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    • 专利摘要:
    The invention relates to a sorption system having a main circuit and an additional circuit for generating cold. The core concept of the invention is that of generating the intermediate-pressure vapor of the additional circuit not in an intermediate-pressure evaporator but rather by throttling the operating medium liquids of the two circuits to intermediate pressure and feeding the intermediate-pressure vapor resulting from the throttling to the absorber (22) of the additional circuit. In the main circuit, substantially operating medium vapor (17) is driven out from a rich solution (15), is condensed (10), is evaporated in a cold-generating low-pressure evaporator (12), and is absorbed by depleted solution (14) in a low-pressure absorber (7). The mixed vapor that is driven out is converted into operating medium vapor (17) in a rectifier (2). Most of the rectification heat is transferred to an additional circuit by introducing the rich solution (24) thereof into the rectifier (2) and coupling out again the depleted solution (20). The latter is enriched by absorption from intermediate-pressure vapor (29) in an intermediate-pressure absorber (22). The intermediate-pressure vapor (29) is formed by throttling (27) operating medium liquid (9a) of the two circuits in a separator (28). The remaining operating medium liquid (9b) is fed in the main circuit to the low-pressure evaporator (12) in a form that is already highly supercooled. For residual rectification, a small sub-stream (16) of the operating medium liquid is introduced into the rectifier (2).
    公开号:NL2019397A
    申请号:NL2019397
    申请日:2017-08-07
    公开日:2018-02-09
    发明作者:Von Reth Anno
    申请人:Von Reth Anno；
    IPC主号:
    专利说明:

    Patent center
    The Netherlands
    Θ 2019397 (21) Application number: 2019397 © Application submitted: 07/08/2017
    APPLICATION FOR APPLICATION (51) Int. CL:
    F25B 15/00 (2017.01)
    (30) Priority: (71) Applicant (s): 06/08/2016 DE 10 2016 009 681.0 Anno von Reth in Paderborn, Germany, DE. (41) Application registered: (72) Inventor (s): 09/02/2018 Anno von Reth in Paderborn (DE). (43) Application published: 13/02/2018 (74) Agent: ir. C.M. Jansen et al. In The Hague.
    ¢ 54) Method for operating a sorption system having a main circuit and an additional circuit for generating cold © The invention relates to a sorption system having a main circuit and an additional circuit for generating cold. The core concept of the invention is that of generating the intermediate-pressure vapor or the additional circuit not in an intermediate-pressure evaporator but rather by throttling the operating medium liquids of the two circuits to intermediate pressure and feeding the intermediate-pressure vapor resulting from the throttling to the absorber (22) or the additional circuit. In the main circuit, substantially operating medium vapor (17) is driven out from a rich solution (15), is condensed (10), is evaporated in a cold-generating low-pressure evaporator (12), and is absorbed by depleted solution (14) in a low-pressure absorber (7). The mixed vapor that is driven out is converted into operating medium vapor (17) in a rectifier (2). Most of the rectification heat is transferred to an additional circuit by introducing the rich solution (24) into the rectifier (2) and coupling out again the depleted solution (20). The latter is enriched by absorption from intermediate-pressure vapor (29) in an intermediate-pressure absorber (22). The intermediate-pressure vapor (29) is formed by throttling (27) operating medium liquid (9a) or the two circuits in a separator (28). The remaining operating medium liquid (9b) is fed into the main circuit to the low-pressure evaporator (12) in a form that is already highly supercooled. For residual rectification, a small sub-stream (16) or the operating medium liquid is introduced into the rectifier (2).
    NL A 2019397
    This publication corresponds to the documents originally submitted.
    P116419NL00
    Title: Method for operating a sorption system having a main circuit and an additional circuit for generating cold
    The invention relates to a method for operating a sorption system, in particular for the two-substance mixture ammonia and water, having a main circuit and an additional circuit.
    For generating cold, sorption systems containing this twosubstance mixture have long been prior art (Wilhelm Nibergall: SorptionsKaltemaschinen in: Rudolf Plank: Handbuch der Kaltetechnik Vol. VII (1959); Cube, Steinle, Lotz, Kunis: Lehrbuch der Kaltetechnik (1997)) . The sorbent has an inherent vapor pressure that has an impact on the process. Certain amounts of the sorbent are evaporated together with the operating medium when heat is supplied to the liquid sorption mixture.
    To eliminate the disadvantageous effect of the sorbent also being driven out, the vapor mixture that is driven out is subjected to rectification. During the rectification, the vapor mixture of ammonia and water is brought into contact with high-quality ammonia content.
    The vapors rising from the heating surfaces are approximately in phase equilibrium with the boiling rich solution. If the water content in the rich solution rises, the water content in the mixed vapor that is driven out also rises. This increases the required return flow amount and / or the amount of ammonia contained therein and the return flow heat that has been dissipated. It is characteristic that the required return flow heat remains relatively low up to an intermediate concentration in the rich solution, but then quickly increases as the concentration of the rich solution decreases, as a result of which the efficiency of the sorption system then rapidly falls.
    In the standard method, nearly pure ammonia liquid is introduced as a partial amount of the condensate into the cold part of the rectification process. This partial amount is not available for generating cold. The generation of this so-called reflux amount fundamentally reduces the generation of cold.
    During the rectification, both a substance exchange and a heat exchange take place between vapor and liquid. Particularly at the cold end of the rectification, excess heat is given off during the exchange process, so that in standard systems a portion of the nearly pure ammonia liquid that has been introduced has been re-evaporated there in particular.
    In the publication DANNIES, J. H .: Die Absorptionskaltemaschine. Hanover: Brücke-Verlag Kurt Schmersow,
    1951, pages 122-133, there is described an absorption system having a desorber including a rectification apparatus and two absorbers, in which system the condensed operating medium is guided into a throttle unit (throttle 4) after passing through a heat exchanger (heat exchanger ) or a throttle (throttle 2) and a further heat exchanger within one of the absorbers (absorber 2). In the throttle unit, the incoming operating medium is split into two sub-streams, one sub-stream being fed via a heat exchanger (countercurrent heat exchanger) into the evaporator and the other substrate being fed via the further heat exchanger (heat exchanger) into the other absorber (absorber 1).
    Other methods for reducing the disadvantages associated with the formation of a large reflux amount are known.
    The return flow amount has been reduced in comparison to the standard method since a partial amount or rich solution has been introduced in supercooled form into the middle section of the rectification process. The described excess heat is used to heat the solution, but at the cost of re-evaporation.
    This method step was coupled by Roland Kahn (Forschungsbericht des Deutschen Kalte- en Klima-technicalen Vereins No. 51 - 1995) with upstream method steps in order to further and the rich solution in an intermediate-pressure absorber. To this end, also nearly pure ammonia hquid is throttled to intermediate pressure and the resulting intermediate-pressure vapor is fed to an intermediate-pressure absorber.
    In DE 10 2004 039 997 B4, an additional circuit is formed into addition to a main circuit, where vapor is driven out by coupling solution or the additional circuit into the rectifier and the solution being heated. The depleted solution of the rectifier having a relatively high ammonia content can be removed from the rectifier and the rich solution can be introduced into the latter at best in slightly super cool form. The circuit of the additional circuit is closed in that a suitable quantity of ammonia liquid is lowered to intermediate pressure and is evaporated again in an intermediate-pressure evaporator and is absorbed in the intermediary pressure absorber or the additional circuit. In the overall system, cold is generated at low temperature in the main circuit and at intermediate temperature in the additional circuit. It is disadvantageous that the market demand for cold consumption at two temperature levels is low.
    The technical problem addressed is that of configuring a sorption system having a main circuit and an additional circuit in such a way that the generation of cold takes place only at one temperature level and as far as possible at the lower temperature level.
    The solution to said problem can be found in the main claim. Further vary can be found in dependent claims.
    The core concept of the invention is that of generating the intermediate-pressure vapor or the additional circuit not in an intermediary pressure evaporator as in DE 10 2004 039 997 B4 but rather by throttling the operating medium liquids or the two circuits to intermediate pressure and feeding the intermediate-pressure vapor resulting from the throttling to the absorber or the additional circuit. In earlier refrigeration systems, this throttled vapor does not contribute to generating cold. Now, only the remaining operating medium liquid must be considered in the main circuit: During the subsequent throttling from intermediate pressure to low pressure, now only a small amount of throttled vapor is produced. Compared to the method according to DE 10 2004 039 997 B4, the amount of liquid generating low-temperature cold through evaporation increases. No intermediate-pressure vapor has been fed to the absorber or the additional circuit from an intermediate-pressure evaporator, and no portion of operating medium hquid need be branched off after the condenser for this purpose.
    To increase the amount of vapor in the rectification process through partial evaporation or the introduced rich additional solution, the latter is not introduced in supercooled form. A small reflux amount has been introduced in order to complete the rectification.
    Advantages of the invention
    In systems, for example according to the Handbuch der Kaltetechnik Vol. VII (1959), the efficiency decreases as the temperature of the generated cold decreases. This progressive drop in efficiency is largely avoided by the method steps according to the invention. The present invention is tailored to systems having a high water content in the vapor that is driven out.
    The cold generation achieved is approximately as high as that achieved according to DE 10 2004 039 997 B4 as the sum of the cold generation at two temperature levels.
    In the operating method according to the invention, preferably ammonia is used as the operating medium and water is used as the sorbent.
    In the operating method according to the invention, also in the additional circuit, the temperature of the generated cold is lowered to that of the main circuit. In addition, most of the rectification heat is transferred to the additional circuit and, compared to the standard system, less return flow hquid is formed in the main circuit and is used for residual rectification. The heat transferred to the depleted solution or the additional circuit in the rectifier is used - in a solution heat exchanger - to heat the rich solution or the additional circuit to boihng point. Since the latter solution was introduced in non-supercooled form, the amount of vapor during the rectification still increases.
    As a first advantageous embodiment, the following method step may be provided: after the rich solution of the additional circuit has been coupled out of the rectifier, a further exchange stage (exchange tray) is arranged in the latter, to which there is fed only enriched return flow hquid from the main circuit.
    A further advantageous embodiment may be consistent in that the first sub-stream or nearly pure operating medium liquid or the main circuit is fed from the separator to an aftercooler inserted in the main circuit.
    One alternative according to the invention using an aftercooler may be configured as follows. An additional method step is provided:
    • the main stream of nearly pure operating medium liquid from the main and additional circuit is split into two sub-streams after the condenser, • the first sub-stream of nearly pure operating medium liquid or the main and additional circuit is fed to the separator, and • the second sub-stream or nearly pure operating medium liquid or the main circuit is fed to the aftercooler inserted in the main circuit.
    Another preferred embodiment may be consistent in that additionally an intermediate-pressure evaporator is inserted in the main and additional circuit, and the nearly pure operating medium liquid is throttled to intermediate pressure, where a resorption sub-circuit is formed which is operated between intermediate and low pressure and which substantially comprises • an intermediate-pressure absorber for absorbing intermediate-pressure vapor, • a degasser for generating low-pressure vapor, and • a solution heat exchanger, with intermediate-pressure vapor from the intermediate-pressure evaporator or the main circuit is fed to the intermediate-pressure absorber and low-pressure vapor from the degasser is fed to the low-pressure absorber or the main circuit, furthermore the following method steps are provided:
    • a second stream of nearly pure operating medium liquid from the main and additional circuit is fed to an intermediate-pressure evaporator or the main and additional circuit, • intermediate-pressure vapor from the main and additional circuit is fed from the intermediate-pressure evaporator or the main and additional circuit to the intermediate-pressure absorber or the main and additional circuit, • both depleted solution from the additional circuit and depleted solution from the resorber sub-circuit are fed to the intermediate pressure absorber or the main and additional circuit for joint absorption, and both rich solution from the resorber sub-circuit and rich solution from the additional circuit are removed from the intermediate-pressure absorber of the main and additional circuit and thus the circuits of the main and additional circuit are separated again, the intermediate- pressure evaporator or the main circuit being expanded to become an intermediate-pressure evaporator or t the main and additional circuit, and the intermediary pressure absorber or the additional circuit being expanded to become an intermediate-pressure absorber or the resorber sub-circuit, and of the additional circuit.
    The invention will be explained below with reference to drawings. Four figures are appended.
    In the figures:
    FIG. 1 shows a sorption system with vapor generation for the additional circuit by means of a separator and final rectification in the main circuit;
    FIG. 2 shows a sorption system with vapor generation for the additional circuit by means of a separator and downstream aftercooler in the main circuit and final rectification in the main circuit;
    FIG. 3 shows a sorption system with vapor generation for the additional circuit by means of a separator and a parallel-connected aftercooler in the main circuit and intermediate rectification in the additional circuit, and
    FIG. 4 shows double cold generation by means of an inserted resorption sub-circuit with vapor generation for the additional circuit by means of a separator and intermediate-pressure evaporator and final rectification in the main circuit.
    FIG. 1 shows a standard system using the two-substance mixture ammonia and water proceeding from DE 10 2004 039 997 B4 with a main circuit and an additional circuit, the system being configured and expanded according to the invention.
    A desorber (1) is supplied with heat from outside by a heat exchange medium (5). The desorber (1) is fed rich solution (15) from the main circuit, said solution being fed from the absorber (7) or the main circuit via a solution heat exchanger (19) or the main circuit. By means of the heat supply, a mixed vapor or operating medium (ammonia) and sorbent (water) and depleted solution (14) or the main circuit is formed. This mixed vapor is removed from the desorber (1) and passed through the solution heat exchanger (19) or the main circuit, it is cooled by heat dissipation and the rich solution (15) or the main circuit is heated in countercurrent.
    The depleted solution (14) or the main circuit is lowered to the low-pressure level by means of a main circuit throttle (6) and is enriched again in the low-pressure absorber (7) or the main circuit with dissipation of heat.
    The mixed vapor or operating medium and sorbent that is generated in the desorber (1) is fed to the rectifier (2), and nearly pure high-pressure operating medium vapor (17) is generated in multiple exchange functions (exchange trays 3a, 3b, 3c ). This vapor is fed to a condenser (10) and is fully condensed while dissipating heat to a third cooling medium (31b).
    The nearly pure operating medium liquid (9) that is produced is split into the return flow liquid or the main circuit (16) and into the main stream or nearly pure operating medium liquid (9a) or the main and additional circuit. The return flow liquid or the main circuit (16) is introduced into the uppermost exchange tray (3a). Here, the amount of return flow liquid is measured out for the rectification of the inflowing mixed vapor from the exchange tray (3b) located therebelow.
    The low-pressure vapor (18) or the main circuit thus produced is absorbed by the depleted solution (depleted or operating medium) (14) or the main circuit in the low-pressure absorber (7) or the main circuit. The absorption heat is transferred to a cooling medium (31). The rich solution (15) or the main circuit thus formed is brought to the high-pressure level or the desorber by means of a first main circuit solution pump (8).
    The main stream or nearly pure operating medium liquid (9a) or the main and additional circuit is lowered to intermediate pressure by means of a throttle (27) or the two circuits and is fed to a separator (28) or the two circuits. As a result of the throttling, intermediate-pressure vapor (29) or the additional circuit and a first operating medium sub-stream (9b) or the main circuit are formed. The two phases are separated in the separator. This first operating medium sub-stream (9b) is lowered to low pressure by a first throttle (11a) or the main circuit and is fed to a low-pressure evaporator (12) or the main circuit and evaporated with heat absorption. From this low pressure evaporator (12), cold is fed to a cold consumer (4) via the cold transport circuit (13).
    The low-pressure vapor (18) or the main circuit thus generated is absorbed by the depleted solution (depleted or operating medium) (14) or the main circuit in the low-pressure absorber (7) or the main circuit. The absorption heat is transferred to a first cooling medium (31). The rich solution (15) or the main circuit thus formed is brought to the high-pressure level or the desorber by means of a first main circuit solution pump (8).
    The intermediate-pressure vapor (29) or the additional circuit is absorbed by the depleted solution (depleted or operating medium) (20) or the additional circuit in the intermediate-pressure absorber (22) or the additional circuit, with dissipation of heat. The absorption heat is transferred to a second cooling medium (31a). By means of an additional circuit solution pump (23), the resulting rich solution (24) or the additional circuit is brought to the high-pressure level of the desorber. After the solution heat exchanger (30) or the additional circuit, it is fed into the second exchange tray (3b) or the rectifier.
    In the main circuit, return flow liquid from the third exchange tray (3c) is introduced into the desorber (1). The depleted solution (20) or the additional circuit is discharged below the third exchange tray (3c) or the rectifier (2) and is fed to the solution heat exchanger (30) or the additional circuit. In the latter, in countercurrent to the depleted solution (20) or the additional circuit, the rich solution (24) or the additional circuit is heated approximately to boihng point. The depleted solution (20) or the additional circuit is lowered to the intermediate-pressure level by means of an additional circuit throttle (21) and is enriched again in the intermediatepressure absorber (22) or the additional circuit, with dissipation of heat.
    In the following figures, the same system parts described in previous figures are identified by the same numerals. Only the modifications to the circuits compared to what has already been shown will be described.
    In FIG. 2, aftercooler (32) or the main circuit is additionally inserted, namely in such a way that ammonia liquid or the main circuit is supercooled successively in the separator (28) and then in the aftercooler (32). In this arrangement, the first operating medium sub-stream (9b) or the main circuit is supercooled for heat dissipation by the aftercooler (32) or the main circuit in countercurrent to the low-pressure vapor (18), and the low-pressure vapor ( 18) is superheated. The first throttle (11a) or the main circuit is arranged after the aftercooler (32). This circuit is particularly suitable for systems with relatively moderate temperatures or the cold that is to be generated.
    In contrast to what is shown in FIG. 2, in FIG. 3 the separator (28) and the aftercooler (32) are connected in parallel. The main stream or nearly pure operating medium liquid (9a) is split into a second liquid sub-stream (26) or the main and additional circuit and into a second liquid sub-stream (9c) or the main circuit. This sub-stream is fed via the aftercooler (32) and the second throttle (lib) or the main circuit to the low-pressure evaporator (12). The second liquid sub-stream (26) or the main and additional circuit is lowered to intermediate pressure by means of a throttle (27) or the two circuits and is fed to the separator (28). In the separator, compared to the circuit or FIG. 1, in each case a reduced amount or intermediate-pressure vapor (28) or the additional circuit and a second liquid sub-stream (9c) or the main circuit is formed.
    This circuit is particularly suitable when the demand for intermediate-pressure vapor is approximately half that or low-pressure vapor.
    In a manner different from what is shown in FIG. 1, in FIG. 3 the depleted solution (20) or the additional circuit is collected and discharged below the second exchange tray (3b) or the rectifier. In the main circuit, the run-off from the first exchange tray (3a) is conveyed past the second exchange tray (3b) into the third exchange tray (3b). The amount of intermediate-pressure vapor is reduced slightly in comparison to the design of the rectifier (2) shown in Figs. 1.
    In FIG. 4, a system corresponding to what is shown in FIG. 1 is expanded by a resorption sub-circuit.
    For cold temperatures around 0 ° C, the method steps in systems in which cold is generated twice can be applied according to the invention. In this case, heat ratios or cold to supplied heat or just above 1 are achieved, and thus are considerably higher than in one-stage systems.
    As is known, with such a system, cold can be generated both in the intermediate-pressure evaporator and in the low-pressure evaporator. For this, a heat supply at a relatively high temperature level is required.
    The vapor driven out has a high water content. This gives rise to relatively high rectification heat upon rectification. Under these conditions, the core concept of the invention can be used to achieve a significant increase in performance by means or additional method steps.
    It is provided to generate intermediate-pressure vapor for the additional circuit not only in the separator but additionally in an intermediate-pressure desorber: A liquid sub-stream (9d) or the main and additional circuit is separated off from the separator (28) . Said sub-stream is fed, unthrottled, to an intermediate-pressure evaporator (33) or the main and additional circuit, which is at the same intermediate pressure, and is evaporated with heat absorption. From this evaporator (33), cold at intermediate pressure is fed to a cold consumer (4) via the cold transport circuit (13). From the evaporator (33), an intermediate-pressure vapor (29a) or the main and additional circuit is absorbed in an intermediate-pressure absorber (22a) or the main and additional circuit together with the intermediate-pressure vapor or the additional circuit ( 29), with dissipation of heat. The amount from the additional circuit in the liquid sub-stream (9d) or the main and additional circuit is such that the corresponding amount of vapor taken together with the amount of the intermediate-pressure vapor (29) from the separator (28) results in optimal rectification through liquid feeds according to the invention from the main and additional circuit.
    From the intermediate-pressure absorber (22a) or the main and additional circuit, both the rich solution (24) or the additional circuit and also a rich resorption solution (35) are removed and thus the circuits of the main and additional circuit are separated . The rich resorption solution (35) or the resorption sub-circuit is fed via a resorption solution heat exchanger (37) to a resorption degasser (40), said solution being lowered to low pressure by means of a resorption throttle (39) before reaching the resorption degasser (40). From the resorption degasser (40), cold is fed to a cold consumer (4) via a second cold transport circuit (13a). In the resorption degasser (40), low-pressure resorption vapor (18a) is driven out by heat absorption and is fed to the absorber (7) or the main circuit for absorption.
    Depleted resorption solution (36) is removed from the resorption degasser (40) and is raised to intermediate pressure by means of a resorption solution pump (38) and is fed via the resorption heat exchanger (37) to the intermediate-pressure absorber (22a ) or the main and additional circuit. The latter is thus fed depleted solution from the resorption subcircuit (36) and also from the additional circuit (20), said solutions usually having different concentrations of ammonia and water. In countercurrent in the resorption heat exchanger (37), the depleted resorption solution (36) is heated and the rich resorption solution (35) is cooled.
    To sum up, the invention is presented as follows:
    The core concept of the invention is that of generating the intermediate-pressure vapor or the additional circuit not in an intermediary pressure evaporator but rather by throttling the operating medium liquids of the two circuits to intermediate pressure and feeding the intermediary pressure vapor resulting from the throttling to the absorber of the additional circuit. In earlier refrigeration systems, this throttled vapor does not contribute to generating cold. Now, only the operating medium liquid must be considered in the main circuit: During the subsequent throttling from intermediate pressure to low pressure, now only a small amount of throttled vapor is produced. Compared to the method according to DE 10
    2004 039 997 B4, the amount of liquid generating low-temperature cold through evaporation increases. The rich additional solution has been introduced in a form that is not super cool, as a result of which the amount of vapor in the rectification process increases. This is completed by introduced operating medium hquid.
    List of reference signs
    In the following list, MC denotes the main circuit, AC denotes the additional circuit, RC denotes the resorption sub-circuit.
    desorber rectifier
    3a first exchange tray in the rectifier
    3b second exchange tray in the rectifier
    3c last exchange tray in the rectifier cold consumer external heat source first MC throttle
    MC low pressure absorber
    MC solution pump
    MC / AC operating medium liquid
    9a main stream or MC / AC operating medium hquid
    9b first MC main stream or operating medium liquid
    9c second MC sub-stream or operating medium liquid
    9d second MC / AC sub-stream or operating medium liquid
    MC / AC condenser
    11a first MC throttle lb second MC throttle
    MC low-pressure evaporator first cold transport circuit
    13a second cold transport circuit depleted MC solution rich MC solution
    MC return flow liquid rectified MC high-pressure operating medium vapor
    MC low pressure vapor
    18a RC low-pressure vapor
    MC solution heat exchanger depleted AC solution
    AC throttle
    AC intermediate pressure absorber
    22a MC / AC intermediate pressure absorber
    AC solution pump rich AC solution second MC / AC liquid stream
    MC / AC throttle separator
    AC intermediate pressure vapor
    29a MC / AC intermediate pressure vapor
    AC solution heat exchanger first cooling medium
    31a second cooling medium
    31b third cooling medium
    MC aftercooler
    MC / AC intermediate-pressure evaporator rich RC solution depleted RC solution
    RC solution heat exchanger
    RC solution pump
    RC throttle
    RC degasser
    权利要求:
    Claims (6)
    [1]
    CONCLUSIONS
    Use method for a sorption installation for a binary mixture of a working agent and a sorbent, which essentially comprises:
    • an expeller (1) for expelling a detergent and sorbent vapor mixture from the rich solution (15); • a rectifier (2) with at least two exchange surfaces to form substantially pure detergent vapor (17); • a condenser ( 10) for condensing the substantially pure operating vapor (17), and optionally a return cooler for partial condensing of the virtually pure operating vapor (17), and a main circuit with • a cold-producing low-pressure evaporator (12), • an absorption - unit (7) for absorption of the low pressure vapor (18), - a solution heat exchanger (19) for performing a heat exchange between poor (14) and rich solution (15), and a secondary circuit which is essentially includes:
    • a secondary absorption unit (22) for the absorption of medium pressure vapor (29), • and secondary solution pump (23) for raising the pressure of the rich solution (24) to the expulsion pressure, • a solution heat -changer (30) for performing a heat exchange between poor (20) and rich solution (24) in the secondary circuit, where • the secondary circuit is used between the expulsion pressure and the average pressure, • for the rich solution ( 24) a higher active agent content in the secondary circuit than for the rich solution (15) in the main circuit, and • a supply of the rich solution (24) from the secondary circuit to the rectifier (2), and • a the poor solution (20) is discharged from the rectifier (2) to the secondary circuit, and • in deviation from the mode of operation of a single circuit, whereby substantially pure operating fluid is supplied and evaporated, rather at least active agent vapor (17) is also expelled from the rich solution (24) of the secondary circuit and the solution of the secondary circuit is heated, characterized in that in the main circuit and in the secondary circuit as devices a separator (28) and an average pressure throttle (27) are added, and wherein the following process steps are added.
    • at least a partial flow of the operating fluid (9a) formed and substantially pure in the condenser (10) is throttled to the medium pressure, and is separated in the separator (28) into medium pressure vapor (29) of the secondary circuit and in main pressure medium pressure fluid (9b), this main pressure medium pressure fluid (9b) is throttled to the low pressure by means of the throttle in the main circuit (11a) and to the low pressure. evaporator (12) is supplied for its evaporation, • the average pressure vapor (29) is fed from the secondary circuit to the average pressure absorption unit (22) of the secondary circuit and fed into the average pressure absorption unit (22) is absorbed, • the rich solution (24) of the secondary circuit is heated at least to boiling temperature, • return liquid (16) from the main circuit is fed to the cold end (3a) of the rectifier, • where, in deviation from the mode of operation of a single circuit, the amount of the return fluid (16) is subjected to a restorification, and the amount of the rich solution (24) of the secondary circuit is so large that in combination with the return fluid (16) of complete rectification takes place in the main circuit.
    [2]
    Use method for a sorption installation according to claim 1, characterized in that, in addition, in the rectifier, in the discharge of the rectifier, after the removal of the rich solution (20) of the secondary circuit from the rectifier, an additional exchange surface (3c) is provided, and because only the outlet of the exchange surface (3a) is supplied to this additional exchange surface (3c), provided above the exchange surface (3b), fed by the secondary circuit.
    [3]
    Method of use for a sorption installation according to claim 1 or claim 2, characterized in that an aftercooler (32) is additionally inserted in the main circuit and in that the following process step is provided:
    • the first partial flow (9b) of substantially pure operating fluid from the main circuit is led from the separator (28) to an input aftercooler (32) of the main circuit.
    [4]
    Method of use for a sorption installation, according to claim 1 or claim 2, characterized in that an aftercooler (32) is additionally inserted in the main circuit, and in addition, the following process steps are provided:
    • the main stream (9a) of substantially pure operating fluid from the main and secondary circuits is split into two substreams after the condenser (10), • the first substream (26) of nearly pure operating fluid from the main and secondary circuits to the separator (28), • the second partial flow (9b) of substantially pure operating fluid from the main circuit is supplied to the inserted aftercooler (32) of the main circuit.
    [5]
    Method of use for a sorption installation, according to claim 1 or claim 2, characterized in that, in addition, a cold-producing medium-pressure evaporator (33) is inserted into the main and secondary circuits to which operating fluid of both circuits is supplied, the agent fluid was pre-throttled to medium pressure, and forming a resorption sub-circuit operating between medium and low pressure, and essentially comprising an average-pressure absorption unit for absorbing average-pressure vapor, • a degasser (40) for producing low-pressure vapor, and • a solution heat exchanger (37), wherein to the average-pressure absorption unit (22a), medium-pressure vapor (29a) of the average-pressure evaporator (33) is supplied from the main circuit, and low pressure vapor (18a) from the degasser (40) is supplied to the low pressure absorption unit (7) of the main circuit, with above and the following process steps are provided:
    • a second stream (9d) of substantially pure operating fluid from the main and secondary circuit is supplied to the medium-pressure evaporator (33); • from the medium-pressure evaporator (33), medium-pressure vapor (29a) of the main and secondary circuits are supplied to the average pressure absorption unit (22a) of the main and secondary circuits, • to the average pressure absorption unit (22a) of the main and secondary circuits both poor solution (20) of the secondary circuit as poor solution (36) of the resorption subcircuit for a common absorption, and • from the medium pressure absorption unit (22a) of the main secondary circuit, both rich solution (35) of the resorption subcircuit as well as rich solution (24) removed from the secondary circuit, whereby the main and secondary circuits are separated again, the average pressure absorption unit (22) of the secondary circuit being removed from knitted into a medium pressure absorption unit (22a) of the resorption section circuit and of the secondary circuit.
    [6]
    Method of use for a sorption installation, according to one of the preceding claims, characterized in that ammonia is used as the active agent and water as the sorbent.
    /
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    同族专利:
    公开号 | 公开日
    DE102016009681B3|2017-10-19|
    NL2019397B1|2018-07-23|
    引用文献:
    公开号 | 申请日 | 公开日 | 申请人 | 专利标题
    DE102004039997B4|2004-05-12|2006-06-14|Reth, Anno von, Dr.|Working method of a sorption plant|
    法律状态:
    优先权:
    申请号 | 申请日 | 专利标题
    DE102016009681.0A|DE102016009681B3|2016-08-06|2016-08-06|Working method of a sorption plant with main and auxiliary circuit for cooling|
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