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    • 专利摘要:
    High performance solar-fossil hybrid plant. The invention relates to a solar-fossil hybrid plant (100a, 100b) comprising: - a solar concentration plant that includes: - at least a first closed circuit with a first heat transfer fluid; - a solar energy receiver (20) for heating the first heat transfer fluid; y - at least one storage medium (22) of thermal energy for storing the first heat transfer fluid; Also comprising the hybrid plant: - a closed main cycle of supercritical co2 including at least one turbine (10) whose working fluid is co2 supercritical and a combustión chamber (16) for burning a fuel, the main cycle being closed of supercritical co2 in thermal communication with the first heat transfer fluid of the solar concentration plant. The combustión chamber (16) is designed to increase a supercritical co2 temperature to an operating temperature of the turbine (10) using heat from the combustión of the fuel, without mixing the exhaust gases of combustión with the co2 working supercritical. (Machine-translation by Google Translate, not legally binding)
    公开号:ES2575352A1
    申请号:ES201431777
    申请日:2014-11-28
    公开日:2016-06-28
    发明作者:Cyrille GRELLIER
    申请人:Abengoa Solar New Technologies SA；
    IPC主号:
    专利说明:

    High performance solar-fossil hybrid plant.
    5 Field of the invention
    The invention belongs to the sector of hybrid plants that combine solar energy with natural gas to produce electricity. Specifically, in the field of hybrid plants that use, among others, supercritical CO2 and steam as turbine fluids.
    Background of the invention
    The technology of combined cycle plants that use a recovery boiler to take advantage of the energy contained in the exhaust gases of a gas turbine is known. Normally, recovery boilers
    15 are used coupled to a Brayton cycle in conventional combined cycles.
    The technology of electric power production plants that use supercritical CO2 as a working fluid (also called a turbine fluid) is still little used but its advantages are known and there are publications about it. Solutions that use supercritical CO2 as a working fluid use in most
    20 of the cases only natural gas as a source of heat. An example of this is patent document US2013 / 0213049 relating to a system for the production of electrical energy with high efficiency using carbon dioxide (CO2) as a working fluid.
    The use of solar energy as a heat source for supercritical CO2 cycles is mentioned in some
    25 patent documents, such as US-2012/0216536, in which a solar plant that operates with supercritical CO2 as a heat transfer fluid is described. This document describes the possibility of hybridization with a conventional Rankine cycle, taking advantage of the excess heat of the Brayton cycle to produce steam.
    30 A combination of the two heat input methods described in the two preceding paragraphs is solar-fuel hybridization. The concept of hybridization of solar-fossil plants consists of incorporating solar energy into cycles that work with fossil energy and have high energy efficiency. This concept applies to CO2 power cycles in US 2013/0118145, in which a system and method of generating electric power with supercritical carbon dioxide heated by hybridizing fossil fuel-solar energy is described. This patent
    35 describes a system that uses a combination of fossil and solar energy to produce energy in a Brayton cyclo.
    On the other hand, the use of energy from the sun during hours of limited or no solar radiation is also a process known and used today in the solar thermal sector; more specifically in solar thermal plants with thermal storage system. An example of this is patent US-7299633,
    40 relative to a solar concentrator with molten salt receiver that incorporates thermal storage.
    The use of a storage system in solar power plants that work with supercritical CO2 as a working fluid is described in US-2012/0216536 and US-7685820. In US-20125/0216536 the thermal storage is done by directly storing the hot CO2 in
    45 supercritical state. In US-7685820, the described system uses molten salts as a thermal storage medium and heat transfer fluid to transmit energy to a supercritical Brayton CO2 cycle.
    Description of the invention
    The present invention relates to a high-performance solar-fossil hybrid plant that has a closed main cycle in which the working fluid is supercritical CO2, and a solar concentration plant that includes a solar receiver and a heat transfer fluid, using the heat transfer fluid to heat the supercritical CO2 of the closed main cycle.
    According to a first aspect of the invention, this refers to a solar-fossil hybrid plant comprising a solar concentration plant and a closed main cycle in which the working fluid is supercritical CO2.
    The solar concentration plant includes:
    60 - at least a first closed circuit with at least one heat transfer fluid;
    -  a solar energy receiver to heat the heat transfer fluid; Y
    -  at least one thermal energy storage means for storing the heat transfer fluid.
    This solar concentration plant is sized to heat at least one heat transfer fluid 65 during the hours of sunshine in sufficient quantity to allow both the uninterrupted daytime electrical production of the plant


    as the nightly electrical production required from storage.
    The main closed supercritical CO2 cycle includes at least one turbine whose working fluid is supercritical CO2 and a combustion chamber to heat the supercritical CO2 by burning a fuel.
    In accordance with the invention:
    - The closed supercritical CO2 main cycle is in thermal communication with the heat transfer fluid of the solar concentration plant, so that the heat transfer fluid heats the supercritical CO2 before it enters the combustion chamber; Y
    - The combustion chamber is designed to increase the temperature of the supercritical CO2 to the operating temperature of the turbine using heat from the combustion of the fuel, without the combustion exhaust gases and the supercritical CO2 being mixed.
    That is, the combustion chamber is designed to give the last temperature jump to the supercritical CO2 until it reaches the operating temperature of the turbine, without the combustion gases being mixed with the supercritical CO2 to be turbined.
    For this, the combustion chamber preferably has a first compartment with an inlet for fuel and an outlet for the exhaust gases from the combustion of the fuel, and a second compartment with a supercritical CO2 inlet and outlet in which the supercritical CO2 temperature, said first and second portions being sealed together so that there is no mixture between the combustion exhaust gases and the supercritical CO2 of the closed cycle. The solar ratio (defined as the ratio of solar energy contributed / total energy contributed) is limited in existing solar-fossil hybrid plants due to the lower yield in the solar part of the cycle. This is avoided in the hybrid plant of the invention by compensating for the low yield of the solar part with a higher yield of the supercritical CO2 cycle.
    Thus, by means of the solar-fossil hybrid plant of the present invention it is possible to increase the solar proportion with respect to the current state of the art, maintaining an equivalent overall yield. Likewise, pollutant emissions from conventional Brayton cycles are reduced, and the overall cost of long-term energy production is reduced by fossil fuel savings.
    In this context, heat transfer fluid is understood as any fluid that can be heated to temperatures above 200 ° C. It is preferably a fluid based on sodium, salts and / or metals. Preferably it has a working temperature higher than 327 ° C.
    Additionally, the performance of the solar-fossil hybrid plant with supercritical CO2 cycle is improved in a preferred embodiment in which the hybrid plant further comprises a secondary cycle with steam as a working fluid, in thermal communication with the exhaust gases from the combustion chamber of the closed supercritical CO2 main cycle. These gases heat the working fluid of the secondary cycle.
    A gas recovery boiler of the supercritical CO2 cycle is preferably used in the secondary steam cycle. In this preferred embodiment, the secondary cycle uses, in the recovery boiler, the exhaust gases of the combustion chamber of the closed main cycle as a source of thermal energy to preheat and evaporate the feed water. The secondary cycle recovery boiler preferably includes at least one evaporator and a feed water preheater. The amount of saturated steam produced in the cycle depends on the energy contained in the exhaust gases of the closed main cycle.
    According to a preferred embodiment, the closed supercritical CO2 main cycle is in thermal communication with the first circuit of the first heat transfer fluid of the solar plant by means of a heat exchanger located upstream of the combustion chamber, so that said first heat transfer fluid heats Supercritical CO2 before entering the combustion chamber.
    In this case, the first heat transfer fluid may also be in thermal communication with the secondary steam cycle, so that the first heat transfer fluid supplies heat energy to the secondary steam cycle.
    According to another preferred embodiment, the plant comprises two heat transfer fluids, where the first heat transfer fluid is heated in the solar plant and the second heat transfer fluid is heated by the first heat transfer fluid by means of a heat exchanger in a second closed circuit. In such a case, the first heat transfer fluid preferably has a maximum working temperature higher than the second heat transfer fluid.
    The second closed circuit with the second heat transfer fluid may also be in thermal communication with the closed supercritical CO2 main cycle, eg, a heat exchanger, in order to provide heat to the supercritical CO2.


    In this second embodiment the second heat transfer fluid may be in thermal communication with the secondary steam cycle, so that the second heat transfer fluid supplies heat energy to the secondary steam cycle.
    This embodiment in which the hybrid plant has two heat transfer fluids, has the advantage of being able to have two fluids with different working temperatures and thus use a first heat transfer fluid of very high temperature that allows to increase the temperature of the working fluid before entering the combustion chamber, thanks to an increase in the heat input of the solar part to the closed main cycle. By using two different heat transfer fluids, one can be compatible with the water in the secondary steam cycle - e.g. a second salt-based heat transfer fluid - and the other can have a very high working temperature, a relatively high solidification temperature, and does not need to be compatible with water - e.g., a first sodium-potassium mixed heat transfer fluid or molten metal - in the closed main cycle.
    In this embodiment, the first heat transfer fluid preferably has a maximum working temperature between 650 ° C and 1100 ° C and the second heat transfer fluid has a maximum work temperature between 550 ° C and 600 ° C.
    The thermal communication between the solar concentration plant and the steam cycle can be carried out by means of at least one superheater and / or a superheater of the secondary cycle: the heat transfer fluid (s) directly or indirectly provides the energy needed in the superheater and / or in the superheater to overheat and reheat the steam produced by the recovery boiler.
    A second aspect of the invention relates to a method for generating electrical energy by means of a closed main cycle of supercritical CO2 that includes a turbine whose working fluid is supercritical CO2 and a combustion chamber for burning fuel, comprising the following steps:
    - heating at least one heat transfer fluid with energy from the sun;
    - transport the hot heat transfer fluid to the main closed CO2 cycle;
    - heating the supercritical CO2 by means of the hot heat transfer fluid before entering the combustion chamber;
    - introducing the supercritical CO2 heated by the heat transfer fluid into a combustion chamber to increase the temperature of the supercritical CO2 to a turbine operating temperature using heat from the combustion of the fuel, without the combustion exhaust gases being mixed with the Supercritical CO2 work; Y
    - generate electrical energy by passing the supercritical CO2 heated in the combustion chamber through the turbine.
    Preferably, before heating the supercritical CO2 with at least one heat transfer fluid, a temperature increase is applied to the supercritical CO2 in a recuperator that recovers the excess heat of the non-supercritical CO2 leaving the turbine.
    The different aspects and embodiments of the invention defined in the preceding paragraphs can be combined with each other, as long as they are compatible.
    Other advantages and additional features of the invention will be apparent from the detailed description that follows and will be particularly noted in the appended claims.
    Brief description of the figures
    To complement the description and in order to help a better understanding of the features of the invention, according to an example of practical implementation thereof, a set of figures is accompanied as an integral part of the description in which, with character Illustrative and not limiting, the following has been represented:
    Figure 1 shows the scheme of a first possible realization of a solar-fossil hybrid plant that includes a supercritical CO2 cycle, a Rankine cycle and with a single heat transfer fluid.
    Figure 2 shows the scheme of a second possible embodiment of a solar-fossil hybrid plant that includes a supercritical CO2 cycle, a Rankine cycle, with two heat transfer fluids.
    The components of the invention are included below:
    100th First realization of the solar-fossil hybrid plant
    10 CO2 turbine


    Compressor 12 Cooler 13
    CO2 closed cycle pump 14
    Recovery 15
    Exchanger 15a First exchanger of the second preferred embodiment of the invention 15b Second exchanger of the second preferred embodiment of the invention 16 Combustion chamber 17 Cooler 18 Exchanger 20 Solar receiver 21 Cold tank 21_I First cold tank of the second embodiment of the invention 21_II Second cold tank of the second embodiment of the invention 22 Hot tank 23 Solar plant pump 24 Second fluid delivery pump of the second embodiment of the invention 30 Recovery boiler 31 Degasifier 32 Secondary steam cycle feed pump 33 Superheater 34 High pressure turbine 35 Second superheater of the second preferred embodiment of the invention 36 First superheater of the second preferred embodiment of the invention 37 Low pressure turbine 38 Condenser 39 Condensate pump 100b Second embodiment of the solar-fossil hybrid plant
    Description of an embodiment of the invention
    In the present description possible configurations, not limiting, of the invention as well as its operation are explained in detail. The description omits and / or simplifies some aspects already known in the sector so as not to complicate the description of the hybrid plant that interests us here.
    In Figure 1 the scheme of a first possible preferred embodiment of a hybrid solar-fossil plant 100a according to the invention is shown.
    This first preferred embodiment of the 100a solar-fossil hybrid plant includes a closed main cycle of supercritical CO2 (Brayton) being this the working fluid or fluid to be turbined, a secondary steam cycle (Rankine), and a cycle corresponding to the heating of a heat transfer fluid from a solar concentration plant.
    The CO2 cycle is considered as the main cycle as it is the cycle in which the greatest amount of electrical energy is produced. The Rankine cycle is considered secondary because it uses the energy not used in the main cycle to produce electricity.
    The solar plant can be any type of concentration solar plant, for example, a tower or parabolic cylinder, which allows heating and storing a heat transfer fluid at high temperature. Temperatures above 450 ° C are considered high.
    In this first preferred embodiment of the invention the solar application heat transfer fluid called

    High temperature has a maximum working temperature that rises between 550 ºC and 600 ºC. It can be, for example, a binary mixture of nitrate salts.
    The solar concentration plant comprises a solar concentration receiver (20) for heating a high temperature heat transfer fluid. This heat transfer fluid is stored cold in a first cold tank (21). From the cold tank (21) it is sent to the solar receiver (20) in which it is heated by concentrating the solar radiation to its hot temperature, close to 567 ° C. Once the hot temperature is reached, the hot heat transfer fluid is stored in a second hot tank (22). From the second hot tank (22), part of the fluid is pumped through a pump (23) to an exchanger (15) of the closed supercritical CO2 main cycle, with which it exchanges heat, and another part (as will be explained later) to a superheater
    (33) and to superheaters (35), (36) of the secondary steam cycle. After the exchanger (15) of the closed main cycle, the heat transfer fluid exits at a temperature close to its cold temperature, approximately 300 ° C, and is sent back directly to the first cold tank (21).
    The main CO2 cycle comprises a supercritical CO2 turbine (10), whose input conditions have been set at a working pressure of 300 bar, a working temperature of 1150 ° C and a "pressure ratio" or pressure ratio of 60 (the "pressure ratio" is the turbine inlet pressure divided by the turbine outlet pressure), a compressor (11), a cooler (12), a pump (13), a recuperator (14), a exchanger (15), a combustion chamber (16) and a cooler (17).
    In the closed main cycle, the CO2 is at point (A) at low pressure, approximately 5 bar, and at room temperature, about 20 ° C; it is compressed in a first compression stage in a compressor (11) until a pressure higher than its critical pressure is reached, that is close to 80 bars. This compression process heats the CO2 to a temperature above 227 ° C (point B). This CO2 compressor (11) is configured to compress the CO2 until it acquires its supercritical properties.
    Next, the supercritical CO2 is cooled in a cooler (12), which can be an air cooler, to a temperature not lower than its critical temperature and subsequently directed to the inlet of a pump (13). In this pump (13) a second pressurization stage is applied, where it reaches the working pressure of the turbine. At the pump outlet (13) (point C), the supercritical CO2 is at a pressure of approximately 300 bar and a temperature slightly higher than the ambient temperature.
    Several temperature increases are then applied to supercritical CO2:
    - First in a supercritical CO2-CO2 recuperator (14) or exchanger: it recovers the excess heat of the CO2 that leaves the turbine (10) (point G) to transmit it to the supercritical CO2 current that leaves the pump (13). At the exit of this recuperator (14) the temperature of the supercritical CO2 is approximately 227 ° C (point D).
    - Then in the supercritical CO2 high temperature heat transfer fluid exchanger (15): the CO2 stream leaving the recuperator (14) is heated using the hot heat transfer fluid coming from the solar plant. The supercritical CO2 outlet temperature after this exchanger (15) is close to the hot temperature of the heat transfer fluid, ie about 557 ° C (point E).
    - Finally in a combustion chamber (16): this combustion chamber (16) is fed with fossil energy, for example natural gas NG, and the thermal energy of natural gas combustion is supplied to supercritical CO2 to reach the conditions of turbine inlet (10), that is, a temperature of 1150 ° C (point F). In the combustion chamber (16) the combustion gases of natural gas are not mixed with the supercritical CO2 to be turbined.
    The supercritical CO2 is then introduced into the turbine (10) from which it leaves at about 5 bars and approximately 377 ° C (point G). At this point G the CO2 is no longer in its supercritical state.
    This non-supercritical CO2 that leaves the turbine (10) is used in the recuperator (14) from which it leaves at a temperature as close as possible to room temperature after having given part of its energy to the CO2 current that leaves the pump (13).
    The main supercritical CO2 cycle is closed by cooling this non-supercritical CO2 stream in a cooler
    (17) up to the permissible compressor inlet temperature (11).
    In addition, and for a better performance of the hybrid plant of the invention, the combustion gases of natural gas leaving the combustion chamber (16) are sent directly to a recovery boiler (30) of the secondary steam cycle. It is a combustion chamber (16) in which the combustion gases of natural gas - which are those that are sent and used in the secondary steam cycle - are not mixed with the supercritical CO2 of the main work cycle. A thermal exchange takes place without mixing fluids.

    The secondary steam cycle comprises a recovery boiler (30), a degasser (31) a feed pump (32), a superheater (33), a high pressure turbine (34), two superheaters (35 and 36), a low pressure turbine (37), a condenser (38) and a condensate pump (39).
    On the other hand, in the secondary steam cycle, the high working pressure has been set, in this example, at 90 bars, the low working pressure at 5.2 bars and the degasser pressure (31) at 2 bars.
    The feed water is pumped from a degasser (31) to the recovery boiler (30) by means of a feed pump (32). At the inlet (point H) of the recovery boiler (30) the water conditions are 90 bar and approximately 127 ° C.
    From the recovery boiler (30) saturated steam comes out at 90 bar and about 307 ° C (point J). Boiler gases, meanwhile, are released into the atmosphere at the lowest allowable temperature.
    Next, the steam is superheated in a superheater (33) thanks to the heat exchange with the heat transfer fluid of the solar plant, up to a temperature close to the hot temperature of the heat transfer fluid, that is, about 557 ° C (point K). The steam is turbined in a high pressure turbine (34) from which it leaves at approximately 5.2 bar and 157 ° C (point L). The outlet steam of the high pressure turbine (34) is reheated in two superheaters (35), (36), in the first superheater (36) the steam is heated thanks to the heat of the heat transfer fluid coming from the solar plant, while that in the second superheater (35) it is thanks to a mixture of fluid from the outlet of the first superheater (36) and from the outlet of the superheater (33), thus reaching the steam again a temperature close to the hot temperature of the fluid heat carrier, about 557 ° C (point M). This superheated steam is turbined in a low pressure turbine (37), from which it leaves at the lowest possible pressure (point N), normally under vacuum conditions, before passing through a condenser (38) and back to the degasser ( 31) by driving a condensate pump (39).
    In the secondary cycle, the superheaters (35), (36) and the superheater (33) are connected such that the hot heat transfer fluid enters both the superheater (33) and the first superheater (36). The second superheater (35) receives the mixture of the heat transfer fluid streams leaving the superheater (33) and the first superheater (36) at an intermediate temperature between 290 ° C and 565 ° C (point P). The heat transfer fluid leaves the second superheater (35) at a temperature close to the cold (point Q) and is sent back to the second cold tank (21) of the solar plant.
    In this first configuration of the present invention, a global solar contribution of approximately 38.5% is estimated by an overall plant efficiency of approximately 53%, which means a considerable improvement over the state of the art.
    In addition, it is possible to reduce the consumption of fossil energy and the corresponding pollutant emissions by replacing part of the contribution of fossil energy necessary for the operation of solar power plants.
    The method for generating electrical energy according to this first preferred embodiment of the invention comprises the following steps:
    - heating at least one heat transfer fluid with energy from the sun;
    - transport the hot heat transfer fluid to the main closed CO2 cycle;
    - increase the temperature to supercritical CO2 in a recuperator (14) that recovers the excess heat
    of non-supercritical CO2 leaving the turbine (10)-heat the supercritical CO2 using the hot heat transfer fluid before entering the chambercombustion (16).- introduce the supercritical CO2 heated by the heat transfer fluid into a combustion chamber (16)to increase the temperature of the supercritical CO2 to an operating temperature of the turbine (10)higher than 1127 ° C using heat from the combustion of the fuel, without mixing the gases ofcombustion exhaust with supercritical working CO2; Y-generate electrical energy by passing the supercritical CO2 heated in the combustion chamber
    (16) by the turbine (10); Y,send the combustion gases generated in the combustion chamber (16) preferably to a boiler ofrecovery (30) to increase the temperature of a working fluid of a secondary cycle, the fluid beingSecondary cycle work preferably steam.
    In this secondary cycle:
    - feed water by pumping it from a degasser (31) to the recovery boiler (30) from which saturated steam comes out;


    - overheat this saturated steam with at least one heat transfer fluid;
    - turbine this superheated steam in a high pressure turbine (34);
    - reheat the outlet steam of the high pressure turbine (34) by at least one heat transfer fluid;
    Y5 -Turbine this superheated steam in a low pressure turbine (37)
    - send the steam to the outlet of the low pressure turbine (37) to a condenser (38) and from there to the degasser (31).
    The diagram of a second possible embodiment of a solar-fossil hybrid plant 100b 10 according to the invention is shown in Figure 2.
    This second embodiment of the 100b solar-fossil hybrid plant also includes a closed main supercritical CO2 cycle (Brayton), which is combined with a solar concentration plant with two heat transfer fluids and a secondary steam cycle (Rankine).
    15 This plant works with two heat transfer fluids:
    - A first heat transfer fluid of very high temperature (hereinafter fluid I) having a temperature
    Maximum working between 650 ºC and 1100 ºC. It can be, for example, a molten metal, sodium or a mixture based on sodium.
    - A second high temperature heat transfer fluid (hereinafter fluid II) having a maximum working temperature between 550 ° C and 600 ° C. It can be, for example, a binary mixture of nitrate salts.
    The purpose of the configuration of this second embodiment of the invention is to increase the temperature of the fluid
    25 before entering the combustion chamber (16), thanks to an increase in the heat input of the solar part. The need to use two heat transfer fluids arises as a result of the inconvenience of using a very high temperature fluid. At present, potentially usable very high temperature heat transfer fluids have these drawbacks:
    30-Most metals have a freezing temperature that is too high preventing their use in low temperature exchangers.
    - Sodium or sodium-based mixtures present risks of explosion and fire in the presence of water preventing their use in Rankine cycle exchangers.
    35 The configuration shown in Figure 2 is especially advantageous because it allows the use of a heat transfer fluid of very high temperature only in the exchangers in which its use does not present a risk of freezing or explosion. According to this embodiment of the invention, of the two heat transfer fluids only the very high temperature fluid I is heated in the solar plant and stored in the first tank (22)
    40 hot. This fluid I is used directly as a heat exchange fluid in the exchangers where there are no risks, and is also used to heat the high temperature fluid II so that this is the heat transfer fluid in the exchangers in which the use of fluid I is not possible.
    The heat exchange fluid exchange of very high temperature (fluid I) - high temperature heat transfer fluid (fluid 45 II) is done in a heat exchanger.
    This second possible embodiment of the hybrid solar-fossil plant of the invention will be explained in detail. (With the same elements as in the embodiment shown in Figure 1, the same reference number is used in this Figure 2).
    50 Fluid I is a sodium-based mixture (for example sodium-potassium mixture) with a maximum working temperature close to 751 ° C. The fluid II has a maximum working temperature between 550 ° C and 600 ° C and can be, for example, a binary mixture of nitrate salts.
    55 Sodium (fluid base I) is very reactive and carries a high risk of using it in exchangers with water or steam. However, it can be used in CO2 exchangers. The configuration shown in this second embodiment allows to benefit from the compatibility of nitrate salts (fluid II) with water in the secondary cycle, and the high working temperature of the sodium-potassium mixture (fluid I) in the cycle Closed main CO2.
    In this second preferred embodiment, the very high temperature fluid I is the fluid heated by the solar plant.
    In the main closed cycle of CO2, the same turbine (10) is considered as the one described in the embodiment of Figure 1, with the same conditions of pressure, temperature and working pressure ratio.


    The cycle from the entrance to the turbine (10) to the exit of the recuperator (14) or supercritical CO2-CO2 exchanger is also identical to that described above.
    5 However, in this embodiment, at the outlet of the recuperator (14) the supercritical CO2, which is at a temperature close to 227 ° C (point D), is sent to two heat exchanger-supercritical CO2 heat exchangers to increase its temperature:
    - A supercritical fluid II – CO2 exchanger (15a): the CO2 stream is heated using the fluid II that
    10 comes from tank 21_II after going through exchanger (18). The supercritical CO2 outlet temperature after this exchanger (15a) is close to the hot temperature of fluid II, that is, about 557 ° C (point R).
    - A supercritical I-CO2 fluid exchanger (15b): in this exchanger (15b) the very high temperature of fluid I, coming from the solar plant, is used to heat the CO2 to a temperature close to 746 ºC (point E ) before entering the combustion chamber (16).
    When leaving this exchanger (15b), the CO2 passes through the combustion chamber (16) whose role is to provide the supercritical CO2 with the energy necessary to reach the turbine inlet conditions (10), that is, a temperature 1150 ° C (point F). The gases from the combustion chamber (16) are sent directly to the recovery boiler (30) of the secondary cycle.
    The secondary cycle is identical in equipment and temperatures at each point to that described in the previous embodiment. However, the flow conditions in the steam cycle are different as the outlet temperature of the combustion chamber gases (16) is higher.
    The heat transfer fluid used to superheat and reheat steam is fluid II that has been previously heated by fluid I.
    As in the previous embodiment, the cold fluid I is stored in a first cold tank (21_I) of the solar plant. The solar receiver (20) is pumped for heating to its hot temperature. Once the hot temperature is reached, in this case close to 751 ° C, the fluid I is stored in the second hot tank (22).
    35 From this second hot tank (22) the fluid I is sent to the exchanger (15b) of the closed main cycle, from which it exits at a temperature higher than the hot temperature of the fluid II (point S). A fluid exchanger (18) I-fluid II is then sent to heat the fluid II to its working temperature. When leaving this exchanger (18) the fluid I is stored in the first cold tank (21_I).
    On the other hand, the fluid II is stored in a cold third tank (21_II), from which it is pumped by a pump (24) to the fluid exchanger (18) I-fluid II to be heated. At the exit of this exchanger (point T):
    - a part of the fluid II is sent to the supercritical fluid II-CO2 exchanger (15a), from which it is sent back to the third cold tank (21_II);
    - another part is sent to the superheater (33) and to the superheaters (35), (36) of the secondary cycle, which operate under the same conditions as in the previous embodiment.
    The method of generating electrical energy according to this second preferred embodiment of the invention comprises the following steps:
    -heat a first heat transfer fluid with energy from the sun;-heating a second heat transfer fluid from the first heat transfer fluid in a heat exchanger
    55 heat (18) -transport the first hot heat transfer fluid to the main closed CO2 cycle; - increasing the temperature to the supercritical CO2 in a recuperator (14) that recovers the excess heat of the CO2 that leaves the turbine (10); -heat the supercritical CO2 through a second hot heat transfer fluid before entering the
    60 combustion chamber (16) in a first heat exchanger (15a); -heating the supercritical CO2 by means of a first hot heat transfer fluid by means of a second heat exchanger (15b) before entering the combustion chamber; - introduce the supercritical CO2 heated in a combustion chamber (16) to increase the temperature of the supercritical CO2 to an operating temperature of the turbine (10) greater than 1127 ° C
    65 using heat from the combustion of the fuel, without mixing the exhaust gases from


    combustion with supercritical working CO2;-generate electrical energy by passing the supercritical CO2 heated in the combustion chamber
    (16) by the turbine (10); Y,send the combustion gases generated in the combustion chamber (16) preferably to a boiler of
    5 recovery (30) to increase the temperature of a working fluid of a secondary cycle, the working fluid of the secondary cycle being preferably steam.
    In this secondary cycle:
    10-feed water by pumping it from a degasser (31) to the recovery boiler (30) from which saturated steam comes out; -overheat this saturated steam with the second heat transfer fluid; -turbing this superheated steam in a high pressure turbine (34); -reheat the steam outlet of the high pressure turbine (34) by at least one superheater (35), to
    15 from the second heat transfer fluid; and -turbing this superheated steam in a low pressure turbine (37) - sending the steam at the outlet of the low pressure turbine (37) to a condenser and from there to the
    degasser (31)
    20 In this text, the word “understand” and its variants (such as “understanding”, etc.) should not be construed as excluding, that is, they do not exclude the possibility that what is described includes other elements, steps, etc.
    On the other hand, the invention is not limited to the specific embodiments that have been described but also covers, for example, the variants that can be made by the average person skilled in the art (for example, in terms of the choice of materials, dimensions, components, configuration, etc.), within what follows from the claims.

    权利要求:
    Claims (22)
    [1]
    1.-Solar-fossil hybrid plant (100a, 100b) comprising:
    5 -a solar concentration plant that includes: -at least a first closed circuit with at least one heat transfer fluid; -a solar energy receiver (20) for heating at least one heat transfer fluid; and - at least one storage means (22) of thermal energy for storing the heat transfer fluid;
    comprising the hybrid plant:
    10-a closed supercritical CO2 main cycle that includes at least one turbine (10) whose working fluid is supercritical CO2 and a combustion chamber (16) to burn a fuel, the main supercritical CO2 closed cycle being in thermal communication with the first heat transfer fluid of the solar concentration plant;
    15 the hybrid plant being characterized by that
    - The combustion chamber (16) is designed to increase a supercritical CO2 temperature up to an operating temperature of the turbine (10) using heat from the combustion of the fuel, without combustion exhaust gases mixing with the supercritical working CO2 .
    [2]
    2. Plant according to claim 1, further comprising a secondary cycle whose working fluid is steam heated by the combustion gases produced in the combustion chamber (16).
    [3]
    3. Plant according to claim 2, wherein the secondary cycle steam is heated by the combustion gases produced in the combustion chamber (16) by means of a recovery boiler (30).
    [4]
    4. Plant according to any of claims 1-3, wherein the closed supercritical CO2 cycle is in thermal communication with the heat transfer fluid circuit of the solar plant by means of a heat exchanger (15) located before the combustion chamber (16).
    [5]
    5. Plant according to any of claims 2-4, wherein the heat transfer fluid is also in thermal communication with the secondary steam cycle.
    [6]
    6. Plant according to claim 5, wherein the heat transfer fluid is in thermal communication with the cycle
    35 by means of at least one superheater (33) and / or at least one superheater (35, 36) of said secondary cycle.
    [7]
    7. Plant according to any of claims 1-6, wherein the heat transfer fluid has a temperature of
    work higher than 327ºC. 40
    [8]
    8. Plant according to any of claims 1-7, comprising two heat transfer fluids wherein the first heat transfer fluid is the fluid heated by the solar plant and the second heat transfer fluid is heated by the first heat transfer fluid in at least a second closed circuit.
    A plant according to claim 8, wherein the first heat transfer fluid has a maximum working temperature higher than the second heat transfer fluid.
    [10]
    10. Plant according to any of claims 8-9, wherein the second heat transfer fluid is in
    Thermal communication with the closed supercritical CO2 main cycle. fifty
    [11]
    eleven. Plant according to any of claims 8-10, wherein the second heat transfer fluid is in thermal communication with the secondary steam cycle.
    [12]
    12. Plant according to any of claims 8-11, wherein said first heat transfer fluid has a
    The maximum working temperature between 650 ° C and 1100 ° C and said second heat transfer fluid has a maximum working temperature between 550 ° C and 600 ° C.
    [13]
    13. Plant according to any of claims 1-13, wherein at least one heat transfer fluid is
    compound based on sodium, salts and / or metals. 60
    [14]
    14. Plant according to any of claims 1-13, wherein the combustion chamber (16) has a first compartment with an inlet for fuel and an outlet for exhaust gases from the combustion of the fuel, and a second compartment with a supercritical CO2 inlet and outlet to increase the temperature of the supercritical CO2, said first and second compartments being sealed together
    65 that there is no mixture between combustion exhaust gases and supercritical working CO2.

    [15]
    15. Method for generating electrical energy by means of a closed supercritical CO2 main cycle that includes a turbine (10) whose working fluid is supercritical CO2 and a combustion chamber (16) for burning fuel, comprising:
    5 -heat at least one heat transfer fluid with energy from the sun; -transport the hot heat transfer fluid to the closed main cycle; -heat the supercritical CO2 by means of the hot heat transfer fluid before entering the combustion chamber (16);
    10 characterized in that the method further includes: - introducing the supercritical CO2 heated by the heat transfer fluid into the combustion chamber (16) to increase the temperature of the supercritical CO2 to an operating temperature of the turbine (10) using heat from the combustion of the fuel, without the combustion exhaust gases being mixed with the supercritical working CO2;
    15 -generate electrical energy by passing the supercritical CO2 heated in the combustion chamber
    (16) by the turbine (10).
    [16]
    16. Method according to claim 15, wherein before heating the supercritical CO2 with at least one fluid
    heat transfer, a temperature increase is applied to the supercritical CO2 in a recuperator (14) that recovers the excess heat of the non-supercritical CO2 leaving the turbine (10).
    [17]
    17. Method according to any of claims 15-16, wherein the combustion gases generated in the combustion chamber (16) are sent to a recovery boiler (30) to increase the temperature of a working fluid of a cycle secondary.
    [18]
    18. Method according to claim 17, wherein the working fluid of the secondary cycle is steam.
    [19]
    19. Method according to any of claims 17-18, wherein the secondary cycle comprises: - feeding water by pumping it from a degasser (31) to the recovery boiler (30) of the
    30 saturated steam comes out; -overheat this saturated steam with at least one heat transfer fluid; -turbing this superheated steam in a high pressure turbine (34); - reheating the outlet steam of the high pressure turbine (34) by at least one heat transfer fluid; Y
    35 -Turbine this superheated steam in a low pressure turbine (37)
    [20]
    20. The method according to any of claims 15-19, wherein the plant comprises two heat transfer fluids using a first heat transfer fluid to heat a second heat transfer fluid, the first heat transfer fluid having a maximum working temperature higher than that of the second heat transfer fluid .
    [21]
    21. Method according to claim 20, wherein the second heat transfer fluid heats the supercritical CO2 of the main cycle in an exchanger (15a) before the supercritical CO2 is heated by the first heat transfer fluid in an exchanger (15b)
    A method according to any one of claims 20-21, wherein the second heat transfer fluid heats the working fluid of the secondary cycle.
    [23]
    23. A method according to any of claims 20-23 wherein the second heat transfer fluid is stored
    in a cold tank (21_II) before being heated by the first heat transfer fluid in an exchanger (18) 50
    [24]
    24. Method according to any of claims 15-23, wherein the heated supercritical CO2 enters the turbine (10) at a temperature greater than 1127 ° C.

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    同族专利:
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    WO2016083654A1|2016-06-02|
    ES2575352B1|2017-04-11|
    引用文献:
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    US9540999B2|2012-01-17|2017-01-10|Peregrine Turbine Technologies, Llc|System and method for generating power using a supercritical fluid|
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    PCT/ES2015/070863| WO2016083654A1|2014-11-28|2015-11-27|High-yield hybrid solar energy-fossil fuel plant|
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