EP0967396A2 - Verfahren zum Betreiben von Turboverdichtern - Google Patents
Verfahren zum Betreiben von Turboverdichtern Download PDFInfo
- Publication number
- EP0967396A2 EP0967396A2 EP99106086A EP99106086A EP0967396A2 EP 0967396 A2 EP0967396 A2 EP 0967396A2 EP 99106086 A EP99106086 A EP 99106086A EP 99106086 A EP99106086 A EP 99106086A EP 0967396 A2 EP0967396 A2 EP 0967396A2
- Authority
- EP
- European Patent Office
- Prior art keywords
- controller
- surge limit
- control
- limiter
- target
- 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.)
- Granted
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Classifications
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F04—POSITIVE - DISPLACEMENT MACHINES FOR LIQUIDS; PUMPS FOR LIQUIDS OR ELASTIC FLUIDS
- F04D—NON-POSITIVE-DISPLACEMENT PUMPS
- F04D27/00—Control, e.g. regulation, of pumps, pumping installations or pumping systems specially adapted for elastic fluids
- F04D27/02—Surge control
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F04—POSITIVE - DISPLACEMENT MACHINES FOR LIQUIDS; PUMPS FOR LIQUIDS OR ELASTIC FLUIDS
- F04D—NON-POSITIVE-DISPLACEMENT PUMPS
- F04D27/00—Control, e.g. regulation, of pumps, pumping installations or pumping systems specially adapted for elastic fluids
- F04D27/02—Surge control
- F04D27/0269—Surge control by changing flow path between different stages or between a plurality of compressors; load distribution between compressors
Definitions
- the invention relates to a method and Device for operating turbocompressors with several mutually influencing controllers.
- Turbocompressors are often equipped with multiple controllers equipped.
- the surge limit controller of a turbocompressor monitors z. B. the location of the compressor operating point in the map and opens if it is too small Compressor throughput a surge control valve for Suction side or to the atmosphere.
- pressure or flow regulators are often used, whose actuator adjustable guide vanes or Throttle valves are.
- the drive can also adjust the speed for capacity adjustment be adjusted.
- An adjustment of the surge limit control valve is affected also the compressor end pressure or the flow to Process.
- An adjustment of the actuator of the process variable controller has an impact on the location of the Operating point in the map and can therefore the surge limit controller intervene.
- surge limit controller is considered more critical Turbo machine protection regulator to the fastest possible Response behavior set.
- fastest controllers available are used that control the fastest valves available.
- the process variable control must match the time behavior of the Process adapted.
- pressure regulations are characterized by significantly longer time constants than those required for surge limit control.
- the surge limit controller regulates one Fault clears much faster than the process variable controller. He has the surge limit control valve in the new one required position before the process variable controller has reacted noticeably. An additional Decoupling of the surge limiters from each other is in not necessary in these cases.
- the surge limit controller reacts to this and opens it Pump limit control valve to protect the compressor Piece.
- the process variable controller notices this and increases the conveying capacity of the Compressor. The result is that the working point away from the surge line.
- the Process variable controller reacts to this by the Delivery capacity of the compressor reduced accordingly. However, this brings the working point back in again the proximity of the surge limit, so that the surge limit controller Pump limit control valve opens again.
- the process begins from the front and can change if the time parameters are not chosen correctly and unfavorable phase position to a continuous oscillation of process size and surge limit control valve to lead.
- the surge limit controller take place among each other. If there is a fault on the suction side of the low pressure stage the pressure ratio increased above this level the working point of this stage moves in In the direction of the surge limit, causing the surge limit controller to engage the low pressure stage may be required the pump limit control valve of the low pressure stage a piece opens. This causes a lowering the final pressure of the low pressure stage or the inlet pressure the high pressure stage. This goes along with one Increase the pressure ratio of the high pressure stage what now open the surge limit control valve of this stage has the consequence.
- the surge limit control valves Because with gas compressors, the surge limit control valves the gas on the pressure side to the suction side relax, causes the high pressure side to open Pump limit control valve an increase in suction pressure this stage and thus an increase in the final pressure of the Low pressure stage. The surge limit control of the low pressure stage this will further intervene forced, the low pressure surge limit control valve opens further.
- the surge limit controller acts more violently than absolutely necessary and the surge limit control valve is opened further than to protect the compressor required. This causes that after the decay pump surge control valves again getting closed. Because the fault in the low pressure part has started, the surge limit controller of the low pressure stage closes this valve again. This increases the final pressure this stage and thus also the suction pressure of the High pressure stage. The pressure ratio of the high pressure stage decreases and the corresponding surge limit controller closes the high-pressure surge limit control valve. this has now again an influence on the low pressure part etc. Are the controls set to open a transient disorder with some Overdrive can respond, a phase shift mutual influence of the two surge limit controllers cannot be excluded.
- the object of the invention is to provide a method for Decoupling the control loops in the way to create that even with the same timing behavior of all sizes vibration-stimulating interaction of the control loops among themselves is avoided.
- a typical machine train for compressing gas consists of three in a row in the direction of flow arranged step groups.
- One of these stages consists of the suction line of the low pressure stage, the compressor, the pressure line and one Blow line with the surge limit control valve, further a flow calculator for calculating the intake flow and a calculator to determine the Delivery head.
- the computers are on signal lines and with the pipes and other signal lines connected to the comparator.
- a comparator determines the difference from the setpoint (delivery head) minus Actual value (flow) and always causes when the Actual value is too small in relation to the setpoint, one Gradual opening of the surge limit control valve until the Actual flow rate exactly that of the respective delivery head dependent target flow corresponds.
- the adjustment takes place according to the invention via the maximum selection, the PI controller and the signal line to the surge limit control valve.
- a check valve decouples the first Compressor from the downstream medium pressure stage.
- the actual flow is smaller than that of the delivery head dependent target flow, is in the comparator determined control difference positive and adjusted via the control line the output of the surge limit controller in Direction of another opening surge control valve.
- the controllers are now given a maximum selection upstream, one input of which is known Difference from the setpoint and actual value of the associated Compressor. This maximum selection becomes the control difference of the other compressor stages also impressed.
- the effect of the system deviation is such that a positive signal lowers the controller output and so that the surge limit control valve opens and a negative one Signal the surge limit control valve closes.
- the maximum selection now causes that whenever one of the three Machinery enters an operating area that is a Opening the surge limit control valve requires this size all three surge limit regulators are impressed and everyone Regulator its associated surge limit control valve via the Control lines opens accordingly. A mutual Influencing is prevented because everyone Pump limit control valves simultaneously and at the same Open the controller setting by the same amount.
- the control difference is a via the signal line First order delay element and an adding Limiter activated.
- This delimiter adds the Signed inputs, d. that is, it subtracts from the control difference that was delayed via the delay element Control difference. Is in steady state this difference zero so that the adder is only that Passes signal of maximum selection.
- the delimiter is set to a range from 0 to 1, it limits negative values to zero.
- the output signal of the delay element follows delayed.
- the control difference can be the output signal of the limiter already become positive when the control difference itself is still negative.
- a constant can be added to the limiter become. This constant causes an offset.
- the output of the limiter only becomes greater than zero if the difference of the two other input variables exceeded the threshold set as a constant Has.
- the correction variable acts on the process variable controller then in such a way that when approaching the surge limit or when the control line is exceeded, the entrance of the Process size controller is changed so that the Effect of the surge limit controller supports and Compressor moves out of the danger area.
- the surge limit controllers or the process variable controller a gradient limiter with integrated input amplifier, Limiter and integrator connected downstream.
- An additional Comparator of the process variable setpoint and the actual process variable activated.
- the difference of this Both values have their own signal line and a limiter and a process variable controller.
- This Process variable controller adjusts the associated actuator (Guide vanes, throttle body, speed) such that the The actual process value corresponds exactly to the setpoint.
- the limiter limits the control difference of the process variable controller. Since the process variable controller is usually switched as a proportional integral controller (PI controller) the limiter limits the gradient for the integral adjustment of the manipulated variable. Will the Limiter set to the limit value zero, changed the manipulated variable of the process variable controller at all no more.
- PI controller proportional integral controller
- the upper and lower limit of the limiter depending on one Process size can be varied. This is the control difference of the surge limit controller as a manipulated variable used.
- a function generator allows the definition a non-linear relationship between system deviation of the surge limit controller and the effective Limiter Limits.
- the function generator can, for. B. be set so that with a system deviation greater than 20% no limitation is effective up to a control difference of 3% can limit the square decrease with the control difference and at one Control difference below 3% the lower limit to zero put. Any other, including non-linear function curve is adjustable if necessary.
- the top and the lower limit can also be configured separately. In this case, two function generators are separated for the upper and lower limits are used.
- the Function encoder also directly on the control parameters of the Process size controller act and this accordingly to adjust.
- the Controller (process variable controller or surge limit controller) Gradient limiter downstream.
- a signal line transfers the controller output variable (process variable controller or surge limit controller) to the input amplifier a gradient limiter.
- This amplifier is on set a high gain, so that at a slight difference between the output of the Controller and the output of the gradient limiter, fed back via an additional signal line, the Limiter receives a large input signal.
- the limits of the limiter determine the gradient for the Adjustment of the integrator.
- the limiter is on the integrator only receives small values small input values and also adjusts its output if there is a deviation at the input of the amplifier only slowly.
- the limit values can be set via another control line the limiter can be adjusted in the same way as previously for the limitation of the control difference of the Pump limit controller has been described.
- the output line of the high pressure stage of the respective Final pressure can be recorded by a pressure transmitter and an additional target / actual value comparator are transferred, with another process variable controller the actuators of the guide vanes each of the three compressor stages can be addressed.
- control parameters are between the maximum selection and the surge limit controller branched off and one Function generator supplied. This transfers its data on the above additional process variable controller.
- an additional limiter only the specially selected controlled variables forwards.
- the invention is based on schematic Embodiments described in more detail.
- each compressor stage (2, 22, 42) own surge limit control valves (5, 25, 45), each in the suction lines (1, 21, 41) of the own compressor stage (2, 22, 42) blow off.
- a machine train for compressing gas consists of three arranged one behind the other in the direction of flow Level groups (2, 22, 42).
- the three-stage compressor consists of the suction lines (1, 21, 41), the low pressure compressor (2), the medium pressure compressor (22) and the high pressure compressor (42), the pressure lines (3, 23, 43), the blow-by lines (4, 24, 44) with the surge limit control valves (5, 25, 45), the flow computers (6, 26, 46) for calculating the intake flow and the computer (7, 27, 47) for the minimum permissible target flow, which results from the final pressure or the delivery head is determined.
- To calculate the Head is also the respective suction pressure and Suction temperature required.
- the associated active lines are not shown.
- the computers (6, 7), (26, 27) and (46, 47) are over Signal lines (8 and 9), (28 and 29) and (48 and 49) with the delivery pipelines and over two each further signal lines (10 and 11), (30 and 31) as well (50 and 51) with the comparators (12, 32 and 52) connected.
- Each comparator (12, 32, 52) determines the Difference from setpoint (delivery head) minus actual value (Flow) and always causes when the actual value in Ratio to setpoint is too small, a gradual one Opening of the corresponding surge limit control valves (5, 25 or 45) until the actual flow rate is exactly that of the respective delivery head dependent target flow corresponds.
- the adjustment is made via a maximum selection (14, 34, 54), the surge limit controller (15, 35, 55) and the signal lines (16, 36, 56) to the surge limit control valve (5, 25, 45).
- the check valve (17, 37) decouples the low pressure compressor (2) from the medium pressure compressor (22).
- the measured values / signals of the target / actual value comparison (12, 32, 52) act via the control line (13, 33, 53) directly to the surge limit controller (15, 35, 55), which the Pump limit control valve (5, 25, 45) via the control line (16, 36, 56).
- the actual flow is smaller than that of the delivery head dependent target flow, the control difference positive and adjusts the output of the surge limit controller (15, 35, 55) towards another opening Valve (5, 25, 45).
- the surge limit regulators (15, 35, 55) become one Maximum selection (14, 34 and 54) upstream, their an input the known difference between setpoint and Actual value of the associated surge limit control Compressor stage is. This maximum selection is the Control difference of the other target / actual value comparators (32 and 52) also stamped. The effect of Control difference is such that a positive signal Controller output (15, 35, 55) and thus the Pump limit control valve (5, 25, 45) opens and on negative signal the surge limit control valve (5, 25, 45) closes.
- the maximum selection (14, 34, 54) now causes that whenever one of the three compressor stages (2, 22 or 42) enters an operating area that includes a Opening the surge limit control valve (5, 22 or 42) requires this size for all three surge limit controllers (15, 35 and 55) and each surge limit controller (15, 35 or 55) its associated surge limit control valve (5, 25, 45) via the control line (16, 36, 56) opens accordingly. A mutual influence is prevented because all surge limit control valves (5, 25, 45) simultaneously and with the same Open the controller setting by the same amount.
- Control difference is one over the signal line (60) First order delay element (61) and an adding Limiter (63) activated.
- This delimiter (63) adds the inputs according to the sign, i. H. he subtracts from the control difference via the delay element (61) delayed control difference. In the stationary State, this difference is zero, so the Adder (64) only the signal of the maximum selection (14) passes on.
- the limiter (63) is on one Range set from 0 to 1, it limits negative ones Values to zero.
- the limiter (63) can have a constant (62) can be added. This constant (62) causes an offset. The output of the limiter (63) will only greater than zero if the difference between the two other input variables (60.1 and 60.2) as Constant set threshold value has exceeded.
- this constant (62) can also be used without the delaying effect of the PT1 link (61) is used become.
- the setpoint / actual value comparator (72) the process variable setpoint and the actual process value is activated. The difference these two values act via the signal line (73) and the limiter (74) on the process variable controller (78). This controller adjusts the associated actuator of the Turbo compressor (guide vanes, throttle element, Speed) in such a way that the actual process value is accurate corresponds to the setpoint.
- the upper and lower Limit of the limiter (74) depending on one Process size can be varied.
- the control difference of the surge limit controller (15) as a manipulated variable used.
- the function generator (75) allows Definition of a nonlinear relationship between Control difference of the surge limit controller and the effective Limiter Limits.
- the process variable controller (78) reacts with its set one (adjustable as a parameter set) Time behavior on the input size.
- a big rule difference on Input causes controller (78) to output its output quickly changed, with a small control difference at the entrance the exit only changes slowly.
- the timing behavior of the output variable can be arbitrary to be influenced.
- the limiter (74) can change the Controller output in one direction or the other completely can be prevented by controlled limitation the controller output (78) can even have positive values in Are controlled in the direction of larger output values, even if the control difference at the input the controller output wants to lower.
- the controller (15/78) (surge limit controller (15) or process variable controller (78)) a gradient limiter (80) downstream.
- the signal line (79) transmits the output size of the controller (15/78) to the input amplifier (81).
- This amplifier (81) is set to a high gain, so that at a slight difference between the output of the Controller (79) and the output of the gradient limiter (84) fed back via the signal line (85) Limiter (82) receives a large input signal.
- the Limit values of the limiter (82) determine the gradient for the adjustment of the integrator (83). Is the Limiter (82) set to small values receives the Integrator (83) only small input values and adjusted its output (84) even if there is a deviation at the input of the amplifier (81) only slowly.
- the limit values of the Limiter (82) can be adjusted in the same way as previously for the limitation of the control difference of the Regulator (15/78) was described.
- FIG. 5 shows a circuit diagram corresponding to FIG. 1 with one on the pressure line (43) after the check valve (57) the third compressor stage (42) arranged Pressure transmitter (20), the control data on a Signal line (88) to a target-actual value comparator (12) and process variable setpoints (89) from the control system receives.
- a process variable controller (78) transmits the target / actual value comparisons (Controlled variables) via a control line (87) to the actuators (18) for adjusting the Guide vanes (19) in the low, medium and high pressure turbo compressor stages (2, 22, 42).
- FIG. 7 shows a circuit diagram of a low-pressure turbocompressor stage (2), in which the control differences of the Target / actual value comparator (12) or from (33) and (53) are first passed to the maximum selection (14). As in FIG. 6, these control data become shown on a surge limit controller (15) and transfer there to the surge limit control valve (5).
- the function generator (75) can also Control data from the maximum selection (14) via a Transfer control line (76) to a limiter (74) are upstream of the process variable controller (78) is. This (78) is connected via a control line (87) the actuator (18) of the guide vanes (19) Low pressure stage (2) connected.
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Abstract
Description
- Fig. 1
- ein Schaltbild zur Reglerentkopplung eines dreistufigen Turboverdichters von Prozeßgasen,
- Fig. 2
- ein Schaltbild mit einer zwischengeschalteten Konstante zwischen einem Soll-/Ist-Wert-Vergleicher und einem Pumpgrenzregler,
- Fig. 3
- ein Schaltbild zur Begrenzung des Gradienten für die Stellgrößenveränderung,
- Fig. 4
- ein Schaltbild eines Gradientenbegrenzers nach einem Prozeßgrößen- oder Pumpgrenzreglers,
- Fig. 5
- ein Schaltbild entsprechend Fig. 1 mit einem an der Druckleitung angeordneten Druckmeßumformer,
- Fig. 6
- ein Schaltbild einer Turboverdichterstufe, bei dem Daten aus der Maximalauswahl zusätzlich einem Prozeßgrößenregler übertragen werden,
- Fig. 7
- ein Schaltbild einer Turboverdichterstufe, bei dem Daten aus der Maximalauwahl einem Begrenzer und danach einem Prozeßgrößenregler übertragen werden.
- 1
- Ansaugleitung
- 2
- Niederdruckkompressor
- 3
- Druckleitung
- 4
- Umblaseleitung
- 5
- Abblaseventil/Pumpgrenzregelventil
- 6
- Durchflußrechner
- 7
- Förderhöhenrechner und Sollwertbildner
- 8
- Signalleitungen
- 9
- Signalleitungen
- 10
- Signalleitungen
- 11
- Signalleitungen
- 12
- Soll-/Ist-Wert-Vergleicher
- 13
- Steuerleitung
- 14
- Maximalauswahl
- 15
- Pumpgrenzregler
- 16
- Steuerleitung zu 5
- 17
- Rückschlagklappe
- 18
- Stellantrieb
- 19
- Leitschaufeln
- 20
- Druckmeßumformer
- 21
- Ansaugleitung
- 22
- Mitteldruckkompressor
- 23
- Druckleitung
- 24
- Umblaseleitung
- 25
- Pumpgrenzregelventil
- 26
- Durchflußrechner
- 27
- Förderhöhenrechner und Sollwertbildner
- 28
- Signalleitung
- 29
- Signalleitung
- 30
- Signalleitung
- 31
- Signalleitung
- 32
- Soll-/Ist-Wert-Vergleicher
- 33
- Steuerleitung
- 34
- Maximalauswahl
- 35
- Pumpgrenzregler
- 36
- Steuerleitung zu 25
- 37
- Rückschlagklappe
- 38
- 41
- Ansaugleitung
- 42
- Hochdruckkompressor
- 43
- Druckleitung
- 44
- Umblaseleitung
- 45
- Pumpgrenzregelventil
- 46
- Durchflußmesser
- 47
- Förderhöhenrechner und Sollwertbildner
- 48
- Signalleitung
- 49
- Signalleitung
- 50
- Signalleitung
- 51
- Signalleitung
- 52
- Soll-/Ist-Wert-Vergleicher
- 53
- Steuerleitung
- 54
- Maximalauswahl
- 55
- Ppmpgrenzregler
- 56
- Steuerleitung zu 56
- 57
- Rückschlagklappe
- 58
- 60
- Signalleitung
- 60.1
- positiver Strang
- 60.2
- negativer Strang
- 61
- Verzögerungsglied, 1. Ordnung
- 62
- Konstante
- 63
- addierender Begrenzer/Limitierer
- 64
- Summierer/Addierer
- 70
- Signalleitung
- 71
- Signalleitung
- 72
- Soll-/Ist-Wert-Vergleicher
- 73
- Signalleitung
- 74
- Begrenzer
- 75
- Funktionsgeber
- 76
- Signalleitung
- 77
- Signalleitung
- 78
- PI-Regler/Prozeßgrößenregler
- 79
- Signalleitung (Reglerausgang)
- 80
- Gradientenbegrenzer
- 81
- Eingangsverstärker
- 82
- Begrenzer
- 83
- Integrator
- 84
- Ausgangsleitung Gradientenbegrenzer
- 85
- Signalleitung für Rückkoppelung
- 86
- Steuerleitung
- 87
- Signalleitung
- 88
- Signalleitung
- 89
- Prozeßgrößen-Sollwerte vom Leitsystem
Claims (17)
- Verfahren zum Betreiben von Turbomaschinen mit mindestens zwei sich gegenseitig beeinflussenden Reglern,
dadurch gekennzeichnet,
daß wechselseitig ausgetauschte Korrekturgrößen eines ersten und eines zweites Reglers, wobei der erste Regler ein Pumpgrenzregler ist, in den Soll/Istvergleich der beiden Regler eingreifen und die Stellgrößenausgänge der beiden Regler derart entkoppeln, daß eine gegenseitige Beeinflussung ausgeschlossen ist oder zumindest deutlich reduziert wird. - Verfahren nach Anspruch 1,
dadurch gekennzeichnet,
daß die Regeldifferenz des ersten Reglers auf eine Extremwertauswahl vor dem zweiten Regler wirkt. - Verfahren nach Anspruch 1,
dadurch gekennzeichnet,
daß die Steuergröße, die das Pumpgrenzregelventil mit maximaler Stellgrößengeschwindigkeit verstellt, von jedem Regler aus auf jedes Stellorgan wirkt. - Verfahren nach Anspruch 1,
dadurch gekennzeichnet,
daß die wirksame Korrekturgröße aus der Differenz aus einer über ein Verzögerungsglied erster Ordnung zeitlich verzögerten ursprünglichen Korrekturgröße und der unverzögerten Größe ermittelt wird. - Verfahren nach Anspruch 4,
dadurch gekennzeichnet,
daß der Korrekturgröße ein Offset aufgeprägt wird. - Verfahren nach den Ansprüchen 4 und 5,
dadurch gekennzeichnet,
daß die Korrekturgröße den Gradienten für die Verstellung einer Stellgröße eines anderen Reglers begrenzt. - Verfahren nach Anspruch 6,
dadurch gekennzeichnet,
daß der Gradient für die Begrenzung der Stellgröße eine lineare oder nichtlineare Funktion der Korrekturgröße ist. - Verfahren nach Anspruch 6 oder 7,
dadurch gekennzeichnet,
daß die Begrenzung für die Stellgröße, abhängig von einer Prozeßgröße, zu- oder abgeschaltet wird. - Verfahren nach Anspruch 6 bis 8,
dadurch gekennzeichnet,
daß die Korrekturgröße auf die Reglerparameter wirkt und diese variiert. - Vorrichtung zur Durchführung des Verfahrens zum Betreiben von mehrstufigen Turboverdichtern mit mindestens zwei sich gegenseitig beeinflussenden Reglern,
dadurch gekennzeichnet,daß jedem Pumpgrenzregler (15, 35, 55) einer Turboverdichterstufe (2, 22, 42) eine Maximalauswahl (14, 34, 54) vorgeschaltet ist, in die aus dem Soll-Ist-Wert-Vergleicher (12, 32, 52) wechselseitig ausgetauschte Korrekturgrößen über Steuerleitungen (13, 33, 53) übertragen werden unddaß der Pumpgrenzregler (15, 35, 55) über Steuerleitungen (16, 36, 56) auf die Pumpgrenzregelventile (5, 25, 45) wirkt. - Vorrichtung nach Anspruch 10,
dadurch gekennzeichnet,daß jedem Soll-Ist-Wert-Vergleicher (12, 32, 52) des Pumpgrenzreglers (15, 35, 55) jeweils ein Verzögerungsglied erster Ordnung (61) und ein addierender Begrenzer (63) nachgeschaltet wird,daß der Begrenzer (63) die Reglerdifferenzeingänge vorzeichengerecht addiert und auf einstellbare Grenzwerte begrenzt unddaß der Addierer (64) die ermittelte Reglerdifferenz (Extremwertauswahl) an den Pumpgrenzregler (15, 35, 55) weitergibt. - Vorrichtung nach Anspruch 11,
dadurch gekennzeichnet,
daß der Korrekturgröße vor dem Begrenzer (63) eine Konstante (62) aufgeprägt wird. - Vorrichtung nach Anspruch 10,
dadurch gekennzeichnet,daß zwischen dem Soll-Ist-Wert-Vergleicher (12, 32, 52) und dem Begrenzer (74) jeweils ein Funktionsgeber (75) zwischengeschaltet ist bzw.daß der Soll-Ist-Wert-Vergleicher (12, 32, 52) über die Steuerleitung (60) direkt mit dem Pumpgrenzregler (15, 35, 55) verbunden ist,daß ein weiterer Soll-Ist-Wert-Vergleicher (72) mit dem Begrenzer (74) gekoppelt ist, der seine Daten an einen Prozeßgrößenregler (78) weiterleitet unddaß der Pumpgrenzregler (15) über eine Signalleitung (60) zusätzlich mit dem Funktionsgeber (75) gekoppelt ist. - Vorrichtung nach Anspruch 10,
dadurch gekennzeichnet,daß dem Regler (15 oder 78) ein Gradientenbegrenzer (80) nachgeschaltet ist, wobei die Daten des Reglers (15 oder 78) auf einen Eingangsverstärker (81) übertragen werden,daß der Eingangsverstärker (81) mit einem Begrenzer (82) und dieser mit einem Integrator (83) verbunden ist unddaß dem Eingangsverstärker (81) die Ausgangsdaten (84) über eine Steuerleitung (85) rückübertragen werden. - Vorrichtung nach Anspruch 10,
dadurch gekennzeichnet,daß an der Druckleitung (43) ein Druckmeßumformer (20) angeordnet ist, der Daten über eine Signalleitung (88) auf einen Soll-Ist-Wert-Vergleicher (12) überträgt,daß ein Prozeßgrößenregler (78) die Soll-Ist-Wertvergleiche (Regelgrößen) über eine Steuerleitung (87) an den Stellantrieb (18) zur Verstellung der Leitschaufeln (19) in den Turboverdichterstufen (2, 22, 42) überträgt unddaß dem Soll-Ist-Wert-Vergleicher (20) Prozeßgrößen Soll-Werte (89) vom Leitsystem übertragen werden. - Vorrichtung nach Anspruch 15,
dadurch gekennzeichnet,daß an der Druckleitung (3) nach der Rückschlagklappe (17) ein Druckmeßumformer (20) angeordnet ist, der über eine Steuerleitung (71) Daten an einen Soll-Ist-Wert-Vergleicher (72) überträgt und diese über eine Signalleitung (73) auf einen Prozeßgrößenregler (78) weiterleitet,daß eine Maximalauswahl (14) Daten aus dem Soll-Ist-Wert-Vergleicher (12) auf einen Funktionsgeber (75) bzw. einen Pumpgrenzregler (15) überträgt,daß die Maximalauswahl (14) weitere Daten über die Steuerleitung (33) und (35) empfängt,daß der Pumpgrenzregler (15) über eine Steuerleitung (16) mit dem Pumpgrenzregelventil (5) verbunden ist,daß die Daten über eine Steuerleitung (76) dem Prozeßgrößenregler (78) übertragen werden unddaß der Prozeßgrößenregler (78) seine Daten über eine Signalleitung (87) auf den Stellantrieb (18) der Leitschaufeln (19) in den Turboverdichterstufen (2, 12, 42) überträgt. - Vorrichtung nach den Ansprüchen 15 bis 16,
dadurch gekennzeichnet,
daß der Funktionsgeber (75) Daten aus der Maximalauswahl (14) über eine Steuerleitung (76) auf einen Begrenzer (74) überträgt, der dem Prozeßgrößenregler (78) vorgeschaltet ist.
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
DE19828368 | 1998-06-26 | ||
DE19828368A DE19828368C2 (de) | 1998-06-26 | 1998-06-26 | Verfahren und Vorrichtung zum Betreiben von zwei- oder mehrstufigen Verdichtern |
Publications (3)
Publication Number | Publication Date |
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EP0967396A2 true EP0967396A2 (de) | 1999-12-29 |
EP0967396A3 EP0967396A3 (de) | 2001-07-25 |
EP0967396B1 EP0967396B1 (de) | 2003-05-07 |
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EP99106086A Expired - Lifetime EP0967396B1 (de) | 1998-06-26 | 1999-03-26 | Verfahren zum Betreiben von Turboverdichtern |
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US (1) | US6164901A (de) |
EP (1) | EP0967396B1 (de) |
DE (2) | DE19828368C2 (de) |
Cited By (3)
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---|---|---|---|---|
WO2010058002A1 (de) | 2008-11-24 | 2010-05-27 | Siemens Aktiengesellschaft | Verfahren zum betrieb eines mehrstufigen verdichters |
CN104533820A (zh) * | 2014-12-26 | 2015-04-22 | 沈阳鼓风机集团自动控制***工程有限公司 | 一种防喘振控制方法及装置 |
US10480521B2 (en) | 2016-04-01 | 2019-11-19 | Fisher-Rosemount Systems, Inc. | Methods and apparatus for detecting and preventing compressor surge |
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RU2263810C2 (ru) * | 1999-12-18 | 2005-11-10 | Роберт Бош Гмбх | Способ и устройство управления силовым агрегатом транспортного средства |
WO2001044642A2 (de) * | 1999-12-18 | 2001-06-21 | Robert Bosch Gmbh | Verfahren und vorrichtung zur steuerung der antriebseinheit eines fahrzeugs |
JP3751208B2 (ja) * | 2001-02-23 | 2006-03-01 | 株式会社神戸製鋼所 | 多段可変速圧縮機の制御方法 |
DE10208676A1 (de) * | 2002-02-28 | 2003-09-04 | Man Turbomasch Ag Ghh Borsig | Verfahren zum Regeln von mehreren Strömungsmaschinen im Parallel- oder Reihenbetrieb |
DE10304063A1 (de) | 2003-01-31 | 2004-08-12 | Man Turbomaschinen Ag | Verfahren zum sicheren Betreiben von Turbokompressoren mit einer Pumpgrenzregelung und einem Pumpgrenzregelventil |
WO2007095537A1 (en) * | 2006-02-13 | 2007-08-23 | Ingersoll-Rand Company | Multi-stage compression system and method of operating the same |
US8173853B2 (en) * | 2006-04-11 | 2012-05-08 | Basf Se | Process for preparing acetylene by partial oxidation of hydrocarbons |
US8017823B2 (en) * | 2006-04-11 | 2011-09-13 | Basf, Se | Process for the manufacture of acetylene by partial oxidation of hydrocarbons |
DE102006030108A1 (de) * | 2006-06-28 | 2008-01-03 | Man Turbo Ag | Vorrichtung und Verfahren zum Durchführen eines Ventiltests an einer Turbomaschine |
US8591199B2 (en) * | 2007-01-11 | 2013-11-26 | Conocophillips Company | Multi-stage compressor/driver system and method of operation |
DE102009004376B4 (de) * | 2009-01-12 | 2016-06-16 | Man Diesel & Turbo Se | Verfahren und System zur Steuerung eines Turbokompressorverbundes |
GB0919771D0 (en) * | 2009-11-12 | 2009-12-30 | Rolls Royce Plc | Gas compression |
IT1402481B1 (it) * | 2010-10-27 | 2013-09-13 | Nuovo Pignone Spa | Metodo e dispositivo che effettua una compensazione del tempo morto di anti-pompaggio basata su modello |
US9074606B1 (en) * | 2012-03-02 | 2015-07-07 | Rmoore Controls L.L.C. | Compressor surge control |
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WO2010058002A1 (de) | 2008-11-24 | 2010-05-27 | Siemens Aktiengesellschaft | Verfahren zum betrieb eines mehrstufigen verdichters |
US8939704B2 (en) | 2008-11-24 | 2015-01-27 | Siemens Aktiengesellschaft | Method for operating a multistage compressor |
CN104533820A (zh) * | 2014-12-26 | 2015-04-22 | 沈阳鼓风机集团自动控制***工程有限公司 | 一种防喘振控制方法及装置 |
US10480521B2 (en) | 2016-04-01 | 2019-11-19 | Fisher-Rosemount Systems, Inc. | Methods and apparatus for detecting and preventing compressor surge |
Also Published As
Publication number | Publication date |
---|---|
DE59905412D1 (de) | 2003-06-12 |
DE19828368A1 (de) | 2000-01-13 |
EP0967396A3 (de) | 2001-07-25 |
DE19828368C2 (de) | 2001-10-18 |
EP0967396B1 (de) | 2003-05-07 |
US6164901A (en) | 2000-12-26 |
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