Control method for an organic rankine cycle
An embodiment of the present invention is a method of controlling an Organic Rankine Cycle system, the system comprising at least one feed pump ( 2 ), at least one heat exchanger ( 3 ), an expansion turbine ( 5 ) and a condenser ( 6 ), the organic Rankine Cycle comprising a feeding phase of an organic working fluid, a heating and vaporization phase of the same working fluid, an expansion and condensation phase of the same working fluid, wherein said method controls an adjusted variable (X), which is a function of an overheating of the organic fluid, by means of a controller ( 20 ) that acts by varying a control variable (Y), which is a parameter of the organic fluid in its liquid phase, and wherein the adjusted variable (X) is a temperature difference (ΔT) between a current temperature of the organic fluid in vapor phase at the turbine inlet and a temperature threshold (Tlim), under which the expansion phase involves the formation of a liquid phase of the organic fluid.
1. A method of controlling an Organic Rankine cycle (ORC) system, the system comprising:
at least one feed pump ( 2 );
at least one heat exchanger ( 3 ), which further comprises a pre-heater, an evaporator and a vapor over-heater;
an expansion turbine ( 5 );
a regenerator ( 8 );
a condenser ( 6 ) and
a control apparatus;
the organic Rankine cycle comprising:
a feeding phase of an organic working fluid,
a heating and vaporization phase of the same working fluid,
an expansion and condensation phase of the same working fluid,
a regeneration phase;
and wherein said method comprises a ramp-up of the system;
wherein said method comprises controlling an adjusted variable (X), which is a function of an overheating of the organic fluid by varying a control variable (Y), which is a parameter of the organic fluid in its liquid phase,
and wherein said control apparatus performs a cycle adjustment to keep said variable (X) equal to a predetermined set point, said cycle adjustment is performed by acting on a flow rate of the organic fluid entering said at least one heat exchanger ( 3 ) which heats and vaporizes said organic fluid;
wherein said flow rate is adjusted by varying at least one feed pump ( 2 ) rotational speed or by adjusting a valve opening, said valve is located downstream of said at least one feed pump ( 2 );
and wherein said adjusted variable (X) is a temperature difference (ΔT) between a current temperature of the organic fluid in vapor phase at a turbine inlet and a temperature threshold (Tlim) under which said expansion and condensation phase involves the formation of a liquid phase of the organic fluid, according to a supercritical cycle;
and wherein said expansion phase produces no liquid formation and thus prevents turbine damage.
2. The method according to claim 1 , wherein said temperature threshold (Tlim) is a function of the vapor pressure in said expansion turbine ( 5 ) and represents a safety margin with respect to a critical condition, which would cause liquid formation during the expansion in the turbine.
3. The method according to claim 1 , wherein said control variable (Y) is a flow rate (Q) of the organic fluid at an inlet of said at least one heat exchanger ( 3 ).
4. The method according to claim 3 , wherein the adjustment of said flow rate (Q) of the organic fluid at inlet of said at least one heat exchanger ( 3 ) is realized by varying a rotational speed (V) of the at least one feed pump ( 2 ) of the organic fluid.
5. The method according to claim 3 , wherein the flow rate (Q) of the organic fluid at the inlet of said at least one heat exchanger ( 3 ) is adjusted by varying an opening degree (x) of said valve located downstream of said at least one feed pump of the organic fluid.
6. The method according to claim 1 , wherein said regenerator ( 8 ) exchanges heat between the organic fluid in a liquid phase, flowing from said at least one feed pump ( 2 ) to said at least one heat exchanger ( 3 ), and the organic fluid in vapor phase flowing towards the condenser ( 6 ).
7. The method according to claim 1 , wherein said ramp up of the system is carried out by:
beginning a starting phase with high values of a temperature difference (ΔT) which would lead to low pressure values in the turbine;
limiting the temperature difference (ΔT) by varying a maximum temperature of a hot thermal source and therefore, by increasing the temperature difference (ΔT), the maximum pressure value reachable in the Organic Rankine cycle (OCR) decreases;
gradually decreasing the value of the temperature difference (ΔT), until the Organic Rankine cycle (OCR) reaches target conditions, either subcritical or hypercritical, achieving that a transient phase from a subcritical cycle to a hypercritical cycle can be gradually performed.
8. A control apparatus for controlling an Organic Rankine cycle (ORC) system, said control apparatus comprising:
an Electronic Control Unit (ECU);
a controller ( 20 );
a data carrier associated to said Electronic Control Unit, and
a computer program configured for performing the method according to claim 1 and wherein said computer program is stored on a computer program product in the data carrier;
and wherein the controller ( 20 ) is a PID (Proportional, Integral and Derivative) controller having as output an adjustment of the flow rate of the organic fluid entering said at least one heat exchanger ( 3 ).