Plant for the conversion of high-efficiency fuel into mechanical energy

Abstract

An energy conversion plant is disclosed having one or more drive units for driving respective loads such as electric motors or centrifugal compressors. The energy conversion plant comprises at least one heat exchange recuperator for heating the pre-compressed carbon dioxide fed to the drive unit by heat produced by the drive unit itself, and a compression and pumping unit for compressing the carbon dioxide. The carbon dioxide is also supplied by a group of fluid source auxiliary plants.

Description

Technical Field

[0001] The present disclosure relates to a plant for the conversion of fuel to mechanical energy for mechanically driven applications and / or for power generation based on a thermodynamic cycle for a plurality of power trains. The thermodynamic cycle operates by using a fluid such as carbon dioxide to transfer the energy generated by the combustion of the fuel. This conversion is highly efficient.

Background Art

[0002] In the field of power generation, fossil fuels are still mainly used. However, as is well known, they have the significant drawback of causing an increase in carbon dioxide (CO2) as well as other emissions. This is one of the causes of the so-called global warming, which is potentially dangerous and is considered to be the cause of future natural disasters.

[0003] At present, alternative energy production systems do not have the ability to replace fossil fuel combustion, at least in the short term. In particular, power production by such alternative methods cannot meet the consumption needs of the evolute population.

[0004] Based on the above, research in the field has been working to improve known power production systems based on fossil fuels or biomass to reduce the production of carbon dioxide introduced into the atmosphere while maintaining a high level of energy efficiency.

[0005] Furthermore, known power production systems based on fossil fuels or biomass have been found to be expensive compared to other systems. In fact, capital expenditure and maintenance costs increase the total cost per megawatt produced. Therefore, the design trend is to decarbonize mechanically driven production operations with lower capital expenditure.

[0006] Accordingly, an improved fuel-to-mechanical energy conversion plant that can improve efficiency and thus reduce the carbon dioxide per kilowatt generated while using oral carbon dioxide introduced into the atmosphere would be welcomed in the art. SUMMARY OF THE INVENTION

[0007] In one aspect, the subject matter disclosed herein is directed to a fuel-to-mechanical energy conversion plant. The energy conversion plant has a fluid feedback line for supplying a fluid, specifically carbon dioxide, and a compression and pumping unit for compressing and increasing the pressure of the fluid feedback line. The energy conversion plant also has a plurality of drive units, each drive unit being connected to drive an associated load, such as a compressor or a generator, by burning fuel and expanding the fluid. The energy conversion plant includes one or more heat exchange recuperators connected between the fluid feedback line and the drive units, and between each drive unit and the compression and pumping unit. Each heat exchange recuperator is arranged to heat the fluid supplied by the fluid feedback line compressed by the compression and pumping unit and sent to the drive unit by exchanging the heat of the expanded discharge fluid from the drive unit. The energy conversion plant also has a group of fluid source auxiliary plants connected to the compression and pumping unit for recovering additional fluid and supplying it to the fluid feedback line.

[0008] In another aspect, the subject matter disclosed herein relates to a fluid source auxiliary plant group that includes one or more plant fluid capture units capable of generating fluid, fluid derived from a plant carbon dioxide capture unit, and a compressor connected to a compression and pumping unit. The compressor is capable of compressing fluid derived from one or more plant carbon dioxide capture units. Additionally, the fluid source auxiliary plant group includes an additional source capable of generating fluid, fluid derived from the additional source, and a compressor connected to a compression and pumping unit. The compressor is capable of compressing fluid derived from the additional source.

[0009] In another aspect, the subject matter disclosed herein relates to a drive unit that includes a combustor that burns fuel, an expander operably connected to the combustor, and a rotating shaft driven by the expander and connected to a load, such as a compressor or a generator.

[0010] In another aspect, the subject matter disclosed herein is directed to the fact that a compression and pumping unit includes a separation unit for separating water from fluid coming from a drive unit after being cooled by at least one heat exchanger recuperator, a compressor for compressing the dehumidified fluid to increase its pressure, a heat exchanger, and a pump for increasing the pressure of the fluid. The pump is disposed between the heat exchanger and a fluid feedback line.

[0011] In a further aspect, the subject matter disclosed herein is directed to an energy conversion plant having one or more fluid extraction lines for extracting fluid under pressure. The extraction line can be connected upstream of a fluid feedback line or a pump.

[0012] In another aspect, the subject matter disclosed herein is directed to a conversion plant from fuel to mechanical energy having a plurality of drive units, each drive unit being connected to an associated load, and the load can be a generator and / or a centrifugal compressor and / or a generator connected to a centrifugal compressor.

Brief Description of the Drawings

[0013] Many of the disclosed embodiments of the present invention, and the attendant advantages thereof, will be better understood and more fully appreciated when considered in connection with the accompanying drawings, by reference to the following detailed description of the invention for carrying out the invention.

Figure 1

Figure 2

[0014] In the various figures, like parts are designated by like reference numerals.

Detailed Description of the Invention

[0015] In the field of power generation where fossil fuels are used, reduction of carbon dioxide emissions, which is known to be dangerous, is required. To conserve energy, there are several power production layouts that can recover heat using a transport fluid. The fluid used can be carbon dioxide. According to one aspect, the present subject matter is directed to a layout of an energy conversion plant comprising a plurality of drive units for driving an associated load, all of the drive units operating based on the recovery of heat generated by the combustion of fossil fuels carried by carbon dioxide. Also, the energy conversion plant can recover carbon from other plants or systems that cannot recover carbon.

[0016] Referring now to the drawings, FIG. 1 shows a conversion plant for converting fuel into mechanical energy, or simply an energy conversion plant, according to a first embodiment, designated generally by reference numeral 1.

[0017] In particular, the energy conversion plant 1 basically comprises a plurality of drive units 2 each connected to its respective load, a plurality of heat exchanger recuperators 3 each connected to one associated drive unit 2, a compression and pumping unit 4 connected to the heat exchanger recuperator 3, a fluid or carbon dioxide feedback line 5 connected between the output of the compression and pumping unit 4 and the heat exchanger recuperator 3, and a carbon dioxide (or any other fluid) source auxiliary plant group 6.

[0018] Continuing to refer to FIG. 1, the energy conversion plant 1 specifically comprises three drive units, namely, a first drive unit 21, a second drive unit 22, and a third drive unit 23.

[0019] The first drive unit 21 particularly includes a combustor 211 and an expander 212 connected to the combustor 211. The combustor 211 has a fuel inlet 214 for introducing the fuel to be burned, an oxidizer inlet 215 for introducing, in the case in question, an additional fluid, namely, carbon dioxide and pure oxygen, and a fluid inlet 216 for supplying the fluid recovered as will be better explained below.

[0020] More specifically, referring to the oxidizer inlet 215, this fluid can be composed of pure oxygen or a mixture of pure oxygen and carbon dioxide taken from the described loop of this solution. The pure oxygen is produced by an industrially easy production method such as an ASU (air separation unit) or any other available system.

[0021] The rotating shaft 213 is also driven by the expander 212. Each drive unit 2 can convert fuel and carbon dioxide as inputs to the combustor 211 into mechanical energy.

[0022] Looking further at the first drive unit 21, this unit is connected to an electromechanical machine E which is connected to the expander 212 via a rotating shaft 213. In this case, the electromechanical machine E is a load on the first drive unit 21. Thus, with this configuration, the first drive unit 21 can convert the chemical energy obtained by burning fuel and expanding carbon dioxide (the fluid used) into electrical energy and, in some cases, feed it into a main power supply (not shown).

[0023] Turning now to the second drive unit 22, this unit also includes a combustor 221 and an expander 222, but in this case is connected to a centrifugal compressor C via the associated rotating shaft 223, with the centrifugal compressor C being a mechanical load in this case. Naturally, different mechanical loads can be provided depending on the need, requirement, or situation. The expander 222 also has a fuel inlet 224, an oxidant inlet 225, and a fluid inlet 226.

[0024] Also, the third drive unit 23, like the first drive unit 21 and the second drive unit 22, includes a combustor 231 and an expander 232. The expander 232 has a fuel inlet 234, an oxidant inlet 235, and a fluid inlet 236. The fluid expander 232 is connected via a rotating shaft 233 to another centrifugal compressor C as a mechanical load in this case as well.

[0025] With the layout shown in FIG. 1, the energy conversion plant 1 drives a generator E for generating electrical energy and two mechanical loads, namely the centrifugal compressor C.

[0026] In some embodiments, a gearbox can be included between the drive units 21, 22, and 23 and the associated loads connected to the associated rotating shafts 213, 223, and 233. The gear ratio of the gearbox varies according to the design needs.

[0027] In other embodiments, a different number of drive units 2 can be envisaged depending on the number and type of loads to be driven.

[0028] For each drive unit 2, namely, the first drive unit 21, the second drive unit 22, and the third drive unit 23, there is an associated heat exchanger recuperator 3. Each heat exchanger recuperator 3 has a first inlet 31 connected to the carbon dioxide feedback line 5, through which high-pressure low-temperature carbon dioxide enters each one of the heat exchanger recuperators 3, and a first outlet 32 connected to the combustor 211 of the associated drive unit 2, specifically to the fluid inlet 216, through which high-pressure high-temperature carbon dioxide is introduced into the combustor of the associated drive unit 2. For example, referring to the first drive unit 21, it is introduced into the combustor 211.

[0029] Also, each heat exchanger recuperator 3 has a second inlet 33 connected to the expander of the associated drive unit 2 via the turbine exhaust flow. For example, referring to the first drive unit 21, it is connected to the expander 212, where low-pressure high-temperature carbon dioxide used as a fluid enters the heat exchanger recuperator 3, and a second outlet 34 connected to the compression and pump system 4, as will be better explained below, from which low-pressure low-temperature fluid (carbon dioxide) is extracted from the heat exchanger recuperator 3.

[0030] The heat exchanger recuperator 3 is configured to heat the high pressure before being introduced into the drive unit 2 to drive the load connected to the drive unit 2, namely, the generator E or the centrifugal compressor C, and expanded by the combustion of fuel (details regarding the pressure and temperature operating range of the fluid, namely, carbon dioxide, are given below). The heat exchanger recuperator 3 heats the carbon dioxide coming from the carbon dioxide feedback line 5 with the heated carbon dioxide of the exhaust flow of the associated drive unit 2. In other words, the heat exchanger recuperator 3 cools the fluid (carbon dioxide), transfers its heat to the high-pressure fluid coming from the carbon dioxide feedback line 5, and then introduces the high-pressure fluid into the drive unit 2.

[0031] The heat exchanger recuperator 3 can include one or more heat exchangers to enable improved extraction of heat from the carbon dioxide feedback line 5.

[0032] Referring further to FIG. 1, it can be seen that a compression and pumping unit 4 is connected between the second outlet 34 of each drive unit 3 and the carbon dioxide feedback line 5. The compression and pumping unit 4 has the function of separating water and generally wet parts from the fluid and increasing the pressure of the fluid before it is reheated by the heat exchanger recuperator 3.

[0033] The compression and pumping unit 4 shown in the first embodiment of the energy conversion plant 1 of FIG. 1 includes a separation unit 41, a compressor 42, a heat exchanger 43, and a pump 44 connected in series.

[0034] In other embodiments, multiple sets of compressors and pumps may be present and may operate in parallel in some cases.

[0035] The separation unit 41 includes an inlet 411 where the exhaust flows from each drive unit 21, 22, and 23 are collected and an outlet 412. The separation unit 41 separates liquid water from the exhaust flows coming from each drive unit 21, 22, and 23 after being cooled by the heat exchanger recuperator 3, as well as from the carbon dioxide source auxiliary plant group 6, as will be described in more detail below.

[0036] After the fluid is dehumidified by the separation unit 41, the compressor 42 connected to the outlet 412 of the separation unit 41 compresses the fluid and thus increases the pressure of the fluid.

[0037] The fluid then passes through the heat exchanger 43, and as a result, the temperature of the fluid becomes ambient temperature.

[0038] Finally, the fluid passes through pump 44 which increases the pressure of the fluid before introducing it into the carbon dioxide feedback line 5 which, as described above, is connected to the first inlet 31 of the heat exchanger recuperator 3.

[0039] Also, the carbon dioxide feedback line 5 includes a carbon dioxide extraction line 51 by which pressurized carbon dioxide can be extracted from the plant 1. The advantages and operation of the extraction line 51 are better explained below.

[0040] The carbon dioxide source auxiliary plant group 6 includes, in the illustrated embodiment, a carbon dioxide capture unit indicated by reference numeral 61 which generates or collects carbon dioxide and has a compressor 611 for compressing the carbon dioxide derived from the plant carbon dioxide capture unit and is connected to the outlet 412 (or alternatively the inlet 411) of the separation unit 41. The carbon dioxide source auxiliary plant group 6 also includes an additional carbon dioxide source generally indicated by reference numeral 62 which is downstream-connected to an associated compressor 621 for compressing the carbon dioxide derived from a general other carbon dioxide source 621 and is connected to the outlet 412 (or alternatively the inlet 411) of the separation unit 41.

[0041] A further carbon dioxide capture unit 61 or generally an additional carbon dioxide source 62 may be added.

[0042] Specifically, the carbon dioxide capture unit 61 or the carbon dioxide source 62 may include, for example, a (CO2) supply source from a blue hydrogen (H2) plant (e.g., autothermal reforming), an acid gas removal unit in an LNG or gas treatment process, a direct air capture technology plant, and / or a (CO2) residue from an ASU unit of an oxygen (O2) plant.

[0043] The operation of the energy conversion plant 1 operates as follows.

[0044] Fuels and fluids, i.e., carbon dioxide in case of problems, enter the combustors of each drive unit 2 through the fuel inlet, oxidant inlet, and fluid inlet. In particular, the fuel and carbon dioxide enter the combustor 211 of the first drive unit 21, the combustor 221 of the second drive unit 22, and the combustor 231 of the third drive unit 23. Then, the expander of each drive unit 2 drives the associated load. More specifically, the expander 212 of the first drive unit 21 drives the generator E, while the expanders 222 of the second drive unit 22 and the expander 232 of the third drive unit 23 drive the associated centrifugal compressor C (or multiple compressors).

[0045] From each of the expanders 212, 222, and 232, carbon dioxide that is expanding but has a high temperature considering the combustion reaction is introduced into the second inlet 33 of the heat exchanger recuperator 3. In particular, in the energy conversion plant 1 according to the first embodiment, the temperature is 500 to 700 °C and the pressure is 20 to 40 bar. Different temperature ranges can be predicted depending on the type of drive unit 2 installed and the load on which each unit is operating.

[0046] Then, after passing through the heat exchanger recuperator 3, the fluid is cooled so that its temperature becomes approximately ambient temperature, but the pressure remains approximately the same. The fluid, i.e., carbon dioxide, exits the heat exchanger recuperator 3 and reaches the inlet 411 (or outlet 412) of the compression and pumping unit 4. In particular, water is extracted from the fluid through the separation unit 41 and discharged through the drain pipe 45.

[0047] The fluid before being compressed by the compressor 42 is at ambient temperature and the pressure hardly changes, i.e., remains at approximately 20 to 40 bar, but the temperature depends on the cooling temperature of the cooling medium. As described above, additional carbon dioxide is added to the flow coming from the compressors 611 and 621 of the carbon dioxide source auxiliary plant group 6 that is generated from the plant carbon dioxide capture unit 61 and the carbon dioxide source 62 and reaches the outlet 412 of the separation unit 41.

[0048] The carbon dioxide collected at the outlet 412 of the separation unit 41 enters the compressor 42. After the compressor 42, the temperature of the fluid depends on the structure of the compressor 42 (the compressor 42 may or may not be intercooled), but the pressure increases to 60 - 100 bar.

[0049] Next, the fluid passes through the heat exchanger 43 and then returns to the cooling fluid / room temperature at the same pressure of 60 - 100 bar.

[0050] Finally, the pressure of the fluid increases to 250 - 350 bar through the pump 44, and the temperature depends on the structure of the pump 44. In fact, the pump 44 in some embodiments may or may not be equipped with an intercooler depending on the pump design. Then, the fluid at ambient temperature and a pressure of 250 - 350 bar is introduced into the carbon dioxide feedback line 5.

[0051] As described above, the feedback line 5 has an extraction line 51 that can directly extract a portion of the carbon dioxide (CO2) in a pressurized and pure state before entering the heat exchanger 3. The amount of carbon dioxide extracted is such that the header pressure of the feedback line 5 is maintained relatively constant (between 250 - 350 bar), but this amount depends on the load of the plant during operation. In other words, the carbon dioxide extracted from the extraction line 51 is directly related to the fuel consumed by the plant 1.

[0052] In other embodiments, when the carbon dioxide product is required at a lower pressure by other possible end - users / applications, the extraction line 51 can also be arranged before (upstream of) the suction of the pump 44. Thus, the plant 1 for converting fuel into mechanical energy has the additional advantage of having the function of producing pure carbon dioxide at different possible pressures. Further, if necessary, two or more extraction lines connected to different areas or points of the carbon dioxide circuit can be provided in the energy conversion plant 1 to extract carbon dioxide at different pressures.

[0053] As described above, the feedback line 5 connects the pump 44 to the first inlet 31 of the heat exchanger recuperator 3. As the carbon dioxide passes through the heat exchanger recuperator 3, it undergoes a temperature increase while maintaining the same pressure. In this way, before entering each of the drive units 21, 22, or 23, the fluid has a pressure of 250 to 350 bar and a temperature of 500 to 700 °C.

[0054] As is clear, the energy conversion plant 1 uses a thermodynamic cycle in which the heat exchanger recuperator 3 recovers part of the heat generated by the drive unit 2, in particular by the expander, and can drive three different loads, even if they are different from each other, through the low emissions of carbon dioxide used as the fluid to be compressed and heated.

[0055] In this way, while maintaining the high efficiency of the plant 1, carbon dioxide captured directly in pressurized form is obtained, which also results in a reduction in capital expenditure for the maintenance of the energy conversion plant 1 itself.

[0056] Thanks to the integration of the carbon dioxide source auxiliary plant group 6, it is possible to compress all the carbon dioxide (CO2) flows with only minor operation flow rate adjustments (about 5%) of the compression and pumping units and send them to the storage part of the plant. This design approach requires fewer compression trains, thus minimizing the CAPEX of the solution, while increasing the plant's availability because the capture system depends on the main power generation cycle of the plant itself. Since the flow rate fluctuations are minor, any abnormal condition (system down or unavailable) of the carbon dioxide flow does not affect the cycle operation.

[0057] Referring now to Figure 2, a second embodiment of the energy conversion plant 1 can be seen. In particular, the layout of the plant 1 is the same as that of the first embodiment, but only one drive unit 21 is provided.

[0058] Also, the compressors 611 and 621 of the carbon dioxide source auxiliary plant group 6 can be connected either to the outlet 412 of the separation unit 41 (refer to the solid lines from the compressors 611 and 612) or to the inlet 411 of the separation unit 41 (refer to the dashed lines from the compressors 611 and 612), similar to the first embodiment shown in FIG. 1. In the latter case, the compressed carbon dioxide is collected together with that coming from the second outlet 34 of the recuperator 3.

[0059] Also, in a modified example, the electromechanical device E may be connected to the rotating shaft 223, and the centrifugal compressor C may be connected downstream of the electromechanical device E. In this layout, the generator / machine E can operate not only as a generator but also as a helper motor for the centrifugal compressor C. The electromechanical device E is actually connected to an electric conversion unit (not shown here for simplicity), and the electric conversion unit enables the electromechanical device E to operate as both a helper motor and a generator when the expander 212 has some surplus power that can be converted into electrical energy.

[0060] The operation of the power plant 1 of the second embodiment is the same as that of the power plant 1 of the first embodiment.

[0061] The advantages of this solution are that the plant efficiency is improved and direct capture of carbon dioxide at high pressure becomes possible.

[0062] Also, the advantages of this solution are that an electric motor-driven compressor train is not required, thus reducing the total capital expenditure of the plant. Also, a flat power output at ambient temperature is achieved and the efficiency is improved. Also, this solution can be applied not only to greenfield but also to brownfield (retrofit) plants.

[0063] Although aspects of the present invention have been described with respect to various specific embodiments, it will be apparent to those skilled in the art that many modifications, variations, and omissions are possible without departing from the spirit and scope of the claims. In addition, unless otherwise specified herein, the order or arrangement of any process or method steps may be changed or rearranged according to alternative embodiments.

[0064] Detailed reference has been made to embodiments of the present disclosure, and one or more examples of these are illustrated in the drawings. Each example is not intended to limit the present disclosure but is provided as an illustration thereof. In fact, it will be apparent to those skilled in the art that various modifications and variations can be made to the present disclosure without departing from the scope or spirit thereof. References throughout this specification to "one embodiment" or "an embodiment" or "some embodiments" mean that a particular feature, structure, or characteristic described in connection with the embodiment is included in at least one embodiment of the disclosed subject matter. Thus, appearances of the phrases "in one embodiment" or "in an embodiment" or "in some embodiments" in various places throughout this specification are not necessarily all referring to the same embodiment. Also, the particular features, structures, or characteristics may be combined in any suitable manner in one or more embodiments.

[0065] When presenting elements of various embodiments, the articles "a", "an", "the", and "said" are intended to mean that there is one or more of the elements. The terms "comprising", "including", and "having" are intended to be non-exclusive and mean that additional elements other than the listed elements may exist.

Claims

1. A fluid feedback line for supplying fluid, A compression and pumping unit for compressing and increasing the pressure of the fluid in the fluid feedback line, One or more drive units, Each drive unit is connected to an associated load, One or more drive units, each of which can drive the associated load by burning fuel and expanding the fluid, At least one heat exchange recuperator, Connected between the fluid feedback line and the drive unit, and between each drive unit and the compression and pumping unit, At least one heat exchange recuperator arranged to heat the fluid supplied by the fluid feedback line compressed by the compression and pumping unit and sent to the drive unit by exchanging the heat of the expanded discharge fluid from the drive unit, An energy conversion plant comprising a fluid source auxiliary plant group connected to the compression and pumping unit for recovering additional fluid and supplying it to the fluid feedback line.

2. The fluid source auxiliary plant group, One or more fluid capture units capable of generating fluid, A compressor connected to the fluid from the fluid capture unit and the compression and pumping unit, the compressor being capable of compressing the fluid from the one or more fluid capture units, the energy conversion plant (1) according to claim 1.

3. wherein the fluid capture unit captures CO from a blue hydrogen H plant such as autothermal reforming, an acid gas removal unit in an LNG or gas treatment process, a direct air capture technology plant, and / or an ASU unit of an oxygen plant ２ from the CO ２ source, the energy conversion plant according to claim 2, comprising residues from an acid gas removal unit in an LNG or gas treatment process, a direct air capture technology plant, and / or an ASU unit of an oxygen plant ２ containing residues.

4. The fluid source auxiliary plant group, One or more additional fluid sources capable of generating fluid, A compressor connected to the fluid from the additional fluid source and the compression and pumping unit, the compressor being capable of compressing the fluid from the additional fluid source, the energy conversion plant according to claim 1.

5. wherein the fluid source is CO from a blue hydrogen plant such as autothermal reforming ２ source, acid gas removal unit in an LNG or gas treatment process, direct air capture technology plant, and / or CO from the ASU unit of an oxygen plant ２ The energy conversion plant (1) according to claim 4, comprising residues.

6. The compression and pumping unit, At least one separation unit for separating water from the fluid coming from the drive unit after being cooled by at least one heat exchanger recuperator, At least one compressor for compressing the dehumidified fluid and increasing the pressure of the fluid, At least one heat exchanger, At least one pump operable to increase the pressure of the fluid, the at least one pump being connected between the heat exchanger and the fluid feedback line, the energy conversion plant (1) according to claim 1.

7. The energy conversion plant according to claim 6, wherein the separation unit includes an inlet where the discharge flow coming from the drive unit is collected and an outlet.

8. The fluid source auxiliary plant group One or more fluid capture units capable of generating fluid, A compressor connected to the fluid from the fluid capture unit and the compression and pumping unit, the compressor being capable of compressing the fluid from the one or more fluid capture units, The energy conversion plant according to claim 7, wherein the compressor connected to the fluid capture unit (61) is connected to the outlet or the inlet of the separation unit.

9. The fluid source auxiliary plant group One or more additional fluid sources capable of generating fluid, A compressor connected to the fluid from the additional fluid source and the compression and pumping unit, the compressor being capable of compressing the fluid from the additional fluid source, The energy conversion plant according to claim 8, wherein the compressor connected to the additional supply source is connected to the outlet or the inlet of the separation unit.

10. The energy conversion plant according to claim 9, wherein the pump increases the pressure of the fluid to 250 to 350 bar.

11. The energy conversion plant according to claim 6, wherein the compressor increases the pressure of the fluid to 60 to 100 bar.

12. The energy conversion plant according to claim 1, comprising at least one extraction line for extracting the fluid under pressure, the extraction line being connected to the fluid feedback line.

13. The compression and pumping unit At least one separation unit for separating water from the fluid coming from the drive unit after being cooled by at least one heat exchanger recuperator, At least one compressor for compressing the dehumidified fluid and increasing the pressure of the fluid, At least one heat exchanger At least one pump operable to increase the pressure of the fluid, the at least one pump being connected between the heat exchanger and the fluid feedback line, The energy conversion plant according to claim 12, wherein the extraction line is connected upstream of the pump (44).

14. A plurality of drive units, A heat exchange recuperator for each drive unit, Each heat exchange recuperator is connected between the fluid feedback line and the associated drive unit, and between the associated drive unit and the compression and pumping unit, The energy conversion plant according to claim 13, wherein each heat exchange recuperator is arranged to heat the fluid supplied by the fluid feedback line before being fed into the associated drive unit by exchanging the heat of the expanded discharge fluid from the associated drive unit.

15. The energy conversion plant according to claim 1, comprising a single heat exchange recuperator connected between the fluid feedback line and each drive unit, and between each drive unit and the compression and pumping unit.

16. The energy conversion plant according to claim 1, wherein the fluid mainly comprises carbon dioxide.

17. The energy conversion plant according to claim 1, wherein the heat exchanger recuperator can include one or more heat exchangers.

18. Each drive unit, A combustor, A fuel inlet for introducing the fuel to be combusted, An oxidant inlet for supplying an oxidant to the combustor, A fluid inlet for supplying the fluid to be expanded, and having a combustor, An expander operably connected to the combustor, Including a rotating shaft driven by the expander and connected to the load, The heat exchanger recuperator, A first inlet connected to the carbon dioxide feedback line, A first outlet connected to the fluid inlet of the combustor of the associated drive unit, At least one second inlet connected to the expander of at least one drive unit, A second outlet connected to the compression and pumping system, the energy conversion plant according to any one of claims 1 to 17.

19. The energy conversion plant according to claim 18, wherein the heat exchanger recuperator has a plurality of second inlets, each of which is connected to one associated expander of the drive unit.

20. The energy conversion plant according to claim 1, wherein the temperature of the fluid fed into the drive unit, which is supplied by the fluid feedback line and heated by the heat exchange recuperator, is 500 to 700 °C.

21. A first drive unit connected to an associated load, A second drive unit connected to an associated load, the energy conversion plant according to claim 1.

22. The load of the first drive unit is a generator, The energy conversion plant according to claim 21, wherein the load of the second drive unit is a generator.

23. The energy conversion plant according to claim 21, comprising a third drive unit connected to an associated load.

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