Patent Application
20200095897
The invention refers to a method for operating a thermodynamic cycle process apparatus, in particular an Organic Rankine Cycle (ORC) apparatus with an expansion machine and a thermodynamic cycle process apparatus which can be operated with the method according to the invention.
If a thermodynamic cycle process apparatus, for example an Organic Rankine Cycle apparatus, is coupled to a generator or a motor/generator unit in order to feed energy into a power grid, the expansion machine is subjected to speeds due to the grid frequency. A similar situation occurs when coupling with another external apparatus, such as a device with a combustion engine, to support it.
It has turned out that, for example, a coupling process of the external apparatus can cause damage to the expansion machine of the thermodynamic cycle process apparatus, especially in the bearing of the rotating elements of the expansion machine. According to the applicant's experience, this damage occurs when power is effectively supplied to the expansion machine. This applies in particular to screw expansion machines.
A coupling of a generator operated with an ORC system is described in EP 1759094 B1. Coupling to the power grid occurs when the measured generator speed matches the grid frequency, which therefore implies a power-free coupling. This speed measurement, however, represents an additional cost or, in the case of (semi-) hermetic machines, is even extremely expensive because the shaft is not directly accessible from the outside. Speed measurement based on the generated voltage is not possible with asynchronous generators that are not connected to the grid or otherwise not magnetized.
The object of the invention is to avoid the aforementioned disadvantages.
The invention describes the solution to the above problem by adding model-based control and/or monitoring to the operation (starting process, normal operation, shutdown) of the thermodynamic cycle process apparatus with the expansion machine.
The solution according to the invention is defined by a method with the features set out in claim 1.
The invention thus discloses a method for controlling a thermodynamic cycle process apparatus, in particular an ORC device, wherein the thermodynamic cycle process apparatus comprises an evaporator, an expansion machine, a condenser and a feed pump, and the expansion machine is coupled to an external apparatus in normal operation, and wherein the method comprises the following steps: measuring an exhaust steam pressure downstream of the expansion machine; and adjusting a volume flow of the feed pump in accordance with a computer-implemented control model of the thermodynamic cycle process apparatus as a function of the measured exhaust steam pressure and a target rotational speed of the expansion machine as input variables of the control model and with the volume flow of the feed pump as output variable of the control model.
The exhaust steam pressure downstream of the expansion machine can be measured between the expansion machine and the feed pump, especially between the expansion machine and the condenser or between the condenser and the feed pump. When measuring between the condenser and the feed pump, the pressure loss of the condenser can either be neglected or it is known and taken into account in the control.
Only the measured exhaust steam pressure or a measured value of the exhaust steam pressure corrected by a correction value is used as input variable in the control model (except for the target rotational speed of the expansion machine). When measuring the exhaust steam pressure between condenser and feed pump, a pressure loss of the condenser and/or pipelines between the expansion machine and the measuring point can be taken into account and the measured exhaust steam pressure corrected accordingly.
The volume flow of the working medium pumped by the feed pump can be controlled in various ways. Setting the speed of the feed pump is one way of adjusting the volume flow of the feed pump, other ways would be a throttle (throttle valve) or a 3-way valve downstream of the pump or adjusting the feed characteristics of the feed pump by adjusting a guide wheel or a piston stroke.
The advantage of the method according to the invention is that the measuring point for the speed measurement required according to the state of the art can be avoided with the help of the model-based control within the scope of the present invention.
The method according to the invention can be further developed in such a way that a starting process of the thermodynamic cycle process apparatus can include the following steps: controlling the expansion machine to a state in which the target rotational speed of the expansion machine is greater than or equal to a predetermined speed of the external apparatus to be coupled to the expansion machine, the external apparatus to be coupled comprising in particular a generator, a generator/motor unit or a device driven by a separate motor; and subsequently coupling the expansion machine to the external apparatus. If the speeds are the same, a power-neutral coupling takes place. If the speed of the expansion device at coupling is (slightly) higher than a synchronous speed, then the effective power of the expansion machine is positive and therefore does not damage the bearings.
Another further development is that the following further steps can be carried out: measuring the live steam pressure upstream of the expansion engine; comparing the measured live steam pressure with a current model live steam pressure according to the control model; and initiating a shutdown process and/or aborting the starting process if the measured live steam pressure is more than a predetermined amount or more than a predetermined fraction below the model live steam pressure which depends on the measured exhaust steam pressure.
The live steam pressure upstream of the expansion machine can be measured between the feed pump and the expansion machine, in particular between the evaporator and the expansion machine or between the feed pump and the evaporator. The live steam pressure could, for example, be measured at the outlet of the feed pump/inlet of the evaporator and corrected for the pressure loss of the evaporator and/or the piping to the inlet of the expansion machine.
This can be further developed to the effect that during the starting process the expansion engine is coupled to the external apparatus only if the measured live steam pressure is greater than or equal to the model live steam pressure.
According to another further development, the following further steps can be carried out: measuring a heat source temperature of a heat source supplying heat to the thermodynamic cycle process apparatus via the evaporator; and starting only if the measured heat source temperature is greater than or equal to a current model heat source temperature according to the control model.
Another further development is that a shutdown of the thermodynamic cycle process apparatus may include the following steps: decoupling the expansion machine from the external apparatus if the live steam pressure and/or the heat source temperature fall below a respective predetermined threshold; and opening a bypass line to bypass the expansion machine.
This can be further developed so that the next step is still carried out: reducing the volume flow (in particular by reducing the rotational speed) of the feed pump until a power-neutral or force-free state of the expansion device is achieved according to the control model, in which the power consumed by the expansion device is equal to the power output by the expansion device or the total force acting on the expansion device in the direction of an axis of rotation of the expansion device is equal to zero.
The control model according to the invention can include analytical and/or numerical and/or tabular relations of the input and output variables.
The above object is also solved by a thermodynamic cycle process apparatus according to claim 10.
The thermodynamic cycle process apparatus according to the invention (in particular an ORC device) comprises an evaporator, an expansion machine, a condenser, and a feed pump, wherein the expansion machine is coupled to an external apparatus during normal operation; wherein the thermodynamic cycle process apparatus further comprises: an exhaust steam pressure measuring device for measuring an exhaust steam pressure downstream of the expansion machine; and a control device for setting a volume flow of the feed pump in accordance with a control model of the thermodynamic cycle process apparatus stored in a memory of the control device as a function of the measured exhaust steam pressure and a target rotational speed of the expansion machine as input variables of the control model and with the volume flow of the feed pump as output variable of the control model. The exhaust steam pressure downstream of the expansion machine can be measured at the points mentioned above in connection with the method according to the invention.
The thermodynamic cycle process apparatus according to the invention can be further developed to the effect that the control device is designed to perform the following steps during a starting process of the thermodynamic cycle process apparatus: controlling the expansion machine to a state in which the target rotational speed of the expansion machine is greater than or equal to a predetermined speed of the external apparatus to be coupled to the expansion machine, the external apparatus to be coupled comprising in particular a generator, a generator/motor unit or a device driven by a separate motor; and subsequently coupling the expansion machine to the external apparatus.
According to another development, the thermodynamic cycle process apparatus further comprises a live steam pressure measuring device for measuring a live steam pressure upstream of the expansion machine; the control device being adapted to compare the measured live steam pressure with a current model live steam pressure according to the control model, and to initiate a shutdown process and/or abort a starting process if the measured live steam pressure is more than a predetermined amount or more than a predetermined fraction below the model live steam pressure. The live steam pressure upstream of the expansion machine can be measured at the points already mentioned above in connection with the method according to the invention.
Another further development is that the thermodynamic cycle process apparatus further comprises: a heat source temperature measuring device for measuring a heat source temperature of a heat source supplying heat to the thermodynamic cycle process apparatus via the evaporator; wherein the control device is adapted to perform the starting process only when the measured heat source temperature is greater than or equal to a current model heat source temperature according to the control model.
According to another further development, the thermodynamic cycle process apparatus further comprises a bypass line as a direct connection between the evaporator and the condenser for bypassing the expansion machine; the control device being adapted to perform the following steps during a shutdown operation of the thermodynamic cycle process apparatus: decoupling the expansion machine from the external apparatus if the live steam pressure and/or the heat source temperature fall below a respective predetermined threshold; and opening the bypass line by means of a valve in the bypass line.
Another further development is that the thermodynamic cycle process apparatus further comprises: a coupling for coupling the expansion apparatus to the external apparatus; and/or a gear for adjusting a speed ratio from the expansion apparatus to the external apparatus.
The further developments mentioned can be used individually or combined as required.
Further features and exemplary embodiments as well as advantages of this invention are explained in more detail below using the drawings. It goes without saying that the embodiments do not exhaust the scope of this invention. It also goes without saying that some or all of the features described below can be combined in other ways.
As an example, an ORC process is assumed in the following to be a thermodynamic cycle process.
In addition, the cycle process apparatus 100 according to the invention includes an exhaust steam pressure measuring device 61 for measuring an exhaust steam pressure downstream of the expansion machine 20. As an example, the exhaust steam pressure measuring device 61 is provided here between the expansion machine 20 and the condenser 30. However, it is also possible to arrange these between the condenser 30 and the feed pump, if necessary taking into account a pressure loss in the condenser 30 in the form of a correction value to the measured exhaust steam pressure.
In addition, a control device 80 is provided for setting a volume flow of the working medium pumped by the feed pump 40 (e.g. by setting a rotational speed of the feed pump (40) in accordance with a control model of the thermodynamic cycle process apparatus (100) stored in a storage (81) of the control device (80), only as a function of the measured exhaust steam pressure (corrected by the said correction value) and a target rotational speed of the expansion machine (20) as input variables of the control model and with the volume flow of the feed pump (40) (e.g. in the form of the rotational speed of the feed pump (40) as output variable of the control model.
In the case of coupling a generator 25 (or a motor/generator unit), a coupling switch 28 may also be provided, which couples the generator 25 (or the motor/generator unit) to or uncouples it from a power grid.
The underlying problem of the solution according to the invention is discussed below.
The invention is based on the following problem. If the expansion machine is operated by a motor, i.e. power is entered, for example, by the generator 25 in motor operation due to a fixed speed specification or by the external process, there is a risk of damage, since the power flow does not correspond to the design point (“defective operation”). The force direction on the rotors of the expansion machine (as shown in
Damage is caused, for example, by abrasion or chip formation due to contact of rotating bodies with the housing, since the force effect is not supported by the bearing (
However, this motor operation occurs automatically if the expansion machine is still at a standstill at the switch-on point (present pressure position cannot overcome the necessary post-compression) or the speed is below the switch-on synchronous speed (connection point a) in
For a better understanding, we speak here of post-compression (more precisely: post-compression power) and post-expansion (more precisely: post-expansion power). In principle, however, this is a different part of the ejection process (PAA) which has to be applied by the expansion machine to eject the medium at the end of the expansion in the chamber of the expansion machine against the exhaust steam pressure pAD. This distinction thus refers to the reference (PAA,ref), where the opening pressure of the chamber is equal to the exhaust pressure behind the chamber.
Thus, the following applies:
For pchamber>PAD:
P
post-expansion
=P
AA;ref
−P
AA,act
; P
post-compression=0
For pchamber<PAD:
P
post-compression
=P
AA;ref
−P
AA,act
; P
post-expansion=0
For pchamber=PAD:
P
post-expansion=0;Ppost-compression=0
For damage-free connection, the expansion machine must therefore be at least at a neutral power point at connection speed (connection point b) in
Before the generator or external process is connected, no power can be dissipated, i.e. the machine may be accelerated uncontrolled to damage if the steam supply is undefined.
Knowledge of the current expansion machine speed would in principle be possible with the aid of a speed measurement. However, this speed measurement represents an additional cost or is only very costly to implement.
The defective condition due to power supply to the expansion machine continues to occur during operation and shutdown if the post-compression power exceeds the expansion power due to insufficient pressure positions (see
P
gross
=P
expansion
+P
post-expansion
+P
post-compression
The pressure ratio π is defined as the ratio of live steam pressure to exhaust steam pressure:
π=PFD/pAD
with
pFD=live steam pressure
pAD=exhaust steam pressure
In addition to the directly measurable pressure ratio used here, the volume ratio ϕ can also be used instead:
ϕ=PAD/PFD
with
PFD=live steam pressure
pAD=exhaust steam pressure
Both ratios (π, ϕ) provide the same result in a first approximation.
Here, the expansion machine 20 is brought to a defined starting point (speed), which prevents damage to the expansion machine when it is switched on. The necessary measured values of flow rate and speed of the expansion machine, which can be determined by expensive measurement technology, are bypassed by model-based control.
This model-based control is based on the basics of the knowledge of the power-neutral point of the expansion machine (as shown in
Furthermore, the speed at which the expansion machine is operated in this power-free state is determined by the steam volume flow supplied. {dot over (V)}FD dependent:
n
EM
={dot over (V)}
FD
FD/(Vchamber*K)
with
nEM=expansion machine speed of rotation
{dot over (V)}FD=live steam volume flow
Vchamber=high pressure chamber volume of the expansion machine
K=chamber number per revolution
Thus the condition of the expansion machine 20 (in particular its speed) can be clearly determined by knowing the live steam pressure, exhaust steam pressure and live steam volume flow (depending on the desired switch-on speed). The above equation for determining the expansion machine speed initially represents the simplest form and can be further improved in accuracy, e.g. by correction by means of a variable speed leakage volume flow. From the expansion machine speed and the other thermodynamic variables, the electrical power and thus e.g. a state of the thermodynamic cycle can be derived.
However, the measurement of the live steam volume flow is a relatively cost-intensive measurement, which thus has a negative influence on the economic efficiency of the overall system.
From the live steam volume flow it is relatively easy to determine the live steam mass flow, which could also be measured in the liquid phase between feed pump 40 and evaporator 10. However, the necessary measuring instruments (e.g. Coriolis) are also associated with considerable costs.
However, there is also a direct relation between the live steam volume flow and the liquid volume flow conveyed by the feed pump, which can be determined via the densities:
{dot over (V)}SP={dot over (V)}FD*PFD/Pfl
with
{dot over (V)}SP=volume flow through the feed pump
{dot over (V)}FD=volume flow through the expansion machine
pFD=density of the live steam through the expansion machine
pfl=density of the liquid medium in the feed pump
It should be noted that the live steam density also depends on the position of the exhaust steam pressure, since it is a function of the live steam pressure (and the live steam temperature). The live steam pressure itself is a function of the exhaust steam pressure in this case of performance-free expansion machine operation. This circumstance (pFD and {dot over (V)}SP) also leads to the fact that a static start behaviour with fixed speed specification of the feed pump depending on the exhaust steam pressure, which depends on the condensation conditions such as e.g. heat sink temperature, can lead to a start process with motor drive (high exhaust steam pressure pAD; sub-synchronous to standstill of the expansion machine) or to an acceleration of the expander beyond the permissible speed (low pAD).
Furthermore, the necessary pressure difference from the neutral point, which the feed pump 40 has to apply, is given as
p
SP
p
FD
−p
AD
Thus the volume flow in the feed pump 40 and the pressure difference which the feed pump 40 has to apply are known. By modelling the feed pump 40, a speed point of the feed pump 40 can now be found at which this condition of pressure difference and flow rate is fulfilled.
This results in a start control which assigns a value for the feed pump speed to each exhaust steam pressure and the associated switch-on speed (target rotational speed of the expansion machine 20) without the need for additional measuring points. A disadvantage is that the actual values of these important measured variables are thus represented by a model and actually remain unknown in the system.
However, the following mechanisms can still jeopardize damage-free switching:
1) A failure of the feed pump (cavitation, motor damage etc.) leads to a lower pressure level/flow rate than is required for damage-free operation.
2) A bypass 50 (
3) The temperature level of the heat source is below the necessary level to be able to evaporate the working medium at the necessary live steam pressure.
The problems under 1)+2) can be avoided by additionally monitoring the achieved process variable of the live steam pressure upstream of the switch-on process. If the pump and bypass behave regularly, this must correspond to the value determined in the modelling. If it deviates downwards, the start can be aborted without damaging the expansion machine 20.
The problem under 3) is avoided by also storing a model of the necessary heat source temperature (THW,
During operation, very small pressure differences from pFD to pAD can occur if there is no heat supply and poor heat dissipation (e.g. high air temperature/water temperature). It is also possible that this may lead to a faulty operation of the system as shown in
In the shutdown program, the temperature position on the heat input side of the system is reduced in the desired manner in order to achieve a safe standstill of the system at moderate temperatures. This lowering, however, reduces the live steam pressure pED and thus the pressure quotient Tr. In extreme cases, this may also result in faulty operation during shutdown.
To prevent this, the hot water temperature (THW) required for safe operation is also monitored by means of a measuring device 63 and the live steam pressure (pFD) by means of a measuring device 62. If the pressure falls below a defined threshold value, the expansion machine is decoupled from the power connection, i.e. neither power is supplied nor discharged, and at the same time the bypass 50 is opened by means of valve 51 in order to reduce the pressure on the live steam side and to allow the system to continue running if necessary. Switching off in relation to a live steam pressure depending on the exhaust steam pressure avoids on the one hand the faulty operation, but on the other hand also that the pressure position is still so high that switching off the expander power connection (decoupling the expansion device) can turn it up uncontrolled before the pressure can be sufficiently reduced via the bypass 50. This safety can be additionally achieved by gradually reducing the feed pump speed to a value corresponding to the zero power point from the modelling. This achieves an operating state in which, in the event of a further control of the expansion machine (of the expander) 20 or of an error in the bypass opening, the expansion machine 20 is operated at a defined speed below a defective speed in a power-neutral manner. Overall, the operating times in the power-neutral range must also be minimised, as the very low bearing load means that operation shortens the service life.
The framework of the control strategy is briefly summarised below and illustrated in
As a result of the modelling, there is a control device 80 of the feed pump 40, which operates without measured values of the expander speed or the flow rate and contains the low pressure (exhaust pressure) as input variable, in order to control to a target rotational speed of the expansion device 20.
In order to ensure the correct functioning of the feed pump 40 and the bypass 50 (a failure in turn leads to faulty motor operation), the live steam pressure and the hot water temperature from the modelling are also used as monitoring variables (falling below model value means deviation in the system with damage potential).
The embodiments shown are only exemplary and the complete scope of the present invention is defined by the claims.
| Number | Date | Country | Kind |
|---|---|---|---|
| 17161565.1 | Mar 2017 | EP | regional |
| Filing Document | Filing Date | Country | Kind |
|---|---|---|---|
| PCT/EP2017/080029 | 11/22/2017 | WO | 00 |
