EP0210264A1

EP0210264A1 - Installation with a heat absorbing and heat releasing process part as well as with heat supply part containing an absorber installation

Info

Publication number: EP0210264A1
Application number: EP86901333A
Authority: EP
Inventors: Georg Prof. Dr. Alefeld
Original assignee: Individual
Current assignee: Individual
Priority date: 1985-02-05
Filing date: 1986-02-05
Publication date: 1987-02-04
Also published as: DE3503863A1; US4770005A; JPS62501618A; WO1986004517A1

Abstract

Installation possédant un élément de traitement (PRT) qui est alimenté en énergie primaire de fonctionnement (P3) par l'intermédiaire d'un élément d'alimentation en chaleur (WVT). L'élément d'alimentation en chaleur (WVT) sert en même temps aussi pour utiliser la chaleur Qo dégagée par le traitement. L'élément d'alimentation en chaleur (WVT) contient un ensemble formé d'un transformateur de chaleur (WT) et d'une pompe à chaleur (WP), fournit l'énergie thermique d'entrée (Q2) requise par l'élément de traitement, absorbe l'énergie thermique de sortie (Q1) de l'élément de traitement et dégage, pour sa part, de la chaleur perdue (QoT), dans une gamme de températures inférieure à celle de la température de la chaleur de sortie de l'élément de traitement.Installation having a processing element (PRT) which is supplied with primary operating energy (P3) via a heat supply element (WVT). The heat supply element (WVT) is also used at the same time to use the heat Qo produced by the treatment. The heat supply element (WVT) contains an assembly formed by a heat transformer (WT) and a heat pump (WP), provides the input thermal energy (Q2) required by the treatment element, absorbs the thermal output energy (Q1) of the treatment element and releases, for its part, waste heat (QoT), in a range of temperatures lower than that of the heat temperature of output from the processing element.

Description

Plant with a heat-absorbing and heat-emitting process part and a heat supply part containing an absorber device

The present invention relates to a system with a process part that requires input heat energy in at least one input heat temperature range and from which output heat energy has to be dissipated in at least one output heat temperature range that is lower than the input heat temperature range, and with a heat supply part that has an absorber device and a Operating power supply contains.

Many processes, in particular material separation processes, require input thermal energy of a certain temperature (s) and give off output or waste heat at a lower temperature (s). Often, e.g. B. in distillation processes such as seawater desalination, the distance between the inlet temperature and the waste heat temperature is relatively small, often only a few Kelvin, and it would therefore be extremely uneconomical to discard the waste heat. A known method for utilizing the waste heat in distillation processes is the so-called vapor compression, ie the steam produced during the distillation is compressed by means of a mechanical compressor, so that it condenses at a higher temperature and the heat of condensation generated can be used as input heat. Plants for vapor compression are also known which contain a heat transformer ⁽ DE-A-3016406). A disadvantage of vapor compression is that mechanical compressors require high-quality drive energy, require a high level of maintenance and are noisy.

From US-A-4402 795 it is known to supply the waste heat or output heat energy given off by a material separation system to a heat transformer which increases the temperature of this output heat energy to such an extent that it can be used as the input heat energy of the system. From US-A-43 50 571 it is known to supply the heat energy required for operation to a material separation plant via an absorber heat pump.

The known devices working with a heat transformer or a heat pump also have certain disadvantages. When a heat transformer is used, the system must be supplied with a relatively large part of the operating energy required for its operation directly in the form of high-quality primary operating heat energy. On the other hand, when a heat pump is used, under otherwise comparable conditions, the overall utilization of the primary operating energy is worse than when a heat transformer is used.

The present invention has for its object to provide a system of the type mentioned that requires only relatively little high-quality primary operating energy for its operation and emits only inferior low-temperature waste heat, so that the thermodynamic efficiency is correspondingly high.

The object is achieved in a system having a process part which requires input thermal energy for operation in at least one input heat temperature range and from which heat energy must be dissipated in operation in at least one output heat temperature range which is lower than the input heat temperature range, and with a heat supply part which Absorber device and an operating energy source, in particular operating heat source ent, solved according to the invention in that the heat supply part as the absorber device contains a combination of a heat transformer and a heat pump, supplies the process part with the input heat energy required by it, absorbs the output heat energy from the process part and in turn between the operating energy part source and a heat sink, the waste heat in a temperature range, which is lower than the initial heat temperature range of the process part, which is taken up by the heat supply part, is switched.

Further developments and advantageous refinements of the system according to the invention are the subject of subclaims.

The system according to the invention enables surprisingly high energy savings to be achieved with relatively little expenditure on equipment, as will be explained in more detail below.

Certain embodiments of the invention are characterized by particularly low outlay on equipment. Other embodiments are optimized with regard to the thermodynamic efficiency. Embodiments are described both for a relatively large and for a relatively small distance between the input heat temperature and output heat temperature of the process part. With regard to the freedom in the construction of the heat supply part, particular advantages result from the fact that the heat supply part is only thermally coupled to the process part, i.e. if the process material is not used as working fluid in the heat supply part.

Devices operating on the absorber principle ("absorber devices") which contain a heat pump part in combination with a heat transformer part are known in principle, for example from EP-A-61721 and the DE magazine Brennst.-Wärme-Kraft 33 (1981 ) No. 12, 486 - 490. However, these publications do not indicate that unusually high energy savings can be achieved by combining a heat transformer and a heat pump in the heat supply part of a process and how this can be done with the given process with as little equipment expenditure as possible . The heat cycle resulting from the present combination is run through several times by the thermal energy and is responsible for the high efficiencies. Preferred exemplary embodiments of the invention are explained in more detail below with reference to the drawings. The nomenclature and the type of representation essentially correspond to those of EP-A-61721, to which express reference is made here.

Show it:

1a shows a schematic representation of the relationships with regard to the heat supply of a process, on the basis of which the problem underlying the invention, the principle of the solution according to the invention of this problem and the surprising progress achieved by the invention are to be explained;

1b is a diagram in which the percentage energy saving (ratio of the primary operating energy to be supplied from the process without a heat transformer and / or heat pump to the external operating energy required when using a heat supply part containing a heat transformer and / or a heat pump) for the various cases discussed with reference to FIG. 1a;

Fig. 2 is a schematic representation of a first embodiment of the invention;

3 to 8 show further schematic representations of the heat supply part of various embodiments of the invention;

9, 9a and 9b show a schematic illustration, a more detailed illustration or an associated steam pressure diagram of a further embodiment of the heat supply part of a system according to the invention; 10 to 13 show diagrams of further heat supply parts;

14, 14a and 14b representations corresponding to FIGS. 9, 9a and 9b, respectively, in FIG. 14a also the one with the heat supply part L according to FIG. 14 thermally coupled process part, namely a water desalination or distillation device, is shown;

15 to 23 are schematic representations of further embodiments of the heat supply part of a system according to the invention;

FIG. 23a shows a vapor pressure diagram for FIG. 23;

24 to 38 show diagrams of further heat supply parts;

39a to 41r show different embodiments of heat pump configurations which can advantageously be used in the heat supply part of embodiments of the invention;

40a to 40r show different heat transformer configurations which can be used advantageously in the heat supply part of a system according to the invention;

41 shows a schematic illustration of a further absorber device for the heat supply part of a system according to the invention;

Fig. 41a shows a modification of Fig. 41;

41b shows a somewhat more precise illustration of the device according to FIG. 41a; 41c shows a modification of FIG. 41b;

41d to 41g are schematic representations which show how certain exchange units of the devices according to FIGS. 41b and 41c can be constructed;

41h shows a modification of FIG. 41c;

41i shows a vapor pressure diagram for the devices according to FIGS. 41b and 41c;

42 is a diagram of another heat supply part;

FIG. 43 is a diagram of a heat supply part, including a heat pump and a two-stage zweistu¬-stage heat pump and a two-stage heat transformer with only a ^single-* Zigen working fluid circuit;

43a shows a more precise illustration of the device according to FIG. 43;

43b shows a vapor pressure diagram for FIG. 43a;

43c shows another possibility of realizing the device according to FIG. 43;

43d shows a modification of a part of the device according to FIG. 43a;

44 to 62 show diagrams of further absorber devices, each containing a combination of a heat pump and a heat transformer;

63 and 63a show a diagram of a further embodiment and the associated vapor pressure diagram; 64 to 71 further schematic representations of embodiments of the heat supply part of a plant according to the invention,

72 to 94 embodiments of the heat supply part of a plant according to the invention, which additionally contains a compressor;

95 and 96 show schemes of a two-stage heat pump or a two-stage heat transformer with particularly advantageous heat exchanger arrangements.

The problem underlying the invention, its solution and the surprising advantage achieved by this are first explained with reference to FIGS. 1a and 1b.

FIG. 1 a shows schematically a plant with a process part PRT and a heat supply part WVT serving for the economical heat supply of the process part. The process part requires thermal energy Q for operation, which partly consumes in the process, partly due to unavoidable losses, e.g. B. due to imperfect heat insulation, is lost and appears in part as waste heat ("initial heat") of the process, in particular in the form of latent or specific heat in the process product. Taken alone, the process part PRT, as shown schematically in FIG. 1a, requires input heat Q, and it gives output heat Q _n and heat Q .. which should be referred to as heat loss and the losses mentioned and those carried by the process material and not included as Q_ recoverable heat. Since the initial heat Q _n generally has a relatively high temperature, it cannot simply be discarded (for example to the environment) for reasons of economy.

According to the US-A-44 02 795 mentioned above, the entire output heat Q- can now be fed to a heat transformer WT. The one

T

Heat transformer WT input heat is denoted by G net, it should be equal to the total available process output heat Q _n , since then the entire output heat of the process is used and the maximum heat recovery is guaranteed. The heat transformer WT is designed so that on the one hand it produces output heat Q _? provides such a high temperature that it can be used as process input heat and accordingly Q, can be reduced accordingly. If one calculates a typical case with lithium bromide / water as the working medium system of the heat transformer, the realistic value 0.48 should be assumed as the efficiency (input heat / output heat) of the heat transformer and the losses Q = 0 should be set there is an energy saving of 48%, as indicated in Fig. 1b on the left ordinate axis.

If you only use a heat pump WP, as is known from US-A-43 50 571, you can use all of the input energy

Process part needed to supply by means of the heat pump, so that accordingly less high-quality operating energy is required. p The heat pump requires high-quality input energy Q,

P also absorbs part G of the output heat Q _{n of} the process and supplies the process part PRT with the entire input heat that the process part requires. This is given off by the heat pump and

P the input heat supplied to the process part is designated Q_ in FIG. 1a and is equal to Q in quantity. If one then calculates the conditions when exclusively using a heat pump WP working with LiBr / FO, for the efficiency of which one can realistically assume 1.70, the result is there is an energy saving of 41%, as plotted on the right ordinate axis in FIG. 1b.

If one now uses a combination of a heat transformer WT with a heat pump WP in the heat supply part WVT, it can actually be expected that there will be some degree of energy saving between 48% and 41%, as shown in FIG. 1b by the dashed line Line is shown. The heat pump and the heat transformer are not independent of one another when used simultaneously in the heat supply part WVT, since they have to divide into the output heat Q «of the process part. If, in addition to the heat transformer WT, there is also a heat pump WP in the heat supply part WVT, the input thermal energy GL of

P heat transformer in favor of the input thermal energy GL

Reduce the heat pump as required

^{Q + Q} ι ^P = ^Q 0

have to be. So input heat is drawn from the heat transformer, which enables a theoretical degree of energy saving of 48%, in favor of the heat pump, which enables a theoretical degree of energy saving of only 41%.

Surprisingly, it has now been shown that the efficiency

P T does not decrease when the ratio of GL / GL increases from 0, but initially rises to a maximum of 62% and only then drops to the lower value of 41%. This surprising effect, which manifests itself in a synergistic "amplification factor" explained below with reference to FIG. 2, can be attributed to the fact that the heat energy GL, which is highly transformed in temperature by the heat transformer WT, passes through the heat cycle and thus also the heat transformer several times, since the heat transformer and the heat pump are coupled to one another at least via the heat flow Q in the process part. The heat transformer and the heat pump can also be thermally coupled directly, in which case the output heat of the heat transformer

PT is partially or completely supplied in the form of thermal energy Q directly to the heat pump. Heat supply parts where the whole

Output heat of the heat transformer is supplied to the heat pump,

PT, ie GL and GL are both zero, are shown in FIGS. 6, 7 and 8. The relationships described above also apply if the heat loss Q _{y is} not equal to zero. Assuming a loss share of 15%, the output heat of the process part is reduced accordingly and thus the maximum degree of energy savings that can be achieved with the heat transformer, it is then only 41%. When using a combination of a heat transformer and a heat pump, however, there is a maximum corresponding to an energy saving of 56.5%. With a loss share of 30%, the saving of the primary operating energy for the process, which can be achieved with the heat transformer alone, is reduced to 34%, nevertheless, by combining a heat transformer with a heat pump, energy savings of 51% can still be achieved.

A first example of how the inventive principle explained with reference to FIGS. 1a and 1b can be realized is shown schematically in FIG. 2. The heat supply part WVT here contains a two-stage heat pump in combination with a two-stage heat transformer, which together contain eight exchange units, that is, only two more than for a two-stage heat transformer of the type shown which requires six exchange units alone, or a heat pump of the shown type alone, which would also need six exchange units, are required.

The two-stage heat pump part WP of the absorber device forming the heat supply part WVT contains six exchange units A to F which are connected to form a single working medium circuit. The term "exchange unit" is defined in the above-mentioned European patent application, and the type of representation in an (In p) / (- 1 / T) diagram, which is used throughout, is explained in this publication. Heat quantity units that are supplied to an exchange unit are shown in FIG. 2 by an arrow pointing to the exchange unit in question; Heating units that are removed from an exchange unit are identified by an arrow pointing away from the exchange unit in question. A unit of thermal energy (hereinafter referred to as "heat") of a relatively high temperature T is supplied to the exchange unit A of the heat pump part operating as the expeller. (When the term "temperature" is used here and below, temperature ranges are generally meant). In the exchange unit B operating as a condenser, a heating unit is heated at a lower temperature T _? free. The third exchange unit C works as an evaporator and absorbs one unit of heat. In the fourth exchange unit D, which works as an absorber, a heating unit is released again at the temperature T_. The exchange unit E, which works as a second evaporator ⁽ desorber), must in turn be supplied with a heating unit at the temperature T. In the sixth exchange unit F, which works as a second absorber, a heating unit is again released at the temperature T. In the above and the following description, the losses which are inevitable in practice are neglected, but this does not change the principle.

The heat pump part is combined with a two-stage heat transformer part WT, which contains the exchange units C to H and which has the four exchange units C to F in common with the heat pump part. G works as a capacitor and H as an expeller (desorber). The absorber device resulting from the combination is coupled to the process part PRT, which requires input heat of temperature T_ and emits output heat of temperature T. A heat unit of temperature T is supplied to the exchange unit A of the heat pump WP from an external heat supply or operating heat source WQ.

The two-stage heat pump A - F supplies three units of heat to the process, but can only absorb two heat units from the process. The third unit of the heat given off by the process is thus available for driving the heat transformer, which then 1 r _u _ heat units of temperature T _? delivers to the process, where r _ω _ is the efficiency of the heat transformer, which is known to be a value has less than 1. An overall efficiency r * is therefore expected.

r * = Q (T ₂ ) / Q (T ₃ ) = r _{wp +} r _wτ ,

where r _{ωp is} the efficiency of the heat pump. Surprisingly, the efficiency r ** that can actually be achieved is considerably greater, for the following reasons: The heat transformer WT at T _? delivered heat quantity 1 r passes through the process and is then available as additional drive heat of the heat transformer.

After going through the process again, there is another

2 additional amounts of heat of the amount 1 r _w _r _wτ = r _ω _ available etc. If these additional amounts are added up

, 2 3 4 ^r wτ ^Γ WT ^Γ WT ^Γ WT -

, we get r _uτ / (1-r _u _), which is greater by the "gain factor 1 / ⁽ 1-r _u _) than the expected contribution r _{u of} the heat transformer.

The overall efficiency r ** of the heat supply part is therefore actually r ** = r + r / (1-r) P WT WT

In Fig. 2, the theoretical efficiency r = 2/3, so that the gain factor for the contribution of the heat transformer is equal to 3. This principle applies in general to the combination of a heat pump and a heat transformer, which are coupled via a process. The process thus receives more input heat and therefore also delivers more output heat, so that theoretically, with one primary heating unit of temperature T, five heating units of temperature T_ can be generated. In practice, these ideal relationships cannot be realized, of course, but

Efficiency ⁽ ratio of the input heat required by the process Q

P ^(Fig. ^1a)) are from about 3.8 to 4.1 to even more to reach ^'heat to the actually required operation Q in practice. The final waste heat is released in the exchange unit G of the heat transformer operating as a condenser at a desired low temperature T _n and is absorbed by a heat sink WS such as the ambient air, cooling water or the like. It is particularly advantageous if the waste heat is used to preheat the process material.

Surprisingly, it is still found that the high efficiency does not have to be bought with correspondingly increased investments. On the contrary, the opposite can be achieved. If one takes as a rough measure of the investment, the ratio of the size of the heat exchanger surfaces in the exchange units to the number of input heat units supplied to the system and one assumes that the size of the heat exchanger surfaces is approximately proportional to the sum of the absolute values of the heat quantities converted in all heat exchanger units of the heat supply part is the result for a single-stage heat transformer, the ratio 4: 1 = 4.0, while the question ^'ratio for the system of Figure 2 are identical. 12: 5 = 2.4 is, therefore 40% lower than the single-stage heat transformer is . For real efficiencies when using the LiBr / H-0 working fluid system, the respective ratios are 4.4 and 2.6 respectively. The greater complexity of the configuration according to FIG. 2 is therefore more than compensated for by the smaller heat exchanger surfaces.

In the following, the vertical arrows on the exchange units only show qualitatively (and not quantitatively) whether heat is supplied or removed from an exchange unit.

The principle explained above can be implemented in a wide variety of ways, and the temperature T, the primary operating heat, the temperature 1 - of the input heat supplied to the process, the temperature 1. Of the heat to be removed from the process and the temperature Tg of the final waste heat and thus choose the distances between these temperatures practically arbitrarily, as in the following using Embodiments should be shown. For thermodynamic reasons it always applies that the greater the difference T, -T _n and the smaller the difference T - T, the higher the efficiency. is. The primary operating energy can also be supplied in whole or in part in the form of mechanical work W via at least one compressor, as will be explained with reference to FIGS. 73 to 96.

In the following figures, only the heat supply part of the system is shown; the source WQ for the primary operating heat of the temperature T, or the mechanical work W, the process part, the input heat of the temperature T_ is supplied and the output heat of the temperature J. and the heat sink WS, which absorbs the waste heat of the temperature T _n , are omitted for simplification. As explained in the above-mentioned European patent specification, the working medium in the representation chosen here circles in a heat pump in the counterclockwise direction and in a heat transformer in the clockwise direction; the function of the various parts of the absorber devices is accordingly shown in the diagrams by a curved arrow.

3 shows a simple embodiment of a heat supply part which contains a single-stage heat pump part WP and a single-stage heat transformer part WT with a total of six exchange units A to F. The heat transformer part and the heat pump part have two exchange units, the exchange units C and D, in common. The exchange unit A, which works as an expeller, is fed with primary operating heat of the temperature T. Heat of temperature T _? for feeding the process, not shown, is taken from the exchange units B and D by heat exchangers. The exchange units C and F absorb heat of the temperature J. from the process via heat exchangers and the ultimate waste heat arises in the exchange unit E at the temperature T-. The heat pump-heat transformer combination shown in FIG. 3 can be modified such that it can supply input heat of several different temperatures to the process and can absorb output heat of several different temperatures from the process. This is shown, for example, in FIG. 4, which differs from FIG. 3 only in that the exchange units A, B, C, D each operate at higher temperatures than in FIG. 3, so that the temperatures of B and D or C and F no longer coincide. 4 supplies the process, not shown, with input heat of temperatures T_ and T ,. and absorbs heat from the process at temperatures T. and T. The other exemplary embodiments which are described below can also be modified in a corresponding manner.

5 shows an exemplary embodiment which also contains six exchange units which form a combination of a single-stage heat pump and a single-stage heat transformer. 3 and 4 are distributed in pairs over three pressure levels, in FIG. 5 only two pressure levels are provided, each containing three exchange units.

The embodiments of the heat supply part of a system according to the invention shown in FIGS. 6 to 10 are distinguished by a relatively large distance between T_ and T. and at the same time a relatively high efficiency. They only contain six exchange units.

6, 7 and 8, the exchange units form a single working fluid circuit. These embodiments correspond to the case mentioned with reference to FIG. 1a that the heat transformer transfers all of its initial heat to the heat source.

TP pump delivers, meaning that GL and GL are both zero. The embodiments according to FIGS. 7 and 8 differ from one another primarily by the pressure ranges in which the different exchange units work.

FIGS. 9 and 10 show embodiments for the heat supply part of a system according to the invention, which contain six exchange units, two of which are in heat exchange with one another, which is indicated by a wavy arrow. These exchange units, which operate in a temperature range between T_ and T-, do not need to be in heat exchange with the associated process part. In the embodiments according to FIGS. 9 and 10, the temperature levels can be very easily adapted to the conditions specified by the process part.

FIG. 9a shows how the absorber device shown schematically in FIG. 9 can be practically implemented. The exchange units A to E are designated with the same capital letters in both figures. Here and also in the following exemplary embodiments, which are described in more detail, it is assumed, for example, that the device works with the proven working fluid system lithium bromide / water.

The exchange unit A working as the expeller is supplied with primary operating heat, for example in the form of live steam, via a heat exchanger 10. The expeller contains a relatively water-rich lithium bromide solution, from which water is evaporated by the supplied heat, which flows through a working gas line 12 to the condenser B, from which the condensed working fluid ⁽ water ⁾ passes through a line 14 to the exchange unit E working as an evaporator , which contains a heat exchanger 16 for supplying the process output heat. The evaporated water is absorbed in the absorber F, from which the heat of absorption over a heat exchanger 18 is fed to the process as input heat. The absorber F is connected to the expeller A via a solution line 20 which contains a pump 22 and a heat exchanger 24 and which carries relatively water-rich lithium bromide solution. The expeller A is connected to a spray head arranged in the absorber F via a line 26 which carries a relatively low-water lithium bromide line, contains a throttle 27 and passes through the heat exchanger 24. From the absorber F, the relatively water-rich lithium bromide solution is passed via a line 28, which passes through a heat exchanger 30 and contains a throttle 31, into the exchange unit C working as an evaporator, in which the condenser B is arranged, so that between the exchange units B and C a heat exchange takes place. The water evaporated in C is condensed in the condenser D and the waste heat accumulating there at low temperature is passed through a heat exchanger 32 and, for. B. removed a cooling tower (not shown).

The 'chokes 15, 27 and 31 can also be formed by the line itself. This also applies to the other exemplary embodiments.

The condensed water is fed from D through a line 34, which contains a pump 36, to a spray head 40 arranged in the evaporator E. The exchange unit E can contain a recirculation device with a pump 38 in order to circulate the water contained therein via the spray head 40. The relatively low-water solution from the evaporator C is returned to the absorber F via a line 42, which contains a pump 44.

The absorber device according to FIG. 9a thus contains two absorption medium or solution circuits with the lines 20 and 26 or 28 and 42. In this way it can be achieved that the temperature difference between the process output heat fed into the exchange unit E (temperature approx .75 C) and the process input heat supplied by the exchange unit F (temperature approx. 125 - 135 ° C) becomes particularly large. In this case, however, two solution pumps are needed, namely the pumps 22 and 44. Another possibility is to not lead the line 42 into the exchange unit F, but via the heat exchanger 24 into the exchange unit A. The solution pump 22 can then be omitted.

The temperature and pressure ratios when using two solution pumps are shown in thick lines in the diagram of FIG. 9b. If only one solution pump were used, this would work in the vapor pressure diagram at the position shown in dashed lines, designated 44a, and the vapor pressure curve of the solution in line 28 would be at the dashed position 28a in FIG. 9b. The vapor pressure line at which the pump 44 operates would correspond to an H_0 concentration of 0.36, and the absorber F would therefore operate in the lower temperature range of approximately 116-125 ° C.

11 shows an embodiment of the heat supply part which contains a two-stage heat pump part WP and a one-stage heat transformer part WT.

12 shows an embodiment of the heat supply part which contains a one-stage heat pump part WP and a two-stage heat transformer part WT.

FIGS. 13 to 18 show embodiments of the heat supply part of a system in which the difference between T- and T .. is relatively small, but the efficiency is very high. . The embodiment according to Figure 13, the sequence of steps (always starting from the stage, which is the primary Betπ ^'ebsenergie supplied) heat pump ^(WP) - the heat pump (WP) - heat transformer (WT) on. The heat is given off to or taken up by the process part at temperatures T ₁ or T _{1 which are} relatively close to T _n . The difference between T and T_ is accordingly large. In the heat pump stage working with the highest pressures and temperatures, two exchange units are thermally coupled. The embodiment according to FIG. 15 has the same step sequence WP-WP-WT as the embodiment according to FIG. 13. While the exchange units of the two heat pump stages in FIG. 13 work in three different pressure levels, the exchange units of the heat pump stages in FIG. 15 work in only two pressure ranges.

FIGS. 14 and 16 show embodiments of the heat supply part of a system according to the invention with the step sequence WP-WT-WT. Here the temperatures T_ and T. are close to the temperature T, the primary operating heat that is supplied to the system. In these embodiments, two exchange units of the heat transformer stage operating at the lower temperatures are thermally coupled.

In FIG. 14a, a plant is shown in simplified form which contains a heat supply part of the type shown in FIG. -14 and is designed for the distillation of water, that is to say, for example, sea water desalination. The exchange units are in the form of towers, in which the fluids flow essentially in the vertical direction and the liquid flows down as a thin film on the surfaces of the heat exchanger elements. The heat exchanger elements contained in the various exchange units can contain tube bundles, which will be explained below with reference to FIG. 41h. 14a, for the sake of simplicity, only one tube of the respective heat exchanger tube bundle is shown. Instead of tube bundles, other heat exchanger elements can of course also be used.

The exchange unit A working as expeller is primary operating heat, for. B. in the form of superheated steam, supplied via a heat exchanger element 100. Relatively water-rich lithium bromide solution is also fed into the expeller A via a line 102, which opens into a spray head arrangement 104, which then along the Heat exchanger element 100 flows downward, water evaporates and relatively low-water lithium bromide solution accumulates in the expeller at the bottom. The water vapor generated in the expeller A flows through a baffle plate arrangement 106 into the exchange unit B working as a condenser, where the water vapor condenses on a heat exchanger element 108 and releases condensation heat thereon. The water accumulating in the condenser B flows through a line 110, which contains a throttle 112, into the exchange unit D, which works as an evaporator. The evaporator D is preferably, as is known, provided with a circulating device 114 which contains a pump and a spray head. A heat exchanger element 116 is arranged in the evaporator D and supplies the heat required for the evaporation. The water vapor generated in the evaporator D flows into the exchange unit C functioning as an absorber, where it is absorbed by relatively low-water lithium bromide solution and releases the heat of absorption to a heat exchanger element 118. The low-water lithium bromide solution in the absorber C is supplied on the one hand by the expeller A via a line 120, which contains a pump 122 and leads through a heat exchanger 124, and on the other hand by the exchange unit E, which works as a second expander, via a line 126, which is a pump 128 contains and goes through a heat exchanger 130. The water-rich lithium bromide solution formed in the absorber C is fed into the expeller A on the one hand via the line 102, which contains a pump 132 and passes through the heat exchanger 124, and on the other hand via a line 134, which contains a pump 136, through the heat exchanger 130 goes and branches into the two lines 134a and 142, fed into the second expeller E or into the desorber G. The water vapor generated in the second expeller E is fed to the exchange unit F working as a second condenser, where it condenses on a heat exchanger element 137 which forms the exchange unit G working on its inside as a desorber. In the desorber G, the lithium bromide solution fed to it from the absorber C via the line 142 is further concentrated by evaporating water. The line 142 contains a control valve 144, passes through a heat exchanger 146 and opens into the Desorber G via a device 148, which distributes the supplied solution in a thin, uniform layer over the surface of the heat exchanger element forming the desorber G.

The low-water solution produced in G is fed to the sump of the second expeller E via a line 150 which passes through the heat exchanger 146 and is conveyed from there to the C by the pump 128. The water vapor is condensed in the exchange unit H of the heat transformer part. The heat of condensation generated in H at the relatively low temperature T is waste heat and is dissipated via a heat exchanger element 152, which can be connected, for example, to a cooling tower (not shown) or the like or can be used to heat the water to be desalinated.

The water condensed in H is fed into the evaporator D via a line 154 which contains a pump 156.

The process part for water desalination described below is integrated into the heat supply part described above, but there is no fluid connection between the heat supply part and the process part.

The salt water to be processed, which is prepared in the usual way (in particular decalcified), is introduced into the heat exchanger element 108 located in the condenser B via an inlet line 157 and device, corresponding to the device 148, and is heated there by the heat of condensation generated in the exchanger unit B, creating water vapor and more concentrated brine. The steam is the desired process product and is removed from the upper part of a collecting container 160 through a steam line 162. The more concentrated brine is fed via a line 164, which contains a pump 166, into the heat exchanger element 118, which is located in the absorber C and is heated by the heat of absorption. There is steam again is fed from a collecting vessel 166 to the steam line 162, while the further concentrated brine is discharged via a line 168 which contains a pump 170 or, according to a preferred embodiment of the invention, is subjected to at least one further distillation process, as will be explained further below should.

The water vapor in line 162 has the temperature T 1 minus the temperature drop at the heat exchangers 108 and 118 and its heat content is used to cover the heat requirements of the evaporator D and of the second expeller E. For this purpose, the line 162 can be connected to input lines 172 and 174 of the heat exchanger element 116 arranged in the evaporator D or a heat exchanger element 176 arranged in the second expeller E, where the water vapor condenses to liquid, pure water, which flows via a water collecting line 178 the intended use is supplied.

If the pressure difference prevailing on a line is sufficient to convey the liquid in question, the pump in question (e.g. pump 122, 136, 144, 166, 170) can be replaced by a control element.

As can be seen from FIG. 14b, the water vapor in B and C arises at a temperature of about 120 C under typical operating conditions, while the exchange units D and E have input heat of a temperature T 1. of only 100 <C are required. A certain temperature difference of, for example, 5 to 7 C between the input heat of the exchange units D and E and the heat at which the water vapor is generated is expedient since the larger this temperature difference, the smaller the heat exchanger surfaces and thus the plant is. However, there is still a temperature difference of 13 to 15 C, which is advantageously used by not connecting the steam line 162 directly to the input lines 172 and 174, but one or more Distillation towers 180 of a conventional type interposed, which can work according to the so-called multi-stage process and require a temperature difference of about 3 to 6 C for operation. The brine is then fed via line 168 into the distillation tower arrangement, which is shown only schematically in FIG. 14a. The distillation tower arrangement is also connected in series between the steam line 162 and the inlet lines 172, 174 via a three-way valve 182 and a shut-off valve 184. The brine ultimately produced in the distillation tower arrangement is discharged via a line 186, and the pure water which is produced is fed into the water collecting line 178. Since the usable temperature range is above 100 ° C., the additional distillation towers can work in the range of atmospheric pressure.

With the system described, an efficiency of approximately 3.4, based on the primary heat of temperature T supplied to expeller A, can be achieved without distillation tower arrangement 180. If an additional distillation tower 180 is used, this efficiency doubles, if two distillation towers are used, this efficiency triples, etc. The efficiency of the system, based on the primary energy requirement, is comparable to that of the best known systems that work with vapor compression even without a distillation tower 180 .

The heat conversion in the exchange units D and C is three times as large as in the exchange units A, B, C and F, which is indicated by a correspondingly broader representation of the units in question. In practice, a pump in a water or solution line can be replaced by a simple control valve if the pressure difference on the line in question is sufficient to ensure the necessary liquid throughput. You can also reduce the number of solution pumps at the expense of efficiency or the temperature difference T-, - T., as shown in Fig. 9a has been explained.

FIG. 14b is, for example, a steam pressure diagram corresponding to FIG. 9b for the heat supply point of the system according to FIG. 14a. As mentioned, the work equipment system is LiBr / H_0.

FIGS. 17 and 18 show two embodiments with the step sequences WP-WP-WT and WP-WT-WT, in which the exchange units work in only two different pressure levels. 17, similar to FIGS. 13 and 15, has the relatively narrow temperature range T - T. close to T _n , in FIG. 18 this temperature range is similar to that in FIGS. 14 a and 16 close to T,. These systems are suitable for the NH, / H _? 0.

Figures 19 to 21 show four-stage heat supply parts for a system according to the invention. 19 and 20, the step sequence is Is-WP-WP-WT-WT. The temperature interval T_-T. lies approximately in the middle between T, and T-. In the ^" highest temperature stage and the lowest temperature stage, there are two exchange units in internal heat exchange with each other. ^' Fig. 21, the two-stage heat transformer part WT contains only a single working fluid circuit. The temperature interval ^~ --r ^~ _* is close to T-, so that these systems are particularly suitable for the separation of temperature-sensitive substances.

22 and 23 show four-stage absorber devices, each with ten exchange units, which work in pairs in five different pressure ranges. In Fig. 22 the step sequence is WP-WP-WP-WT, in Fig. 23 WP-WT-WT-WT. FIG. 23 is similar to FIG. 14 and differs from it essentially only by two further exchange units I and K, which form with the exchange units G and H a heat transformer circuit in which H and I are in heat exchange with one another. The vapor pressure diagram for the absorber device according to FIG. 23 is shown in FIG. 23a. The device according to FIG. 23 is used as the expeller Exchange unit A is supplied with a unit of operating heat. The exchange unit B supplies one unit and the exchange unit C four units of heat of temperature J. to the process, not shown. The exchange unit D absorbs four units of process output heat and the exchange unit E one unit of process output heat of temperature T. from the process, and the exchange unit K emits one unit of waste heat to the environment. In comparison to Fig. 14, the temperature difference is T - T. somewhat lower, namely 20 C instead of about 25 C, but the efficiency is higher, namely about 4 to 4.2. The device according to FIG. 23 can be operated similarly to that according to FIG. 14a.

Figures 24 and 25 show four-stage absorber devices with only four pressure levels. The step sequences are WP-WP-WP-WT or WP-WT-WT-WT. In the former case, the temperature interval is T _? -T_, at low temperatures, say in the vicinity of T, while in the case of ^'Fig. 25 this temperature interval so high in the vicinity of T, is located.

FIGS. 26 to 29 show absorber devices which are distinguished by a particularly large distance between T and T. In all of these devices, two exchange units are in heat exchange with one another. This heat exchange can be complete, but it does not need it. Thus, in FIGS. 26 and 27, heat T can be supplied or removed at a temperature T between T_ and T ₁ depending on how the heat exchange is designed.

The absorber devices according to FIGS. 26 and 27 contain a heat pump-heat transformer combination with a single working fluid circuit according to FIG. 6. In FIG. 26, this combination is preceded by a simple heat pump circuit which has two exchange units in common with the combination. In FIG. 27, the combination is followed by a simple heat transformer circuit, which exchanges E and F with the combination has in common. A vapor pressure diagram for the absorber device according to FIG. 27 is shown in FIG. 27a. The distance T ^ -T. here is 113-50 = 63 ° C, so that this system is well suited for drying paper or lignite, for example, which is heated in power plants.

The absorber devices according to FIGS. 28 and 29 differ from those according to FIGS. 26 and 27 in that they have an additional exchange unit X and Y. The working fluid throughput can now be largely freely selected in all three stages, and an additional one can then be selected Temperature range T. or T _ remove or supply heat. The configurations according to 6, 7 and 8 can be modified by such an additional exchange unit X or Y.

30 shows a further exemplary embodiment of an absorber device which operates at a temperature range T between ^~ and T. Can absorb heat from the process or give it to him. Fig.

31 shows an exemplary embodiment of an absorber device which is located in a between T- and T-. lying temperature range T _? Can give off heat to the process or absorb from it. Here, too, the heat exchange represented by a wavy arrow is not complete, ie that in FIG. 30 the heat-exchanging unit does not have to supply all the heat that the heat-absorbing exchange unit requires. For the absorber devices according to Fig.

The same applies to 32 to 35; here too, if the heat exchange is incomplete, an additional temperature range T is available for the absorption of heat from the process or the transfer of heat to the process.

FIGS. 36 to 38 show further exemplary embodiments with different positions of the different temperature ranges. The. System according to Fig. 38 can be modified by omitting the connections between D and F and between C and E when there is complete heat exchange between E and D. 39a-39r shows a series of heat pump configurations with increasing efficiency, which can advantageously be used in a system according to the invention. 39 has the lowest efficiency and that according to FIGS. 39p and 39q have the highest efficiency. However, with increasing efficiency, the number of exchange units and thus the expenditure on equipment increases. However, there are many applications in which one of these two factors is relevant and it is a great advantage of the present invention that an optimal configuration is available for each special case.

Figures 40a to 40r show heat transformer configurations with increasing efficiency. By combining a heat transformer part according to FIG. 40 and a heat pump part according to FIG. 39, advantageous systems according to the invention can be realized. You can either choose one of the heat pump configurations as a starting point and supplement it with a heat transformer part, or you can start from an advantageous heat transformer configuration and combine it with a suitable heat pump configuration.

FIGS. 41 to 45 show how the heat pump configuration according to FIG. 39b can be combined with a heat transformer part. The configuration according to FIG. 39b is emphasized by thicker lines. It is generally true that there are special advantages if the combined heat transformer and heat pump configurations have as many exchange units as possible in common. For example, a combination of the configurations according to FIG. 68 corresponding to FIG. 39q and 40q only a single exchange unit more than one of these configurations alone.

In Fig. 41 the heat pump according to Fig. 39 is the simplest Heat transformer acc. 40a combined, which contains four exchange units, of which it shares three with the heat pump. FIG. 42 shows a combination of the heat pump according to FIG. 39b with the heat transformer according to FIG. 40c. 43 shows a first combination of the heat pump according to FIG. 39b with the heat transformer according to FIG. 40b. Fig. 44 is a combination of Fig. 39b with Fig. 40d and Fig. 45 is a second possible combination of Fig. 39b with Fig. 40b.

41a to 41i will now be used to explain how the absorber devices according to. 41 and 42 can be practically implemented. FIG. 41a shows the diagram of FIG. 41 again, the exchange units being labeled A to K. Fig. 41b shows in a simplified manner how the arrangement with the exchange units A to K can be implemented if the system is to be accommodated in a room of limited height: the exchange units are then not designed like a tower, as in Fig. 9a, but are essentially horizontal extending, elongated housing, as shown for example in section in Fig. 41b.

The exchange unit A 'working as an expeller contains a heat exchanger element 200 for supplying the primary operating heat of the temperature T ,. The resulting water vapor is condensed in the condenser B, the resulting water flows via a line 202, which contains a throttle 204, into the evaporator C, to which heat of the temperature T. is fed via a heat exchanger element 206. The evaporated water is absorbed in absorber D. The water-rich solution formed in the absorber D flows via a line 208, which leads through a heat exchanger 210 and contains a throttle 212, into the second expeller E, to which heat of the temperature T _{1 is} fed from the process via a heat exchanger element 214. The expelled steam is partly absorbed in the second absorber F and partly condensed in the second condenser K, which contains a heat exchanger element 216, via which the resulting heat of condensation of temperature T ₀ ⁽ waste heat ^{) is} removed. The water-rich solution formed in the absorber F is fed via a line 218 which contains a pump 220 and introduced into the first expeller A through a heat exchanger 222. From the expeller A, relatively low-water solution is introduced into the absorber F via a line 224, which passes through the heat exchanger 222 and contains a throttle 226, via a spray head. From the second expeller E, a relatively low-water solution is introduced into the absorber D via a line 228, which contains a pump 230 and leads through the heat exchanger 210. From the second condenser K, the condensed water is introduced via a line 232, which contains a pump 234, into the evaporator 206, which is provided with a recirculation device 236. If the system is used similarly to that according to FIG. 14a for water desalination, the treated raw water is fed via a line 238 to a heat exchanger element 240 arranged in the condenser B, where water vapor is generated by the heat of condensation. The water vapor is separated from the brine in a vessel 242 and fed to a vapor manifold 244. The brine is passed out of the vessel 242 through a heat exchanger element 246 arranged in the absorber D, where steam is generated again, which is separated from the remaining brine in a second vessel 248 and fed to the steam collecting line 244. The brine from the vessel 248 is fed to a heat exchanger element 250, which is located in the second absorber F. The resulting steam is separated from the brine in a vessel 252 and fed to the steam collecting line 244. The brine is removed from the vessel 252 via a line 254. Lines 244 and 254 correspond to lines 162 and 168 in FIG. 14a and, like these, can lead to one or more distillation towers (not shown in FIG. 41b), from which steam corresponding to a lower condensation temperature is then introduced into heat exchanger elements 206 and 214 .

By means of two further exchange units G, H, the absorber device according to FIG. 41 can be made as shown in FIG. 42, as shown in broken lines in FIG. 41a. One possibility of realizing these additional exchange units is shown in FIG. 41c. Part of the water-rich solution from D is over a ,

- 30 -

Line 256, which contains a valve 258 and leads through a heat exchanger 260, is fed through a heat exchanger element 216 arranged in the condenser K to the exchange unit G working as a desorber. The steam which is generated by the heat of condensation supplied via the heat exchanger element 216 is condensed in the exchange unit H, which works as a condenser, the heat of condensation of the temperature T is fed to a cooling tower or the like. The condensed water is fed from H into the evaporator C via a pump 266. The relatively low-water solution from the desorber G is fed to the suction side of the pump 230 via a line 268, which contains a pump 270 and leads through the heat exchanger 260. The remaining part of the system, not shown in FIG. 41c, can be constructed as described with reference to FIG. 41b.

In Fig. 41c a triple exchange unit E-F-K is required, this can be designed as it is shown in more detail in Fig. 41d. The heat exchanger elements 214, 250 and 216 can, as shown, consist of coils or tube bundles.

If the base area of the system is limited and replacement units in the form of towers are to be used instead of exchange units with horizontally elongated housings, a configuration can be used as shown in vertical section in FIG. 41e and in cross section in FIG. 41f is. In Fig. 41e, the heat exchanger elements 214, 250 and 216 are each only symbolized by a single tube, in which. In practice, it can be tube bundles, as shown in section in Fig. 41f. The tube bundles can also be arranged in different sectors of the tubular housing, as shown in FIG. 41g.

FIG. 41h shows a system part corresponding to FIG. 41c, in which only double exchange units are required and the pump 230 omitted. Here, the condenser K fed by steam from E is housed as a heat exchanger element in the exchange unit G, which is located in the same housing as the exchange unit H. The condensed water from K is fed into the evaporator C via an expansion tank 272 and a pump 274. The exchange units E and F share a second housing. The low-water solution from E is fed into the desorber G via a line 276, which leads through a heat exchanger 278 and contains a throttle. The relatively low-water solution from the desorber G is introduced into the absorber D via the line 228, which contains the pump 270 and leads through the heat exchanger 278. The other parts of the system are designed as explained with reference to FIG. 41b.

41i shows the vapor pressure diagram for the absorber device according to FIG. 41b with solid lines and the supplemented unit according to FIG. 41c with dashed lines. One sees that is reduced by the zusätz¬ exchanges units G and H, the waste heat temperature of about 45 ° C ^_ in setting-in accordance with Fig. 41b to just over 20 ⁹ in the apparatus of FIG. 41c, which with a corresponding improvement the efficiency is connected.

43a a plant is shown in more detail, which contains a heat supply unit according to FIG. 43 and can be used, for example, for water desalination. The exchange unit A working as the expeller is supplied with operating heat of the temperature T 1, for example in the form of superheated steam, via a heat exchanger element 300. Relatively water-rich lithium bromide solution is also fed into the expeller A via a line 302. The steam produced condenses in a heat exchanger element 304 arranged in the condenser B, to which raw water which has been treated is fed via a line 306. The steam generated in the heat exchanger element 304 is separated from the brine in a vessel 308 and fed to a steam collecting line 310. The water condensed in the condenser B is fed in via a line 312 which contains a throttle 314 the exchange unit C operating as an evaporator, which is provided with a water circulation device 316. The heat of vaporization is supplied by a heat exchanger element 318, which is arranged in C and is heated by condensation of steam, which is supplied to it from line 310 either directly or, as in FIG. 14a, via one or more distillation towers 320 and line 324 .

The brine from the vessel 308 is passed via a line 324, which contains a pump 326, into a heat exchanger element 328, which is arranged in the exchange unit D working as an absorber and is heated by the heat of absorption, which is due to the absorption of the water vapor by the relative low-water solution is generated, which is fed into the absorber D via a line 330 from the exchange unit E operating as expeller. The line 330 contains a pump 332 and leads through a heat exchanger 334. The relatively water-rich solution is introduced into the expeller E from the absorber D via a line 336, which contains a pump 338 and leads through the heat exchanger 334. The steam generated in the heat exchanger element 328 is separated off in a separating vessel 340 and fed to the steam collecting line 310. The remaining brine is introduced from the separation vessel 340 via a line 342, which contains a pump 344, into a heat exchanger element 346, which is arranged in the exchange unit F working as an absorber and is heated by the heat of condensation of the water vapor generated in the second expeller E. The resulting steam is separated in a separation vessel 348 and fed to the manifold 310. The brine is introduced via a line 350, which contains a pump 352, into the distillation tower 320, which further distillation towers can be connected in series to determine the difference between the temperature of the steam in the line 310 and the temperature in the heat exchanger element 318 and the other, steam-heated heat exchanger elements 352 and 354 is needed. From the absorber F, the relatively water-rich solution is fed via a line 356, which contains a pump 358 and through a heat exchanger 360, into the exchange unit G, which works as a desorber

ERS _ATZ SHEET initiated, which is heated by the heat exchanger element 54 connected to the steam line 324. The resulting steam condenses in the condenser H, which contains a heat exchanger element 366, through which the waste heat of the temperature T _{n is} removed. The condensed water is led from H into the evaporator C via a line 368, which contains a pump 370. The solution from the desorber G is returned to the expeller A via the line 302, which contains a pump 372 and passes through the heat exchanger 360 and a further heat exchanger 374. The relatively low-water solution from the expeller A is introduced into the absorber F via a line 376, which contains a pump 378 and passes through the heat exchanger 374. The waste heat generated in 366 can be used to preheat the raw water supplied via line 306.

43c shows how the absorber device with the exchange units A to H can be realized using horizontally extending exchange unit arrangements. Corresponding parts are designated with the same reference numerals as in Fig. 43a. In addition, two lines 307 and 309 are shown, each of which contains a control valve and are used to equalize the solution between the two solution circuits.

43d shows a modification of part of the device according to FIG. 43a. This modification can also be carried out analogously in FIG. 43c. 43a, the entire solution is passed from F to G, in FIG. 43d 'part of the solution is passed into the exchange unit A via a line 380, which contains a pump 382 and leads through the heat exchanger 374. The solution is introduced into the exchange unit F from the exchange unit G via a line 384, which contains a pump 385 and leads through the heat exchanger 360. Another part of the solution is branched off from the line 380 between the pump 382 and the heat exchanger 374 via a valve 359 and through the heat exchanger 360 into the

REPLACEMENT B _L ATT Expeller G fed. Otherwise, the arrangement corresponds to that according to FIG. 43a. The advantage of this modification is that T_ - T. is larger for given T- and T than for Fig. 43a.

The vapor pressure diagram of the absorber device containing the exchange units A to H according to FIG. 43a in the acc. Fig. 43d modified form, the efficiency of which is approximately 4.1, is shown in Fig. 43b.

FIGS. 46 to 48 show combinations which contain a heat transformer part according to FIG. 40b which is emphasized by thicker lines and which is combined with a heat pump part according to FIGS. 39a or 35c or 39d.

FIGS. 49 to 51 show combinations of the heat pump configuration according to FIG. 39g with a heat transformer configuration according to FIGS. 40a, 40b and 40g. ^•

FIGS. 52 to 54 show combinations of the heat pump configuration according to FIG. 39n with a heat transformer configuration according to FIG. 40a or FIG. 40b or FIG. 40n.

FIGS. 55 to 57 show combinations of the heat pump configuration according to FIG. 39m with a heat transformer configuration according to FIG. 40a or FIG. 40b or FIG. 40n.

FIGS. 58 and 59 show how the heat transformer configuration according to FIG. 40n can be combined with a heat pump configuration according to FIG. 39b. The heat transformer configuration could also be combined analogously to FIG. 48 by a single further exchange unit with a heat pump configuration according to FIG. 39a.

FIGS. 60 and 61 show how a heat pump configuration according to FIG. 39e is combined with a heat transformer configuration according to FIGS. 40a and 40b, respectively. Figure 62 is a combination 39e with the heat transformer configuration according to FIG. 40g.

FIGS. 63 and 64 show combinations of the heat pump configuration according to FIG. 39i with the heat transformer configuration according to FIGS. 40a and 40b. 63, which is used for a gentle concentration of temperature-sensitive substances, such as e.g. of M lch and has an efficiency of about 4.2 is shown in Fig. 63a.

FIGS. 65 and 66 show the combination of a heat transformer configuration according to FIG. 40i with a heat pump configuration according to FIGS. 39a and 39b.

FIGS. 67 and 68 show the combination of a heat pump configuration according to FIG. 39h with a heat transformer configuration according to FIGS. 40b and 40h.

69 and 70 show the combination of a heat transformer configuration according to FIG. 40h with a heat pump configuration according to FIGS. 39b and 39h. FIG. 73 shows the combination of a heat pump configuration according to FIG. 39h with a heat transformer configuration according to FIG. 40a. The exemplary embodiments according to FIGS. 67 to 70 show particularly clearly the high apparatus savings which can be achieved by the combinations described. Functionally, the configuration according to FIG. 39h is a three-stage heat pump. With just one additional exchange unit working at T _n , you get a combination of a functional three-stage heat pump with a functional two-stage heat transformer. 68, two additional exchange units provide a combination of a functional three-stage heat pump with a functional three-stage heat transformer. The same applies to FIGS. 69 and 70.

The heat pump part of the heat pump-heat transformer combination of a system according to the invention can also be a - 36 -

Replace or expand compressor heat pump stage as shown in Figures 72-94.

FIGS. 72 and 73 correspond to FIGS. 5 and 3 with the exception that the absorber heat pump stage WP of the devices according to FIGS. 3 and 5 is replaced by a compressor heat pump stage.

74 corresponds approximately to that of FIG. 15; 75 corresponds to that of FIG. 13; 76 corresponds to that of FIG. 16; the device according to FIG. 77 corresponds to that of FIG. 14; 78 corresponds to that of FIG. 24; 79 corresponds to that of FIG. 22; the device according to FIG. 80 corresponds to that of FIG. 20; the device according to FIG. 81 corresponds to that of FIG. 19; the device according to FIG. 82 contains the configuration according to FIG. 6 and a z-additional compressor K which is connected between the exchange units of the highest and the second highest pressure range. FIG. 83 also contains the configuration according to FIG. 6 and additionally a compressor heat pump circuit with a compressor K whose suction side is connected to the exchange units operating in the highest pressure range of the configuration according to FIG. 6 and whose outlet is connected to an additional exchange unit working as a condenser, 6 which is in heat exchange with the highest pressure range and higher temperature ranges of the configuration according to FIG. 6 and which is connected to the exchange unit of the configuration according to FIG. 6 via a conduit carrying liquid water and containing a throttle works in the lower temperature range of the highest pressure range of this configuration.

FIG. 84 again contains the configuration according to FIG. 6; the compressor K is here, however, between those in the middle and upper

REPLACEMENT LEAF 6, and in the part of the device according to FIG. 84 corresponding to FIG. 6, an internal heat exchange is provided between the exchange unit working in the upper temperature range of the middle pressure range and the exchange unit working in the lower temperature range of the upper pressure range .

The device according to FIG. 85 corresponds to that according to FIG. 26. The device according to FIG. 86 is analogous to that according to FIG. 7;

The device according to FIG. 87 is similar to that according to FIG. 86 with the exception that an additional exchange unit X is provided, so that the working medium throughput in the heat pump circuit WP and in the heat transformer circuit WT can be set independently, so that one can switch between T _? and T. lying temperature T can take heat from the exchange unit X or feed heat into the exchange unit X.

The device according to FIG. 88 is analogous to FIG. 6. The device according to FIG. 89 contains an additional exchange unit X analogous to FIG. 87, so that here too a medium temperature range T is available for removing or supplying heat .

90 corresponds to that according to FIG. 9.

91 corresponds to that of FIG. 53.

The device according to FIG. 92 is a combination of the device according to FIG. 2 with an additional compressor heat pump stage, which contains a compressor connected between the exchange units C and A.

Fig. 93 corresponds to Fig. 92 only here the compressor is connected between the exchange units E and D.

Fig. 94 corresponds to Fig. 92, only here the compressor is connected between the exchange units F and A. FIG. 95 shows a two-stage heat pump configuration of the type shown in FIG. 39c with an additional, particularly advantageous heat exchanger arrangement in somewhat more detail. The heat pump configuration according to FIG. 95 contains a first stage working in a relatively high pressure range with the exchange units A, B, E, F and a stage working in a relatively low range with the exchange units C, D, E, F The exchange units B and E are connected by a liquid working medium, such as water, carrying line 900, which contains a throttle 902. The exchange units A and C as well as C and F are connected by conventional absorbent or solution circuits 904 and 906, each of which contains a heat exchanger 908 and 910, respectively. Furthermore, lines for vaporous working fluid are provided between the exchange units A and B, between C and D and E and F (in principle line 900 could also lead from B to D).

The arrangement of the exchange units and the lines corresponds to the representation in a vapor pressure diagram, for example similar to that in FIG. 14b. B and C can be in heat exchange with each other, but this is not necessary. According to one aspect of the present invention, there is a device 912 for heat exchange between the liquid working fluid in line 900 of the working fluid circuit operating at higher pressures and a partial flow of the working fluid-rich absorbent (solution) in line 914 of the working fluid circuit or absorber operating at lower pressures ¬ tion medium circuit provided. For this purpose, the line 914 leading from F to C, which contains a pump 916 and, as said, carries working fluid-rich absorbent, for example water-rich lithium bromide solution, is provided with a branch line 918, which contains a control valve 920, through the heat exchanger 912 leads and the leading through the heat exchanger 910 Part of line 914 bridged. In the configuration shown, the line 914 leads past the exchange unit C through the heat exchanger 908 directly to the exchange unit (expeller) A. Here, too, the line 914 could serve through the exchange unit C, but then a further pump would be required between C and A.

FIG. 96 shows an entirely analogous modification of a two-stage heat transformer of the type shown in FIG. 40c. Here too, a heat exchange between liquid working fluid, which flows in a line 930 of a working fluid circuit working at relatively high pressures, takes place in the heat exchange with a partial flow of the working fluid-rich absorption medium, which flows in the absorption medium circuit of the working fluid circuit working at relatively low pressures. Since the configurations according to FIGS. 95 and 96 work quite appropriately with regard to the heat exchanger 912, a further explanation is not necessary.

95 and 96 can be used in general with all absorber devices which contain two heat pump or heat transformer stages of the type explained above. The internal heat exchange represented by a wavy part is not essential for the function of the special heat exchanger 912 described.

Finally, it should also be mentioned that in distillation and desalination plants which contain distillation towers, as is shown, for example, in FIGS. 14a and 43a, the brine also first through the distillation towers and then through those with a heat supply device equipped system can be directed according to the invention. It is also possible to change the order of the units in the system, which the brine flows through one after the other.

Claims

1.System with a process part which requires input heat energy in at least one input heat temperature range (T_) and from which heat energy in at least one output heat temperature range (T_.), Which is lower than the input heat temperature range (T_), and which has to be dissipated Heat supply part which contains an absorber device and an operating energy source (WQ), characterized in that the heat supply part (WVT) contains a combination of a heat transformer (WT) and a heat pump (WP) which supplies the input heat energy required by the process part to the process part, the output heat energy from Process part takes up and in turn between the operating energy source (WQ) and a heat sink, the waste heat in a temperature range CT _fi ), which is lower than the initial heat temperature range (T.) of the process part, from the heat supply part, is connected.

2. Plant according to claim 1, characterized in that the combination includes a heat transformer part and a heat pump part, which together contain only a single working fluid circuit ⁽ Fig. 6, 7, 26, 27).

3. Plant according to claim 1, characterized in that the heat pump and the heat transformer have at least one exchange unit in common.

4. Plant according to claim 1, characterized in that the heat pump contains a functionally multi-stage heat pump part with only a single working fluid circuit (Fig. 39 o, Fig. 39 q).

5. Plant according to claim 1 or 4, characterized in that the heat transformer is a functionally multi-stage heat transformer

REPLACEMENT LEAF contains gate part with only a single working fluid circuit (Fig. 40o, Fig. 40q).

6. Plant according to one of the preceding claims, characterized by a device for preheating the process material by the waste heat of the heat transformer part.

7. System, in particular according to claim 1 with a two-stage heat pump part, which contains a working fluid circuit working in a predetermined, relatively high pressure range and a working fluid circuit working in a relatively low pressure range with respect to the predetermined pressure range, characterized by a device for heat exchange between the liquid Working fluid in the working fluid circuit working in the relatively high pressure range and a partial flow of the working fluid-rich absorbent in the working fluid circuit working in the relatively low pressure range (FIG. 95).

8. System, in particular according to claim 1 or 7 with a heat transformer part, which contains a working fluid circuit working in a predetermined, relatively high pressure range and a working fluid circuit working in a relatively low pressure range with respect to the predetermined pressure range, characterized by a device for heat exchange between the liquid working fluid in the working fluid circuit working in the relatively high pressure range and a partial flow of the working fluid-rich absorption medium in the working fluid circuit working in the relatively low pressure range (FIG. 96).