to high temperature electrolysis.

The corresponding to 6 generated water vapor (8a) is in 7 used in a steam electrolysis (8d) to separate superheated steam (8c) into hydrogen (8e) and oxygen (8f) at temperatures above 700 ℃ in a known process. Both substances are taken from the electrolyser (8d) at high temperature and are passed first through a steam superheater (8g) and then through a water heater (8h) to release the heat. The water for steam generation (8) is taken from a steam drum (8b). In this combination, an electricity credit of 70% of the heat of the water vapor generated is attributed to the absorption power-cooling cycle, since the heat of vaporization of the water replaces electrical energy to the same extent.

In contrast to the representations of 2 until 5 as a further variant, only low-pressure steam (49) generated in the resorption cycle is fed to the low-pressure absorber (2) and only expanded ultra-low-pressure steam (19b) from the turbine (14) is fed to the low-pressure absorber (1).

In the degasser (43) the refrigeration takes place. Cold transfer takes place to the low pressure gas (9b) of the closed gas turbine (6b). Heat is introduced via the generated water vapor (8c) and electricity via a water vapor electrolyzer (8d) for hydrogen generation (8e).

the 8th shows solar thermal heat utilization and operation in base load mode.

Both solar thermal power generation and hydrogen production are capital intensive. The profitability therefore depends to a large extent on the useful life of the conversion apparatus, expressed by the number of hours per year.

The following procedure is provided for a base load mode of operation. Solar radiation (6j) is directed onto a particle receiver (6i) by means of mirrors (6k). Ceramic balls are usually used for this. There the particles are heated to high temperatures (850 to 1000 ℃). At least part of the high-temperature heat is temporarily stored. The particles are conveyed into a high-temperature thermal store (6f) by means of a particle transport device (6h). From this thermal energy store (6f), the particles are routed to the heater (6d) of a closed gas turbine (6b).

After the heat has been removed, the particles are fed into a medium-temperature thermal store (6g). The temperature level of this store is 450 to 600 ℃ From this store (6g) the particles are directed to the particle receiver (6i) for harvesting solar radiation.

From the low-pressure gas (9c), heat is introduced into the absorption power-cooling cycle in a waste heat boiler (5), as is shown in 3 and 7 is shown. Their complete circuits and associated apparatus are in 8th not shown.

With high-temperature storage, the period of solar radiation (in the example with 3500 h per year) for base load operation (in the example with 7500 h per year) of the closed gas turbine in the absorption power-cooling cycle for electrolysis is extended. The storage time of the particles is relatively short. A storage time of approx. 15 hours is considered sufficient in solar thermal power plants.

Of the various electrolysis processes, water vapor electrolysis is most efficient in the high-temperature range, particularly since about one-fifth of the energy to be supplied is in the form of water vapor and this can be provided at low cost.

Steam electrolysis can only be carried out at high temperatures (over 700 ℃) and is therefore suitable for continuous operation. This requirement is met with solar thermal power generation, in contrast to volatile power supply, e.g. by wind. As already described, the water vapor in the absorption power-cooling cycle is generated in an energy-saving manner by means of power-heat coupling.

Reference List

1

Ultra-low pressure absorber

2

low pressure absorber

3

medium pressure absorber

5

waste heat boiler

5a

steam superheater

5du

water evaporation and overheating

5eco

economizer

6a

open gas turbine

6b

compressor

6c

regenerative counterflow heat exchanger

6d

closed gas turbine

6e

heater

6f

high temperature storage

6g

medium temperature storage

uh

particle transport device

6i

particle receiver

6y

solar radiation

6k

mirror

6m

combustion chamber

7

water stream

7b

gas turbine cooler

8th

steam generator

8a

Steam

8b

steam drum

8c

superheated steam

8d

steam electrolyser

8e

hydrogen

8f

oxygen

8g

steam superheater

8h

water heater

8i

electricity

9

exhaust

9a

working medium supply air

9b

high pressure gas

9c

Working medium low-pressure gas

11a

third solution pump

11b

fourth solution pump

11c

circulation pump

12

second solution heat exchanger

12a

third solution heat exchanger

12b

fifth solution heat exchanger

13

desorber

13a

high-pressure trickle expeller

14

turbine

15

generator

16

poor absorption circuit solution

16a

first partial flow of poor absorption cycle solution

16b

Main flow of lean absorption cycle solution

16c

second partial flow of lean absorption cycle solution

17

first throttle

17a

second throttle

18

rich absorption circuit solution

18a

first partial flow of enriched absorption cycle solution

18b

second partial stream of enriched absorption circuit solution

18c

third partial stream of enriched absorption circuit solution

18d

Main stream of rich absorption cycle solution

18e

first partial flow of rich absorption cycle solution

18f

second partial flow of rich absorption cycle solution

18g

third partial stream of rich absorption cycle solution

18p

Two-phase mixture of the absorption cycle

19

water-rich ammonia vapour

19a

superheated water-rich ammonia vapour

19b

ultra-low pressure steam

19c

low pressure steam

19d

aqueous ammonia vapour

19e

Valve

20

heat consumers

21

first solution pump

21a

second solution pump

22

first solution heat exchanger

26

Mixed flow of lean solutions of the absorption and compression cycle

26a

poor solutions of the absorption and compression cycle

27

third throttle

28

rich solutions of the absorption and compression cycle

28a

Main flow of rich solutions of the absorption and compression cycle

29

enriched solution of the absorption and the compression cycle

31

sixth solution pump

33

Medium-pressure trickle ejector

36

poor compression circuit solution

38

rich compression circuit solution

39

Medium Pressure Ammonia Vapor

41

fifth solution pump

42

fourth solution heat exchanger

43

degasser

44

vapor separator

46

poor resorption circuit solution

47

fourth throttle

48

rich resorption circuit solution

49

Low pressure vapor of the resorption cycle

49a

Ultra-low pressure vapor of the resorption cycle

Claims (15)

Method of operation of an absorption power cooling cycle for a two-component mixture of ammonia and water for utilizing a heat input from an external thermal energy carrier, comprising: for generating electricity, a cycle referred to below as an absorption cycle with the following main components: • at least one waste heat boiler (5) and a desorber (13) or high-pressure trickle expeller (13a) for expelling a mixed vapor of ammonia and water from a rich absorption cycle solution (18), or from a main stream (18d) of a rich absorption cycle solution, • a steam superheater 5a for superheating a high-pressure steam (19) of ammonia and water, • a turbine (14) driving a generator (15) to expand the overheated high-pressure steam (19) from ammonia and water, • a low-pressure absorber (1) and a low-pressure absorber (2) to absorb an expanded low-pressure steam (19b), or for absorption of an expanded low-pressure vapor (19c) by means of a poor absorption cycle solution (16), • at least one solution heat exchanger (12, 12a) for heat transfer from poor absorption cycle solution (16) to the rich absorption cycle solution (18), • the poor absorption cycle solution (16) being recycled through a desorber (13) or high-pressure trickle expeller (13a) is used to generate high-pressure steam, to generate refrigeration in a cycle referred to below as the resorption cycle and in a cycle referred to as the compression cycle with the following main components in the resorption cycle • a degasser (43) that provides cooling to expel a low-pressure steam (49a) of the resorption cycle or a low-pressure steam (49) of the resorption circuit from a rich resorption circuit solution (48), • a medium-pressure absorber (3) for absorbing medium-pressure ammonia vapor (39) expelled in the compression circuit by means of poor resorption circuit solution (46), with the following main components in the compression circuit: • at least one medium-pressure expeller (33) for ejecting medium-pressure ammonia vapor (39) from a rich compression circuit solution (38), • at least one ultra-low-pressure absorber (1) or low-pressure absorber (2) for absorbing the ultra-low-pressure vapor (49a) or low-pressure vapor (49 ) by means of a poor compression circuit solution (36) , characterized in that • the external heat input is carried out from a gas in the absorption circuit and in the compression circuit, • a low-pressure absorber (1) and a low-pressure absorber (2) are arranged for absorption and all poor absorption circuit solutions (16 , 16b) and the lean compression circuit solution (36) is fed to the ultra-low pressure absorber (1) and the rich absorption circuit solution (18) and the rich compression circuit solution (38) are removed from the low-pressure absorber (2), • and the vapor (49 , 49a) only one of the two absorbers (1 or 2) is fed to absorption and absorbed there, • the other absorber (2 or 1), to which no vapor generated in the deaerator is fed for absorption, only vapor from the absorption circuit is fed, • and pressure and temperature level in the desorber (13) or high-pressure trickle expeller (13a ) of the absorption circuit is arranged higher than in the medium-pressure expeller (33) of the compression circuit, • whereby the pressure in the ultra-low-pressure absorber (1) is lower than in the low-pressure absorber (2), • the low-pressure absorber (2) enriched solutions (29) of the absorption and compression circuit from the ultra-low pressure absorber (1) via a first solution pump (21), • the resorption circuit being designed such that the water content of the poor resorption circuit solution (46) corresponds at most to the water weight content of the rich absorption circuit solution (18). and furthermore the absorption power cooling cycle is combined with a turbine system comprising a gas turbine (6a, 6d), the cooling capacity generated in the degasser (43) being used to cool the working medium (9a, 9c) of one of the gas turbines before it enters in a compressor (6b) to cool the gas turbines. Working method of an absorption power-cooling cycle claim 1 , characterized in that the superheated high-pressure steam (19) to be expanded from ammonia and water is adjusted to a water content of 3 to 10 percent by weight - preferably 6 percent by weight - the adjusted water-rich ammonia vapor (19a) at least in a second section of the expansion with partial condensation is relaxed and • the set water-rich ammonia vapor or parts of the water-rich ammonia vapor (19a) are expanded to a pressure of 1.1 to 4 bar, preferably 1.5 to 2.5 bar. Working method of an absorption power-cooling cycle claim 1 or 2 , characterized in that both ultra-low-pressure steam (19b) and low-pressure steam (19c) are removed from the turbine (14) at a respective pressure level of the ultra-low-pressure absorber (1) or the low-pressure absorber (2) and fed to the respective absorber (1, 2). . Working method of an absorption power-cooling cycle according to one of Claims 1 until 3 , characterized in that the resorption circuit is additionally designed with the following process steps: • Rich resorption circuit solution (48) is fed into a degasser (43), • In the degasser (43), the process step of expulsion is carried out by using external heat input at a temperature level below the ambient temperature, the rich resorption circuit solution (48) is converted into a two-phase mixture of the resorption circuit, • the two-phase mixture of the resorption circuit is then fed to a steam separator (44) and separated into almost pure ammonia vapor from the resorption circuit and lean resorption circuit solution (46), • the almost pure ammonia vapor into one under the same pressure absorber (1 or 2) for absorption, • the poor resorption cycle solution (46) is raised to medium pressure by means of a fifth solution pump (41) and is fed to a medium-pressure absorber (3) for absorption, • and the rich resorption nskreislösung (48) is lowered by means of throttle (47) of the resorption circuit from medium pressure to the pressure of the degasser (43). Working method of an absorption power-cooling cycle claim 4 , characterized in that the absorption circuit and the compression circuit are additionally designed with the following process steps: • a main flow of rich absorption circuit solution (18d) is introduced into a waste heat boiler (5) and converted into a two-phase mixture (18p) by means of external heat input, • the two-phase mixture (18p ) then introduced into the bottom of the desorber (13) and a second partial flow (18b) of enriched absorption circuit solution is introduced into the top of the desorber (13), • the process steps rectification and expulsion are arranged in the desorber (13) by in the bottom of the desorber (13) a separation of the two-phase mixture (18p) into vapor phase and liquid phase takes place, • in the desorber (13) in a known manner by passing through several trough-like surfaces arranged at different heights, a material and heat exchange between vapor and solution is carried out, • here from the Sump of desorber (13) ascending very water free cher ammonia vapor desorbed to form aqueous ammonia vapor (19d) and • supplied second partial flow (18b) of rich absorption cycle solution converted into heated solution with reduced ammonia content and this heated solution is introduced into the bottom of the desorber (13) and • by lean absorption cycle solution (16) from the Bottom of the desorber (13) is discharged and passed through trough-like surfaces for heat transfer, with the passage being carried out in the countercurrent principle to the temperature of the surfaces, whereby from the supplied second partial flow (18f) rich absorption circuit solution additional aqueous ammonia vapor (19d) and water-rich solution are formed, • where the in the bottom of the desorber (13) introduced water-rich solutions are combined with the liquid phase obtained in the phase separation to poor absorption cycle solution (16), • then according to an existing in the wet steam area equilibrium between steam and liquid via the second partial flow (18f) of rich absorption cycle solution, the water content of the water-containing ammonia vapor (19d) exiting at the top of the desorber (13) is determined, • the lean absorption cycle solution (16) is discharged from the desorber (13) after indirect heat transfer has taken place and a first partial flow of the lean absorption cycle solution (16a) is separated, • the remaining main flow (16b) of lean absorption cycle solution is passed through a second solution heat exchanger (12) for heat transfer, with the amount of the main flow (16b) being dimensioned so large that the first partial flow (18e ) rich absorption circuit solution is heated to boiling temperature, • then the main stream (16b) of poor absorption circuit solution is lowered to the lowest pressure level by means of a first throttle (17) and introduced into the lowest pressure absorber (1) for absorption, • enriched solutions (29) of the absorption circuit and the compression circuit are taken from the ultra-low pressure absorber (1) and fed to the low-pressure absorber (2) for absorption, • a first partial stream (18e) of rich absorption circuit solution from the stream (28) of rich solutions of the absorption circuit and the compression circuit is separated and raised to the high pressure level by means of a fourth solution pump (11b) and heated in the second solution heat exchanger (12), • then the first partial flow (18e) of rich absorption cycle solution is divided into a second (18f) and a third partial flow (18g) of rich absorption cycle solution • the third partial flow (18g) of richer absorption cycle solution is mixed with the aqueous ammonia vapor (19d) prior to overheating and evaporated in the waste heat boiler (5) to increase the proportion of water, • with the amount of the third partial flow (18g) of richer absorption cycle solution in the water-rich ammonia vapor a water weighta proportion of 6 percent by weight is set, • the superheated, water-rich ammonia vapor (19a) is fed to the turbine (14), • the remaining main stream of rich solutions (28a) of the absorption circuit and the compression circuit is raised to medium pressure by means of the second solution pump (21a) and used to absorb heat is routed to the first solution heat exchanger (22), • the rich compression cycle solution (38) is then separated, • the remaining main flow of rich absorption cycle solution (18d) is raised to high pressure by means of the third solution pump (11a) and passed through the third solution heat exchanger (12a) for heat absorption and then is routed to the waste heat boiler (5) for heat transfer, • the first partial flow of the lean absorption circuit solution (16a) is lowered to medium pressure by means of the second throttle (17a) and with lean compression circuit solution (36) for heat transfer through the third (12a) and then through the first Solution heat exchanger (22) is passed and then by means of it Most throttle (27) is lowered to the lowest pressure and introduced into the lowest-pressure absorber (1) for absorption. Working method of an absorption power-cooling cycle claim 5 , characterized in that the absorption circuit is supplemented with the following process step: • in the waste heat boiler (5), a second partial stream of lean absorption circuit solution (16c) is introduced into the two-phase mixture (18p) of the absorption circuit that is being formed, the introduction taking place at a temperature of the two-phase mixture between 10 and 20 Kelvin above a boiling point of the rich absorption circuit solution (18). Working method of an absorption power-cooling cycle claim 4 , characterized in that the absorption circuit and the compression circuit are additionally designed with the following process steps: • rich absorption circuit solution (18) is introduced into a waste heat boiler (5) and converted into a two-phase mixture (18p) by means of external heat, • a third partial flow of enriched absorption circuit solution (18c) is introduced into the two-phase mixture (18p) of the absorption cycle that forms, with the introduction taking place at a temperature of the two-phase mixture between 10 and 20 Kelvin above a boiling temperature of the rich absorption cycle solution, • the two-phase mixture (18p) then into the bottom of a desorber ( 13) and a second partial stream (18b) of enriched absorption circuit solution is introduced into the top of the desorber (13), • the process steps rectification and expulsion are arranged in the desorber (13) by separating the two-phase mixture in the bottom of the desorber (13). ischs (18p) takes place in the vapor phase and liquid phase, • in the desorber (13) in a known manner, a mass and heat exchange between vapor and solution is carried out in the passage through several trough-like surfaces arranged at different heights, • here from the sump of the desorber (13) ascending, very water-rich ammonia vapor is desorbed to form water-rich ammonia vapor (19) and the second partial stream (18b) fed in is converted from enriched absorption circuit solution into heated solution with a reduced ammonia content, and this heated solution is introduced into the bottom of the desorber (13), • by then poor absorption circuit solution ( 16) is discharged from the bottom of the desorber (13) and passed through the trough-like surfaces for heat transfer, with the passage being carried out in countercurrent to the temperature of the surfaces, 19) and water-rich solution are formed, • the low-ammonia solutions fed into the bottom of the desorber (13) are combined with the liquid phase obtained in the phase separation to form the poor absorption cycle solution (16), • then corresponding to an equilibrium between vapor and liquid in the wet-steam region the enriched absorption circuit solution (18b) the proportion of water at the top of the desorber (13) escaping water-rich ammonia vapor (19) is determined, • the overheated water-rich ammonia vapor (19a) is fed to the turbine (14), • the poor absorption circuit solution (16) is discharged from the desober (13) after indirect heat transfer has taken place and a first partial flow of the lean absorption cycle solution (16a) is separated, • the remaining main flow (16b) of lean absorption cycle solution is passed through a second solution heat exchanger (12) for heat transfer, with the amount of the main flow (16b) being dimensioned so large that the first partial flow (18a ) enriched absorption circuit solution is heated to boiling temperature, • then the main stream (16b) of poor absorption circuit solution is lowered to the lowest pressure level by means of a first throttle (17) and introduced into the lowest pressure absorber (1) for absorption, • enriched solutions (29) of the absorption circuit and the compression circuit are removed taken from the ultra-low pressure absorber (1) and de m low-pressure absorber (2) for absorption, • the first partial flow (18a) of enriched absorption cycle solution is taken from the low-pressure absorber (1) and raised to high-pressure level by means of a fourth solution pump (11b) and heated in a second solution heat exchanger (12), • then the first partial flow (18a) of enriched absorption cycle solution is divided into a second (18b) and third partial flow (18c) of enriched absorption cycle solution, • rich solutions (28) of the absorption cycle and the compression cycle are raised to medium pressure by means of the second solution pump (21a) and for heat absorption by the first solution heat exchanger (22), • then the rich compression cycle solution (38) is separated, the remaining rich absorption cycle solution (18) is raised to high pressure by means of the third solution pump (11a) and passed to the waste heat boiler (5) for heat transfer, • the first partial flow the poor absorption cycle solution g (16a) is lowered to medium pressure by means of the second throttle (17a) and passed through the first solution heat exchanger (22) with the poor compression circuit solution (36) for heat transfer and then lowered to ultra-low pressure by means of the first throttle (27) and fed into the ultra-low-pressure absorber (1) is initiated for absorption. Working method of an absorption power-cooling cycle claim 4 , characterized in that the absorption circuit and the compression circuit are additionally designed with the following process steps: • external heat being introduced into a circulating, aqueous heat transfer medium (7) in the waste heat boiler (5) and the heat transfer medium (7) for indirect heat dissipation by a high-pressure trickle expeller ( 13a), • lean absorption circuit solution (16) is discharged from the bottom of the high-pressure trickle expeller (13a) and passed through the high-pressure trickle expeller (13a) for indirect heat dissipation, • a second partial flow of rich absorption circuit solution (18f) into the head of the high-pressure trickle expeller (13a) is initiated, • the expulsion process step is carried out in the high-pressure trickle expeller (13a) by using an indirect heat-emitting heat transfer medium (7) and poor absorption circuit solution (16) to drive out aqueous ammonia vapor (19d) from the second partial stream (18f) of rich absorption circuit solution and poor absorption circuit solution (16) is formed, • the heat transfer medium (7) is discharged from the high-pressure trickle expeller (13a), and first passed through the third solution heat exchanger (12a) to release heat and then passed to the compression circuit for heat transfer, • enriched solutions (29) of the absorption cycle and the compression cycle are removed from the ultra-low pressure absorber (1) and fed to the low-pressure absorber (2) for absorption, • the rich absorption cycle solution (18) is separated from the stream (28) of rich solutions of the absorption cycle and the compression cycle and • by means of a fourth solution pump (11b) is raised to the high pressure level and first heated in a second solution heat exchanger (12) and then brought to the boiling point in the third solution heat exchanger (12a), • is then separated into a second (18f) and a third partial flow (18g) of rich absorption circuit solution, • the third partial flow (18g) richer absorption cycle solution is added to the water-containing ammonia vapor (19d) before overheating and evaporated in the waste heat boiler (5) to increase the proportion of water, and the overheated water-rich ammonia vapor (19a) is fed to the turbine (14), • with the amount of the third partial flow (18g) rich absorption circuit solution in water-rich ammonia vapor, a water weight percentage of 6 percent by weight is set, • the poor absorption circuit solution (16) lowered to medium pressure by means of a second throttle (17a) and with Poor compression circuit solution (36) passed through the second solution heat exchanger (12) to release heat and then lowered to the lowest pressure by means of the first throttle (27) and introduced into the lowest-pressure absorber (1) for absorption. Working method of an absorption power-cooling cycle according to one of Claims 5 , 6 , 7 or 8th , characterized in that the absorption circuit is additionally designed with the following process steps: • a circulating aqueous heat transfer medium (7) is passed through a medium-pressure trickle expeller (33) for indirect heat dissipation, • rich compression circuit solution (38) is introduced into the head of the medium-pressure trickle expeller (33). , • the expulsion process step is carried out in the medium-pressure trickle expeller (33), in that almost pure medium-pressure ammonia steam (39) is expelled from rich compression circuit solution (38) by means of an indirect heat-emitting heat carrier (7) and lean compression circuit solution (36) is formed, • the in the medium-pressure trickle expeller (33) expelled medium-pressure ammonia vapor (39) is conducted to a medium-pressure absorber (3) of the resorption circuit which is at the same pressure, • the lean compression circuit solution (36) is discharged from the sump of the medium-pressure trickle expeller (33), • the rich compression circuit solution (38) is medium s sixth solution pump (31) is raised from low pressure to medium pressure and passed to the medium-pressure trickle expeller (33). • the heat transfer medium (7) - supported by a circulating pump (11c) - is routed back to the waste heat boiler (5), and • heat is introduced into the waste heat boiler (5) from an external heat source. Working method of an absorption power-cooling cycle according to one of Claims 5 until 9 , characterized in that a closed gas turbine (6d) is arranged in the turbine system, the low-pressure gas (9c) of the closed gas turbine (6d) being passed through the degasser (43) as an external heat source for pre-cooling, the low-pressure gas (9c) and the rich resorption circuit solution (48) are performed in countercurrent. Working method of an absorption power-cooling cycle according to one of Claims 5 until 9 , characterized in that an open gas turbine (6a) is arranged in the turbine system, with the supply air (9a) of the open gas turbine (6a) being passed through the degasser (43) as an external heat source for pre-cooling, with the supply air (9a) and the rich resorption circuit solution (48) are performed in countercurrent. Working method of an absorption power-cooling cycle claim 10 or 11 , characterized in that the turbine system is designed as a water-steam turbine system that includes an economizer (5eco) and an open (6a) or a closed gas turbine (6d) are used in the turbine cycle, • wherein a in the economizer (5eco) from an exhaust gas ( 9) one of the gas turbines (6a, 6d), recovered heat is used as an external heat source for entry into the absorption power-cooling cycle, • and the supply air (9a) of one of the gas turbines (6a, 6d) for pre-cooling by the degasser ( 43) is passed, the supply air (9a) and the rich resorption cycle solution (48) being passed in countercurrent. Working method of an absorption power-cooling cycle claim 10 , characterized in that the absorption power-cooling cycle is combined with a steam generator (8), and • heat is removed from the waste heat boiler (5) to generate steam, • for which purpose the waste heat boiler (5) is designed for an inlet temperature of at least 220 ℃ and a high pressure ratio of at least 4.5 is set in the closed gas turbines (6d) and • the steam generation can be used to feed a steam electrolyzer (8d). Working method of an absorption power-cooling cycle claim 10 , characterized in that the closed gas turbine (6d) is used with a regenerative counterflow heat exchanger (6c), • wherein heat accumulators (6f, 6g) comprising ceramic particles and preferably used for solar thermal energy are also arranged, of which a first heat accumulator (6f) contains heat with a temperature of at least 800 ℃ and a second heat accumulator (6g) provides heat with a temperature between 450 and 600 ℃, • and provided heat can be fed into the closed gas turbine (6d) for heat input. Working method of an absorption power-cooling cycle according to one of Claims 10 until 14 , characterized in that expanded ultra-low pressure steam (19b) from the turbine (14) preferably the ultra-low-pressure absorber (1) and low-pressure steam (49) of the resorption circuit are preferably fed to the low-pressure absorber (2) for absorption.

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