Carbon capture process

Abstract

A CO2 capture process comprising: -Hydrating quicklime materials (16) and / or quick dolomitic lime materials (16') to produce hydrated materials (17); - Transferring at least a portion of the heat generated during the hydration to at least one energy distribution unit (20); - Controlling at least one secondary working medium flow (52.1, 52.2, 52.3) and / or at least one secondary electric power flow (62) between at least one energy distribution unit (20) and at least one energy utilization unit (30.1, 30.2, 30.3, 30.4); -Capturing at least some CO2 from at least one stream containing CO2 (71, 71*) to reduce the CO2 content in said stream, in at least one CO2 treatment unit (35.1, 35.2, 35.3).

Description

CARBON CAPTURE PROCESSTechnical Field[1] The present invention pertains to a process for carbon capture and a system therefor.Background Art[2] CO2 emissions linked to human activities are recognized as being responsible for climate change. Efforts are being made to decrease the quantity of CO2 released into the atmosphere.[3] In this regard, quicklime (alternatively hydrated lime) produced from a source of calcium carbonate such as natural limestone, can be used for capturing CO2 according to the following reaction:CaO + CO2 -> CaCOs + heat AH= -178 kJ / mol (Equation 1 ) AlternativelyCa(OH)2+ CO2 -> CaCO3+ H2O AH= -113 kJ / mol (Equation 2)[4] The formed carbonate can then be calcined again to produce lime and substantially pure CO2 for use or sequestration:CaCOs + heat -> CaO + CO2 AH= 178 kJ / mol (Equation 3)[5] The heat necessary for the calcination can be provided by the combustion of fuel or other types of heat sources (e.g. electrical kiln). Industrial oxygen can be advantageously used instead of air in order to avoid dilution of the CO2 with nitrogen from the air.[6] After a purification step, both the CO2 resulting from the decomposition of calcium carbonate and from the combustion of fuel can be sequestered.[7] The produced lime or hydrated lime can then be re-exposed to atmospheric air or flue gases for subsequent CO2 capture.[8] Traditionally, the heat generated during a lime hydration process (see Equation 4 below) is not recovered, even though the heat generated during hydration (slaking) is significant, representing on third of the heat required to decarbonate limestone material.CaO + H2O -> Ca(OH)2 + heat AH= -65 kJ / mol (Equation 4)[9] There are at least two main processes commonly used to produce hydrated lime: wet slaking, where quicklime is hydrated with a large amount of water to form a milk of lime, and dry hydration, which generates hydrated lime powder. Industrial applications for hydrated lime primarily involve : flue gas treatment such as removal of sulfur dioxide and hydrogen chloride, agriculture, and water treatment.

[0010] Lime hydrate compositions are more effective in capturing carbon in the atmosphere or flue gases than quicklime, as lime hydrate presents a higher specific surface area and / or porous volume, allowing for improved reaction rates.

[0011] Because of environmental considerations, the production capacity of hydrated lime is expected to grow because of its efficacy as a CO2 capture sorbent. This growth will also lead to an increased amount of heat generated during the slaking process. If nothing is done, this source of waste heat would be released into the atmosphere and lost.

[0012] Furthermore, a CO2 capture system typically encompasses several subsystems that require a significant amount of energy of different types. These types include a hot source needed in the base amine process to desorb CO2 and a cold source for the CO2 purification unit using cryogenic liquefaction. Additionally, an electricity source is also needed to operate these systems (compression of CO2 gas, pumping of amine solvent, etc.) or, alternatively, to drive fans for a direct air capture process. Currently, heat, cold or power needs are supplied by combustion of fuel or electrical network. With a growing demand for such CO2 capture systems, energy demand is expected to soar. Continuing to rely on the electrical network as the main source, especially when produced from burning fossil fuels, is neither economically nor environmentally sound, rendering such an approach suboptimal.

[0013] US2020108346A1 , WO2023140985A1 , US2019359894A1 and CN114991885A 711340 disclose CO2 capture processes according to the state of the art.Aims of the Invention

[0014] The invention aims to provide a solution to overcome at least one drawback of the teachings provided by the prior art.

[0015] In particular, the present invention aims to optimize the energy efficiency of capturing CO2, and consequently, the overall energy consumption, advantageously, this optimization being achieved through an optimized integration of different energy sources.

[0016] More preferably, the present invention aims to exploit the energy potential of a hydration unit in a CO2 capture context.Summary of the Invention

[0017] For the above purpose, the invention is directed to a CO2 capture process comprising the following steps:-supplying quicklime materials and / or quick dolomitic lime materials to a hydration unit; -a least partly hydrating said materials in the hydration unit with water as liquid and / or vapor to produce hydrated materials; -transferring at least a portion of the heat generated during the hydration to at least one primary working medium flow and optionally transforming the at least one working medium flow into a primary electrical power flow in a first power generation system;- capturing at least some CO2 from at least one CO2 containing stream to reduce the CO2 content in said stream, in at least one CO2 treatment unit; -exchanging energy between at least one energy distribution unit and at least one energy utilization unit by using energy exchanges with at least one of — at least one secondary working medium flow and / or — at least one secondary electric power flow;-controlling (at least one of) the at least one secondary working medium flow and / or the at least one secondary electric power flow between the at least one energy distribution unit and the at least one energy utilization unit, preferably depending on the power and / or energy need of the at least one energy utilization unit, ^transferring, preferably in the at least one energy distribution unit, at least one of: --energy such as heat and / or mechanical energy, from the at least one primary working medium flow to the at least one secondary working medium flow, and / or — electric energy from the primary electrical power flow to the at least one secondary electric power flow.

[0018] According to specific embodiments of the invention, the CO2 capture process comprises one or more of the following features / steps:- the at least one energy utilization unit comprises a first energy utilization unit, said unit comprising or consisting of the at least one CO2 treatment unit;- the at least one CO2 treatment unit comprises at least one of: o a CO2 purification unit, such as a pressure or temperature swing adsorption apparatus, a chemical or physical absorption apparatus, a membrane separation apparatus, an amine-based gas treating apparatus, or cryogenic gas treating apparatus, said unit having an inlet supplied with a first of the at least one CO2-containing stream and a first outlet with a CO2-enriched stream and a second outlet with a CO2-depleted stream; o a CO2 carbonator unit with an inlet supplied with a second of the at least one CO2-containing stream and an outlet with a CO2-depleted stream, said unit being adapted to contact at least one of the hydrated materials, the quicklime materials and / or the quick dolomitic lime materials with CO2, thereby forming synthetic carbonated materials, preferably as powder and / or shaped bodies; o a direct air capture unit capturing CO2 in a third of the at least one CO2-containing stream as ambient air or conditioned air, thereby forming synthetic carbonated materials, preferably as powder and / or shaped bodies, said unit being either :- adapted to contact at least one of the hydrated materials, the quicklime materials and / or the quick dolomitic lime materials with said CO2-containing steam, or- adapted to contact carbonate ions resulting from the dissolution of some of the CO2 of said CO2-containing steam with ions from the dissolution at least one of the hydrated materials, the quicklime materials and / or the quick dolomitic lime materials;- the at least one CO2 treatment unit comprises the CO2 purification unit and optionally at least one of the CO2 carbonator unit and / or the direct air capture unit;- decarbonating at least one of limestone materials, dolomitic stone materials, at least some of the synthetic carbonated materials produced in theCCh carbonator unit, at least some of the synthetic carbonated materials produced in the direct air capture unit, or other synthetic carbonated materials, in particular produced in another plant , in a decarbonation reactor, thereby forming the quicklime materials and / or the quick dolomitic lime materials and optionally at least a portion of the first of the at least one CCh-containing stream, preferably the decarbonation reactor being a shaft kiln, a regenerative multi-shaft kiln, such as a parallel flow regenerative kiln, an annular kiln, a fluidized bed calciner, a circulated fluidized bed calciner, an entrained bed calciner or an electrolysis unit;- forming the at least a portion of the first of the at least one CCh-containing stream from the decarbonation reactor;- feeding the decarbonation reactor with at least some of the synthetic carbonated materials produced in at least one of the CO2carbonator unit and / or the direct air capture unit;- forming at least a portion of the second of the at least one CCh-containing stream in a power plant combusting fuel, in particular burning fossil fuel, and generating in said plant at least one of: energy, such as heat and / or mechanical energy, transferred to one of the at least one secondary working medium flow and / or electricity transferred to one of the at least one secondary electric power flow;- the at least one energy utilization unit comprises a second energy utilization unit, said second energy utilization unit comprising or consisting of the decarbonation reactor and optionally at least one of:- a cooling unit for cooling the quicklime materials and / or the quick dolomitic lime materials produced in the decarbonation reactor and / or- a pre-heating unit for heating at least part of one of the limestone materials, the dolomitic stone materials ,the at least some of the synthetic carbonated materials produced in the CO2 carbonator unit, the at least some of the synthetic carbonated materials produced in the direct air capture unit, or the other synthetic carbonated materials to be processed in the decarbonation reactor;- the at least one energy utilization unit further comprises a third energy utilization unit, which comprises or consists of a heating network, in particular a district heating network, said process further comprising supplying the heating network using heat from one of the at least one secondary working medium flow or heat from at least one tertiary working medium flow; the at least one energy utilization unit further comprises a fourth energy utilization unit, which consists of or comprises a heat driven chiller such as an ammonia absorption refrigeration unit, said process further comprising mixing a first medium such as ammonia with a second medium such as water, pumping said mixture in a desorber or boiler, separating the first medium from the second medium by evaporation using the heat at from one of the at least one secondary working medium flow, optionally said process further comprising cooling at least a cold utilization unit, such as the cryogenic gas treating apparatus or a centralized cooling network, with the heat driven chiller;- transferring at least a portion of energy, such as heat and / or mechanical energy from one or more of the at least one utilization unit to another of the at least one utilization unit via one or more of the at least one secondary working medium flow in a cascade configuration;- storing some of the heat and / or electric energy supplied by at least one of: - the at least one primary working medium flow and / or the primary electrical power flow, respectively, and / or-the at least one secondary working medium flow and / or the at least one secondary electrical power flow, into an energy storage unit preferably selected from the group comprising a heat sink, a heat battery, a hot water storage tank, a regenerator, a battery, an energy storage dam and a thermo-chemical energy storage unit, in particular thermo-chemical energy storage unit comprising at least one of a first storing unit with at least some of the hydrated materials and / or a second storing unit with some of the quicklime materials and / or some of the quick dolomitic lime materials;- reducing or interrupting the hydration process, when at least one of the following conditions is met:- the global energy need of the at least one energy utilization unit is below a first predefined threshold, and / or;- the availability of renewable energy is above a second predefined threshold, in particular during day shift, preferably when solar energy source ensures at least a portion of the energy supply,- increasing the hydration process when the global energy need of the at least one energy utilization unit is above a third predefined threshold.- the hydration unit is not fed with the limestone materials, the dolomitic stone materials, the synthetic carbonated materials produced in the CO2 carbonator unit, the synthetic carbonated materials produced in the direct air capture unit, nor the other synthetic carbonated materials;- the primary working medium flow circulates in a closed loop circuit; one or more of the at least one secondary working medium flow circulate in one or more corresponding closed loop circuits.- the primary working medium of the primary working medium flow is a liquid medium, a gaseous medium or a combination thereof.- capturing CO2 in the third of the at least one CO2-containing stream, as conditioned air, in the direct air capture unit, said unit comprising at least one direct air capture conditioning unit adapted to adjust at least one of: -an operational parameter such as a conditioned air flow rate, a relative humidity level of the conditioned air flow, a temperature of the conditioned air flow, and / or- another operational parameter related to the feeding of sorbent, namely at least one of the hydrated materials, the quicklime materials and / or the quick dolomitic lime materials, to the direct air capture unit, such as : an inventory of the hydrated materials, a flow of the hydrated materials, an inventory of the quicklime materials, a flow of the quicklime materials, an inventory of quick dolomitic lime materials or a flow of quick dolomitic lime materials;- the energy exchanges with the at least one secondary working medium flow comprise:- transferring energy, such as heat and / or mechanical energy, from a first set of the at least one secondary working medium flow to one or more of the at least one energy utilization unit, and / or-transferring energy, such as heat and / or mechanical energy, from said utilization unit to a second set of the at least one secondary working medium flow;- the energy exchanges with the at least one secondary working medium flow comprise transferring energy, such as heat and / or mechanical energy, from or to one or more of the at least one energy utilization unit via a third set of the at least one secondary working medium flow;- transferring at least a portion of energy, such as heat and / or mechanical energy, from one or more of the at least one utilization unit to another of the at least one utilization unit via the at least one tertiary work medium flow without passing through the at least one energy distribution unit.- transferring heat:- from one of the first or third set of the at least one secondary working medium flow to one of the at least one CO2 treatment unit of the first of the at least utilization unit, and / or- from one of the at least one CO2 treatment unit of the first of the at least utilization unit to one of the second or third set of the at least one secondary working medium flow.- transferring at least a part of the heat collected in the cooler unit to one of the second set of the at least one secondary working medium flow or to one of the at least one primary working medium flow,- transferring heat from one of the second or third set of the at least one secondary working medium flow to the preheating unit;- transforming one of the at least one secondary electric power flow from the at least one energy distribution unit into heat for the decarbonation reactor or using said electric power flow to drive an electrolysis unit in the decarbonation reactor;- the at least one energy utilization unit further comprises a fifth energy utilization unit, which comprises or consists of at least one element selectedfrom the group comprising: a fuel dryer, a carbonated material dryer, a hydrate dryer, a steam generator for generating mechanical energy and / or electricity in a turbine, an electricity producing unit such as an organic ran- kine cycle apparatus, a thermal or electrical chiller and / or a thermal desalination unit and preferably transferring the heat from the first set of the at least one secondary working medium flow to said element, and optionally transferring electric energy from said element to one of the at least one secondary electric power flow;- the step of transferring energy, such as heat and / or mechanical energy, from the at least one primary working medium flow to at least one secondary working medium flow comprises transferring at least a portion of the heat from the at least one primary working medium flow to one or more of the at least one secondary working medium flow via at least one heat exchanger, at least one heat pump, at least one turbine, at least one turbo charger or any combination of them;- the step of transferring energy, such heat and / or mechanical energy, from the at least one primary working medium flow to at least one secondary working medium flow comprises forming one or more of the at least one secondary working medium flow with at least a portion of the at least one primary working medium flow, preferably using at least one valve and / or fluid diverter;- the step of transferring electrical energy from the primary electrical power flow to the at least one secondary electric power flow comprises forming the at least one secondary electrical power flow with at least a portion of the primary electrical power flow, preferably by using an electric distributor and / or a transformer; the at least one primary or secondary working medium flow is a working fluid flow, a heat transfer medium flow, a solid bed or any combination thereof; the at least one primary working medium flow comprises a first and optionally second primary working medium flow, further comprising transforming the first working medium flow into the primary electrical powerflow and / or the second primary working medium flow in the first power generation system; the at least one primary working medium flow comprises a first and optionally second primary working medium flow, further comprising compressing the first working medium flow into the second primary working medium flow in a compression unit;- the step of transferring energy such as heat and / or mechanical energy, from the at least one primary working medium flow to at least one secondary working medium flow comprises at least one of:- transferring at least a portion of the heat from the at least one primary working medium flow to one or more of the at least one secondary working medium flow via at least one heat exchanger, at least one heat pump, at least one turbine, at least one turbo charger or any combination of them;- forming one or more of the at least one secondary working medium flow with at least a portion of the at least one primary working medium flow, preferably using at least one valve and / or fluid diverter;- the step of transferring in the at least one energy distribution unit is performed free of electric power flow and / or electric power generation; and / or- said process is free of transforming any working medium flow into any electrical power flow preferably in any power generation system.

[0019] The invention can also be related to a CO2 capture system, preferably adapted to carry out a process according to any of the preceding claims, said system comprising: -an hydration unit adapted to, at least partly, slake quicklime materials and / or quick dolomitic lime materials with water as liquid and / or vapor;- at least one energy distribution unit; -a primary working medium circuit arrangement for circulating at least one primary working medium flow, preferably fluidly connected to the at least one energy distribution unit; -optionally a primary electric power circuit network for circulating a primary electrical power flow between the at least one energy distribution unit and a first power generation system supplied with a first of the at least one primary working medium flow, preferably said first power generation system generating a second of the at least one primary working medium flow;- at least one energy utilization unit;- at leastone CO2 treatment unit, preferably a first of the at least one utilization unit comprising or consisting of the at least one CO2 treatment unit; -at least one of: a secondary working medium circuit arrangement circulating at least one secondary working medium flow fluidly connected to the at least one energy distribution unit and the at least one energy utilization unit, and / or a secondary electric power network circulating at least one secondary electric power flow connected to least one energy distribution unit and the at least one energy utilization unit; wherein the at least one energy distribution unit is configured to control the distribution of the at least one secondary working medium flow and / or the at least one secondary electric power flow between the at least one energy distribution unit and the at least one energy utilization unit.

[0020] According to specific embodiments of the invention, the CO2 capture system comprises one or more of the following features:- the maximal distance between any pair of the following elements: the hydration unit, the at least one energy distribution unit and the at least one energy utilization unit, in particular the at least one CO2 treatment unit, is less than 10 km, preferably less than 1 km;- the at least one CO2 treatment unit is adapted to capture at least some CO2 from at least one CO2 containing stream, said unit comprising at least one of: o a CO2 purification unit, such as a pressure or temperature swing adsorption apparatus, a chemical or physical absorption apparatus, an amine-based gas treating apparatus, a membrane separation apparatus or cryogenic gas treating apparatus, said unit having an inlet supplied with a first of the at least one CO2-containing stream and a first outlet with a CO2-enriched stream and a second outlet with a CO2-depleted stream; o a CO2 carbonator unit with an inlet supplied with a second of the at least one CO2-containing stream and an outlet with a CO2-depleted stream, said unit being adapted to contact at least one of the hydrated materials, the quicklime materials and / or the quick dolomiticlime materials, with CO2, thereby forming synthetic carbonated materials. o a direct air capture unit for capturing CO2 in a third of the at least one CO2-containing stream as ambient air or conditioned air, thereby forming synthetic carbonated materials, said unit being either- adapted to contact at least one of the hydrated materials, the quicklime materials and / or the quick dolomitic lime materials with said CO2-containing steam, or- adapted to contact carbonate ions resulting from the dissolution of some of the CO2 of said CO2-containing steam with ions from the dissolution at least one of the hydrated materials, the quicklime materials and / or the quick dolomitic lime materials.- one of the at least one energy utilization unit comprises one or more elements selected from the group comprising: a fuel dryer, a carbonated material dryer, a hydrate dryer, a steam generator for generating mechanical energy and / or electricity in a turbine, an electricity producing unit such as an organic rankine cycle apparatus, a thermal or electrical chiller, a thermal desalination unit and / or a district heating; one of the at least one energy utilization unit, which comprises or consist in a decarbonation reactor adapted to transform limestone materials, dolomitic stone materials, at least some of synthetic carbonated materials produced in the CO2 carbonator unit, at least some of synthetic carbonated materials produced in the direct air capture unit or the other synthetic carbonated materials, in particular produced in another plant, into the quicklime materials and / or quick dolomitic lime materials, and forming an exhaust gas stream exiting said reactor via an exhaust opening ; a first CO2-containing circuit in fluid communication with the exhaust opening of decarbonation reactor, said circuit being in fluid communication with one of the at least one CO2 treatment unit, in particular the CO2 purification unit;- a second CO2-containing circuit in fluid communication with a exhaust opening a power plant adapted to bum fossil fuel or biomass, said circuitbeing in fluid communication with one of the at least one CO2 treatment unit, in particular at least one of the CO2 carbonator unit, the CO2 purification unit and / or the direct air capture unit;- an energy storage unit selected from the group comprising a heat sink, a heat battery, a regenerator, a battery, a heat battery, a thermo-chemical energy storage unit, a hot water storage tank, an energy storage dam, a first storing unit with some of the hydrated materials or a second storing unit with some of the quicklime materials and / or the quick dolomitic lime materials, said unit being adapted to store some of the energy supplied by at least one of one of the at least one primary working medium flow, the primary electrical power flow, one of the least one secondary working medium flow and / or one of the at least one secondary electric power flow;- the at least one distribution unit comprises at least one of: a heat exchanger, a valve, a fluid diverter, a turbine, a generator, a turbocharger, a transformer, an electric distributor or any combination of them.

[0021] Thanks to the measures of the invention, the process / system according to the present invention can be implemented in different types of ecosystem, such as industrial ecosystem allowing use of the heat in other process, an ecosystem connected to district heating, an ecosystem linked to a capture of CO2 on a customer site.

[0022] The measure allows to manage the energy distribution among the different energy users of these ecosystems allowing valorize the energy.

[0023] They allow the recovering of the hydration energy enabling to decrease the energy footprint of the overall CO2 capture process up to by approximately 25%.

[0024] For instance, the heat generated by the hydration reaction can be supplied to a CO2 treatment unit and / or other energy utilization units. If the CO2 treatment unit is a carbonator treating a diluted CO2 stream (autothermal condition not achieved), the hydrated composition and heat generated by the hydrator can be directly supplied to the carbonator. If the CO2 treatment unit involves a CO2 purification unit (also known as CO2 enrichment unit) for treating CO2 generated by a decarbonation reactor, the hydration unit can be directly supplied with thequicklime produced by the decarbonation reactor. Additionally, the surplus energy can be utilized either on the production site or at other locations. The presence of an energy distribution unit facilitates the routing of energy from various sources to users (e.g. CO2 treatment unit) within the network, the energy distribution unit, the hydration unit, and one or more supplementary energy utilization units, thereby minimizing energy wastage.Brief Description of Drawings

[0025] Aspects of the invention will now be described in more detail with reference to the appended drawings, wherein same reference numerals illustrate the same features.

[0026] Figures 1 to 20 shows the first to the twentieth embodiments according to the invention.

[0027] List of reference symbolsDetailed description

[0028] The present invention will now be described more fully hereinafter with reference to the accompanying drawings, in which embodiments of the invention are shown. This invention may however be embodied in many different forms and should not be construed as limited to the embodiments set forth herein; rather, these embodiments are provided for thoroughness and completeness.

[0029] Figure 1 describes a first embodiment of a CO2 capture system according to the invention. The system comprises a hydration unit 10 fed with decarbonated materials 16, 16’ produced in a decarbonation unit 37, namely a lime kiln. The decarbonated material 16, 16’ is preferably selected from the group comprising quicklime 16, quick dolomitic lime 16’ or a combination thereof. At leasta portion of the heat generated during the hydration is transferred to a primary working medium flow 51 .1 , such as oil or steam, that is circulated in a closed loop between the energy distribution unit 20 and the hydration unit 10. The primary working medium flow 51.1 is heated in the hydration unit 10. This heat is then redistributed to different energy utilization units 30.1 , 30.2, 30.3, via secondary working medium flows 52.1 , such as steam.

[0030] The energy distribution unit 20 controls the secondary working medium flows 52.1 towards the energy utilization units 30.1 , 30.2, 30.3. To achieve this, an heat exchanger unit 20.1 is positioned between the primary working medium flow circuit and the secondary working medium flow circuit. This arrangement facilitates the transfer of heat carried by the primary working medium flow 51.1 to the secondary working medium flows 52.1. In Figure 1 , the secondary working medium flow circuit constitutes an open circuit with a source of liquid water at one end and the heat utilization units 30.1 , 30.2, 30.3 at the other. A valve arrangement V1 , V2, V3 is provided to regulate the secondary working medium flows 52.1 .

[0031] In Figure 1 , the first heat utilization unit 30.1 comprises or consists in a CO2 purification unit 35.1 , namely an amine-based gas treating apparatus, the second heat utilization unit 30.2 comprises or consists in the decarbonation reactor 37, and the third heat utilization unit 30.3 comprises or consists in a district heating network 39. For the third heat utilization unit 30.3, other applications are possible such as an Organic Rankine Cycle apparatus (ORC).

[0032] In the decarbonation reactor 37, the secondary working medium stream 52.1 is employed to preheat the carbonated materials 6, 6’, 6* being supplied to the kiln, through a heat exchanger 37.1. The decarbonation reactor 37 produces a CO2-containing stream 71 resulting from the release of CO2 from the carbonated materials 6, 6’, 6 * heated within a temperature range of 800°C to 1200°C. The heating of the carbonated materials 6, 6’, 6* to such temperature range can be done directly or indirectly and by using electrical heating or fuel combustion, such as carbon containing fuel or hydrogen.. If carbon containing fuel are used, the CCh-containing stream 71 could contain the CO2 resulting from this combustion.

[0033] In the amine-based gas treating apparatus 35.1 , a lean amine-based solvent comes into contact with a CO2-containing stream 71 to capture the CO2present in that stream, resulting in the production of a CCh-depleted stream 73 and an amine-based sorbent enriched with CO2. Subsequently, CO2 is desorbed from the CO2-enriched amine-based sorbent upon exposure to heat, since the solubility of CO2 in the amine-based sorbent decreases with rising temperature. This desorption process gives rise to a concentrated CO2 stream 75, suitable for sequestration or usage (not shown in Figure 1 ). The required heat for the desorption process is, at least partly, supplied by the secondary working medium flow 52.1 through a heat exchange unit 35.11. Before an amine-based sorbent is brought into contact with the CO2-containing stream 71 , it undergoes cooling to enhance its CO2 solubility, in the heat exchanger unit 35.12. Furthermore, prior exiting the amine-based gas treating apparatus 35.1 , the concentrated CO2 stream 75, undergoes cooling to segregate impurities, facilitated by an additional cooling stream 53 and the heat exchanger unit 35.12. The heat recovered from the additional cooling stream 53, combined with the residual heat of the secondary working medium flow, can be directed to the district heating network 39. After transferring heat to the district heating network 39, the secondary working medium flow 52.1 can be recirculated back to the distribution unit 20 (This configuration is not shown in Figure 1 but , for instance, in Figures 13 to 16).

[0034] In Figure 1 , the energy distribution unit 20 manages the control and distribution of the three secondary working medium flows 52.1 based on the power requirements of the three energy utilization units 30.1 , 30.2, 30.3. Preferably, the three secondary working medium flows 52.1 are controlled via valves allowing the flow rate of the working medium and therefore their power. Such a control is advantageously because the power demands vary. For instance, in summer the demand from the district heating network 39 is lower and more heat is available for the amine-based gas treating apparatus 35.1 and for the preheating 37.1 of the decarbonation reactor 37. In this context, valve V1 is closed or substantially closed compared to Valve V2 and V3. During hot summer days, the energy demanded preheating of the carbonated materials 6, 6’, 6* is reduced, implying that more energy is available for the amine-based gas treating apparatus 35.1 , reducing its energy demand with regards to an external energy source.

[0035] A second embodiment, as shown in Figure 2, differs from the firstembodiment in that an additional heat exchanger is arranged to better match temperatures needs of the applications.

[0036] A third embodiment, as shown in Figure 3, differs from the first embodiment in its utilization of steam generated within the hydration unit 20 as the primary working medium 51.1. Within the hydration unit 10, the water supplied is in steam form and / or liquid state, and it is directly and / or indirectly heated through the slaking reaction. In the former scenario (directly heated), the water steam generated as a result of the exothermic slaking reaction is recuperated. In the latter scenario (indirectly heated), liquid water or water steam circulating in cooling passages formed in the wall of the hydration unit or immerged inside the material contained in the hydration unit absorbs the heat generated by the slaking reaction.

[0037] A fourth embodiment according to Figure 4 differs from the third embodiment in that the heat exchanger is not located in the energy distribution unit 20.

[0038] The embodiment represented in Figure 4 comprises an arrangement for producing steam for an amine-based CO2 treating apparatus. Preferably, the modelized operating conditions for this embodiment are the followings:• Pressure in hydration unit 10 is (about) atmospheric pressure;• Decarbonated material 16 mainly consists in quicklime CaO (presence of quick dolomitic materials 16’ being marginal or null) and is fed to the hydration unit (about) 20 °C;• Liquid water 7 is fed in the hydrating unit at (about) 20 °C;• Water / quicklime ratio is fixed at 0.71 kg of water per kg of quicklime;• Hydration reaction enthalpy is (about) 1 .16 MJ / kg of quicklime (exothermal);• Heat losses is about 5%;• Temperature of hydrated materials 17 mainly consisting of Ca(OH)2 and excess water after completion of hydration reaction is (about) 125 °C;• (About) 1.32 kg of hydrated materials 17, mainly consisting Ca(OH)2 are produced and discharged from hydration reactor;Excess water is vaporized resulting in a steam flow of (about) 0.38 kg at (about) 125 °C which is equivalent to a thermal energy flow rate of (about) 1 .01 MJ / kg of quicklime;• Said steam flow is sent to a heat exchanger where it transfers energy to a secondary working medium flow 52.1 (steam) redistributed to energy utilization unit 35.1 (amine-based CO2 treating gas apparatus) enabling desorption of (about) 0,29 t CO2 per kg of quicklime;• CO2-depleted stream 73 and concentrated CO2 stream 75 exit amine treating apparatus at 70 °C and 120 °C respectively and can therefore be directed to a heat exchanger 35.13 where thermal energy is transferred to a tertiary working medium 53 redistributed to another utilization unit 30.3 which consists in district heating network 39.

[0039] A fifth embodiment according to Figure 5 differs from the first embodiment by forming the secondary working flows 52.1 using the primary working flow 51 .1 .

[0040] A sixth embodiment according to Figure 6 differs from the first embodiment in that the heat generated in the hydration unit 10 is converted into a primary electrical power flow within a power generation system 15, such as a steam turbine or an Organic Rankine Cycle apparatus (ORC). The energy distribution unit 20 takes in charge of controlling of the redistribution of the secondary electrical power flows 62 to the different energy utilization units 30.1 , 30.2 ,30.3, where the electrical energy is transformed into thermal energy by means of resistors 35.16, 37.6, 39.6 or heat pump (not illustrated). Preferably, transformers are interposed between the primary electrical power flow 61 and the secondary electrical power flow 62 Alternatively or complementary to the transformers, electric power switches can be provided to control the supply of the electric power from the primary to the secondary electrical power flow.

[0041] A seventh embodiment according to Figure 7 differs from the first embodiment by employing the steam expanded 51 .2 within the power generation system 15 as a primary working medium flow 51 .2. In this embodiment, the energy distribution unit 20 ensures both the distribution of the electric power flows 62 tothe different energy utilization units 30.1 , 30.2, 30.3 and the distribution of the secondary working medium flow 52.1 to the district heating network 39.

[0042] The embodiment represented in Fig. 7 comprises an arrangement for producing electricity in an ORC turbine and distributing the unused energy in district heating network. Preferably, the modelized operating conditions for this embodiment are the followings:• Pressure in hydration unit 10 is (about) atmospheric pressure;• Decarbonated material 16 mainly consisting of quicklime CaO (presence of quick dolomitic materials 16’ being marginal or null) and is fed from the lime kiln 37 to the hydration unit at (about) 300 °C;• Liquid water 7 is fed in hydrating section at (about) 20 °C;• Water / quicklime ratio is fixed at 0.75 kg of water per kg of quicklime;• Hydration reaction enthalpy is (about) 1 .16 MJ / kg of quicklime (exothermal);• Heat losses is about 5%;• Temperature of hydrated materials 17, Ca(OH)2 are produced and excess water after completion of hydration reaction is (about) 200 °C;• (About) 1.32 kg of hydrated material Ca(OH)2 17 is produced and discharged from hydration reactor;• Excess water is vaporized resulting in a steam flow of (about) 0.43 kg at (about) 200 °C which is equivalent to a thermal energy flow rate of (about) 1 .20 MJ / kg of quicklime;• Said steam flow is sent to a heat exchanger where it transfers energy to a primary working medium flow 51.1 ;• The heat is converted to electricity in an organic rankine cycle apparatus where the cold source is water at 60 °C. The efficiency of the organic rankine cycle is about 12 % therefore producing (about) 40 kWh of electricity per kg of quicklime;The water used as cold source is then directed to heat exchanger 20.1where thermal energy is transferred to a secondary working medium flow 52.1 (hot water) redistributed to energy utilization unit 30.3 which consists in district heating network 39.

[0043] A eighth embodiment according to Figure 8 differs from the seventh embodiment in that the distribution unit 20 is also an multi energy converting unit, wherein the energy of the primary working medium flow is distributed as heat to a secondary working medium flow 52.1 , as mechanical energy to a second secondary working medium flow filling a compressed air reservoir 36 for pneumatic applications, and a remaining part as electrical energy to a primary electric energy flow 61 . The compressed air reservoir 36 is or can be part of a further energy utilization unit.

[0044] A ninth embodiment according to Figure 9 differs from the seventh embodiment in that the first energy utilization unit 30.1 is a direct air capture unit 35.3 adapted to capture CO2 from a conditioned air stream 71 *, thereby forming at least some synthetic carbonated materials 6*. The contactor is configured to contact at least one of the hydrated materials 17, the quicklime materials 16 and / or the quick dolomitic lime materials 16 with the CCh-containing steam 71 *, namely the conditioned air stream produced by an air capture conditioning unit adapted to adjust at least one of a conditioned air flow rate. Alternatively, the synthetic carbonated materials 6* is produced through the following two steps process involving a strong alkali base, in particular KOH :- Liquid solution of KOH is contacted CO2-containing stream 71 * and reacts with CO2 to form a liquid solution containing K2CO3 (under its ionic species K+and CO32’);- The formed carbonate ions COs2' is contacted with Ca2+ions resulting from the at least partial dissolution of the at least hydrated materials 17 and the quicklime materials 16 to form precipitated calcium carbonate CaCO3(caustization reaction).

[0045] The dissolution of some of the CO2 of the CO2-containing steam 71 * is achieved through contacting the CO2-containing steam 71 * with water, in particular via sprinkling water droplets in the CO2-containing steam 71 *. The water droplets enriched with carbonate ions capture from the CO2-containing steam 71*, are thencollected in a collecting basin. The solution contained in said basin is further circulated to a pellet reactor (kind a of second receptacle) where the precipitation of the carbonate takes place resulting from the introduction of the hydrated material 17 or quicklime materials 16. The precipitated synthetic carbonated materials 6* in solid form is then separated from the solution using solid-liquid separation techniques such as decantation or filtration. The solution depleted in carbonate is circulated back from the pellet reactor to the contacting means (e.g. sprinkler) to pursue the CO2 capture cycle.

[0046] A tenth embodiment according to Figure 10 differs from the nineth embodiment in that an additional heat utilization unit, namely a cryogenic gas treating apparatus 35.1 , is provided to treat the fumes generated by said lime kiln 37.

[0047] A eleventh embodiment according to Figure 11 differs from the first embodiment in that an energy storage unit, specifically a heat battery 40 is provided. When the power produced by the hydration unit 10 exceeds the demand of the energy utilization units 30.1 , 30.2, 30.3, the surplus power is stored in the heat battery 40, in the form of sensible heat. The accumulated thermal energy can subsequently be utilized when the power demand rises above the power supply capacity, or when the energy cost from an external power supply source exceeds a defined threshold or to participate to the electricity grid balancing. Alternative forms of energy storage systems can also be envisioned, such as water dams.

[0048] A twelfth embodiment according to Figure 12 differs from the first embodiment in that a complementary secondary working medium flow 52.2 is provided to absorb the heat from the cooler 35.13 located within the amine-based gas treating apparatus 35.1. The complementary second working medium flow 52.2 is routed back to the distribution unit 20 prior being transferred into the district heating network 39.

[0049] A thirteenth embodiment according to Figure 13 differs from the twelfth embodiment in that the complementary secondary working medium flow 52.1 , downstream from the district heating network 39 is used as the secondary working medium flow that is supplied to the heat utilization unit 30.1 , 30.2.

[0050] A fourteenth embodiment according to Figure 14 differs from the first embodiment at least in that:- an additional heat utilization unit, namely a cryogenic gas treating apparatus35.1 , is provided to treat the fumes generated by said lime kiln 37.- the first heat utilization unit 30.1 is a CO2 carbonator unit 35.2 adapted to capture CO2 from fumes from a plant.

[0051] In Figure 14, the cryogenic gas treating apparatus 35.1 is supplied with electric energy from an external source that ensures the compression work (via electric driven compressor(s)) of the CO2 containing stream 71 supplied by the kiln 37. Once compressed to values up to around 25 bars the CO2 containing stream 71 undergoes cooling to induce liquefaction of the CO2 contained in the CO2 containing stream 71 prior undergoing distillation. The compression is generally achieved via multiple compression stages with intermediate cooling. For sake of simplicity Figure 14 shows a single stage. A portion of the heat resulting from the compression work recovered via the cooling is transferred from the cryogenic gas treating apparatus 35.1 to the energy utilization unit 30.3 and 30.2 via the energy distribution unit 20. A further cooling stage before the distillation is necessary to reach negative temperatures, using a cryogenic cold source such as a chiller. The energy utilization unit 30.1 comprises a CO2 carbonator 35.2 with an inlet supplied with the CO2-containing stream 71 emitted by the plant and an outlet with a CO2- depleted stream 73. In the CO2 carbonator 35.2, the CO2-containing stream 71 is contacted with hydrated materials 17, thereby forming synthetic carbonated materials 6*. In order to ensure fast carbonation reaction in the CO2 carbonator35.2, temperatures above 400 °C, preferably close to 650 °C is are preferred. If the concentration of CO2 is sufficient in the CO2-containing stream 71 , the heat generated by the carbonatation is sufficient to maintain suitable temperatures above 400 °C, preferably close to 650 °C, despite the presence of diluting gas. Any excess of heat produced by the exothermic reaction is transferred to the secondary working medium flow 52.3. In case the concentration of diluting gas is too high, heat from the primary working circuit 51.1 or other energy utilization units is transferred to the CO2 carbonator 35.2, via the same secondary working medium flow 52.3.

[0052] A fifteenth embodiment according to Figure 15 differs from the thirteenth embodiment at least in that the cryogenic gas treating apparatus 35.1 and the decarbonation reactor 37 are not located on the same location as the energy distribution unit 20.

[0053] A sixteenth embodiment according to Figure 16 differs from the fourteenth embodiment in that a fourth heat utilization unit 30.4 comprises a heat- driven chiller, in particular an ammonia absorption refrigeration unit. The refrigeration cycle comprises the following steps:• - evaporating ammonia by indirect heat exchange from the stream to be cooled• - mixing ammonia with water, pumping said mixture in a boiler heated by the secondary working medium flow 52.1 thereby separating ammonia from the water through evaporation.• Condensing ammonia through indirect cooling using for instance ambient air• Decrease the ammonia pressure and recirculate it to the evaporator.In this embodiment, the synthetic carbonate 6* is used for other applications (not show on Figure 16).

[0054] Furthermore, the CCh-containing stream 71 produced by the plant is combined with the CCh-containing stream 71 generated by the kiln 37 before being fed in the CO2 carbonator unit 35.2.

[0055] A seventeenth embodiment according to Figure 17 differs from the fourteenth embodiment in that it comprises a further energy utilization unit comprising or consisting of a absorption chiller 38 such as in Figure 16. The “cold” generated in the chiller is used to cold the compressed stream (viz 53) to a temperature in the range from minus 35 to minus 25 to cool the CO2 containing stream before its distillation.

[0056] A eighteenth embodiment according to Figure 18 differs from the first embodiment at least in that:- the decarbonation reactor 37 is a flash calciner (also known as entrained bed);- the primary working medium flow 51 .1 is formed with the steam generated during the hydration. This steam is subsequently subjected to additional heating (in a suspension heat exchanger 37.9 while cooling the decarbonated materials 16, 16’ exiting the second heat utilization unit 30.2.

[0057] A nineteenth embodiment according to Figure 19 differs from the eighteenth embodiment at least in that the primary working medium flow 51.1 circulates in a closed loop and is indirectly heated by both the hydration process and in a heater 37.8 recovering wasted heat from the cooling of the decarbonated materials 16, 16’ produced in the flash calciner 37.

[0058] A twentieth embodiment according to Figure 20 differs from the nineteenth embodiment in at least in that the secondary working medium flows 52.1 are circulated in closed loop circuits. One of the secondary working medium flow 52.2 is heated in a heater 37.8 recovering wasted heat from the cooling of the decarbonated materials 16, 16’ produced in the flash calciner 37.

[0059] All the embodiments according to Figures 1 to 20 shows a single energy distribution unit 20. Alternatively to any of these embodiments, the control of the energy distribution can be ensured by a plurality of distribution units.

[0060] All the embodiments according to Figures 1 to 20 shows a single CO2 carbonator unit 35.2. Alternatively to any of these embodiments, the purification can be ensured by a plurality of CO2 carbonator units 35.2 preferably arranged in series or parallel.

[0061] All the embodiments according to Figures 1 to 20 shows a hydration unit 10. Alternatively to any of these embodiments, the hydration can be ensured by a plurality of distribution units.

[0062] By a primary, secondary or tertiary working medium flow 51.1 , 51.2, 52.1 , 52.2, 52.3, 53 is meant a flow of a medium whose internal energy is increased following an energy transfer, such as a heat transfer or thermodynamics work. Such a medium is in a form of a fluid (e.g. gas or liquid) or a combination of fluid and solid (e.g. moving fluid bed). Typically such a working medium is a working fluid as defined in thermodynamics. Such a working fluid can change phase. More preferably, said working fluid is a heat transfer fluid (e.g. oil, water),a heat carry medium (e.g. hot water, steam), an hydraulic fluids (e.g. oil), or a pneumatic fluid (e.g. compressed air).

[0063] By quicklime materials 16 are meant materials fitting the formula aCaCO3.bMgCO3.cCaMg(CO3)2.xCaO.yMgO.zCa(OH)2.tMg(OH)2.ul, wherein I are impurities; a, b, c, z, t and u each being mass fractions > 0 and < 50%, x and y each being mass fractions > 0 and < 100%, with x > 50% by weight, based on the total weight of said materials.

[0064] By quick dolomitic lime materials 16’ are meant materials fitting the formula aCaCO3.bMgCO3.cCaMg(CO3)2.xCaO.yMgO.zCa(OH)2.tMg(OH)2.ul, wherein I are impurities; a, b, c, z, t and u each being mass fractions > 0 and < 50%, x and y each being mass fractions > 0 and < 100%, with x + y > 50% by weight, based on the total weight of said materials.

[0065] By limestone materials 6 are meant materials fitting the formula: aCaCO3.bMgCO3.cCaMg(CO3)2.xCaO.yMgO.zCa(OH)2.tMg(OH)2.ul, wherein I are impurities; x, y, z, t and u each being mass fractions > 0 and < 90%, a, b and c each being mass fractions > 0 and < 100%, with a + b + c > 10% by weight, based on the total weight of said materials, preferably x, y, z, t and u each being mass fractions > 0 and < 50%, a, b and c each being mass fractions > 0 and < 100%, with a > 50% by weight, based on the total weight of said materials.

[0066] By dolomitic stone materials 6’ are meant materials fitting the formula: aCaCO3.bMgCO3.cCaMg(CO3)2.xCaO.yMgO.zCa(OH)2.tMg(OH)2.ul, wherein I are impurities; x, y, z, t and u each being mass fractions > 0 and < 90%, a, b and c each being mass fractions > 0 and < 100%, with a + b + c > 10% by weight, based on the total weight of said materials, preferably x, y, z, t and u each being mass fractions > 0 and < 50%, a, b and c each being mass fractions > 0 and < 100%, with b+ c > 30% by weight, based on the total weight of said materials.

[0067] By hydrated materials 17 are meant materials fitting the formula aCaCO3.bMgCO3.cCaMg(CO3)2. xCaO.yMgO.zCa(OH)2.tMg(OH)2.ul, wherein I are impurities; a, b, c, and u each being mass fractions > 0 and < 50% (preferably less than 10%), z and t each being mass fractions > 0 and < 100%, with z + t > 10% by weight, preferably z + 1 > 50% by weight, x and y each being mass fractions> 0 and < 100%, with x + y <90% by weight, based on the total weight of said materials.

[0068] By synthetic carbonated materials 6* are meant materials obtained through either:- the carbonation of at least one of quicklime materials 16, quick dolomitic lime materials 16’ and hydrated materials 17 with CO2, or- the precipitation of chemical species resulting from ions resulting from the dissolution at least one of quicklime materials 16, quick dolomitic lime materials 16’ and hydrated materials 17, with carbonate ions of resulting from the dissolution of CO2, such synthetic carbonated materials fitting the formula: aCaCO3.bMgCO3.cCaMg(CO3)2.xCaO.yMgO.zCa(OH)2.tMg(OH)2.ul, wherein I are impurities; x, y, z, t and u each being mass fractions > 0 and < 90%, a, b and c each being mass fractions > 0 and < 100%, with a + b + c > 10% by weight, based on the total weight of said synthetic carbonated materials, preferably x, y, z, t and u each being mass fractions > 0 and < 50%, a, b and c each being mass fractions > 0 and < 100%, with a + b + c > 50% by weight.

[0069] Embodiments according to the invention are also defined by the following clauses :A1 . A CO2 capture process comprising the following steps:• Supplying quicklime materials (16) and / or quick dolomitic lime materials (16’) to a hydration unit (10);• A least partly hydrating said materials in the hydration unit (10) with water (7) as liquid and / or vapor to produce hydrated materials (17);• Transferring at least a portion of the heat generated during the hydration to at least one primary working medium flow (51 .1 , 51 .2) and optionally transforming the at least one working medium flow into a primary electrical power flow (61 ) in a first power generation system (15);Capturing at least some CO2 from at least one CO2 containing stream (71 , 71 *) to reduce the CO2 content in said stream, in at least one CO2 treatment unit (35.1 , 35.2, 35.3);• Exchanging energy between at least one energy distribution unit (20) and at least one energy utilization unit (30.1 , 30.2, 30.3, 30.4) by using energy exchanges with at least one of : o at least one secondary working medium flow (52.1 , 52.2, 52.3) and / or; o at least one secondary electric power flow (62);• Controlling at least one of the at least one secondary working medium flow (52.1 , 52.2, 52.3) and / or the at least one secondary electric power flow (62) between the at least one energy distribution unit (20) and the at least one energy utilization unit (30.1 , 30.2, 30.3, 30.4), preferably depending on the power and / or energy need of the at least one energy utilization unit (30.1 , 30.2 , 30.3, 30.4);• Transferring, preferably in the at least one energy distribution unit (20), at least one of: o energy such as heat and / or mechanical energy, from the at least one primary working medium flow (51 .1 , 51 .2) to the at least one secondary working medium flow (52.1 , 52.2, 52.3), and / or o electric energy from the primary electrical power flow (61 ) to the at least one secondary electric power flow (62).A2. The process according to Clause A1 , wherein the at least one (energy) utilization unit (30.1 ) comprises a first (energy) utilization unit (30.1 ),said unit comprising or consisting of the at least one CO2 treatment unit (35.1 , 35.2, 35.3).A3. The process according to any of the preceding clauses, wherein the at least one CO2 treatment unit (35.1 , 35.2, 35.3) comprises at least one of:• a CO2 purification unit (35.1 ), such as a pressure or temperature swing adsorption apparatus, a chemical or physical absorption apparatus, a membrane separation apparatus, an amine-based gas treating apparatus, or cryogenic gas treating apparatus, said unit having an inlet supplied with a first of the at least one CO2-contain- ing stream (71 ) and a first outlet with a CO2-enriched stream (75) and a second outlet with a CO2-depleted stream (73);• a CO2 carbonator unit (35.2) with an inlet supplied with a second of the at least one CO2-containing stream (71 ) and an outlet with a CO2-depleted stream (73), said unit being adapted to contact at least one of the hydrated materials (17), the quicklime materials (16) and / or the quick dolomitic lime materials (16’) with CO2, thereby forming synthetic carbonated materials (6*), preferably as powder and / or shaped bodies;• a direct air capture unit (35.3) capturing CO2 in a third of the at least one CO2-containing stream (71 , 71 *) as ambient air or conditioned air, thereby forming synthetic carbonated materials (6*), preferably as powder and / or shaped bodies, said unit being either :- adapted to contact at least one of the hydrated materials, the quicklime materials and / or the quick dolomitic lime materials with said CO2-containing steam, or- adapted to contact carbonate ions resulting from the dissolution of some of the CO2 of said CO2-containing steam with ions from the dissolution at least one of the hydrated materials, the quicklime materials and / or the quick dolomitic lime materials.A4. The process according to Clause A3, wherein the at least one CO2 treatment unit (35.1 , 35.2, 35.3) comprises the CO2 purification unit (35.1 ) and optionally at least one of the CO2 carbonator unit (35.2) and / or the direct air capture unit (35.3).A5. The process according to Clause A1 or A2, preferably in combination with Clause A3 or A4, further comprising decarbonating at least one of limestone materials (6), dolomitic stone materials (6’), at least some of the synthetic carbonated materials (6*) produced in in the CO2 carbonator unit (35.2), at least some of the synthetic carbonated materials (6*) produced in the direct air capture unit (35.3), or other synthetic carbonated materials (6*), in particular produced in another plant, in a decarbonation reactor (37), thereby forming the quicklime materials (16) and / or the quick dolomitic lime materials (16’) and optionally at least a portion of the first of the at least one CO2-containing stream (71 ), preferably the decarbonation reactor (37) being a shaft kiln, a regenerative multi-shaft kiln, such as a parallel flow regenerative kiln, an annular kiln, a fluidized bed calciner, a circulated fluidized bed calciner, an entrained bed calciner or an electrolysis unit.A6. The process according to Clause A4 in combination with Clause A5, further comprising feeding the decarbonation reactor (37) with at least some of the synthetic carbonated materials (6*) produced in at least one of the CO2 carbonator unit (35.2) and / or the direct air capture unit (35.3).A7. The process according to Clause A6, further comprising forming at least a portion of the second of the at least one CCh-containing stream in a power plant combusting fuel, in particular burning fossil fuel, and generating in said plant at least one of: energy, such as heat and / or mechanical energy, transferred to one of the at least one secondary working medium flow (52.1 , 52.2, 52.3) and / or electricity transferred to one of the at least one secondary electric power flow (62).A8. The process according to any of Clauses A1 to A4 or A6 to A7 in combination with Clause A5, wherein the at least one energy utilization unit (30.1 , 30.2, 30.3, 30.4) comprises a second energy utilization unit (30.2), said second energy utilization unit (30.2) comprising or consisting of the decarbonation reactor (37) and optionally at least one of:- a cooling unit (37.8) for cooling the quicklime materials (16) and / or the quick dolomitic lime materials (16’) produced in the decarbonation reactor (37) and / or- a pre-heating unit (37.1 ) for heating at least part of one of the limestone materials (6), the dolomitic stone materials (6’), the at least some of the synthetic carbonated materials (6*) produced in the CO2 carbonator unit (35.2), the at least some of the synthetic carbonated materials (6*) produced in the direct air capture unit (35.3), or the other synthetic carbonated materials (6*) to be processed in the decarbonation reactor (37).A9. The process according to any of the preceding clauses, wherein the at least one energy utilization unit (30.1 , 30.2, 30.3, 30.4) further comprises a third energy utilization unit (30.3), which comprises or consists of a heating network, in particular a district heating network (39), said process further comprising supplying the heating network using heat from one of the at least one secondary working medium flow (52.1 , 52.2, 52.3) or heat from at least one tertiary working medium flow (53).A10. The process according to any of Clauses A1 , A2 or A5 to A9, preferably in combination with any of Clause A3 or A4, wherein the at least one energy utilization unit (30.1 , 30.2, 30.3, 30.4) further comprises a fourth energy utilization unit (30.4), which consists of or comprises a heat driven chiller (38) such as an ammonia absorption refrigeration unit, said process further comprising mixing a first medium such as ammonia with a second medium such as water, pumping said mixture in a desorber or boiler, separating the first medium from the second medium by evaporation using the heat at from one of the at least one secondary working medium flow, optionally said processfurther comprising cooling at least a cold utilization unit, such as the cryogenic gas treating apparatus or a centralized cooling network, with the heat driven chiller.A11 . The process according to any of the preceding clauses, further comprising transferring at least a portion of energy, such as heat and / or mechanical energy from one or more of the at least one utilization unit (30.1 ,30.2, 30.3, 30.4) to another of the at least one utilization unit (30.1 , 30.2,30.3, 30.4) via one or more of the at least one secondary working medium flow (52.1 , 52.2, 52.3) in a cascade configuration.A12. The process according to any of the preceding clauses, further comprising storing some of the heat and / or electric energy supplied by at least one of:- the at least one primary working medium flow (51 .1 , 51 .2) and / or the primary electrical power flow (61), respectively, and / or-the at least one secondary working medium flow (52.1 , 52.2, 52.3) and / or the at least one secondary electrical power flow (62), into an energy storage unit (40) preferably selected from the group comprising a heat sink, a heat battery, a hot water storage tank, a regenerator, a battery, an energy storage dam and a thermo-chemical energy storage unit, in particular thermo-chemical energy storage unit comprising at least one of a first storing unit with some of the hydrated materials (17) and / or a second storing unit with some of the quicklime materials (16) and / or some of the quick dolomitic lime materials (16’).A13. The process according to any of the preceding clauses, further comprising either :- reducing or interrupting the hydration process, when at least one of the following conditions is met:- the global energy need of the at least one energy utilization unit (30.1 , 30.2, 30.3, 30.4) is below a first predefined threshold, and / or;- the availability of renewable energy is above a second predefined threshold, in particular during day shift, preferably when solar energy source ensures at least a portion of the energy supply, or- increasing the hydration process when the global energy need of the at least one energy utilization unit (30.1 , 30.2, 30.3, 30.4) is above a third predefined threshold.A14. The process according to any of the preceding clauses, wherein the hydration unit (10) is not fed with the limestone materials (6), the dolomitic stone materials (6’), the synthetic carbonated materials (6*) produced in the CO2 carbonator unit (35.2), the synthetic carbonated materials (6*) produced in the direct air capture unit (35.3), nor the other synthetic carbonated materials (6*).A15. The process according to any of the preceding clauses, wherein the primary working medium flow circulates in a closed loop circuit and / or wherein one or more of the at least one secondary working medium flow circulate in one or more corresponding closed loop circuits.A16. The process according to any of the preceding clauses, wherein the primary working medium of the primary working medium flow is a liquid medium, a gaseous medium or a combination thereof.A17. The process according to any of the preceding clauses, further comprising capturing CO2 in the third of the at least one CO2-containing stream, as conditioned air (71*), in the direct air capture unit (35.3), said unit (35.3) comprising at least one direct air capture conditioning unit adapted to adjust at least one of:-an operational parameter such as a conditioned air flow rate, a relative humidity level of the conditioned air flow, a temperature of the conditioned air flow, and / or- another operational parameter related to the feeding of sorbent, namely at least one of the hydrated materials, the quicklime materials and / or the quick dolomitic lime materials, to the direct air capture unit, such as : an inventory of the hydrated materials, a flow of the hydrated materials, an inventory of the quicklime materials (16), a flow of the quicklime materials (16), an inventory of quick dolomitic lime materials (16’) or a flow of quick dolomitic lime materials (16’).A18. The process according to any of the preceding clauses, wherein the energy exchanges with the at least one secondary working medium flow (52.1 , 52.2, 52.3) comprise:• transferring energy, such as heat and / or mechanical energy, from a first (52.1 ) set of the at least one secondary working medium flow to one or more of the at least one energy utilization unit (30.1 , 30.2, 30.3, 30.4), and / or• transferring energy, such as heat and / or mechanical energy, from said utilization unit (30.1 , 30.2, 30.3, 30.4) to a second set (52.2) of the at least one secondary working medium flow.A19. The process according to any of the preceding clauses, wherein the energy exchanges with the at least one secondary working medium flow comprise transferring energy, such as heat and / or mechanical energy, from or to one or more of the at least one energy utilization unit (30.1 , 30.2, 30.3, 30.4) via a third set (52.3) of the at least one secondary working medium flow.A20. The process according to any of the preceding clauses, further comprising transferring at least a portion of energy, such as heat and / or mechanical energy, from one or more of the at least one utilization unit (30.1 ,30.2, 30.3, 30.4) to another of the at least one utilization unit (30.1 , 30.2,30.3, 30.4) via the at least one tertiary work medium flow (53) without passing through the at least one energy distribution unit (20).A21 . The process according to any of the preceding clauses, further comprising transferring heat:- from one of the first (52.1 ) or third set (52.3) of the at least one secondary working medium flow to one of the at least one CO2 treatment unit (35.1 , 35.2, 35.3) of the first of the at least utilization unit (30.1 ), and / or- from one of the at least one CO2 treatment unit (35.1 , 35.2, 35.3) of the first of the at least utilization unit (30.1 ) to one of the second (52.3) or third set (52.3) of the at least one secondary working medium flow.A22. The process according to any of the preceding clauses, further comprising transferring at least a part of the heat collected in the cooler unit (37.8) to one of the second set (52.2) of the at least one secondary working medium flow or to one of the at least one primary working medium flow (51 .1 , 51 .2), and / or-transferring heat from one of the second (52.2) or third set (52.3) of the at least one secondary working medium flow to the preheating unit (37.1 ).A.23 The process according to any of the preceding clauses, further comprising transforming one of the at least one secondary electric power flow (62) from the at least one energy distribution unit (20) into heat for the decarbonation reactor (37) or using said electric power flow (62) to drive an electrolysis unit in the decarbonation reactor (37).A24. The process according to any of the preceding clauses, wherein the at least one energy utilization unit (30.1 , 30.2, 30.3, 30.4) further comprises a fifth energy utilization unit, which comprises or consists of at least one element selected from the group comprising: a fuel dryer, a carbonated material dryer, a hydrate dryer, a steam generator for generating mechanical energy and / or electricity in a turbine, an electricity producing unit such as an organic rankine cycle apparatus, a thermal or electrical chiller and / or a thermal desalination unit and preferably transferring the heat from the first set (52.1 ) of the at least one secondary working medium flow to said element, and optionallytransferring electric energy from said element to one of the at least one secondary electric power flow (62).A25. The process according to any of the preceding clauses, wherein the step of transferring energy, such as heat and / or mechanical energy, from the at least one primary working medium flow (51 .1 , 51 .2) to at least one secondary working medium flow (52.1 , 52.2, 52.3) comprises transferring at least a portion of the heat from the at least one primary working medium flow (51.1 , 51 .2) to one or more of the at least one secondary working medium flow (52.1 , 52.2, 52.3) via at least one heat exchanger, at least one heat pump, at least one turbine , at least one turbo charger or any combination of them.A26. The process according to any of the preceding clauses, wherein the step of transferring energy, such heat and / or mechanical energy, from the at least one primary working medium flow (51 .1 , 51 .2) to at least one secondary working medium flow (52.1 , 52.2, 52.3) comprises forming one or more of the at least one secondary working medium flow (52.2) with at least a portion of the at least one primary working medium flow (51 .1 ), preferably using at least one valve and / or fluid diverter.A27. The process according to any of the preceding clauses, wherein the step of transferring electrical energy from the primary electrical power flow (61 ) to the at least one secondary electric power flow (62) comprises forming the at least one secondary electrical power flow (62) with at least a portion of the primary electrical power flow (61 ), preferably by using an electric distributor and / or a transformer.A28. The process according to any of the preceding clauses, wherein the at least one primary (51.1 , 51 .2) or secondary (52.1 , 52.2, 52.3) working medium flow is a working fluid flow, a heat transfer medium flow, a solid bed or any combination thereof.A29. The process according to any of the preceding clauses, wherein the at least one primary working medium flow (51.1 , 51 .2) comprises a first (51.1 ) and optionally second (51 .2) primary working medium flow, further comprising transforming the first working medium flow (51.1 ) into the primary electrical power flow (61 ) and / or the second primary working medium flow (51 .2) in the first power generation system (15),A30. The process according to any of the preceding clauses, wherein the at least one primary working medium flow (51.1 , 51 .2) comprises a first (51.1 ) and optionally second (51 .2) primary working medium flow, further comprising compressing the first working medium flow (51.1 ) into the second primary working medium flow (51.2) in a compression unit.A30bis. The process according to any of the preceding clauses A1 to A24 or A27 to A30, wherein the step of transferring energy such as heat and / or mechanical energy, from the at least one primary working medium flow (51 .1 , 51 .2) to at least one secondary working medium flow (52.1 , 52.2, 52.3) comprises at least one of: o transferring at least a portion of the heat from the at least one primary working medium flow (51 .1 , 51 .2) to one or more of the at least one secondary working medium flow (52.1 , 52.2, 52.3) via at least one heat exchanger, at least one heat pump, at least one turbine, at least one turbo charger or any combination of them; and / or o forming one or more of the at least one secondary working medium flow (52.1 , 52.2, 52.3) with at least a portion of the at least one primary working medium flow (51 .1 , 51 .2), preferably using at least one valve and / or fluid diverter.A31 . The process according to any of the preceding clauses, wherein the step of transferring in the at least one energy distribution unit (20) is performed free of electric power flow and / or electric power generation.A32. The process according to any of the preceding clauses, wherein said process is free of transforming any working medium flow into any electrical power flow preferably in any power generation system.B1 . A CO2 capture system, preferably adapted to carry out a process according to any of the preceding clauses, said system comprising:• an hydration unit (10) adapted to, at least partly, slake quicklime materials (16) and / or quick dolomitic lime materials (16’) with water (7) as liquid and / or vapor;• at least one energy distribution unit (20);• a primary working medium circuit arrangement for circulating at least one primary working medium flow (51 .1 , 51 .2), preferably fluidly connected to the at least one energy distribution unit (20);• optionally a primary electric power circuit network for circulating a primary electrical power flow (61 ) between the at least one energy distribution unit (20) and a first power generation system (15) supplied with a first (51.1 ) of the at least one primary working medium flow, preferably said first power generation system generating a second (51.2) of the at least one primary working medium flow;• at least one energy utilization unit (30.1 , 30.2, 30.3, 30.4);• at least one CO2 treatment unit (35.1 , 35.2, 35.3), preferably a first of the at least one utilization unit (30.1) comprising or consisting of the at least one CO2 treatment unit (35.1 , 35.2, 35.3) at least one of:- a secondary working medium circuit arrangement circulating at least one secondary working medium flow (52.1 , 52.2, 52.3) fluidly connected to the at least one energy distribution unit (20) and the at least one energy utilization unit (30.1 , 30.2, 30.3, 30.4), and / or- a secondary electric power network circulating at least one secondary electric power flow (62) connected to least one energy distribution unit (20) and the at least one energy utilization unit (30.1 , 30.2, 30.3); wherein the at least one energy distribution unit (20) is configured to control the distribution of the at least one secondary working medium flow (52.1 , 52.2, 52.3) and / or the at least one secondary electric power flow (62) between the at least one energy distribution unit (20) and the at least one energy utilization unit (30.1 , 30.2, 30.3).B2. The system according to the preceding clause, wherein the maximal distance between any pair of the following elements: the hydration unit (10), the at least one energy distribution unit (20) and the at least one energy utilization unit (30.1 , 30.2, 30.3, 30.4), in particular the at least one CO2 treatment unit (35.1 , 35.2, 35.3), is less than 10 km, preferably less than 1 km.B3. The system according to any of Clauses B1 to B2, wherein the at least one CO2 treatment unit (35.1 , 35.2, 35.3) is adapted to capture at least some CO2 from at least one CO2 containing stream (71 , 71 *), said unit (35.1 , 35.2, 35.3) comprising at least one of:• a CO2 purification unit (35.1 ), such as a pressure or temperature swing adsorption apparatus, a chemical or physical absorption apparatus, an amine-based gas treating apparatus, a membrane separation apparatus or cryogenic gas treating apparatus, said unit having an inlet supplied with a first of the at least one CCh-contain- ing stream (71 ) and a first outlet with a CCh-enriched stream (75) and a second outlet with a CCh-depleted stream (73);• a CO2 carbonator unit (35.2) with an inlet supplied with a second of the at least one CCh-containing stream (71 ) and an outlet with a CCh-depleted stream (73), said unit being adapted to contact at least one of the hydrated materials (17), the quicklime materials (16) and / or the quick dolomitic lime materials (16’), with CO2, thereby forming synthetic carbonated materials (6*).• a direct air capture unit (35.3) for capturing CO2 in the third of the at least one CO2-containing stream as ambient air or conditioned air, thereby forming synthetic carbonated materials (6*), said unit being either- adapted to contact at least one of the hydrated materials (27), the quicklime materials (16) and / or the quick dolomitic lime materials (16’) with said CO2-containing steam, or- adapted to contact carbonate ions resulting from the dissolution of some of the CO2 of the CO2-containing steam with ions from the dissolution at least one of the hydrated materials, the quicklime materials and / or the quick dolomitic lime materials.B4. The system according to any of Clauses B1 to B3, wherein one of the at least one energy utilization unit comprises one or more elements selected from the group comprising: a fuel dryer, a carbonated material dryer, a hydrate dryer, a steam generator for generating mechanical energy and / or electricity in a turbine, an electricity producing unit such as an organic rankine cycle apparatus, a thermal or electrical chiller, a thermal desalination unit and / or a district heating.B5. The system according to any of Clauses B1 to B4, wherein one of the at least one energy utilization unit (30.2), which comprises or consist in a decarbonation reactor (37) adapted to transform limestone materials (6), dolomitic stone materials (6’), at least some of the synthetic carbonated materials (6*) produced in the CO2 carbonator unit (35.2), at least some of the synthetic carbonated materials (6*) produced in the direct air capture unit (35.3),or the other synthetic carbonated material (6*), in particular produced in another plant , into the quicklime materials (16) and / or quick dolomitic lime materials (16’), and forming an exhaust gas stream (71 ) exiting said reactor via an exhaust opening.B6. The system according to any of Clauses B1 to B5, further comprising a first CO2-containing circuit in fluid communication with the exhaust opening of decarbonation reactor (37), said circuit being in fluid communication with one of the at least one CO2 treatment unit (35.1 , 35.2, 35.3), in particular the CO2 purification unit (35.1 ).B7. The system according to any of Clauses B1 to B6, further comprising a second CCh-containing circuit in fluid communication with at least one of a exhaust opening of a power plant adapted to burn fossil fuel or biomass, said circuit being in fluid communication with one of the at least one CO2 treatment unit (35.1 , 35.2, 35.3), in particular at least one of the CO2 carbonator unit (35.2), the CO2 purification unit (35.1 ) and / or the direct air capture unit (35.3).B8. The system according to any of Clauses B1 to B7, further comprising an energy storage unit (40) selected from the group comprising a heat sink, a heat battery, a regenerator, a battery, a heat battery, a thermo-chemical energy storage unit, a hot water storage tank, an energy storage dam, a first storing unit with some of the hydrated materials or a second storing unit with some of the quicklime materials and / or the quick dolomitic lime materials, said unit being adapted to store some of the energy supplied by at least one of one of the at least one primary working medium flow, the primary electrical power flow, one of the least one secondary working medium flow and / or one of the at least one secondary electric power flow.B9. The system according to any of Clauses B1 to B8, wherein the at least one distribution unit comprises at least one of: a heat exchanger, avalve, a fluid diverter, a turbine, a generator, a turbocharger, a transformer, an electric distributor or any combination of them.

[0070] While the invention has been illustrated and described in detail in the drawings and foregoing description, such illustration and description are to be considered illustrative or exemplary and not restrictive. Other variations to the disclosed embodiments can be understood and effected by those skilled in the art in practicing the claimed invention, from a study of the drawings, the disclosure and the appended claims. In the claims, the word “comprising” does not exclude other elements or steps, and the indefinite article “a” or “an” does not exclude a plurality. The mere fact that certain measures are recited in mutually different dependent claims does not indicate that a combination of these measures cannot be used to advantage. Any reference signs in the claims should not be construed as limiting the scope.

[0071] The foregoing description details certain embodiments of the invention. It will be appreciated, however, that no matter how detailed the foregoing appears in text, the invention may be practiced in many ways, and is therefore not limited to the embodiments disclosed. It should be noted that the use of particular terminology when describing certain features or aspects of the invention should not be taken to imply that the terminology is being re-defined herein to be restricted to include any specific characteristics of the features or aspects of the invention with which that terminology is associated.

Claims

Claims1 . A CO2 capture process comprising the following steps:• Supplying quicklime materials (16) and / or quick dolomitic lime materials (16’) to a hydration unit (10);• A least partly hydrating said materials in the hydration unit (10) with water (7) as liquid and / or vapor to produce hydrated materials (17);• Transferring at least a portion of the heat generated during the hydration to at least one primary working medium flow (51 .1 , 51 .2) and optionally transforming the at least one working medium flow into a primary electrical power flow (61 ) in a first power generation system (15);• Capturing at least some CO2 from at least one CO2 containing stream (71 , 71 *) to reduce the CO2 content in said stream, in at least one CO2 treatment unit (35.1 , 35.2, 35.3);• Exchanging energy between at least one energy distribution unit (20) and at least one energy utilization unit (30.1 , 30.2, 30.3, 30.4) by using energy exchanges with at least one of : o at least one secondary working medium flow (52.1 , 52.2, 52.3) and / or; o at least one secondary electric power flow (62);• Controlling at least one of the at least one secondary working medium flow (52.1 , 52.2, 52.3) and / or the at least one secondary electric power flow (62) between the at least one energy distribution unit (20) and the at least one energy utilization unit (30.1 , 30.2, 30.3, 30.4), depending on the power need of the at least one energy utilization unit (30.1 , 30.2 , 30.3, 30.4);Transferring in the at least one energy distribution unit (20), at least one of: o energy as heat and / or mechanical energy, from the at least one primary working medium flow (51 .1 , 51 .2) to the at least one secondary working medium flow (52.1 , 52.2, 52.3), and / or o electric energy from the primary electrical power flow (61 ) to the at least one secondary electric power flow (62);• Transferring at least a portion of energy as heat and / or mechanical energy from one or more of the at least one utilization unit (30.1 , 30.2, 30.3, 30.4) to another of the at least one utilization unit (30.1 , 30.2, 30.3, 30.4) via one or more of the at least one secondary working medium flow (52.1 , 52.2, 52.3) in a cascade configuration. wherein the at least one energy utilization unit (30.1 ) comprises a first energy utilization unit (30.1 ), said unit comprising or consisting of the at least one CO2 treatment unit (35.1 , 35.2, 35.3).

2. A CO2 capture process comprising the following steps:• Supplying quicklime materials (16) and / or quick dolomitic lime materials (16’) to a hydration unit (10);• A least partly hydrating said materials in the hydration unit (10) with water (7) as liquid and / or vapor to produce hydrated materials (17);Transferring at least a portion of the heat generated during the hydration to at least one primary working medium flow (51 .1 , 51 .2);Capturing at least some CO2 from at least one CO2 containing stream (71 , 71 *) to reduce the CO2 content in said stream, in at least one CO2 treatment unit (35.1 , 35.2, 35.3);• Exchanging energy between at least one energy distribution unit (20) and at least one energy utilization unit (30.1 , 30.2, 30.3, 30.4) by using energy exchanges with at least one secondary working medium flow (52.1 , 52.2, 52.3);• Controlling at least one of the at least one secondary working medium flow (52.1 , 52.2, 52.3) between the at least one energy distribution unit (20) and the at least one energy utilization unit (30.1 , 30.2, 30.3, 30.4), depending on the power need of the at least one energy utilization unit (30.1 , 30.2 , 30.3, 30.4);• Transferring in the at least one energy distribution unit (20), energy as heat and / or mechanical energy, from the at least one primary working medium flow (51.1 , 51 .2) to the at least one secondary working medium flow (52.1 , 52.2, 52.3); wherein the at least one energy utilization unit (30.1 ) comprises a first energy utilization unit (30.1 ), said unit comprising or consisting of the at least one CO2 treatment unit (35.1 , 35.2, 35.3).

3. The process according to any of the preceding claims, wherein the at least one CO2 treatment unit (35.1 , 35.2, 35.3) comprises at least one of:• a CO2 purification unit (35.1 ), such as a pressure or temperature swing adsorption apparatus, a chemical or physical absorption apparatus, a membrane separation apparatus, an amine-based gas treating apparatus, or cryogenic gas treating apparatus, said unithaving an inlet supplied with a first of the at least one CCh-contain- ing stream (71 ) and a first outlet with a CCh-enriched stream (75) and a second outlet with a CCh-depleted stream (73);• a CO2 carbonator unit (35.2) with an inlet supplied with a second of the at least one CCh-containing stream (71 ) and an outlet with a CCh-depleted stream (73), said unit being adapted to contact at least one of the hydrated materials (17), the quicklime materials (16) and / or the quick dolomitic lime materials (16’) with CO2, thereby forming synthetic carbonated materials (6*), preferably as powder and / or shaped bodies;• a direct air capture unit (35.3) capturing CO2 in a third of the at least one CO2-containing stream (71 , 71 *) as ambient air or conditioned air, thereby forming synthetic carbonated materials (6*), preferably as powder and / or shaped bodies, said unit being either :- adapted to contact at least one of the hydrated materials, the quicklime materials and / or the quick dolomitic lime materials with said CO2-containing steam, or- adapted to contact carbonate ions resulting from the dissolution of some of the CO2 of said CO2-containing steam with ions from the dissolution at least one of the hydrated materials, the quicklime materials and / or the quick dolomitic lime materials.

4. The process according to Claim 3, wherein the at least one CO2 treatment unit (35.1 , 35.2, 35.3) comprises the CO2 purification unit (35.1 ) and optionally at least one of the CO2 carbonator unit (35.2) and / or the direct air capture unit (35.3).

5. The process according to Claim 3 or 4, further comprising decarbonating at least one of limestone materials (6), dolomitic stone materials (6’), at least some of the synthetic carbonated materials (6*) produced in in theCO2carbonator unit (35.2), at least some of the synthetic carbonated materials (6*) produced in the direct air capture unit (35.3), or other synthetic carbonated materials (6*), in particular produced in another plant, in a decarbonation reactor (37), thereby forming the quicklime materials (16) and / or the quick dolomitic lime materials (16’) and optionally at least a portion of the first of the at least one CCh-containing stream (71 ), preferably the decarbonation reactor (37) being a shaft kiln, a regenerative multishaft kiln, such as a parallel flow regenerative kiln, an annular kiln, a fluidized bed calciner, a circulated fluidized bed calciner, an entrained bed calciner or an electrolysis unit.

6. The process according to Claim 4 in combination with Claim 5, further comprising feeding the decarbonation reactor (37) with at least some of the synthetic carbonated materials (6*) produced in at least one of the CO2carbonator unit (35.2) and / or the direct air capture unit (35.3).

7. The process according to Claim 6, further comprising forming at least a portion of the second of the at least one CCh-containing stream in a power plant combusting fuel, in particular burning fossil fuel, and generating in said plant at least one of: energy as heat and / or mechanical energy, transferred to one of the at least one secondary working medium flow (52.1 , 52.2, 52.3) and / or electricity transferred to one of the at least one secondary electric power flow (62).

8. The process according to any of Claims 1 to 4 or 6 to 7 in combination with Claim 5, wherein the at least one energy utilization unit (30.1 , 30.2, 30.3, 30.4) comprises a second energy utilization unit (30.2), said second energy utilization unit (30.2) comprising or consisting of the decarbonation reactor (37) and optionally at least one of:- a cooling unit (37.8) for cooling the quicklime materials (16) and / or the quick dolomitic lime materials (16’) produced in the decarbonation reactor (37) and / or- a pre-heating unit (37.1 ) for heating at least part of one of the limestonematerials (6), the dolomitic stone materials (6’), the at least some of the synthetic carbonated materials (6*) produced in the CO2 carbonator unit (35.2), the at least some of the synthetic carbonated materials (6*) produced in the direct air capture unit (35.3), or the other synthetic carbonated materials (6*) to be processed in the decarbonation reactor (37).

9. The process according to any of the preceding claims, wherein the at least one energy utilization unit (30.1 , 30.2, 30.3, 30.4) further comprises a third energy utilization unit (30.3), which comprises or consists of a heating network, in particular a district heating network (39), said process further comprising supplying the heating network using heat from one of the at least one secondary working medium flow (52.1 , 52.2, 52.3) or heat from at least one tertiary working medium flow (53).

10. The process according to any of Claims 1 , 2 or 5 to 9, preferably in combination with any of Claim 3 or 4, wherein the at least one energy utilization unit (30.1 , 30.2, 30.3, 30.4) further comprises a fourth energy utilization unit (30.4), which consists of or comprises a heat driven chiller (38) such as an ammonia absorption refrigeration unit, said process further comprising mixing a first medium such as ammonia with a second medium such as water, pumping said mixture in a desorber or boiler, separating the first medium from the second medium by evaporation using the heat at from one of the at least one secondary working medium flow, optionally said process further comprising cooling at least a cold utilization unit, such as the cryogenic gas treating apparatus or a centralized cooling network, with the heat driven chiller.11 . The process according to any of Claims 2 to 10, further comprising transferring at least a portion of energy as heat and / or mechanical energy from one or more of the at least one utilization unit (30.1 , 30.2, 30.3, 30.4) to another of the at least one utilization unit (30.1 , 30.2, 30.3, 30.4) via one or more of the at least one secondary working medium flow (52.1 , 52.2, 53.3) in a cascade configuration.

12. The process according to any of the preceding claims, further comprising storing some of the heat and / or electric energy supplied by at least one of:- the at least one primary working medium flow (51 .1 , 51 .2) and / or the primary electrical power flow (61 ), respectively, and / or-the at least one secondary working medium flow (52.1 , 52.2, 52.3) and / or the at least one secondary electrical power flow (62), into an energy storage unit (40) preferably selected from the group comprising a heat sink, a heat battery, a hot water storage tank, a regenerator, a battery, an energy storage dam and a thermo-chemical energy storage unit, in particular thermo-chemical energy storage unit comprising at least one of a first storing unit with some of the hydrated materials (17) and / or a second storing unit with some of the quicklime materials (16) and / or some of the quick dolomitic lime materials (16’).

13. The process according to any of the preceding claims, further comprising either :- reducing or interrupting the hydration process, when at least one of the following conditions is met:- the global energy need of the at least one energy utilization unit (30.1 , 30.2, 30.3, 30.4) is below a first predefined threshold, and / or;- the availability of renewable energy is above a second predefined threshold, in particular during day shift, preferably when solar energy source ensures at least a portion of the energy supply, or- increasing the hydration process when the global energy need of the at least one energy utilization unit (30.1 , 30.2, 30.3, 30.4) is above a third predefined threshold.

14. The process according to any of the preceding claims, wherein the hydration unit (10) is not fed with the limestone materials (6), the dolomitic stone materials (6’), the synthetic carbonated materials (6*) produced in the CO2carbonator unit (35.2), the synthetic carbonated materials (6*) produced in the direct air capture unit (35.3), nor the other synthetic carbonated materials (6*).

15. The process according to any of the preceding claims, wherein the primary working medium flow circulates in a closed loop circuit and / or wherein one or more of the at least one secondary working medium flow circulate in one or more corresponding closed loop circuits.

16. The process according to any of the preceding claims, wherein the primary working medium of the primary working medium flow is a liquid medium, a gaseous medium or a combination thereof.

17. The process according to any of the preceding claims, further comprising capturing CO2 in the third of the at least one CCh-containing stream, as conditioned air (71*), in the direct air capture unit (35.3), said unit (35.3) comprising at least one direct air capture conditioning unit adapted to adjust at least one of:-an operational parameter such as a conditioned air flow rate, a relative humidity level of the conditioned air flow, a temperature of the conditioned air flow, and / or- another operational parameter related to the feeding of sorbent, namely at least one of the hydrated materials, the quicklime materials and / or the quick dolomitic lime materials, to the direct air capture unit, such as : an inventory of the hydrated materials, a flow of the hydrated materials, an inventory of the quicklime materials (16), a flow of the quicklime materials (16), an inventory of quick dolomitic lime materials (16’) or a flow of quick dolomitic lime materials (16’).

18. The process according to any of the preceding claims, wherein the energy exchanges with the at least one secondary working medium flow (52.1 , 52.2, 53.3) comprise:• transferring energy as heat and / or mechanical energy, from a first (52.1 ) set of the at least one secondary working medium flow to one or more of the at least one energy utilization unit (30.1 , 30.2, 30.3, 30.4), and / or• transferring energy as heat and / or mechanical energy, from said utilization unit (30.1 , 30.2, 30.3, 30.4) to a second set (52.2) of the at least one secondary working medium flow.

19. The process according to any of the preceding claims, wherein the energy exchanges with the at least one secondary working medium flow comprise transferring energy as heat and / or mechanical energy, from or to one or more of the at least one energy utilization unit (30.1 , 30.2, 30.3, 30.4) via a third set (52.3) of the at least one secondary working medium flow.

20. The process according to any of the preceding claims, further comprising transferring at least a portion of energy as heat and / or mechanical energy, from one or more of the at least one utilization unit (30.1 , 30.2, 30.3, 30.4) to another of the at least one utilization unit (30.1 , 30.2, 30.3, 30.4) via the at least one tertiary work medium flow (53) without passing through the at least one energy distribution unit (20).21 . The process according to any of the preceding claims, further comprising transferring heat:- from one of the first or third set (52.1 , 52.2) of the at least one secondary working medium flow to one of the at least one CO2 treatment unit (35.1 , 35.2, 35.3) of the first of the at least utilization unit (30.1 ), and / or- from one of the at least one CO2 treatment unit (35.1 , 35.2, 35.3) of the first of the at least utilization unit (30.1 ) to one of the second or third set (52.2) of the at least one secondary working medium flow.

22. The process according to any of the preceding claims, further comprising transferring at least a part of the heat collected in the cooler unit (37.8) toone of the second set (51 .2) of the at least one secondary working medium flow or to one of the at least one primary working medium flow (51.1 , 51 .2), and / or-transferring heat from one of the second or third set (52.3) of the at least one secondary working medium flow to the preheating unit (37.1 ).

23. The process according to any of the preceding claims, further comprising transforming one of the at least one secondary electric power flow (62) from the at least one energy distribution unit (20) into heat for the decarbonation reactor (37) or using said electric power flow (62) to drive an electrolysis unit in the decarbonation reactor (37).

24. The process according to any of the preceding claims, wherein the at least one energy utilization unit (30.1 , 30.2, 30.3, 30.4) further comprises a fifth energy utilization unit, which comprises or consists of at least one element selected from the group comprising: a fuel dryer, a carbonated material dryer, a hydrate dryer, a steam generator for generating mechanical energy and / or electricity in a turbine, an electricity producing unit such as an organic rankine cycle apparatus, a thermal or electrical chiller and / or a thermal desalination unit and preferably transferring the heat from the first set (52.1 ) of the at least one secondary working medium flow to said element, and optionally transferring electric energy from said element to one of the at least one secondary electric power flow (62).

25. The process according to any of the preceding claims, wherein the step of transferring energy as heat and / or mechanical energy, from the at least one primary working medium flow (51.1 , 51 .2) to at least one secondary working medium flow (52.1 , 52.2, 52.3) comprises transferring at least a portion of the heat from the at least one primary working medium flow (51.1 , 51 .2) to one or more of the at least one secondary working medium flow (52.1 , 52.2, 52.3) via at least one heat exchanger, at least one heat pump, at least one turbine , at least one turbo charger or any combination of them.

26. The process according to any of the preceding claims, wherein the step of transferring energy, heat and / or mechanical energy, from the at least one primary working medium flow (51 .1 , 51 .2) to at least one secondary working medium flow (52.1 , 52.2, 52.3) comprises forming one or more of the at least one secondary working medium flow (52.1 , 52.2, 52.3) with at least a portion of the at least one primary working medium flow (51 .1 ,51 .2), preferably using at least one valve and / or fluid diverter.

27. The process according to any of the preceding claims, wherein the step of transferring electrical energy from the primary electrical power flow (61 ) to the at least one secondary electric power flow (62) comprises forming the at least one secondary electrical power flow (62) with at least a portion of the primary electrical power flow (61 ), preferably by using an electric distributor and / or a transformer.

28. The process according to any of the preceding claims, wherein the at least one primary (51.1 , 51 .2) or secondary (52.1 , 52.2, 53.3) working medium flow is a working fluid flow, a heat transfer medium flow, a solid bed or any combination thereof.

29. The process according to any of the preceding claims, wherein the at least one primary working medium flow (51.1 , 51 .2) comprises a first (51.1 ) and optionally second (51.2) primary working medium flow, further comprising transforming the first working medium flow (51.1 ) into the primary electrical power flow (61 ) and / or the second primary working medium flow (51 .2) in the first power generation system (15),30. The process according to any of the preceding claims, wherein the at least one primary working medium flow (51.1 , 51 .2) comprises a first (51.1 ) and optionally second (51.2) primary working medium flow, further comprising compressing the first working medium flow (51.1 ) into the second primary working medium flow (51.2) in a compression unit.31 . The process according to any of the preceding claims 1 to 25 or 28 to 30, wherein the step of transferring energy as heat and / or mechanical energy, from the at least one primary working medium flow (51 .1 , 51 .2) to at least one secondary working medium flow (52.1 , 52.2, 52.3) comprises at least one of:• transferring at least a portion of the heat from the at least one primary working medium flow (51 .1 , 51 .2) to one or more of the at least one secondary working medium flow (52.1 , 52.2, 52.3) via at least one heat exchanger, at least one heat pump, at least one turbine, at least one turbo charger or any combination of them; and / or• forming one or more of the at least one secondary working medium flow (52.1 , 52.2, 52.3) with at least a portion of the at least one primary working medium flow (51 .1 , 51 .2), preferably using at least one valve and / or fluid diverter.

32. The process according to any of the preceding claims, wherein the step of transferring in the at least one energy distribution unit (20) is performed free of electric power flow and / or generating electric power.

33. The process according to any of the preceding claims, wherein said process is free of transforming any working medium flow into any electrical power flow preferably in any power generation system.

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