EP2937630B1 - Procédé de fonctionnement d'un système pour un cycle fermé thermodynamique doté d'un évaporateur à plusieurs flux, dispositif de commande pour un système, système pour un cycle fermé thermodynamique doté d'un évaporateur à plusieurs flux et agencement d'un moteur à combustion interne et d'un système - Google Patents

Procédé de fonctionnement d'un système pour un cycle fermé thermodynamique doté d'un évaporateur à plusieurs flux, dispositif de commande pour un système, système pour un cycle fermé thermodynamique doté d'un évaporateur à plusieurs flux et agencement d'un moteur à combustion interne et d'un système Download PDF

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Publication number
EP2937630B1
EP2937630B1 EP15000459.6A EP15000459A EP2937630B1 EP 2937630 B1 EP2937630 B1 EP 2937630B1 EP 15000459 A EP15000459 A EP 15000459A EP 2937630 B1 EP2937630 B1 EP 2937630B1
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EP
European Patent Office
Prior art keywords
evaporator
pressure drop
working medium
individual
control device
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Not-in-force
Application number
EP15000459.6A
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German (de)
English (en)
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EP2937630A1 (fr
Inventor
Niklas Waibel
Daniel Stecher
Gerald Dr. Fast
Tim Horbach
Jens Niemeyer
Max Lorenz
Mathias Müller
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Rolls Royce Solutions GmbH
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MTU Friedrichshafen GmbH
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Publication date
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Publication of EP2937630A1 publication Critical patent/EP2937630A1/fr
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Classifications

    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25B—REFRIGERATION MACHINES, PLANTS OR SYSTEMS; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS
    • F25B39/00—Evaporators; Condensers
    • F25B39/02—Evaporators
    • F25B39/028—Evaporators having distributing means
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F22—STEAM GENERATION
    • F22B—METHODS OF STEAM GENERATION; STEAM BOILERS
    • F22B29/00—Steam boilers of forced-flow type
    • F22B29/06—Steam boilers of forced-flow type of once-through type, i.e. built-up from tubes receiving water at one end and delivering superheated steam at the other end of the tubes
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F22—STEAM GENERATION
    • F22B—METHODS OF STEAM GENERATION; STEAM BOILERS
    • F22B35/00—Control systems for steam boilers
    • F22B35/06—Control systems for steam boilers for steam boilers of forced-flow type
    • F22B35/10—Control systems for steam boilers for steam boilers of forced-flow type of once-through type

Definitions

  • the invention relates to a method for operating a system for a thermodynamic cycle according to claim 1, a control device for a system for a thermodynamic cycle according to claim 11, a system for a thermodynamic cycle according to claim 12 and an arrangement of an internal combustion engine and a corresponding system according to Claim 13.
  • the organic Rankine cycle is particularly suitable for the use of waste heat, for example in the industrial sector or for waste heat utilization of internal combustion engines, or for use in geothermal power plants.
  • the evaporator is formed Stationaritig. On the one hand, this can serve to be able to include a plurality of heat sources in the cyclic process; on the other hand, a multi-flow design of a single, integral evaporator can be advantageous as a result of the production. In such a parallel operation of multiple evaporator floods, however, there is the problem of increased susceptibility to thermodynamic instabilities.
  • the invention is therefore based on the object to provide a method for operating a system for a thermodynamic cycle, wherein the system despite a multi-flow evaporator shows a reduced tendency to thermodynamic instabilities, so that the method allows stable and safe operation of the system.
  • the invention is further based on the object to provide a control device for a system, a system for a thermodynamic cycle and an arrangement of an internal combustion engine and such a system, also achieved a reduced tendency to thermodynamic instabilities and ensures safe operation at high power output becomes.
  • a system for a thermodynamic cycle is operated with a multi-flow evaporator, wherein the evaporator has at least two evaporator flows.
  • the evaporator floods are matched to one another with regard to at least one operating parameter of the individual evaporator floods.
  • the evaporator floods are equated with respect to the at least one operating parameter. This prevents the various evaporator floods from developing into greatly differing operating states, which at the same time minimizes the risk that one of the evaporator floods becomes unstable, in particular exhibits Ledinegg instability.
  • a pressure drop across the evaporator is regulated.
  • a pressure drop across the evaporator is regulated.
  • the minimum total pressure drop to be ensured depends on an operating point of the system, in particular overheating of the working medium downstream of the evaporator. It shows that the system tends to less and less instabilities, the greater the overheating of the working medium, the farther the system is operated from the saturated steam curve of the working medium away.
  • the minimum total pressure drop to be given can be made smaller, the higher the working medium at the evaporator outlet or the downstream of the evaporator is overheated.
  • differences in the pressure drop over the individual evaporator floods are less significant as a percentage, so that a higher stability is already given insofar as the pressure drop across the evaporator is greater.
  • the pressure drop is preferably regulated as a function of an operating point of the system to a suitable desired pressure drop.
  • the pressure drop across the evaporator as a whole is here and hereinafter also referred to as total pressure drop. This is to be distinguished from the pressure drop across the individual evaporator floods, which may differ from the total pressure drop due to individual fluctuations of the evaporator.
  • a third embodiment of the method is preferred in which both the evaporator floods are matched to one another, in particular the same, with respect to at least one operating parameter of the individual evaporator floods, and a pressure drop across the evaporator is also regulated.
  • a higher-level control circuit for controlling the total pressure drop is preferably provided, wherein the equalization or equalization of the evaporator floods is achieved by a subordinate control.
  • the evaporator flows are aligned with respect to a flow of working fluid to each other.
  • the evaporator flows are equated with respect to the flow.
  • the term "flow" in particular a mass flow of the working medium is addressed by the evaporator floods. It is thus preferably ensured that each evaporator flood always accounts for the same proportion of the total mass flow of the working medium in the system.
  • the total mass flow is again preferably predetermined by a conveying device, in particular by the conveying capacity of the conveying device, which is preferably designed as a feed pump.
  • the individual evaporator flows are equalized or compared to one another with respect to a temperature of the working medium downstream of an evaporation region of the individual evaporator flows.
  • a temperature of the working medium in the region of an exit from the evaporator flows is used here. It turns out that the corresponding temperature is characteristic of the heat absorbed in the individual evaporator flow, with equality of the temperatures ensures equality of the thermodynamic state of the working medium in the floods and thus ultimately equality of mass flow through the individual evaporator floods.
  • An advantage of the use of a temperature of the working medium as operating parameters of the individual evaporator flows in the context of the method is that temperature sensors are provided in the region of the outlets from the evaporator floods anyway for monitoring the system, so that can be dispensed with additional, expensive sensors and in particular additional flow sensors.
  • this procedure is only possible if the system is operated with overheating of the working medium, since otherwise the temperatures downstream of the evaporation area in the evaporator floods are determined by the pressure prevailing there. Unless much there is a pronounced unequal distribution between the evaporator floods, wherein a single flood is not operated within the two-phase region, then there are no deviations in the temperatures of the individual floods.
  • the equalization of the evaporator floods with respect to the flow of working medium can be applied both during operation of the system with superheated working medium and during operation of the system in the wet steam area.
  • the alignment with respect to flow rates measured by flow sensors may be more accurate and therefore more stable than the relatively indirect adjustment based on the temperature of the working medium.
  • An embodiment of the method is also preferred, which is characterized in that the pressure drop across the evaporator is controlled by actuating actuators, wherein the actuators are associated with the individual evaporator flows.
  • actuators are typically provided in any case in order to be able to vary passage cross sections through the individual evaporator flows separately from one another. Thus, it requires so far to regulate the pressure drop no separate components.
  • the adjusting elements are designed as valves.
  • the passage cross sections through the individual evaporator floods - preferably independently of each other - can be adjusted in a simple and cost-effective manner.
  • An exemplary embodiment of the method is also preferred, which is characterized in that the evaporator floods are matched to one another by varying manipulated variables for adjusting elements, wherein the adjusting elements are assigned to the individual evaporator floods and limit a flow through the evaporator floods.
  • the adjusting elements are preferably designed as valves. In this respect, it is preferably the previously mentioned adjusting elements, with which preferably also the pressure drop across the evaporator is controlled.
  • the manipulated variables specify a functional position of the various control elements, so that ultimately the flow through the individual evaporator floods can be determined by presetting the manipulated variables.
  • the manipulated variables in dependence on a flow of working fluid through the individual floods and / or depending on a Temperature of the working medium downstream of an evaporation range of the individual evaporator flows are varied to equalize the evaporator floods with respect to at least one of these operating parameters.
  • the variation of the manipulated variables acting on the adjusting devices for varying the functional positions of the adjusting elements requires both a simple and cost-effective design of the system and at the same time a very precise application of the method.
  • An embodiment of the method is also preferred, which is characterized in that the manipulated variables are renormed so that an actuating element controlled with a maximum value of the manipulated variables is maximally opened.
  • a manipulated variable results for each evaporator flood, whereby one of these different manipulated variables again has one greatest value. As a rule, this does not correspond to the largest possible value for the manipulated variable, which corresponds to a maximum opening of the actuating element. If the manipulated variables determined in this way are passed on unchanged to the adjusting elements, this means that they have an overall smaller opening than would be required for equality.
  • the largest determined value of the manipulated variables is now set to the maximum possible value, which corresponds to a maximum opening of the actuating element.
  • the remaining, smaller manipulated variables are scaled linearly according to the change of the largest value.
  • actuators with linear characteristic are used in the context of the method, in particular valves with linear valve characteristic.
  • valves with linear valve characteristic are used in the context of the method.
  • the renormalization described above is possible in a particularly simple manner, with a simple, linear Scaling the various manipulated variables ensures constant ratios of the various set by the control elements flow cross sections.
  • a method is also preferred, which is characterized in that the manipulated variables are changed by the regulation of the pressure drop.
  • the pressure drop control therefore preferably acts on the manipulated variables calculated in the context of the approximation of the evaporator flows and changes their values in order to regulate the pressure drop.
  • the control of the pressure drop limits the manipulated variables. This is particularly preferred when the manipulated variables are renormed before they are forwarded to the adjusting elements. It is then namely in the context of the approximation of the evaporator floods always one of the control elements open a maximum wide.
  • An embodiment of the method is also preferred, which is characterized in that a desired flow for the working medium is calculated by the individual evaporator flows by dividing the total mass flow in the system by the number of evaporator flows. This ensures equality of the floods, each individual evaporator flood the same proportion of the total mass flow of the working medium Target specification imprinted receives.
  • the total mass flow is preferably predetermined by the conveyor, in particular by the delivery rate of the conveyor, preferably by the speed of the feed pump. It is possible that a default value for the conveyor is used as the total mass flow. Alternatively, it is possible that the delivery rate of the conveyor detected and from this a total mass flow in the system is determined, in particular calculated.
  • a flow sensor preferably in the form of a measuring turbine, downstream of the conveyor is provided, which is arranged and designed so that through it the total mass flow in the system can be detected.
  • the total mass flow is preferably used and divided by the number of evaporator flows in order to determine the target specification for each evaporator flow, which is then identical for each of the evaporator flows.
  • An embodiment of the method is also preferred, which is characterized in that a target temperature of the working medium downstream of an evaporation range of the individual evaporator floods is calculated as an average over the different temperatures of the working medium downstream of the evaporation ranges of the individual evaporator floods or as the mean temperature of the working medium downstream of the Evaporator floods is measured separately. It is thus possible for the temperature of the working medium to be measured in each evaporator flow downstream of an evaporation region, in particular in the region of a flood outlet from the evaporator flow. From the different temperature measurements of the individual evaporator floods, an average value is calculated, which is then used as the setpoint temperature in the context of the method.
  • the individual evaporator floods are adjusted to the setpoint temperature or equaled.
  • a mean temperature of the working medium downstream of the evaporator floods preferably downstream of merging the various evaporator floods, is measured and used as a target in the process.
  • thermodynamic state of the working medium in the individual evaporator floods it is possible to equate the thermodynamic state of the working medium in the individual evaporator floods.
  • this also preferably results in an equalization of the flow in the various evaporator floods, since this determines as an essential parameter overheating of the working medium in the evaporator floods.
  • an adjustment of the evaporator floods to a setpoint temperature can be particularly be carried out simply and inexpensively, especially because expensive flow sensors, which are preferably designed as measuring turbines, can be dispensed with.
  • An embodiment of the method is also preferred, which is characterized in that a desired pressure drop across the evaporator is read from a characteristic field as a function of at least one operating parameter of the system. It has been found that the pressure drop across the evaporator to be maintained for the power yield and stability of the system depends on its operating point. Too low pressure drop leads to system instabilities, while too high a pressure drop reduces the overall efficiency of the system and its power output, especially since the conveyor must work against an unnecessarily high pressure drop in the evaporator. In that regard, for each operating point of the system there is an optimal desired pressure drop, which is preferably stored in a characteristic field as a function of operating point.
  • the at least one operating parameter is preferably selected from a group consisting of a mass flow in the system, a temperature of the working medium downstream of the evaporator or at the evaporator outlet, and an overheating of the working medium downstream of the evaporator or at the evaporator outlet.
  • the characteristic field is spanned over the mass flow of the working medium and the overheating thereof. It describes the minimum presettable differential pressure across the evaporator to be maintained to ensure safe operation of the system. It should not lead to an unstable system behavior in the individual evaporator floods due to not exactly simultaneously occurring transitions in the vapor state occurring pressure fluctuations compared to the predetermined pressure drop. In particular, these pressure fluctuations should not be significant as a percentage of the total pressure drop across the evaporator. The total pressure drop is then - as already described - preferably predetermined by throttling the individual control elements of the evaporator flows.
  • the system is operated with an overheating of the working medium.
  • the individual evaporator flows are preferably adjusted with respect to a temperature of the working medium downstream of the evaporation region, in particular equal, in this way the thermodynamic state of the working medium in the individual evaporator flows and ultimately the flow through the evaporator floods can be equated. It can be dispensed with expensive flow sensors. Becomes one of the evaporator floods, for example due to the Ledinegg instability, flows through working medium less than the other evaporator floods, resulting in greater overheating of the working medium in this flood.
  • the overheating can therefore be used as a criterion for throttling the control elements.
  • An adjustment of the temperatures of the working medium causes at a given pressure downstream of the evaporator readily an approximation of the various superheaters. But it is also possible that the pressure downstream of the evaporator is detected and used to determine the overheating. This pressure determines the position of the boiling point of the working medium in the evaporator and thus the overheating at a given temperature.
  • An embodiment of the method in which the system is operated in the wet steam area is also preferred.
  • the working medium is thus not overheated, but it is generated saturated steam in admixture with liquid portions of the working medium.
  • the temperature in the evaporator and downstream of the evaporator then depends in a predetermined manner on the pressure downstream of the evaporator, so that they can not be used to equalize the different evaporator flows. Therefore, in this case, preference is given to equality with respect to the flow through the individual evaporator flows.
  • the operation of the system in the wet steam area may nevertheless be useful, in particular in connection with a waste heat recovery, because so possibly higher power yields of the system are possible, as if this is operated in the overheating regime.
  • An embodiment of the method is preferred, which is characterized in that an organic Rankine cycle process (ORC process) is performed in the system.
  • ORC process organic Rankine cycle process
  • This cycle is particularly suitable for stationary use, for example in geothermal power plants, or for waste heat recovery, especially in industrial plants or in conjunction with internal combustion engines.
  • the object is also achieved by providing a control device for a system for operating a thermodynamic cycle with the features of claim 13.
  • the control device is set up to equalize different evaporator flows with respect to at least one operating parameter of the individual evaporator flows to one another, and / or to regulate a pressure drop across the evaporator.
  • Particularly preferred is the Control device configured to carry out a method according to one of the previously described embodiments. This realizes for the control device, the advantages that have already been explained in connection with the method.
  • the control device is preferably set up to carry out such a method by being firmly implemented in an electronic structure, in particular a hardware of the control device.
  • a computer program product is loaded into the control device, which has instructions on the basis of which such a method can be carried out when the computer program product is running on the control device.
  • the control device has an interface to at least one sensor for detecting an operating parameter of the individual evaporator flows, in particular flow sensors separately assigned to the evaporator floods and / or temperature sensors separately assigned to the evaporator floods.
  • the control device preferably has an interface to a differential pressure sensor for detecting a pressure drop across the evaporator, or to two pressure sensors, a first upstream of the evaporator and a second downstream of the evaporator, wherein a pressure drop across the evaporator as a difference can be determined between the measured values of the two sensors.
  • the control device preferably has an interface to the individual evaporator flows respectively associated adjusting elements in order to be able to influence a passage cross section through the evaporator floods individually.
  • the control device preferably has an interface to a flow sensor, which is arranged upstream of a division of the working medium on the individual evaporator flows and downstream of a conveyor for conveying the working medium along a circuit of the system. In this case, a total mass flow of the working medium in the circuit can be detected by the control device with the aid of the flow sensor.
  • the control device preferably has an interface to the conveyor in order to predetermine and / or detect its delivery rate, wherein in this way information about the total mass flow in the system can be obtained.
  • the object is also achieved by providing a system for a thermodynamic cycle, in particular for operating a thermodynamic cycle, with the features of Claim 12 is created.
  • the system has a multi-flow evaporator which has at least two evaporator flows. Each evaporator flow is associated with an actuating element which is arranged and arranged for varying a passage cross section through the associated evaporator flow.
  • the system has a control device, in particular a control device according to one of the embodiments described above, wherein the control device is operatively connected to the adjusting elements and arranged to adjust by variation of manipulated variables for the adjusting elements, the evaporator floods with respect to at least one operating parameter to each other and / or one To regulate pressure drop across the evaporator.
  • an actuator is arranged upstream of an evaporation region of the evaporator flow.
  • the actuating element is arranged in front of an evaporator inlet.
  • the adjusting elements are operatively connected to the control device for driving and in particular for carrying out the method.
  • the system has - seen in the flow direction of the working medium along a circuit - a conveyor, which is preferably designed as a feed pump, the evaporator, an expansion device, and a capacitor. Furthermore, the system preferably has a temperature sensor associated therewith in each evaporator flow. Alternatively or additionally, each evaporator flow preferably a flow sensor is arranged. The various sensors are operatively connected to the control device. The flow sensors are preferably arranged upstream of the adjusting elements. The temperature sensors are preferably arranged downstream of the evaporation region, in particular downstream of an exit of the individual flows from the evaporator.
  • the system further preferably includes a differential pressure sensor having a first metering location upstream of the evaporator and upstream of a distribution to the individual evaporator passages, and a second metering point downstream of the evaporator, and preferably downstream of merging the individual evaporator passages operatively connected to the controller to measure pressure drop across the evaporator.
  • a differential pressure sensor having a first metering location upstream of the evaporator and upstream of a distribution to the individual evaporator passages, and a second metering point downstream of the evaporator, and preferably downstream of merging the individual evaporator passages operatively connected to the controller to measure pressure drop across the evaporator.
  • a pressure sensor is arranged, wherein the pressure drop as the difference of the measured values of the two pressure sensors in the control device can be calculated, which is operatively connected to the two pressure sensors for this purpose.
  • the system also includes a temperature sensor downstream of the merging of the evaporator flood
  • the system preferably includes a flow sensor upstream of the split on the individual evaporator flows and downstream of the conveyor, which is operatively connected to the controller for detecting a total mass flow in the system.
  • the control device is also preferably operatively connected to the conveyor for specifying and / or detecting their delivery rate.
  • the conveyor is preferably designed as a speed-controlled feed pump.
  • the expansion device is designed as a volumetric expansion machine, in particular as a reciprocating piston engine, as a vane machine, as a Roots expander or as a scroll expander.
  • the expansion device is designed as a screw expander. It has been found that a screw expander has especially in connection with an ORC process particularly favorable properties and high power output. This is especially true when the system is operated in the wet steam area. However, the screw expander can also be advantageously used during operation of the system with overheating of the working medium. Alternatively, it is also possible for the expansion device to be designed as a turbomachine, in particular a turbine.
  • the expansion device preferably via a shaft - operatively connected to a generator by which the released in the expansion device mechanical work is converted into electrical energy.
  • the mechanical work released in the expansion device may continue to be used as such, for example to assist an internal combustion engine.
  • the system is preferably configured to perform an organic Rankine cycle. This is particularly suitable for waste heat utilization in stationary or mobile applications, in particular for waste heat utilization in industrial processes or for the use of waste heat of an internal combustion engine.
  • the system is set up for utilizing the waste heat of an internal combustion engine.
  • the waste heat contained in the exhaust gas of the internal combustion engine and / or the waste heat covered by a coolant of the internal combustion engine in the system is possible to use the waste heat contained in the exhaust gas of the internal combustion engine and / or the waste heat covered by a coolant of the internal combustion engine in the system.
  • the arrangement is preferably designed as a mobile arrangement, wherein the internal combustion engine particularly preferably serves to drive a motor vehicle, in particular a heavy land vehicle, a rail vehicle or particularly preferably a watercraft, in particular a ship, and especially a ferry. But it is also possible that the arrangement is used stationary, for example, for stationary power generation, in particular to cover an emergency power or peak demand. Also for driving stationary units such as pumps, the internal combustion engine of the arrangement is suitable.
  • the mechanical energy converted in the expansion device of the system is supplied directly to the internal combustion engine for its support, for example, being transmitted directly to a crankshaft of the internal combustion engine.
  • electrical energy generated by a generator operatively connected to the expansion device via an electric motor of the crankshaft Internal combustion engine is supplied again.
  • electrical energy generated by a generator operatively connected to the expansion device to be fed into a power grid, for example into a vehicle electrical system of a motor vehicle equipped with the internal combustion engine, or into a separate power grid.
  • the overall efficiency of the internal combustion engine can be increased by the arrangement of the system.
  • the internal combustion engine of the arrangement is preferably designed as a reciprocating engine.
  • the internal combustion engine is used to drive in particular heavy land or water vehicles, such as mine vehicles, trains, the internal combustion engine is used in a locomotive or a railcar, or ships. It is also possible to use the internal combustion engine to drive a defense vehicle, for example a tank.
  • An exemplary embodiment of the internal combustion engine is preferably also stationary, for example, used for stationary power supply in emergency operation, continuous load operation or peak load operation, the internal combustion engine in this case preferably drives a generator.
  • a stationary application of the internal combustion engine for driving auxiliary equipment, such as fire pumps on oil rigs, is possible.
  • the internal combustion engine in the field of promoting fossil raw materials and in particular fuels, for example oil and / or gas, possible. It is also possible to use the internal combustion engine in the industrial sector or in the field of construction, for example in a construction or construction machine, for example in a crane or an excavator.
  • the internal combustion engine is preferably designed as a diesel engine, as a gasoline engine, as a gas engine for operation with natural gas, biogas, special gas or another suitable gas.
  • the internal combustion engine when the internal combustion engine is designed as a gas engine, it is suitable for use in a cogeneration plant for stationary power generation.
  • the description of the method on the one hand and the control device, the system and the arrangement on the other hand are to be understood as complementary to each other.
  • Features of the controller, system, or assembly that have been explicitly or implicitly described in the context of the method are preferably individually or combined with each other features of a preferred embodiment of the controller, system, or assembly.
  • Procedural steps that are explicit or implicit in connection with the Control device, the system or the arrangement have been described, preferably individually or combined with each other steps of a preferred embodiment of the method.
  • the method is preferably characterized by at least one method step, which is caused by at least one feature of the control device, the system or the arrangement.
  • the control device, the system or the arrangement are preferably characterized by at least one feature, which is due to at least one method step of the method.
  • Fig. 1 shows an arrangement 1, which has an internal combustion engine 3 and a system 5 for a thermodynamic cycle.
  • the system 5 and the internal combustion engine 3 are operatively connected to one another such that waste heat of the internal combustion engine 3 can be utilized in the system 5 by supplying the waste heat of the internal combustion engine 3 to an evaporator 7 of the system 5.
  • This is preferably waste heat from the exhaust gas of the internal combustion engine 3, which is supplied to the evaporator 7.
  • the system 5 has a circuit 9 for a working medium.
  • the system 5 is preferably set up for carrying out an ORC process, wherein ethanol is particularly preferably used as the working medium.
  • a conveyor 11 In the flow direction of the working medium along the circuit 9 are seen - in this order - a conveyor 11, the evaporator 7, an expansion device 13 and a capacitor 15 are arranged.
  • the working medium is first conveyed by the conveyor 11 along the circuit 9 through the evaporator, where it absorbs waste heat of the internal combustion engine 3, and wherein it is preferably vaporized. Subsequently, the working medium is expanded in the expansion device 13, doing mechanical work. Subsequently, the working medium in the condenser 15 is cooled again, preferably condensed, and fed again to the conveyor 11.
  • the evaporator 7 is formed Centerflutig. In the specific embodiment shown, it has four evaporator flows 19.1, 19.2, 19.3, 19.4.
  • the conveyed by the conveyor 11 working fluid is divided upstream of the evaporator 7 in a division 21 to the individual evaporator flows 19, which are merged downstream of the evaporator 7 in a merge 23 again.
  • An evaporation region 25 of the evaporator flows 19 is arranged in the evaporator 7.
  • a problem with such a multi-flow evaporator is that it tends to thermodynamic instabilities, in particular to the so-called Ledinegg instability.
  • the flow through this evaporator flow 19 decreases sharply, whereby the effect further amplified.
  • the heat transfer in the evaporator 7 is greatly reduced overall, because virtually a flood is completely blocked. An inadmissible overheating of the working fluid in the blocked evaporator flow 19 may be the result. This in turn can lead to deposits that permanently reduce the heat transfer in the evaporator 7, whereby the energy yield of the entire system is reduced. If the blocked evaporator flow 19 suddenly flows through working medium again, thermal shock can cause irreversible damage to the evaporator 7.
  • a control device 27 is provided which is adapted to equalize the evaporator flows 19 with respect to at least one operating parameter, in particular for equalization of the evaporator floods 19 with respect to the operating parameter, and / or to control a pressure drop across the evaporator 7.
  • the controller 27 is set up in a particularly preferred manner both for the adjustment of the evaporator flows 19 with respect to the at least one operating parameter as well as for regulating the pressure drop across the evaporator. 7
  • each of the evaporator flows 19 has a flow sensor 29.1, 29.2, 29.3, 29.4, the flow sensors 29 preferably being arranged downstream of the partition 21 and upstream of the evaporator 7.
  • the system 5 has a total flow sensor 31, which is provided downstream of the conveyor 11 and upstream of the partition 21, so that by means of the total flow sensor 31, a total mass flow in the circuit 9 can be detected.
  • the control device 27 is operatively connected both to the flow sensors 29 and to the total flow sensor 31.
  • the total mass flow in the control device 27 may be calculated from the delivery rate of the delivery device 11, or for the total mass flow rate to be predetermined by the control device 27 and for the delivery device 11 to be controlled accordingly.
  • a desired flow for the working medium is preferably calculated by the individual evaporator flows 19 from the control device 27 by dividing the total mass flow by the number of evaporator flows 19, in this case by four. The flow through the individual evaporator flows 19 is then regulated to this desired flow.
  • Each evaporator flow is an actuator 33.1, 33.2, 33.3, 33.4 arranged, with which a passage cross-section of the associated evaporator flow 19 is variable.
  • the adjusting elements 33 are preferably designed as valves. They are operatively connected to the control device 27 and are driven by this to equalize the evaporator flows 19 together.
  • evaporator flows 19 with respect to the flow of working medium, equality with respect to the temperature of the working medium downstream of the evaporator region 25 is preferably provided.
  • temperature sensors 35.1, 35.2, 35.3, 35.4 arranged in the Evaporator floods 19 temperature sensors 35.1, 35.2, 35.3, 35.4 arranged. These are preferably arranged downstream of the evaporator 7 or of the evaporation region 25 and upstream of the combination 23.
  • a desired temperature for the approximation of the evaporator flows 19 is preferably calculated as the mean value of the measured values of the individual temperature sensors 35.1, 35.2, 35.3, 35.4.
  • a desired temperature it is also possible for a desired temperature to be a mean temperature which is detected downstream of the combination 23 by means of an overall temperature sensor 37.
  • the temperature sensors 35 and / or the total temperature sensor 37 are operatively connected to the control device 27. Regardless of whether the equalization of the evaporator flows 19 takes place with respect to the flow or with respect to the temperature of the working medium, the control device 27 acts in any case for equality to the control elements 33rd
  • a first pressure sensor 39 upstream of the evaporator 7 and upstream of the partition 21 is arranged, wherein a second pressure sensor 41 downstream of the evaporator 7 and downstream of the merger 23 is arranged.
  • the pressure drop across the evaporator 7 can be calculated as the difference between the measured values of the first pressure sensor 39 and the second pressure sensor 41.
  • the pressure sensors 39, 41 are operatively connected to the control device 27. This also acts to control the pressure drop on the actuators 33rd
  • a differential pressure sensor is provided which can directly measure a differential pressure. This is then preferably connected to a first measuring point at the location of the first pressure sensor 39 and to a second measuring point at the location of the second pressure sensor 41.
  • Fig. 2 shows a schematic representation of a detail of an embodiment of the method, namely in particular a control element 43 for controlling the flow through one of the evaporator floods 19.1, 19.2, 19.3, 19.4.
  • a control element 43 is preferably provided for each of these evaporator flows 19, it being sufficient to describe its function for one of the evaporator flows 19.
  • a desired value 45 which is either a desired flow or a target temperature.
  • the target flow is preferably calculated as the total mass flow in the circuit 9 divided by the number of evaporator flows 19.
  • the setpoint temperature is preferably calculated as the mean value of Measured values of the temperature sensors 35.1, 35.2, 35.3, 35.4, or it is the measured value of the total temperature sensor 37.
  • control element 43 is also a corresponding actual value 47, which is either an actual value for the flow for the specifically considered evaporator flood 19.1, 19.2, 19.3, 19.4 or else a temperature of the working medium measured downstream of the evaporation zone 25 in this tide 19.1, 19.2, 19.3, 19.4, measured using the temperature sensor 35.1, 35.2, 35.3, 35.4 associated with the tide. Furthermore, in the control member 43 is an actual manipulated variable 49 for the concretely considered evaporator flood 19 associated actuator 33 a.
  • these input values are computed with one another in a computing element 51, resulting in a difference manipulated variable 53 as the output value. This goes into a controller 55, which finally outputs a desired manipulated variable 57.
  • Fig. 3 shows a second detail of the embodiment of the method according to FIG. 2 ,
  • the control elements 43.1, 43.2, 43.3, 43.4 are shown for the various evaporator flows 19, each in accordance with FIG. 2 explained form are formed and accordingly output the desired manipulated variables 57.1, 57.2, 57.3, 57.4. It turns out that the adjusting elements 33 are not directly controlled by the desired manipulated variables 57.
  • a renormalization element 59 wherein that of the setpoint manipulated variables 57.1, 57.2, 57.3, 57.4, which has the largest value, is set to the maximum permissible value for controlling the adjusting elements 33, so that the largest setpoint Actuated variable actuating element 33 has its maximum possible opening.
  • the other manipulated variables 57 are scaled accordingly, so that their relationships with each other remain the same. This is particularly possible if the adjusting elements 33 have linear characteristics.
  • the renormalization element 59 results in the renormalized desired manipulated variables 61.1, 61.2, 61.3, 61.4.
  • the control elements 33 would now be controlled with the renormal desired manipulated variables 61.
  • the renormalization in the renormalization member 59 would then ensure that at a given mass flow in the circuit 9, a minimum pressure drop across the evaporator 7 sets because the evaporator flows 19 - under the condition of their equality - have maximum wide passage cross sections at the location of the actuating elements 33.
  • a pressure drop control is provided for the pressure drop across the evaporator 7.
  • a map 63 is defined over a total mass flow 65, which is preferably determined by the total flow sensor 31, and a further operating parameter 67 of the system 5, wherein the map 63 values for a minimum presettable pressure drop or desired pressure drop 69 as a function of the total mass flow 65th and the operating parameter 67.
  • the operating parameter 67 is preferably a temperature of the working medium downstream of the evaporator 7, in particular at the evaporator outlet, namely the previously determined mean temperature or separately measured by the total temperature sensor 37 temperature, and / or a pressure of the working medium downstream of the evaporator 7, in particular at the evaporator outlet, and / or overheating of the working medium downstream of the evaporator 7, in particular used at the evaporator outlet.
  • a thermodynamic state of the working medium downstream of the evaporator 7, in particular at the evaporator outlet detectable via the temperature, pressure and / or superheating, wherein the predetermined pressure drop 69 to be preselected depends on this thermodynamic state.
  • a differential element 71 an actual pressure drop 73, which is preferably measured by means of the pressure sensors 39, 41, and the desired pressure drop 69 are calculated together, resulting in a desired-actual deviation 75.
  • this is converted into a global difference manipulated variable 79, taking into account the characteristics of the control elements 33.
  • This is in turn converted by a controller 81 into a limiting input 83, which is ultimately divided by a divider 85 87.1, 87.2, 87.3, 87.4.
  • the renormalized desired manipulated variables 61 are offset with the limit specifications 83, which ultimately results in resulting manipulated variables 89.1, 89.2, 89.3, 89.4.
  • the limiting specification 83 causes throttling of the adjusting elements 33, so that by means of the pressure drop control, the pressure drop across the evaporator 7 can be increased by throttling the adjusting elements 33, if this is operating point dependent required to ensure the stability of the system.

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  • Engineering & Computer Science (AREA)
  • Physics & Mathematics (AREA)
  • Thermal Sciences (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Chemical & Material Sciences (AREA)
  • Combustion & Propulsion (AREA)
  • Engine Equipment That Uses Special Cycles (AREA)

Claims (13)

  1. Procédé pour faire fonctionner un système (5) pour un processus en circuit fermé thermodynamique comprenant un évaporateur à plusieurs flux (7), qui présente au moins deux flux d'évaporateur (19.1, 19.2, 19.3, 19.4), les flux d'évaporateur (19.1, 19.2, 19.3, 19.4) étant équilibrés les uns aux autres par rapport à au moins un paramètre de fonctionnement des flux d'évaporateur individuels (19.1, 19.2, 19.3, 19.4), et/ou une chute de pression en travers de l'évaporateur (7) étant régulée,
    les flux d'évaporateur (19.1, 19.2, 19.3, 19.4) étant équilibrés les uns aux autres en faisant varier des grandeurs de commande pour des éléments de commande (33.1, 33.2, 33.3, 33.4) qui limitent un écoulement à travers les flux d'évaporateur (19.1, 19.2, 19.3, 19.4) et qui sont associés aux flux d'évaporateur individuels (19.1, 19.2, 19.3, 19.4),
    caractérisé en ce que les grandeurs de commande sont renormées de telle sorte qu'un élément de commande (33.1, 33.2, 33.3, 33.4) commandé avec une valeur maximale des grandeurs de commande soit ouvert au maximum.
  2. Procédé selon la revendication 1, caractérisé en ce que les flux d'évaporateur (19.1, 19.2, 19.3, 19.4) sont équilibrés les uns aux autres par rapport à un écoulement de fluide de travail et/ou par rapport à une température du fluide de travail en aval d'une région d'évaporation (25) des flux d'évaporateur individuels (19.1, 19.2, 19.3, 19.4).
  3. Procédé selon l'une quelconque des revendications précédentes, caractérisé en ce que la chute de pression en travers de l'évaporateur (7) est régulée par commande d'éléments de commande (33.1, 33.2, 33.3, 33.4) associés aux flux d'évaporateur individuels (19.1, 19.2, 19.3, 19.4).
  4. Procédé selon l'une quelconque des revendications précédentes, caractérisé en ce que les éléments de commande (33.1, 33.2, 33.3, 33.4) sont réalisés sous forme de soupapes.
  5. Procédé selon l'une quelconque des revendications précédentes, caractérisé en ce que les grandeurs de commande sont modifiées, notamment limitées, par régulation de la chute de pression.
  6. Procédé selon l'une quelconque des revendications précédentes, caractérisé en ce qu'un écoulement de consigne pour le fluide de travail à travers les flux d'évaporateur individuels (19.1, 19.2, 19.3, 19.4) est calculé en tant que débit massique total dans le système (5) divisé par le nombre des flux d'évaporateur (19.1, 19.2, 19.3, 19.4).
  7. Procédé selon l'une quelconque des revendications précédentes, caractérisé en ce qu'une température de consigne pour le flux de travail en aval de la région d'évaporation (25) est calculée en tant que valeur moyenne par le biais de la température du fluide de travail en aval de la région d'évaporation (25) des flux d'évaporateur individuels (19.1, 19.2, 19.3, 19.4), ou est mesurée séparément sous forme de température moyenne.
  8. Procédé selon l'une quelconque des revendications précédentes, caractérisé en ce qu'une chute de pression de consigne dépendant d'au moins un paramètre de fonctionnement du système (5) est lue à partir d'un champ caractéristique (63).
  9. Procédé selon l'une quelconque des revendications précédentes, caractérisé en ce que le système (5) fonctionne avec une surchauffe du fluide de travail ou dans une plage de vapeur humide.
  10. Procédé selon l'une quelconque des revendications précédentes, caractérisé en ce qu'un processus en cycle de Rankine organique est mis en oeuvre dans le système (5).
  11. Dispositif de commande (27) pour un système (5) pour un processus en circuit fermé thermodynamique comprenant un évaporateur à plusieurs flux (7), le dispositif de commande (27) étant prévu pour équilibrer les uns aux autres les flux d'évaporateur (19.1, 19.2, 19.3, 19.4) par rapport à au moins un paramètre de fonctionnement des flux d'évaporateur individuels (19.1, 19.2, 19.3, 19.4) et/ou le dispositif de commande (27) étant prévu pour réguler une chute de pression en travers de l'évaporateur (7), le dispositif de commande étant prévu pour mettre en oeuvre un procédé selon l'une quelconque des revendications 1 à 10.
  12. Système pour un processus en circuit fermé thermodynamique, comprenant un évaporateur à plusieurs flux (7), qui présente au moins deux flux d'évaporateur (19.1, 19.2, 19.3, 19.4), à chaque flux d'évaporateur (19.1, 19.2, 19.3, 19.4) étant associé un élément de commande (33.1, 33.2, 33.3, 33.4) qui est disposé et prévu pour faire varier une section transversale de passage à travers le flux d'évaporateur associé (19.1, 19.2, 19.3, 19.4) et comprenant un dispositif de commande (27) selon la revendication 11, qui est en liaison fonctionnelle avec les éléments de commande (33.1, 33.2, 33.3, 33.4) et qui est prévu, par variation de grandeurs de commande pour les élément de commande (33.1, 33.2, 33.3, 33.4), pour équilibrer les uns aux autres les flux d'évaporateur (19.1, 19.2, 19.3, 19.4) par rapport à au moins un paramètre de fonctionnement des flux d'évaporateur individuels (19.1, 19.2, 19.3, 19.4) et/ou pour réguler une chute de pression en travers de l'évaporateur (7).
  13. Agencement comprenant un moteur à combustion interne (3) et un système (5) pour mettre en oeuvre un processus en circuit fermé thermodynamique, caractérisé en ce que le système est réalisé selon la revendication 12.
EP15000459.6A 2014-03-31 2015-02-16 Procédé de fonctionnement d'un système pour un cycle fermé thermodynamique doté d'un évaporateur à plusieurs flux, dispositif de commande pour un système, système pour un cycle fermé thermodynamique doté d'un évaporateur à plusieurs flux et agencement d'un moteur à combustion interne et d'un système Not-in-force EP2937630B1 (fr)

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DE102014206043.5A DE102014206043B4 (de) 2014-03-31 2014-03-31 Verfahren zum Betreiben eines Systems für einen thermodynamischen Kreisprozess mit einem mehrflutigen Verdampfer, Steuereinrichtung für ein System, System für einen thermodynamischen Kreisprozess mit einem mehrflutigen Verdampfer, und Anordnung einer Brennkraftmaschine und eines Systems

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US10161270B2 (en) * 2015-09-03 2018-12-25 Avl Powertrain Engineering, Inc. Rankine cycle pump and recuperator design for multiple boiler systems
DE102016218936B4 (de) 2016-09-29 2022-10-06 Rolls-Royce Solutions GmbH Verfahren zum Betreiben eines Systems zur Durchführung eines thermodynamischen Kreisprozesses, System zur Durchführung eines thermodynamischen Kreisprozesses und Anordnung mit einem solchen System und einer Brennkraftmaschine

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US9927159B2 (en) 2018-03-27
DE102014206043A1 (de) 2015-10-01
US20150276283A1 (en) 2015-10-01
DE102014206043B4 (de) 2021-08-12

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