High-temperature electrolyzer system optimized by an intermediate circuit recovery module

Abstract

Title of the invention: High-temperature electrolyzer system optimized by an intermediate circuit recovery module. The invention relates to a system comprising an EHT electrolyzer (1), a first steam supply line (2), a first hydrogen outlet line (4), a second oxygen outlet line (3), a first heat exchange module (5) configured to ensure heat exchange between the first steam supply line (2) and the first hydrogen outlet line (4), characterized in that the system comprises a first module for recovering the thermal energy of the hydrogen at the outlet of the first heat exchange module (5) for the benefit of the first supply line (2),the recovery module comprising a first intermediate heat exchanger (6) arranged on the first discharge line (4) downstream of the first heat exchange module (5) and configured to transfer the thermal energy of the dihydrogen to an intermediate fluid, and a first intermediate steam generator (50) arranged on the first steam supply line (2) configured to transfer the thermal energy of the intermediate fluid to liquid water. Figure for the abstract: Fig. 1,

Description

Title of the invention: High temperature electrolyzer system optimized by an intermediate circuit recovery module Technical field

[0001] The present invention relates to the field of solid oxide fuel cells (SOFC, English acronym for "Solid Oxide Fuel Cell") and that of high temperature water electrolysis (EHT, or EVHT for high temperature water vapor electrolysis, or HTE English acronym for High Temperature Electrolysis, or HTSE English acronym for High Temperature Steam Electrolysis), also solid oxide (SOEC, English acronym for "Solid Oxide Electrolyte Cell"). It finds application particularly for optimizing the energy consumption of a SOEC electrolyzer system. STATE OF THE ART

[0002] Electrolysis of water is an electrolytic reaction that decomposes water into oxygen and hydrogen gas with the help of an electric current according to the reaction: H2O -> H2 + 1 / 2 02.

[0003] To carry out the electrolysis of water, it is advantageous to carry it out at a high temperature, typically between 600 and 950°C, because part of the energy required for the reaction can be provided by heat, which is cheaper than electricity, and the activation of the reaction is more efficient at high temperature and does not require a catalyst.A solid oxide electrolysis cell or "SOEC" (an English acronym for "Solid Oxide Electrolyte Cell") comprises in particular: - a first porous conductive electrode, or "cathode", intended to be supplied with water vapor for the production of dihydrogen, - a second porous conductive electrode, or "anode", through which the dioxygen produced by the electrolysis of the water injected onto the cathode escapes, and - a solid oxide membrane (dense electrolyte) sandwiched between the cathode and the anode, the membrane being anionically conductive for high temperatures, usually temperatures above 600 °C. By heating the cell to at least this temperature and injecting an electric current I between the cathode and the anode, a reduction of the water on the cathode occurs, which generates dihydrogen (H2) at the cathode and dioxygen at the anode.To implement high-temperature electrolysis, it is known to use an SOEC type electrolyser consisting of a stack of elementary patterns, each comprising a solid oxide electrolysis cell, consisting of three anode / electrolyte / cathode layers superimposed on each other, and interconnection plates made of metal alloys also called bipolar plates, or interconnectors. The interconnectors have the following characteristics: function of ensuring both the passage of electric current and the circulation of gases in the vicinity of each cell (water vapor injected, hydrogen and oxygen extracted in an EHT electrolyser; air and hydrogen injected and water extracted in an SOFC stack) and of separating the anode and cathode compartments which are the gas circulation compartments on the side of the anodes and cathodes of the cells respectively.

[0004] To carry out the electrolysis of water vapor at high temperature EHT, water vapor H2O is injected into the cathode compartment.

[0005] Under the effect of the current applied to the cell, the dissociation of water molecules in vapor form is carried out at the interface between the hydrogen electrode (cathode) and the electrolyte: this dissociation produces dihydrogen gas H2 and oxygen ions. The dihydrogen is collected and evacuated at the outlet of the hydrogen compartment. The oxygen ions migrate through the electrolyte and recombine into dioxygen O2 at the interface between the electrolyte and the oxygen electrode (anode).

[0006] For the effective implementation of electrolysis by the stack, the stack is brought to a temperature above 600°C, usually a temperature between 600°C and 950°C, the gas supply is started at a constant flow rate and an electrical power source is connected between two terminals of the stack in order to circulate the current I therein.

[0007] The efficiency of the transformation of electricity into hydrogen is a key point in ensuring the competitiveness of the technology. The electricity consumption mainly takes place during the electrolysis reaction itself, but nearly 30% of the electrolyser's consumption comes from the thermal / hydraulic fluid management system. That is to say, the architecture external to the electrolyser and the management of fluids and thermal energy in this architecture.

[0008] The evaporation of the water used in the electrolyser is the largest energy consumption of this thermal / hydraulic management system. Conventionally, this function is provided by an electric steam generator which consumes 20% of the overall consumption of the electrolyser.

[0009] Furthermore, in general a significant portion of energy is released into the ambient environment. For example, during the phase of drying the hydrogen and its compression it is necessary to significantly cool this mixture in order to allow the condensation of the water present in the water / hydrogen mixture. This condensation takes place very largely at a temperature lower than the evaporation temperature of the water at the inlet of the electrolyser, which means that a very small portion of this condensation energy is usable.

[0010] There is therefore a need to minimize this consumption by optimizing the architecture and fluid management of the electrolyzer system.

[0011] An object of the present invention is therefore to propose an electrolyser system high temperature optimized by an intermediate circuit recovery module.

[0012] Other objects, features, and advantages of the present invention will become apparent from the following description and accompanying drawings. It is understood that other advantages may be incorporated. SUMMARY

[0013] To achieve this objective, according to one embodiment, a system is provided comprising

[0014] a high temperature electrolyser (HTE),

[0015] a first supply line of the electrolyser configured to supply the electrolyser with water vapour,

[0016] a first electrolyzer discharge line configured to discharge dihydrogen from the electrolyzer,

[0017] a second electrolyzer discharge line configured to discharge oxygen from the electrolyzer,

[0018] a first heat exchange module configured to provide heat exchange between the first water vapor supply line and the first dihydrogen discharge line.

[0019] The system being characterized in that it comprises a first module for recovering the thermal energy from the dihydrogen at the outlet of the first heat exchange module for the benefit of the first water vapor supply line, the recovery module comprising

[0020] a first intermediate exchanger arranged on the first discharge line downstream of the first heat exchange module and configured to transfer the thermal energy from the dihydrogen to an intermediate fluid, and

[0021] a first intermediate steam generator arranged on the first steam supply line configured to transfer thermal energy from the intermediate fluid to liquid water,

[0022] a first intermediate fluid circuit configured to receive an intermediate fluid and provide the fluid connection between the first intermediate exchanger and the first intermediate steam generator.

[0023] This arrangement makes it possible to recover the calories from the dihydrogen produced by the electrolyser for the benefit of the production of water vapor. By the present system, the recovery module allows both the cooling of the dihydrogen and the production of steam. Thus, the electrical consumption of the system is greatly reduced.

[0024] Thus, the system uses the heat from the dihydrogen at the outlet of the electrolyser, but preferably after the first heat exchange module so that the thermal rejection of the dihydrogen is exploited at a lower temperature by a generator of steam via an intermediate circuit. The calories recovered from the dihydrogen are reinjected at a temperature higher than the evaporation temperature of the water on the water vapor supply line and preferably upstream of an electric steam generator.

[0025] Advantageously, the use of an intermediate circuit between the first dihydrogen discharge line and the intermediate steam generator makes it possible to have a remote steam generator and not an exchanger between the dihydrogen discharge line in which water and dihydrogen circulate. The intermediate circuit presents a great modularity of the recovery module, because it also makes it possible to envisage recovering the calories at other places in the system such as for example downstream on the dihydrogen discharge line or even on the dioxygen discharge line, and this without complicating the structure of the recovery module.

[0026] The system thus makes it possible to reduce the electrical consumption of the system by increasing the thermal power drawn.

[0027] The system according to the invention has an overall efficiency improved by 3% compared to a conventional configuration. BRIEF DESCRIPTION OF THE FIGURES

[0028] The aims, objects, as well as the characteristics and advantages of the invention will emerge more clearly from the detailed description of an embodiment thereof which is illustrated by the following accompanying drawings in which:

[0029] [Fig.l] [Fig.l] is a functional diagram representing the system according to a first embodiment of the invention.

[0030] [Fig.2] [Fig.2] represents a functional diagram representing an inter circuit mediator.

[0031] [Fig.3] [Fig.3] is a functional diagram representing the system according to a second embodiment of the invention

[0032] The drawings are given by way of example and are not limiting of the invention. They constitute schematic representations of principle intended to facilitate the understanding of the invention and are not necessarily on the scale of practical applications. DETAILED DESCRIPTION

[0033] Before beginning a detailed review of embodiments of the invention, optional features which may possibly be used in combination or alternatively are set out below:

[0034] According to one example, the system comprises a third module for recovering thermal energy from the dihydrogen at the output of the first heat exchange module 5. for the benefit of the first water vapor supply line 2, the third recovery module comprising a heat pump and an intermediate circuit,

[0035] the intermediate circuit comprising

[0036] a second intermediate exchanger 7 arranged on the first discharge line 2 downstream of the first heat exchange module 5 and configured to transfer the thermal energy from the dihydrogen to an intermediate fluid, and

[0037] a third intermediate fluid circuit 32 configured to receive an intermediate fluid and ensure the fluid connection between the second intermediate exchanger 7 and the heat pump,

[0038] the heat pump comprising

[0039] a fluid circuit 27 configured to receive a heat transfer fluid,

[0040] an evaporator 25 arranged on the intermediate fluid circuit 32 downstream of the second intermediate exchanger 7 and configured to transfer the thermal energy from the intermediate fluid to the heat transfer fluid,

[0041] a compressor 26 configured to compress the heat transfer fluid,

[0042] a condenser 23 arranged on the first water vapor supply line 2 upstream of the first heat exchange module 5 and configured to transfer the thermal energy from the heat transfer fluid to the liquid water,

[0043] an expander 24 configured to expand the heat transfer fluid,

[0044] the fluid circuit 27 being configured to fluidly connect the evaporator 25 to the compressor 26, the compressor 26 to the condenser 23, the condenser 23 to the expansion valve 24 and the expansion valve 24 to the evaporator 25.

[0045] According to one example, the system comprises a fifth intermediate exchanger 12 arranged on the first dihydrogen discharge line 4 downstream of the second intermediate exchanger 7 and in parallel with the second intermediate exchanger 7 on the third intermediate fluid circuit 32 configured to transfer the thermal energy from the dihydrogen to the intermediate fluid.

[0046] According to one example, the system comprises a sixth intermediate exchanger 15 arranged on the first dihydrogen discharge line 4 downstream of the fifth intermediate exchanger 12 and in parallel with the second intermediate exchanger 7 and the fifth heat exchanger 12 on the intermediate fluid circuit 32 configured to transfer the thermal energy from the dihydrogen to the intermediate fluid.

[0047] According to one example, the system comprises an electric steam generator 28 arranged on the first water supply line 2 upstream of the first heat exchange module 5.

[0048] According to one example, the electric steam generator 28 is arranged downstream of the first steam generator 50 and preferably downstream of the condenser 23.

[0049] According to one example, the system comprises a second recovery module in de pressure of the thermal energy of the dihydrogen at the outlet of the first heat exchange module 5 for the benefit of the first water vapor supply line 2, the depression recovery module comprising

[0050] a third intermediate exchanger 8 arranged on the first discharge line 4 downstream of the first heat exchange module 5 and configured to transfer the thermal energy from the dihydrogen to an intermediate fluid,

[0051] an expander 40 and a compressor 41 arranged upstream of the first heat exchange module 5 on the first steam supply line 2 and defining between them a depression section of the first steam supply line 2

[0052] a second intermediate steam generator 60 arranged on the depression portion of the first steam supply line 2 configured to transfer the thermal energy from the intermediate fluid to the liquid water,

[0053] a second intermediate fluid circuit configured to receive an intermediate fluid and ensure the fluid connection between the third intermediate exchanger (8) and the second steam generator 60.

[0054] According to one example, the electric steam generator 28 is arranged on the depression portion downstream of the second steam generator 60 and preferably downstream of the condenser 23.

[0055] According to one example, the first steam supply line 2 comprises a main branch on which the steam generator 50 is arranged and a vacuum branch comprising the vacuum section, the main branch and the vacuum branch being arranged in parallel.

[0056] According to one example, the system comprises a second supply line 10 of the electrolyser configured to supply the electrolyser 1 with air.

[0057] According to one example, the system comprises a second heat exchange module 11 configured to provide heat exchange between the second air supply line 10 and the second oxygen discharge line 3.

[0058] According to one example, the system comprises a fourth intermediate heat exchanger 9 arranged between the second oxygen discharge line 10 and on the first intermediate fluid circuit, in parallel with the first intermediate exchanger 6.

[0059] According to one example, the system comprises a seventh intermediate exchanger 29 arranged on the second dioxygen discharge line 10 downstream of the first heat exchanger 9 and in parallel with the second intermediate exchanger 7 on the third intermediate fluid circuit 32 configured to transfer the thermal energy from the dioxygen to the intermediate fluid.

[0060] According to one possibility, the system comprises at least a first air cooler or a second heat exchanger arranged on the first di- hydrogen, downstream of the first intermediate exchanger.

[0061] According to one possibility, the system comprises at least a second air cooler or a third heat exchanger arranged on the first di-hydrogen evacuation line, downstream of the second heat exchanger.

[0062] According to one example, the system comprises a liquid / gas separator downstream of the first air cooler and upstream of the second intermediate exchanger.

[0063] Upstream and downstream, inlet, outlet, at a given point are taken in reference to the direction of circulation of the fluid.

[0064] A parameter “substantially equal / greater / less than” a given value means that this parameter is equal / greater / less than the given value, to within plus or minus 10%, or even plus or minus 5%, of this value.

[0065] The numbering first, second, third, etc. n must be understood without limitation and without link to the need to have n-1 or an n+1.

[0066] The system according to the invention comprises a high temperature electrolyser 1 (EHT). Preferably, the electrolyser 1 is of the SOEC type, the English acronym for “Solid Oxide Electrolyte Cell”, i.e. solid oxide.

[0067] The system comprises several supply and discharge lines connected to the electrolyser 1. Thus, a line is understood to mean a pipe, a tube or a set of pipes or tubes which allow the transport of fluid to and from the electrolyser 1.

[0068] The system according to the invention comprises a first supply line 2 of the electrolyser 1 capable of supplying the electrolyser 1 with water vapor. According to one possibility, the first supply line 2 is configured to supply the electrolyser 1 with water vapor, by which it is meant that the first supply line 2 can supply a mixture of water vapor and other gas(es) for example air or dihydrogen or carbon dioxide. Upstream in this first supply line 2, the water vapor is not yet formed and the first supply line 2 is configured to receive liquid water. According to a preferred possibility, the first supply line 2 comprises a first portion receiving liquid water and a second portion, downstream of the first portion, receiving water vapor.Preferably, the first portion is located upstream of a steam generator 28 and the second portion is located downstream of said steam generator 28.

[0069] The system according to the invention comprises a first discharge line 4 capable of discharging dihydrogen (H2) from the electrolyser 1. Preferably, the first discharge line 4 receives the dihydrogen. The dihydrogen is advantageously produced by the electrolyser 1. The dihydrogen is in gaseous form. The first discharge line 4 can discharge a mixture of dihydrogen and water vapour, called residual, not having been decomposed by electrolyser 1.

[0070] The system according to the invention comprises a second discharge line 3 capable of discharging dioxygen (O2) from the electrolyser 1. Preferably, the second discharge line 3 receives the dioxygen. The dioxygen is advantageously produced by the electrolyser 1. The dioxygen is in gaseous form. The second discharge line 3 discharges, according to one possibility, a gas enriched in dioxygen, for example air enriched in dioxygen.

[0071] In the remainder of the description, the first supply line 2 is called the first water vapor supply line 2, the first discharge line 4 is called the first dihydrogen discharge line 4 and the second discharge line 3 is called the second dioxygen discharge line 3 without being limiting on the gas, fluid or mixture that can be transported in these lines.

[0072] According to one possibility, the system comprises a first heat exchange module 5 configured to ensure a heat exchange between the first water vapor supply line 2 and the first dihydrogen discharge line 4. This heat exchange module is configured to transfer the calories of the dihydrogen from the electrolyser 1 to the water intended to supply the electrolyser 1. A flow of dihydrogen gas ensures the increase in temperature of the water flow while also making it possible to cool the flow of dihydrogen discharged and which is advantageously dried and / or compressed for use.

[0073] The first heat exchange module 5 comprises, according to one embodiment, at least one heat exchanger 5a configured to ensure the heat transfer of dihydrogen to water vapor. According to a preferred embodiment, the first heat exchange module 5 comprises two heat exchangers 5a, 5b arranged in series between the first supply line 2 and the first discharge line 4. This arrangement makes it possible to provide a second heat exchanger 5b adapted to the temperature of the dihydrogen at the outlet of the electrolyser 1, conventionally of the order of 700°C, and a more usual first heat exchanger 5a adapted to the temperature of the dihydrogen after passing through a heat exchanger, i.e. conventionally of the order of 330°C. In this way, the components are optimized for the temperatures and heat transfers to be carried out.

[0074] According to one embodiment, the system comprises a second supply line 10 capable of supplying the electrolyser 1 with air. Preferably, the second supply line 10 receives air. According to one possibility, the second supply line 10 is configured to supply air to the electrolyser 1, by which it is meant that the second supply line 10 can supply air, the air being for example a gas mixture which makes it possible to sweep the cell of the electrolyser 1 and to carry away the oxygen produced by the electrolyser 1.

[0075] According to this embodiment, it is advantageous for the system according to the invention to comprise a second heat exchange module 11 configured to ensure a heat exchange between the second air supply line 10 and the second oxygen discharge line 3. This heat exchange module 11 is configured to transfer the calories of the oxygen from the electrolyser 1 to the air intended to supply the electrolyser 1. A flow of oxygen gas ensures the increase in the temperature of the air flow, which also makes it possible to cool the flow of oxygen discharged.

[0076] The second heat exchange module 11 comprises, according to one embodiment, at least one heat exchanger 11a configured to ensure the heat transfer of the oxygen to the air. According to a preferred embodiment, the second heat exchange module 11 comprises two heat exchangers 11a, 11b arranged in series between the second supply line 10 and the second discharge line 3. This arrangement makes it possible to provide a second heat exchanger 11b adapted to the temperature of the oxygen at the outlet of the electrolyser 1, conventionally of the order of 700°C, and a first heat exchanger 11b, the most usual, adapted to the temperature of the oxygen after passing through a heat exchanger, i.e. conventionally of the order of 330°C. In this way, the components are optimised for the temperatures and heat transfers to be carried out.

[0077] The system preferably comprises a compressor 30 arranged on the second supply line 10 intended for the air supply. The compressor 30 is preferably arranged upstream of the second heat exchange module 11, if it is present. The compressor 30 is intended to ensure the compression of the air intended to be supplied to the electrolyser 1. The compression of the air advantageously contributes to increasing the temperature of the air before it enters the electrolyser 1.

[0078] According to one possibility, the system comprises at least one additional heat source configured to heat the water vapor entering the electrolyser 1 to a predefined target temperature. The additional heat source is advantageously arranged on the first water vapor supply line 2, preferably downstream of the first heat exchange module 5. The additional heat source is for example an electric heater 14.

[0079] According to one possibility, the system comprises at least one additional heat source configured to heat the air entering the electrolyser 1 to a predefined target temperature. The additional heat source is advantageously arranged on the second air supply line 10, preferably downstream of the second heat exchange module 11. The additional heat source is for example an electric heater 13.

[0080] According to one possibility, the system comprises an electric steam generator 28. The electric steam generator 28 is intended to produce water vapor from liquid water. The electric steam generator 28 is supplied with energy, in particular electrical energy, to ensure the increase in the temperature of the liquid water above its evaporation temperature. The electric steam generator 28 is a component constituting the main energy consumption of an electrolyzer system according to the state of the art. The electric steam generator 28 is arranged on the first water vapor supply line 2, preferably upstream of the first heat exchange module 5. The electric steam generator 28 is preferably arranged downstream of the first intermediate steam generator 50 so as to ensure the evaporation of the liquid water before it passes into the electric steam generator 28, which limits the electrical consumption. The inlet water is advantageously already at least partially in a two-phase state.Conventionally, water is not 100% in the vapor state. The objective of this steam generator 28 is to produce superheated steam. For example, the evaporation temperature of the liquid water entering the electric steam generator 28 is of the order of 110°C or of the order of 70°C in the case of a vacuum steam generator for example as illustrated in [Fig.3].

[0081] According to one aspect of the invention, the system comprises a module for recovering thermal energy from the dihydrogen at the outlet of the heat exchange module 5 for the benefit of the first water vapor supply line 2.

[0082] Advantageously, the recovery module is called the first recovery module and comprises a first intermediate exchanger 6, a first intermediate fluid circuit and a first intermediate steam generator 50.

[0083] The first intermediate fluid circuit is configured to receive an intermediate fluid and ensures the fluid connection between the first intermediate exchanger 6 and the first intermediate steam generator 50. This intermediate circuit is advantageously a low temperature circuit. Low temperature is understood to mean a temperature of the circulating fluids between 25°C and 90°C.

[0084] The first intermediate exchanger 6 arranged on the first discharge line 2 preferably downstream of the first heat exchange module 5, more precisely downstream of the first heat exchanger 5a of the first heat exchange module 5, configured to transfer the thermal energy from the dihydrogen to the intermediate fluid. The first heat exchanger 6 is fluidically connected to the intermediate fluid circuit by a fluid connection 500 ensuring the fluid connection of the first intermediate exchanger 6 to the first intermediate steam generator 50 and by a fluid connection 501 ensuring the fluid connection of the first intermediate steam generator 50 to the first intermediate exchanger 6. By way of example, the intermediate fluid entering the first heat exchanger 6 is at a temperature temperature of the order of ambient temperature, for example between 18 and 30°C and leaves said intermediate exchanger 6 at a temperature of the order of 70°C. Advantageously, the incoming fluid is in a two-phase state, that is to say that one part is in a liquid state and another part is in a gaseous state.

[0085] The first fluid circuit is based on the same principle as the third intermediate circuit 32, notably illustrated in [Fig.2] and as the second intermediate circuit. Preferably, the first intermediate fluid circuit comprises a main branch 510 arranged between the first intermediate steam generator 50 and the fluid connection 500 configured for the circulation of the intermediate fluid from the first intermediate steam generator 50 to the first intermediate exchanger 6 and a main branch 511 arranged between the fluid connection 501 and the intermediate steam generator 50 configured for the circulation of the intermediate fluid from the first intermediate exchanger 6 to the first intermediate steam generator 50.By way of example, the intermediate fluid entering the first intermediate steam generator 50 is at a temperature of the order of ambient temperature, for example between 18 and 30°C, and leaves said intermediate steam generator 50 at a temperature of the order of 110°C for a generator at atmospheric pressure and of the order of 70°C in the case where the steam generator operates under vacuum, as for example illustrated in [Fig.3].

[0086] The first intermediate steam generator 50 is configured to transfer thermal energy from the intermediate fluid to the liquid water circulating in the first steam supply line 2. The intermediate steam generator 50 is arranged on the first steam supply line 1, preferably upstream of the first exchanger 5a of the first heat exchange module. According to a first embodiment, the intermediate steam generator 50 is arranged on the first steam supply line 1 upstream of the electric steam generator 28. According to a second embodiment, the intermediate steam generator 50 is arranged on the first steam supply line 1 in parallel with the electric steam generator 28.

[0087] According to one aspect of the invention, the system comprises a second module for recovering thermal energy from the dihydrogen at the outlet of the heat exchange module 5 for the benefit of the first water vapor supply line 2. According to the invention, the second thermal energy recovery module is a depression recovery module.

[0088] Advantageously, the vacuum recovery module comprises an intermediate exchanger 8, called the third intermediate exchanger 8, an intermediate fluid circuit called the second intermediate fluid circuit, an intermediate steam generator 60 called the second intermediate generator, an expander 40 and a 41 compressor.

[0089] The expander 40 and the compressor 41 are arranged on the first steam supply line 1 and define between them a vacuum section. The vacuum section of the first steam supply line 1 extends from the outlet of the expander 40 to the inlet of the compressor 4L. The expander 40 and the compressor 41 are both arranged on the first steam supply line 1 upstream of the first heat exchange module 5.

[0090] The second intermediate fluid circuit is configured to receive an intermediate fluid and ensure the fluid connection between the intermediate exchanger 8 and the intermediate steam generator 60. This intermediate circuit is advantageously a low temperature circuit. Low temperature is understood to mean a temperature of the circulating fluids between 25°C and 90°C.

[0091] The third intermediate heat exchanger 8 is arranged on the first dihydrogen discharge line 4, downstream of the first heat exchange module 5, more preferably downstream of the first intermediate heat exchanger 6 and preferably upstream of a second intermediate exchanger 7, preferably upstream of a possible air cooler 16 and / or liquid / gas separator 17.

[0092] The vacuum recovery module comprises a second intermediate generator 60 arranged on the first steam supply line, advantageously on the vacuum section. Preferably, the intermediate generator 60 is arranged upstream of the condenser 23 which is advantageously arranged on the vacuum section in the case where the latter is present.

[0093] The second intermediate steam generator 60 is configured to transfer the thermal energy of the intermediate fluid to the liquid water circulating in the first steam supply line 2. The intermediate steam generator 60 is arranged on the first steam supply line 1 on the section under vacuum, that is to say between the expander 40 and the compressor 4L. The intermediate steam generator 60 is preferably arranged upstream of the electric steam generator 28. Thus, the vacuum recovery module proposes to reduce the pressure in a section of the first steam supply line 2 in order to reduce the boiling temperature of the water circulating in the first supply line 2. The vacuum is then preferably compensated by recompression to atmospheric pressure.The section which is depressurized surrounds at least the second intermediate steam generator 60 and preferably also the compressor 23 and / or the electric generator 28.

[0094] Preferably, the boiling of the water takes place at a temperature lower than the temperature of the thermal discharge from the electrolyser 1 and in particular the temperature of the oxygen and the hydrogen, which promotes the exchange and therefore the exploitation of the discharges. thermal.

[0095] According to one embodiment, the system comprises at least one pump arranged on the first water vapor supply line 2 configured to set the liquid water in motion in the first supply line 2.

[0096] The third heat exchanger 8 is fluidically connected to the second intermediate fluid circuit by a fluid connection 600 ensuring the fluid connection of the third intermediate exchanger 8 to the second intermediate steam generator 60 and by a fluid connection 601 ensuring the fluid connection of the second intermediate steam generator 60 to the intermediate exchanger 8.

[0097] Preferably, the intermediate fluid circuit comprises a main branch 610 arranged between the second intermediate steam generator 60 and the fluid connection 600 configured for the circulation of the intermediate fluid from the intermediate steam generator 60 to the third intermediate exchanger 8 and a main branch 611 arranged between the fluid connection 601 and the intermediate steam generator 60 configured for the circulation of the intermediate fluid from the intermediate exchanger 8 to the intermediate steam generator 60. By way of example, the intermediate fluid entering the intermediate steam generator 60 is at a temperature of the order of 90°C and leaves said intermediate steam generator 60 at a temperature of the order of 35°C.

[0098] According to one aspect of the invention, the system comprises a third module for recovering thermal energy from the dihydrogen at the outlet of the heat exchange module 5 for the benefit of the first water vapor supply line 2.

[0099] According to one possibility, the recovery module comprises a heat pump and an intermediate circuit.

[0100] Advantageously, the intermediate circuit comprises a third intermediate fluid circuit 32 configured to receive an intermediate fluid and a second intermediate exchanger 7 arranged on the first discharge line 2 preferably downstream of the first heat exchange module 5, more precisely downstream of the first heat exchanger 5a of the first heat exchange module 5, configured to transfer the thermal energy from the dihydrogen to the intermediate fluid, preferably downstream of the first intermediate heat exchanger 6. The third intermediate fluid circuit 32 makes it possible to ensure the fluid connection between the second intermediate exchanger 7 and the heat pump. This third intermediate circuit 32 is advantageously a low-temperature circuit. Low temperature is understood to mean a temperature of the circulating fluids between 25°C and 90°C.

[0101] The second heat exchanger 7 is fluidically connected to the third intermediate fluid circuit 32 by a fluid connection 400 ensuring the fluid connection of the second intermediate exchanger 7 to the evaporator 25 and by a fluid connection 401 ensuring the fluid connection of the evaporator 25 to the second intermediate exchanger 7. By way of example, the intermediate fluid entering the second heat exchanger 7 is at a temperature of the order of 25°C and leaves said second heat exchanger 7 at a temperature of the order of 70°C. By way of example, these temperatures are valid for the different heat exchangers arranged on the first intermediate circuit and on the second intermediate circuit.

[0102] Preferably, the third intermediate fluid circuit 32 comprises a main branch 410 arranged between the evaporator 25 and the fluid connection 401 configured for the circulation of the intermediate fluid from the evaporator 25 to the intermediate exchanger and a main branch 411 arranged between the fluid connection 400 and the evaporator 25 configured for the circulation of the intermediate fluid from the intermediate exchanger to the evaporator 25. By way of example, the intermediate fluid entering the evaporator 25 is at a temperature of the order of 90°C and leaves said evaporator 25 at a temperature of the order of 35°C.

[0103] The heat pump is configured to transfer thermal energy from the intermediate fluid to the liquid water circulating in the first steam supply line 2.

[0104] The heat pump comprises a condenser 23, an expansion valve 24, at least one evaporator 25, and a compressor 26. The heat pump comprises a fluid circuit 27 capable of receiving a heat transfer fluid.

[0105] The heat transfer fluid is, for example, a fluid conventionally used in heat pumps such as 1234yf: 2,3,3,3-tetrafluoropropene (HFO-1234yf), or R245FA pentafluoropropane, or R290 propane.

[0106] The fluid circuit 27 ensures the fluid connection of the components of the heat pump, preferably in a closed circuit.

[0107] According to one embodiment, the fluid circuit 27 comprises a fluid connection 200 connected between the outlet of the compressor 26 and the inlet of the condenser 23. Advantageously, the fluid circuit 27 comprises a fluid connection 201 connected between the outlet of the condenser 23 and the inlet of the expander 24. Advantageously, the fluid circuit 27 comprises a fluid connection 202 connected between the outlet of the expander 24 and the inlet of the evaporator 25. Advantageously, the fluid circuit 27 comprises a fluid connection 203 connected between the outlet of the evaporator 25 and the inlet of the compressor 26.

[0108] According to the invention, the condenser 23 of the heat pump is arranged on the first water vapor supply line 2, preferably upstream of the first intermediate steam generator 50 or the outlet fluid connection of the first intermediate steam generator 50. This arrangement makes it possible to transmit calories from the heat transfer fluid to the liquid water circulating in the first supply line 2 upstream of the first intermediate steam generator 50 and preferably upstream of the electric steam generator 28. By way of example, the water entering the condenser 23 is at a temperature of the order of ambient temperature in the atmospheric pressure embodiment such as for example illustrated in [Fig.l] and leaves said condenser 23 at a temperature of the order of 110°C. or the water entering the condenser 23 is at a temperature of the order of 70°C, advantageously in the two-phase state in the depression embodiment such as for example illustrated in [Fig.3] and leaves said condenser 23 at a temperature of the order of 75°C.

[0109] The present invention makes it possible to exploit the fatal heat of the system and more particularly the thermal discharges of the dihydrogen produced. The heat pump is an active system making it possible to reinject upstream of the first intermediate steam generator 6, and preferably upstream of the electric steam generator 28, and at a temperature higher than the evaporation temperature of the water, the calories taken from the dihydrogen produced.

[0110] According to one embodiment, the first recovery module of the system comprises a fourth intermediate heat exchanger 9 arranged on the first water vapor supply line 2 and on the second oxygen discharge line 3. The fourth intermediate heat exchanger 9 is preferably arranged on the second discharge line 3. This fourth intermediate heat exchanger 9 is configured to ensure the thermal transfer of calories taken from the flow of oxygen discharged from the electrolyser 1 and circulating in the second discharge line 3 for the benefit of the water vapor supply line 2 via the first intermediate fluid circuit and the first intermediate steam generator 50.

[0111] The fourth heat exchanger 9 is fluidically connected to the intermediate fluid circuit by a fluid connection 503 ensuring the fluid connection of the fourth intermediate exchanger 9 to the first steam generator 50 and by a fluid connection 502 ensuring the fluid connection of the first steam generator 50 to the fourth intermediate exchanger 9.

[0112] Preferably, the fluidic connection 503 is fluidically connected to the main branch 511 configured for the circulation of the intermediate fluid from the intermediate exchanger 9 to the first steam generator 50. Preferably, the fluidic connection 502 is fluidically connected to the main branch 510 configured for the circulation of the intermediate fluid to the intermediate exchanger 9.

[0113] The fourth intermediate exchanger 9 is advantageously arranged in parallel with the first intermediate exchanger 6.

[0114] According to a preferred embodiment, the third recovery module and more precisely the intermediate circuit comprises a seventh intermediate exchanger 29 arranged on the second dihydrogen discharge line 3. The seventh intermediate exchanger 29 is a heat exchanger configured to ensure the transfer of calories from the dihydrogen discharged from the electrolyser 1 to the benefit of the intermediate fluid for use in the heat pump of the third recovery module.

[0115] The seventh heat exchanger 29 is fluidically connected to the intermediate fluid circuit 32 by a fluid connection 406 ensuring the fluid connection of the seventh intermediate exchanger 29 to the evaporator 25 and by a fluid connection 407 ensuring the fluid connection of the evaporator 25 to the seventh intermediate exchanger 29.

[0116] Preferably, the fluidic connection 406 is fluidically connected to the main branch 411 configured for the circulation of the intermediate fluid 29 from the intermediate exchanger to the evaporator 25. Preferably, the fluidic connection 407 is fluidically connected to the main branch 410 configured for the circulation of the intermediate fluid 29 to the intermediate exchanger.

[0117] According to one embodiment, the second recovery module of the system comprises a twelfth intermediate heat exchanger 39 arranged on the second oxygen discharge line 3 and on the second intermediate circuit. This twelfth intermediate heat exchanger 39 is configured to ensure the thermal transfer of calories taken from the oxygen flow discharged from the electrolyser 1 and circulating in the second discharge line 3 for the benefit of the water vapour supply line 2 via the second intermediate fluid circuit and the second intermediate vapour generator 60.

[0118] The twelfth heat exchanger 39 is fluidically connected to the intermediate fluid circuit by a fluid connection 603 ensuring the fluid connection of the twelfth intermediate exchanger 39 to the second steam generator 60 and by a fluid connection 602 ensuring the fluid connection of the second steam generator 60 to the twelfth intermediate exchanger 39.

[0119] Preferably, the fluidic connection 603 is fluidically connected to the main branch 1 configured for the circulation of the intermediate fluid from the intermediate exchanger 39 to the second steam generator 60. Preferably, the fluidic connection 602 is fluidically connected to the main branch 0 configured for the circulation of the intermediate fluid to the intermediate exchanger 39.

[0120] The twelfth intermediate exchanger 39 is advantageously arranged in parallel with the third intermediate exchanger 8.

[0121] According to one embodiment, the system comprises means for processing the flow of dihydrogen produced. The dihydrogen produced by the electrolyser 1 and which comes out of the latter via the first discharge line 4 firstly has a very high temperature corresponding to the reaction temperature of the electrolyser 1. However, for its use, the dihydrogen must preferably be brought back to a temperature close to ambient temperature. Furthermore, the dihydrogen discharged from the electrolyser 1 via the first discharge line 4 may include water vapour carried along with the flow of dihydrogen. It is therefore also preferred to separate the dihydrogen from any water vapour carried along with it, by drying it.

[0122] The system according to the invention advantageously comprises for this purpose at least a first treatment stage intended for the drying and / or compression of the dihydrogen produced.

[0123] Advantageously, the first treatment stage is advantageously arranged downstream of the second intermediate exchanger 7 of the third recovery module.

[0124] According to one possibility, the first treatment stage comprises a heat exchanger. The heat exchanger is arranged on the first discharge line 4, preferably downstream of the intermediate exchanger 7. This heat exchanger is, according to a first possibility, an air cooler 16, i.e. a heat exchanger between a fluid and a gas, the gas being set in motion by a fan. According to another possibility, the heat exchanger is a standard cooler, i.e. without a fan, this solution being, however, less efficient. According to the possibility not shown in the figures, the heat exchanger ensures the heat exchange between the fluid and a gas and in particular air intended for supplying the electrolyser 1.

[0125] The first treatment stage advantageously comprises a liquid / gas separator 17 arranged downstream of the air cooler 16. The separator 17 makes it possible to separate the liquid water from the gaseous dihydrogen, the liquid water resulting from the cooling of the water vapor in the air cooler 16 below its condensation point.

[0126] According to a preferred possibility, the system comprises a second treatment stage arranged downstream of the first treatment stage on the first discharge line 4. The second treatment stage makes it possible to complete the drying of the dihydrogen. The second treatment stage advantageously comprises a heat exchanger which, as for the first stage, can be a standard cooler, an air cooler 19 or a third heat exchanger between a fluid (dihydrogen) and the air intended to supply the electrolyser 1. The second stage comprises a liquid / gas separator 20. Preferably, the system comprises, between the first treatment stage and the second treatment stage, a compressor 18 configured to allow the second treatment by the air cooler 19 by first increasing the temperature of the mixture so as to be able to cool it again.

[0127] At the end of the first treatment stage and / or the second treatment stage, if present, the liquid water is preferentially recycled by being returned to the first water vapor supply line 2 by a water recycling line 21. The water recycling line is fluidically connected to the first supply line 2, preferentially upstream of the first intermediate generator 50. The dihydrogen is used and in particular stored after conventional treatments.

[0128] The system preferably comprises a pump on the water recycling line 21. The pump is configured to set in motion the liquid water circulating in the water recycling line 21 and coming in particular from the gas / liquid separators 17, 20.

[0129] According to a preferred embodiment of the invention, the third recovery module and more specifically the intermediate circuit comprises an intermediate exchanger arranged at the level of a treatment stage, preferably at the level of each treatment stage.

[0130] The intermediate circuit of the third recovery module advantageously comprises an intermediate exchanger 12 called fifth intermediate exchanger 12 without being limiting or linked to the need to have another intermediate exchanger. The fifth intermediate exchanger 12 is preferably arranged downstream of the compressor 18 and preferably upstream of the air cooler 19.

[0131] The intermediate circuit of the third recovery module advantageously comprises an intermediate exchanger 15 called sixth intermediate exchanger 15 without being limiting or linked to the need to have another intermediate exchanger. The sixth intermediate exchanger 15 is preferably arranged downstream of the compressor 22 and preferably upstream of the air cooler 31.

[0132] If the system comprises other treatment stages downstream of the second treatment stage, the third recovery module may comprise an nth intermediate exchanger arranged at the level of this other treatment stage advantageously downstream of a compressor and upstream of an air cooler.

[0133] According to one embodiment of the invention, the intermediate exchangers of the intermediate circuit are arranged on the intermediate fluid circuit in parallel with each other as illustrated in [Fig.2]. This arrangement greatly facilitates the modularity of the system and the number of intermediate exchangers used.

[0134] The fifth intermediate exchanger 12 is fluidically connected to the main branch 410 by a fluid connection 403 and to the main branch 411 by a fluid connection 402.

[0135] The sixth intermediate exchanger 15 is fluidically connected to the main branch 410 by a fluid connection 405 and to the main branch 411 by a fluid connection 404.

[0136] According to a possibility not shown, the system comprises an intermediate exchanger arranged on a cold heat source external to the system such as by example a source of thermal discharges.

[0137] According to a preferred embodiment of the invention, the first recovery module and more specifically the intermediate fluid circuit comprises an intermediate exchanger arranged at the level of a treatment stage, preferably at the level of each treatment stage.

[0138] The first recovery module advantageously comprises an intermediate exchanger 35 called the eighth intermediate exchanger 35 without being limiting or linked to the need to have another intermediate exchanger. The eighth intermediate exchanger 35 is preferably arranged downstream of the compressor 18 and preferably upstream of the air cooler 19.

[0139] The first recovery module advantageously comprises an intermediate exchanger 37 called the tenth intermediate exchanger 37 without being limiting or linked to the need to have another intermediate exchanger. The tenth intermediate exchanger 37 is preferably arranged downstream of the compressor 22 and preferably upstream of the air cooler 31.

[0140] If the system comprises other treatment stages downstream of the second treatment stage, the third recovery module may comprise an nth intermediate exchanger arranged at the level of this other treatment stage advantageously downstream of a compressor and upstream of an air cooler.

[0141] According to one embodiment of the invention, the intermediate exchangers of the intermediate circuit are arranged on the intermediate fluid circuit in parallel with each other as illustrated in [Fig.2] for the fluid circuit 32. This arrangement greatly facilitates the modularity of the system and the number of intermediate exchangers used.

[0142] The eighth intermediate exchanger 35 is fluidically connected to the main branch 510 by a fluid connection 504 and to the main branch 511 by a fluid connection 505.

[0143] The tenth intermediate exchanger 37 is fluidically connected to the main branch 510 by a fluid connection 506 and to the main branch 511 by a fluid connection 507.

[0144] According to a preferred embodiment of the invention, the second recovery module and more specifically the intermediate fluid circuit comprises an intermediate exchanger arranged at the level of a treatment stage, preferably at the level of each treatment stage.

[0145] The second recovery module advantageously comprises an intermediate exchanger 36 called ninth intermediate exchanger 36 without being limiting or linked to the need to have another intermediate exchanger. The ninth intermediate exchanger 36 is preferably arranged downstream of the compressor 18 and preferably- initially upstream of the air cooler 19.

[0146] The second recovery module advantageously comprises an intermediate exchanger 38 called the eleventh intermediate exchanger 38 without being limiting or linked to the need to have another intermediate exchanger. The eleventh intermediate exchanger 38 is preferably arranged downstream of the compressor 22 and preferably upstream of the air cooler 31.

[0147] If the system comprises other treatment stages downstream of the second treatment stage, the third recovery module may comprise an nth intermediate exchanger arranged at the level of this other treatment stage advantageously downstream of a compressor and upstream of an air cooler.

[0148] According to one embodiment of the invention, the intermediate exchangers of the intermediate circuit are arranged on the intermediate fluid circuit in parallel with each other as illustrated in [Fig.2] for the fluid circuit 32. This arrangement greatly facilitates the modularity of the system and the number of intermediate exchangers used.

[0149] The ninth intermediate exchanger 36 is fluidically connected to the main branch 610 by a fluid connection 604 and to the main branch 611 by a fluid connection 605.

[0150] The eleventh intermediate exchanger 38 is fluidically connected to the main branch 610 by a fluid connection 606 and to the main branch 611 by a fluid connection 607.

[0151] The electrolyser 1 receives water vapour and advantageously air and discharges dihydrogen and dioxygen.

[0152] The fluid connections are preferably direct, according to one possibility additional organs can be integrated while respecting the relative positioning of the components cited below.

[0153] Preferably, the electrolyser 1 is fluidically connected to the first steam supply line 2. The first steam supply line 2 ensures the fluidic connection of components arranged upstream of the electrolyser 1 on said first supply line 2. The following description is made starting upstream of the electrolyser 1 and following the direction of circulation of the water and / or steam in the first supply line 2.

[0154] According to the embodiment illustrated in [Fig. 1], the first supply line 2 ensures the fluid connection to the inlet of the condenser 23, then the fluid connection of the outlet of the condenser 23 to the inlet of the first intermediate steam generator 50, the fluid connection of the outlet of the first intermediate steam generator 50 to the inlet of the electric steam generator 28, then the fluid connection of the outlet of the electric steam generator 28 to the inlet of the first exchange module thermal 5, preferably to the first heat exchanger 5a, then the fluid connection of the outlet of the first heat exchanger 5a to the inlet of the second heat exchanger 5b, then the fluid connection of the outlet of the second heat exchanger 5b to the inlet of the electric heater 14, then the fluid connection of the outlet of the electric heater 14 to the inlet of the electrolyser 1.

[0155] According to the embodiment illustrated in [Fig.2], the water inlet feeds two parallel branches. A first branch corresponding to the portion under depression advantageously comprising a fluid connection J ensuring the arrival of liquid water in the pressure reducer 40, then the fluid connection of the outlet of the pressure reducer 40 to the inlet of the second low-pressure intermediate steam generator 60, then the fluid connection of the outlet of the second intermediate steam generator 60 advantageously to the inlet of the condenser 23 if present, then the fluid connection of the outlet of the condenser 23 to the inlet of the electric steam generator 28, then the fluid connection of the outlet of the electric steam generator 28 to the inlet of the compressor 41.A second branch corresponding to the atmospheric pressure supply line and advantageously comprising a fluid connection O ensuring the arrival of liquid water in the first intermediate generator 50 then a fluid connection P ensuring the exit of the water vapor from the first intermediate generator 50 and advantageously the connection with the fluid connection N of the compressor 41 outlet then opening at the inlet of the heat exchange module 5. .

[0156] Preferably, the electrolyser 1 is fluidically connected to a first dihydrogen discharge line 4. The first discharge line 4 ensures the fluidic connection of components arranged downstream of the electrolyser 1 on said first discharge line 4. The following description is made starting from the electrolyser 1 and following the direction of circulation in the first discharge line 4 from the electrolyser 1.

[0157] According to the embodiment illustrated in [Fig.1], the first discharge line 4 ensures the fluidic connection of the electrolyser 1 with the inlet of the first heat exchange module 5, more preferably with the second heat exchanger 5b, then the fluidic connection of the second heat exchanger 5b to the first heat exchanger 5a, then the fluidic connection of the first heat exchanger 5a to the inlet of the first intermediate heat exchanger 6, then the fluidic connection of the outlet of the first intermediate heat exchanger 6 to the inlet of the second intermediate exchanger 7, then the fluidic connection of the outlet of the second intermediate exchanger 7 to the inlet of the air cooler 16, then the fluidic connection of the inlet of the air cooler to the inlet of the liquid / gas separator 17, then the fluidic connection of the outlet of the liquid / gas separator 17 to the inlet of the compressor 18, then advantageously the fluidic connection of the outlet of the com . presser 18 to the inlet of the fifth intermediate exchanger 12, then the fluidic connection of the fifth intermediate exchanger 12 to the air cooler 19, then the fluidic connection of the air cooler 19 to the liquid / gas separator 20, advantageously, the fluidic connection of the outlet of the liquid / gas separator 20 to the inlet of the compressor 22, then the fluidic connection of the outlet of the compressor to the inlet of a sixth heat exchanger 15, then the fluidic connection of the outlet of the sixth heat exchanger 15 to the inlet of an air cooler 31, then the fluidic connection of the outlet of the air cooler 31 to the inlet of the separator 34, then from the outlet of the separator 34 to directly or indirectly the storage of the dihydrogen.

[0158] According to the embodiment illustrated in [Fig.2], the first discharge line 4 ensures the fluidic connection of the electrolyser 1 with the inlet of the first heat exchange module 5, more preferably with the second heat exchanger 5b, then the fluidic connection of the second heat exchanger 5b to the first heat exchanger 5a, then the fluidic connection of the first heat exchanger 5a to the inlet of the first intermediate heat exchanger 6, then the fluidic connection of the outlet of the first intermediate heat exchanger 6 to the inlet of the third intermediate exchanger 8, then the fluidic connection of the outlet of the third intermediate exchanger 8 to the inlet of the second intermediate exchanger 7, then the fluidic connection of the outlet of the second intermediate exchanger 7 to the inlet of the air cooler 16, then the fluidic connection of the inlet of the air cooler to the inlet of the liquid / gas separator 17,then the fluid connection from the outlet of the liquid / gas separator 17 to the inlet of the compressor 18, then advantageously the fluid connection from the outlet of the compressor 18 to the inlet of the eighth intermediate exchanger 35, then the fluid connection from the outlet of the eighth intermediate exchanger 35 to the inlet of the ninth intermediate exchanger 36, then the fluid connection from the outlet of the ninth intermediate exchanger 36 to the inlet of the fifth intermediate exchanger 12, then the fluid connection from the fifth intermediate exchanger 12 to the air cooler 19, then the fluid connection from the air cooler 19 to the liquid / gas separator 20, advantageously, the fluid connection from the outlet of the liquid / gas separator 20 to the inlet of the compressor 22, then the fluid connection from the outlet of the compressor to the inlet of the tenth intermediate exchanger 37,then the fluid connection from the outlet of the tenth intermediate exchanger 37 to the inlet of the eleventh intermediate exchanger 38, then the fluid connection from the outlet of the eleventh intermediate exchanger 38 to the inlet of the sixth heat exchanger 15, then the fluid connection from the outlet of the sixth heat exchanger 15 to the inlet of an air cooler 31, then the fluid connection from the outlet of the air cooler 31 to the inlet of the separator 34, then from the outlet of the separator 34 to directly or indirectly the storage of the dihydrogen.

[0159] Preferably, the electrolyser 1 is fluidically connected to a second oxygen discharge line 3. The second discharge line 3 ensures the fluidic connection of components arranged downstream of the electrolyser 1 on said second discharge line 3. The following description is made starting from the electrolyser 1 and following the direction of circulation in the second discharge line 3 from the electrolyser 1.The second discharge line 3 ensures the fluidic connection of the electrolyser 1 with the second heat exchange module 11, more preferably with the second heat exchanger 11b, then the fluidic connection of the second heat exchanger 11b to the first heat exchanger 11a, then the fluidic connection of the first heat exchanger 11a to the inlet of the fourth intermediate exchanger 9, then the fluidic connection of the outlet of the fourth intermediate exchanger 9 to the inlet of the seventh intermediate exchanger 29, then a fluidic outlet connection of the seventh intermediate exchanger 29 according to the embodiment illustrated in [Fig.l] or according to the embodiment illustrated in [Fig.2], the fluid connection from the outlet of the fourth intermediate exchanger 9 to the inlet of the twelfth intermediate exchanger 39, then the fluid connection from the outlet of the second intermediate exchanger 39 to the inlet of the seventh intermediate exchanger 29, then a fluid connection from the outlet of the seventh intermediate exchanger 29.

[0160] Preferably, the electrolyser 1 is fluidically connected to the second air supply line 10. The second supply line 10 ensures the fluidic connection of components arranged upstream of the electrolyser 1 on said second supply line 10. The second supply line 10 ensures the fluidic connection of the compressor 12 to the first heat exchanger 11a, then the fluidic connection of the first heat exchanger 11a to the second heat exchanger 11b, then the fluidic connection of the second heat exchanger 11b to the electric heater 13, then the fluidic connection of the electric heater 13 to the electrolyser 1. According to a possibility not shown, upstream of the compressor 30, the second supply line ensures the fluidic connection of a heat exchanger replacing the air cooler 16 and / or 19 to the compressor 30.

[0161] The intermediate circuit as illustrated in [Fig.2] comprises an intermediate fluid circuit 32 ensuring the fluid connection of the intermediate exchanger(s) 7, 12, 15, 29, and the heat pump, more precisely the evaporator 28. According to the embodiment in which there are several intermediate exchangers 7, 12, 15, 29, they are arranged in parallel with each other. The intermediate fluid circuit 32 advantageously comprises a pump 33 intended to circulate the intermediate fluid in the intermediate fluid circuit 32.

[0162] The system advantageously comprises fluid connections described below

[0163] Concerning the first supply line 2, according to the embodiment illustrated in [Fig.l], it advantageously comprises a fluid connection A connected to the inlet of the condenser 23. The fluid connection A makes it possible to introduce into the condenser 23, water in particular which may come from the recycling water circulating in the recycling line 21.

[0164] Advantageously, the first supply line 2 comprises a fluid connection B connected between the outlet of the condenser 23 and the inlet of the first intermediate steam generator 50.

[0165] Advantageously, the first supply line 2 comprises a fluid connection C connected between the outlet of the first intermediate steam generator 50 to the inlet of the electric steam generator 28.

[0166] Advantageously, the first supply line 2 comprises a fluid connection D connected between the output of the electric steam generator 28 and the inlet of the first heat exchanger 5a of the heat exchange module 5.

[0167] Advantageously, the first supply line 2 comprises a fluid connection E connected between the outlet of the first heat exchanger 5a of the heat exchange module 5 and the inlet of the first heat exchanger 5a of the heat exchange module 5 allowing recirculation of the water from the electro ten hours is carried away with the hydrogen fluid.

[0168] Advantageously, the first supply line 2 comprises a fluid connection F connected between the outlet of the first heat exchanger 5a and the inlet of the second heat exchanger 5b.

[0169] Advantageously, the first supply line 2 comprises a fluid connection G connected between the outlet of the second heat exchanger 5b and the inlet of the heater 14.

[0170] Advantageously, the first supply line 2 comprises a fluid connection H connected between the outlet of the electric heater 14 and the inlet of the electrolyser 1.

[0171] Concerning the first supply line 2, according to the embodiment illustrated in [Fig.l], it advantageously comprises a fluid connection I bringing water to the supply line 2. The fluid connection I makes it possible to supply two parallel branches with water, including the section under depression and the branch comprising the first intermediate steam generator 50.

[0172] Advantageously, the first supply line 2 comprises a fluid connection I ensuring the fluid connection J between the fluid connection I and the inlet of the second intermediate steam generator 60. The fluid connection J comprises the pressure reducer 40.

[0173] Advantageously, the first supply line 2 comprises a fluid connection K ensuring the fluid connection between the output of the second generator of steam 60 and condenser inlet 23.

[0174] Advantageously, the first supply line 2 comprises a fluid connection L ensuring the connection between the outlet of the condenser 23 and the inlet of the electric generator 28.

[0175] Advantageously, the first supply line 2 comprises a fluid connection M ensuring the fluid connection between the output of the electric generator 28 and the inlet of the compressor 41.

[0176] Advantageously, the first supply line 2 comprises a fluid connection N ensuring the fluid connection between the outlet of the compressor 22 and the inlet of the first heat exchanger 5a.

[0177] Advantageously, the first supply line 2 comprises a fluid connection O ensuring the fluid connection between the fluid connection I and the inlet of the first intermediate steam generator 50.

[0178] Advantageously, the first supply line 2 comprises a fluid connection P ensuring the fluid connection between the outlet of the first intermediate steam generator 50 and the fluid connection N.

[0179] Advantageously, the first supply line 2 comprises a fluid connection F connected between the outlet of the first heat exchanger 5a and the inlet of the second heat exchanger 5b.

[0180] Advantageously, the first supply line 2 comprises a fluid connection G connected between the outlet of the second heat exchanger 5b and the inlet of the heater 14.

[0181] Advantageously, the first supply line 2 comprises a fluid connection H connected between the outlet of the electric heater 14 and the inlet of the electrolyser 1.*

[0182] Concerning the first evacuation line 4, it advantageously comprises a first fluid connection 300 between the outlet of the electrolyser 1 and the inlet of the second heat exchanger 5b of the first heat exchange module 5.

[0183] Advantageously, the first evacuation line 4 comprises a fluid connection 301 between the outlet of the second heat exchanger 5b of the first heat exchange module 5 and the inlet of the first heat exchanger 5a of the first heat exchange module 5.

[0184] Advantageously, the first discharge line 4 comprises a fluid connection 302 between the outlet of the first heat exchanger 5a and the inlet of the steam generator 6.

[0185] According to the embodiment illustrated in [Fig.l]:

[0186] Advantageously, the first evacuation line 4 comprises a fluid connection 303 between the outlet of the steam generator 6 and the inlet into the first intermediate exchanger 7.

[0187] Advantageously, the first evacuation line 4 comprises a fluid connection 304 between the outlet of the second intermediate exchanger 7 and the inlet of the first air cooler 16.

[0188] Advantageously, the first evacuation line 4 comprises a fluid connection 305 between the first air cooler outlet 16 and the inlet of the separator 17.

[0189] Advantageously, the first discharge line 4 comprises a fluid connection 306 between the outlet of the separator 17 and the inlet of the compressor 18.

[0190] Advantageously, the first discharge line 4 comprises a fluid connection 307 between the outlet of the compressor 18 and the inlet of the second intermediate exchanger 12.

[0191] Advantageously, the first evacuation line 4 comprises a fluid connection 308 between the outlet of the second intermediate exchanger 12 and the inlet of the air cooler 19.

[0192] Advantageously, the first evacuation line 4 comprises a fluid connection 309 between the outlet of the air cooler 19 and the inlet of the separator 20.

[0193] Advantageously, the first discharge line 4 comprises a fluid connection 310 between the outlet of the separator 20 and the inlet of the compressor 30.

[0194] Advantageously, the first discharge line 4 comprises a fluid connection 311 between the outlet of the compressor 30 and the inlet of the sixth intermediate exchanger 15.

[0195] Advantageously, the first evacuation line 4 comprises a fluid connection 312 between the outlet of the sixth intermediate exchanger 15 and the inlet of the air cooler 31.

[0196] Advantageously, the first evacuation line 4 comprises a fluid connection 313 between the outlet of the air cooler 31 and the inlet of the separator 34.

[0197] Advantageously, the first evacuation line 4 comprises a fluid connection 314 ensuring the exit of the dihydrogen from the separator 34.

[0198] According to an embodiment illustrated in [Fig.2]:

[0199] advantageously, the first evacuation line 4 comprises a fluid connection 315 between the outlet of the first intermediate exchanger 6 and the inlet of the third intermediate exchanger 8;

[0200] Advantageously, the first evacuation line 4 comprises a fluid connection 316 between the outlet of the third intermediate exchanger 8 and the inlet of the second intermediate exchanger 7.

[0201] Advantageously, the first evacuation line 4 comprises a fluid connection 304 between the outlet of the second intermediate exchanger 7 and the inlet of the first air cooler 16.

[0202] Advantageously, the first evacuation line 4 comprises a fluid connection 305 between the first air cooler outlet 16 and the inlet of the separator 17.

[0203] Advantageously, the first discharge line 4 comprises a fluid connection 306 between the outlet of the separator 17 and the inlet of the compressor 18.

[0204] Advantageously, the first discharge line 4 comprises a fluid connection 317 between the outlet of the compressor 18 and the inlet of the eighth intermediate exchanger 35.

[0205] Advantageously, the first evacuation line 4 comprises a fluid connection 318 between the outlet of the eighth intermediate exchanger 35 and the inlet of the ninth intermediate exchanger 36.

[0206] Advantageously, the first evacuation line 4 comprises a fluid connection 319 between the outlet of the ninth intermediate exchanger 36 and the inlet of the fifth intermediate exchanger 12.

[0207] Advantageously, the first evacuation line 4 comprises a fluid connection 308 between the outlet of the second intermediate exchanger 12 and the inlet of the air cooler 19.

[0208] Advantageously, the first evacuation line 4 comprises a fluid connection 309 between the outlet of the air cooler 19 and the inlet of the separator 20.

[0209] Advantageously, the first discharge line 4 comprises a fluid connection 310 between the outlet of the separator 20 and the inlet of the compressor 30.

[0210] Advantageously, the first discharge line 4 comprises a fluid connection 320 between the outlet of the compressor 22 and the inlet of the tenth intermediate exchanger 37.

[0211] Advantageously, the first evacuation line 4 comprises a fluid connection 321 between the outlet of the tenth intermediate exchanger 37 and the inlet of the eleventh intermediate exchanger 38.

[0212] Advantageously, the first evacuation line 4 comprises a fluid connection 322 between the outlet of the eleventh intermediate exchanger 38 and the inlet of the sixth intermediate exchanger 15.

[0213] Advantageously, the first evacuation line 4 comprises a fluid connection 312 between the outlet of the sixth intermediate exchanger 15 and the inlet of the air cooler 31.

[0214] Advantageously, the first evacuation line 4 comprises a fluid connection 313 between the outlet of the air cooler 31 and the inlet of the separator 34.

[0215] Advantageously, the first evacuation line 4 comprises a fluid connection 314 ensuring the exit of the dihydrogen from the separator 34.

[0216] Concerning the second oxygen evacuation line 3, it advantageously comprises a fluid connection 100 between the outlet of the electrolyser 1 and the inlet of the second heat exchanger 11 b of the second heat exchange module 11.

[0217] Advantageously, the second evacuation line 3 comprises a fluid connection 101 between the outlet of the second heat exchanger 11 b and the inlet of the first heat exchanger 11 a of the second heat exchange module 11.

[0218] Advantageously, the second evacuation line 3 comprises a fluid connection 102 between the outlet of the first heat exchanger 11a and the inlet of the heat exchanger 9.

[0219] According to the embodiment illustrated in [Fig.l], advantageously, the second discharge line 3 comprises a fluid connection 103 between the outlet of the heat exchanger 9 and the inlet of the seventh intermediate exchanger 29. Advantageously, the second discharge line 3 comprises a fluid connection 104 between the outlet of the seventh intermediate exchanger 29 and the outside.

[0220] According to the embodiment illustrated in [Fig.2], advantageously, the second discharge line 3 comprises a fluid connection 105 between the outlet of the heat exchanger 9 and the inlet of the twelfth intermediate exchanger 39. Advantageously, the second discharge line 3 comprises a fluid connection 106 between the outlet of the twelfth intermediate exchanger 39 and the inlet of the seventh intermediate exchanger 29. Advantageously, the second discharge line 3 comprises a fluid connection 104 between the outlet of the seventh intermediate exchanger 29 and the outside.

[0221] Concerning the second air supply line 4, it comprises, according to a possibility not shown, a fluid connection 110 between the outlet of a heat exchanger replacing the air cooler 16 and the inlet of the compressor 30.

[0222] Advantageously, the second supply line 4 comprises a fluid connection 111 between the outlet of the compressor 30 and the inlet of the first heat exchanger 11a of the second heat exchange module 11.

[0223] Advantageously, the second supply line 4 comprises a fluid connection 112 between the outlet of the first heat exchanger 11a and the inlet of the second heat exchanger 11b of the second heat exchange module 11.

[0224] Advantageously, the second supply line 4 comprises a fluid connection 113 between the outlet of the second heat exchanger 11 b and the inlet of the electric heater 13.

[0225] Advantageously, the second supply line 4 comprises a fluid connection 114 between the outlet of the electric heater 13 and the inlet of the electrolyser 1.

[0226] In operation, according to the first embodiment illustrated in [Fig.l], the liquid water arrives in the first water vapor supply line 2, more precisely in the first portion via the fluid connection A. The fluid connection A is advantageously connected to the inlet of the condenser 23. The liquid water enters the condenser 23. The temperature of the water increases by transferring the calories from the heat transfer fluid of the heat pump to the liquid water. In the condenser 23, the heat transfer fluid transmits its calories to the water which ensures the condensation of the heat transfer fluid in the condenser 23. The heated liquid water leaves the condenser 23 via the fluid connection B at a temperature advantageously close to the evaporation temperature, i.e. at + / -5 °C and, preferably, enters directly into the first intermediate steam generator 50. The liquid water is transformed into steam by the intermediate steam generator 50 which recovers the thermal energy from the dihydrogen produced by the electrolyser 1 at least by the first intermediate exchanger 6.Depending on the energy transmitted to the first intermediate generator 50, the water leaves it and preferentially enters directly through the fluid connection C into the electric steam generator 28.

[0227] The liquid water introduced through connection A may be water from a water network or recycled water from the system's separators or a mixture of the two.

[0228] According to the invention, the energy to be supplied by the electric steam generator 28 for the transformation of liquid water into water vapor is reduced thanks to the first thermal energy recovery module and advantageously to the third thermal energy recovery module, in particular to the condenser 23 of the heat pump.

[0229] The water vapor leaves the electric steam generator 28 via the fluid connection D and enters, preferably directly, the first heat exchange module 5, preferably the first heat exchanger 5a. The water vapor is heated in the first heat exchanger 5a by recovering the calories from the hydrogen circulating in the first heat exchanger 5a. The superheated water vapor leaves the first heat exchanger 5a via the fluid connection F and enters, preferably directly, the second heat exchanger 5b. The water vapor is heated again in the second heat exchanger 5b by recovering the calories from the hydrogen circulating in the second heat exchanger 5b. The superheated water vapor leaves the second heat exchanger 5b via the fluid connection G and enters, preferably directly, the electric heater 14, if necessary.The electric heater 14 provides the final temperature rise that may be necessary for the water vapor to reach a predefined target temperature to enter the electrolyzer 1. The water vapor leaves the electric heater 14 via the fluid connection H and enters, preferably directly, the electrolyzer 1.

[0230] In operation, according to the second embodiment illustrated in [Fig.2], the liquid water arrives in the first water vapor supply line 2, more precisely in the first portion through the fluid connection. Liquid water arrives through the fluid connection I and feeds the two branches of the first supply line 2.

[0231] The water circulating in the fluid connection I enters, preferably directly, into the fluid connection J and therefore into the expansion valve 40. The liquid water is put under vacuum at the outlet of the expansion valve 40. The liquid under vacuum enters via the fluid connection J into the second intermediate steam generator 60. In the second intermediate steam generator 60, the water under vacuum is heated thanks to the supply of calories recovered on the first dihydrogen evacuation line 3 and in particular by the third intermediate exchanger 8, possibly the ninth intermediate exchanger 36, the eleventh intermediate exchanger 38, the twelfth intermediate exchanger 39. The superheated liquid water leaves the second intermediate steam generator 60 via the fluid connection K and enters, preferably directly, into the condenser 23.In the condenser 23, the superheated liquid water in depression is heated by the condenser 23 of the heat pump. The superheated liquid water leaves the condenser 23 via the fluid connection L and preferably enters directly into the electric steam generator 28. If the electric steam generator 28 is in operation, because the heated liquid water requires an additional heat supply, the water leaves the electric steam generator 28 via the fluid connection M and enters, preferably directly, into the compressor 4L. The compressor 41 makes it possible to raise the pressure of the water circulating in the section in depression to 1 atmospheric pressure. The water vapor at atmospheric pressure leaves the compressor 41 via the fluid connection N and preferably enters directly into the 1st heat exchanger 5a of the first heat exchange module 5. .

[0232] At the level of the other branch, the water circulating in the fluid connection I enters, preferably directly, into the fluid connection O and enters, preferably directly into the first intermediate steam generator 50. In the first intermediate steam generator 50, the water is heated at atmospheric pressure by the calories recovered on the first dihydrogen evacuation line 3 and in particular by the first intermediate exchanger 6, and possibly by the eighth intermediate exchanger 35, the tenth intermediate exchanger 37, the fourth intermediate exchanger 9. The water is advantageously transformed into steam in the first intermediate steam generator 50 and leaves it via the fluid connection P entering preferably directly into the fluid connection N.

[0233] The water vapor is heated in the first heat exchanger 5a by recovering the calories from the dihydrogen circulating in the first heat exchanger 5a. The superheated water vapor leaves the first heat exchanger 5a via the fluid connection F and enters, preferably directly, the second heat exchanger 5b. The water vapor is heated again in the second heat exchanger 5b by recovering the calories from the dihydrogen circulating in the second heat exchanger 5b. The superheated water vapor leaves the second heat exchanger 5b via the fluid connection G and enters, preferably directly, the electric heater 14, if necessary. The electric heater 14 provides the final temperature rise that may be necessary for the water vapor to reach a predefined target temperature to enter the electrolyser 1. The water vapor leaves the electric heater 14 via the fluid connection H and enters, preferably directly, the electrolyser 1.

[0234] One or more pumps may be placed on the various fluid connections to set the liquid water in motion and advantageously ensure pressurization of the first supply line 2.

[0235] The electrolyser 1 is supplied with electric current at a predefined voltage and intensity to ensure electrolysis and therefore the production of dihydrogen and dioxygen.

[0236] The dihydrogen leaves the electrolyser 1 via the first discharge line, via the fluid connection 300 and enters, preferably directly, the first heat exchange module 5, preferably the second heat exchanger 5b. The dihydrogen leaves the electrolyser in the hot gaseous state; it is necessary to lower its temperature in order to use and / or store it. The calories from the dihydrogen are therefore recovered via the first supply line and more precisely the steam circulating therein. In the second heat exchanger 5b, the dihydrogen sees its temperature lowered by transfer of calories to the benefit of the water vapor circulating in the second heat exchanger 5b. The cooled dihydrogen leaves the second heat exchanger 5b via the fluid connection 301 and enters, preferably directly, the first heat exchanger 5a.In the first heat exchanger 5a, the dihydrogen sees its temperature lowered again by transfer of calories to the benefit of the water vapor circulating in the first heat exchanger 5a. The cooled dihydrogen leaves the first heat exchanger 5a via the fluid connection 302 and enters, preferably directly, the first intermediate exchanger 6. By passing through the first intermediate exchanger 6, the dihydrogen is cooled, because it gives up calories to the intermediate fluid circulating in the first intermediate fluid circuit.

[0237] According to the first embodiment illustrated in [Fig. 1], the dihydrogen leaves the first intermediate exchanger 6 via the fluid connection 303 and enters, preferably directly, the second intermediate exchanger 7. In this second intermediate exchanger 7, the dihydrogen is cooled, because it gives up calories to the intermediate fluid circulating in the intermediate fluid circuit 32. The dihydrogen leaves the second intermediate exchanger 7 via the fluid connection 304 and enters, preferably directly, the first air cooler 16. The dihydrogen leaves the first air cooler 16 via the fluid connection 305 and enters, preferably directly, the liquid / gas separator 17 ensuring the condensation of the dihydrogen. The dihydrogen leaves the liquid / gas separator 17 via the fluid connection 306 and undergoes, if necessary, a new compression with a view to a new condensation. In this case, the dihydrogen leaves the liquid / gas separator 17 via the fluid connection 306 and enters, preferably directly, the compressor 18 from where it leaves via the fluid connection 307 and enters, preferably directly, the fifth intermediate exchanger 12.By passing through the fifth intermediate exchanger 12, the dihydrogen is cooled, because it gives up calories to the intermediate fluid circulating in the intermediate fluid circuit 32. The dihydrogen leaves the fifth intermediate exchanger 12 via the fluid connection 308 and enters, preferably directly, the second air cooler 19 ensuring the cooling of the dihydrogen. The dihydrogen leaves the air cooler 19 via the fluid connection 309 and enters, preferably directly, the liquid / gas separator 20 ensuring the condensation of the dihydrogen. The condensed dihydrogen leaves the liquid / gas separator 20 via the fluid connection 310 and undergoes, if necessary, a new compression with a view to a new condensation.In this case, the dihydrogen leaves the liquid / gas separator 20 via the fluid connection 310 and enters, preferably directly, the compressor 30 from where it leaves via the fluid connection 311 and enters, preferably directly, the sixth intermediate exchanger 15. By passing through the sixth intermediate exchanger 15, the dihydrogen is cooled, because it gives up calories to the intermediate fluid circulating in the intermediate fluid circuit 32. The dihydrogen leaves the sixth intermediate exchanger 15 via the fluid connection 312 and enters, preferably directly, the second air cooler 31 ensuring the cooling of the dihydrogen. The dihydrogen leaves the air cooler 31 via the fluid connection 313 and enters, preferably directly, the liquid / gas separator 34 ensuring the condensation of the dihydrogen.The condensed dihydrogen exits the liquid / gas separator 34 through the fluid connection 314 and can be used or stored. The condensed liquid water recovered from the liquid / gas separator 17, 20, 34 can be recycled into the first water vapor supply line 2 by fluid connection with the water recycling line 21.

[0238] According to the second embodiment illustrated in [Fig.2], the dihydrogen leaves the first intermediate exchanger 6 via the fluid connection 315 and preferably enters directly into the third intermediate exchanger 316. The dihydrogen leaves the third intermediate exchanger 316 and enters, preferably directly, into the second intermediate exchanger?. The dihydrogen leaves the second intermediate exchanger 7 via the fluid connection 304 and preferably enters directly into the air cooler 16. The dihydrogen leaves the first air cooler 16 via the fluid connection 305 and enters, preferably directly, into the liquid / gas separator 17 ensuring the condensation of the dihydrogen. The dihydrogen leaves the liquid / gas separator 17 via the fluid connection 306 and undergoes, if necessary, a new compression for a new condensation.In this case, the dihydrogen leaves the liquid / gas separator 17 via the fluid connection 306 and enters, preferably directly, the compressor 18 from where it leaves via the fluid connection 317 and enters, preferably directly, the eighth intermediate exchanger 35. The dihydrogen leaves the eighth intermediate exchanger 35 via the fluid connection 318 and enters, preferably directly, the ninth intermediate exchanger 36. The dihydrogen leaves the ninth intermediate exchanger 36 via the fluid connection 319 and enters, preferably directly, the fifth intermediate exchanger 12. By passing through the fifth intermediate exchanger 12, the dihydrogen is cooled, because it gives up calories to the intermediate fluid circulating in the intermediate fluid circuit 32.The dihydrogen leaves the fifth intermediate exchanger 12 via the fluid connection 308 and enters, preferably directly, the second air cooler 19 ensuring the cooling of the dihydrogen. The dihydrogen leaves the air cooler 19 via the fluid connection 309 and enters, preferably directly, the liquid / gas separator 20 ensuring the condensation of the dihydrogen. The condensed dihydrogen leaves the liquid / gas separator 20 via the fluid connection 310 and undergoes, if necessary, a new compression with a view to a new condensation. In this case, the dihydrogen leaves the liquid / gas separator 20 via the fluid connection 310 and enters, preferably directly, the compressor 30 from where it leaves via the fluid connection 320. By passing through the fifth intermediate exchanger 12, the dihydrogen is cooled, because it gives up calories to the intermediate fluid circulating in the intermediate fluid circuit 32.The dihydrogen leaves the fifth intermediate exchanger 12 via the fluid connection 308 and enters, preferably directly, the second air cooler 19 ensuring the cooling of the dihydrogen. The dihydrogen leaves the air cooler 19 via the fluid connection 309 and enters, preferably directly, the liquid / gas separator 20 ensuring the condensation of the dihydrogen. The condensed dihydrogen leaves the liquid / gas separator 20 via the fluid connection 310 and undergoes, if necessary, a new compression for a . new condensation. In this case, the dihydrogen leaves the liquid / gas separator 20 via the fluid connection 310 and enters, preferably directly, the compressor 30 from where it leaves via the fluid connection 320. The dihydrogen preferably enters directly the tenth intermediate exchanger 37. The dihydrogen leaves the tenth intermediate exchanger 37 via the fluid connection 321 and enters, preferably directly, the eleventh intermediate exchanger 38. The dihydrogen leaves the eleventh intermediate exchanger 38 via the fluid connection 322 and enters directly the sixth intermediate exchanger 15. The dihydrogen leaves the sixth intermediate exchanger 15 via the fluid connection 312 and enters, preferably directly, the second air cooler 31 ensuring the cooling of the dihydrogen.The dihydrogen leaves the air cooler 31 through the fluid connection 313 and enters, preferably directly, the liquid / gas separator 34 ensuring the condensation of the dihydrogen. The condensed dihydrogen leaves the liquid / gas separator 34 through the fluid connection 314 and can be used or stored.

[0239] The oxygen produced by the electrolyser leaves via the second discharge line 3, via the fluid connection 100 and enters, preferably directly, the second heat exchange module 11, preferably the second heat exchanger 11b. The oxygen leaves the electrolyser in the hot gaseous state; it is necessary to lower its temperature for discharge into the air. The calories from the oxygen are therefore advantageously recovered via the second supply line 10 and more precisely the air circulating therein. In the second heat exchanger 11b, the oxygen sees its temperature lowered by transfer of calories to the benefit of the air circulating in the second heat exchanger 11b. The cooled oxygen leaves the second heat exchanger 11b via the fluid connection 101 and enters, preferably directly, the first heat exchanger 11a.In the first heat exchanger 11a, the oxygen again sees its temperature lowered by transfer of calories to the benefit of the air circulating in the first heat exchanger 11a. The cooled oxygen leaves the first heat exchanger 11a via the fluid connection 102 and advantageously enters, preferably directly, the fourth intermediate exchanger 9 of the recovery module. Passing through the fourth intermediate exchanger 9, the oxygen again sees its temperature lowered by transfer of calories to the benefit of the liquid water circulating in the intermediate exchanger 9.

[0240] According to a first embodiment illustrated in [Fig. 1], the air leaves the intermediate exchanger 9 via the fluid connection 103 and enters, preferably directly, a fourth intermediate exchanger 29. In the seventh intermediate exchanger 29, the dihydrogen is cooled, because it gives off calories to the intermediate fluid. circulating in the intermediate fluid circuit 32. The dihydrogen leaves the seventh intermediate exchanger 29 via the fluid connection 104 and is released into the air.

[0241] According to a second embodiment illustrated in [Fig.2], the air leaves the fourth intermediate exchanger 9 via the fluid connection 105 and preferably enters directly into the twelfth intermediate exchanger 39. The air leaves the second intermediate exchanger 39 via the fluid connection 106 and preferably enters directly into the seventh intermediate exchanger 29. The dihydrogen leaves the seventh intermediate exchanger 29 via the fluid connection 104 and is released into the air.

[0242] According to one possibility, air is supplied to the electrolyser 1. The air arrives via the second supply line 10. Advantageously, the air passes through the second heat exchanger replacing the air cooler 16 and recovers calories from the dihydrogen circulating in the heat exchanger. This first heat exchange ensures a first heating of the air. The air leaves the heat exchanger via the fluid connection 110 and enters, preferably directly, the compressor 30. According to the illustrated possibility, the air is compressed by the compressor 30 and its temperature increases. The air enters the compressor 30 via the fluid connection 110. The air leaves the compressor 30 via the fluid connection 111 and enters, preferably directly, the second heat exchange module 11, preferably the first heat exchanger 11a.The air is heated in the first heat exchanger 11a by recovering the calories from the oxygen circulating in the first heat exchanger 11a. The superheated air leaves the first heat exchanger 11a through the fluid connection 112 and enters, preferably directly, the second heat exchanger 11b. The air is heated again in the second heat exchanger 11b by recovering the calories from the oxygen circulating in the second heat exchanger 11b. The superheated air leaves the second heat exchanger 11b through the fluid connection 113 and enters, preferably directly, the electric heater 13 if necessary. The electric heater 13 provides the final temperature rise that may be necessary for the air to reach a predefined target temperature for entering the electrolyser 1. The air leaves the electric heater 13 through the fluid connection 114 and enters, preferably directly, the electrolyser 1.

[0243] List of References

[0244] 1 Electrolyzer

[0245] 2 Water vapor supply line

[0246] 3 Oxygen evacuation line

[0247] 4 Hydrogen evacuation line

[0248] 5a First heat exchanger of the first heat exchange module

[0249] 5b Second heat exchanger of the first heat exchange module

[0250] 6 First Intermediate Exchanger

[0251] 7 Second intermediate exchanger

[0252] 8. Third Intermediate Exchanger

[0253] 9 Fourth Intermediate Exchanger

[0254] 10 Air supply line

[0255] 1 the First heat exchanger of the second heat exchange module

[0256] 11b Second heat exchanger of the second heat exchange module

[0257] 12 Fifth intermediate exchanger

[0258] 13 Electric heater

[0259] 14 Electric heater

[0260] 15 Sixth intermediate interchange

[0261] 16 Air cooler

[0262] 17 Liquid / Gas Separator

[0263] 18 Compressor

[0264] 19 Air cooler

[0265] 20 Liquid / Gas Separator

[0266] 21 Water recycling line

[0267] 22 Compressor

[0268] 23 Condenser

[0269] 24 Regulator

[0270] 25. Evaporator

[0271] 26. Compressor

[0272] 27 Fluid circuit

[0273] 28. Electric steam generator

[0274] 29. seventh heat exchanger

[0275] 30. Compressor

[0276] 31. Air cooler

[0277] 32. third Intermediate fluid circuit

[0278] 33. Pump

[0279] 34. Separator

[0280] 35. Eighth Intermediate Interchange

[0281] 36. Ninth Intermediate Exchanger

[0282] 37. Tenth Intermediate Exchange

[0283] 38. Eleventh Intermediate Exchange

[0284] 39. Twelfth Intermediate Exchange

[0285] 40. Regulator

[0286] 4L Compressor

[0287] 50. First low pressure steam generator

[0288] 60. Second low temperature steam generator

[0289] A Fluid connection entering the condenser 23

[0290] B Fluid connection between the condenser 23 and the first intermediate generator 50

[0291] C Fluid connection between the first intermediate generator 50 and the electric steam generator 28

[0292] D Fluid connection between the electric steam generator 28 and the first heat exchanger 5 a

[0293] E Fluid connection between the first heat exchanger 5a and the fluid connection D.

[0294] F Fluid connection between the first heat exchanger 5a and the second heat exchanger 5b

[0295] G Fluid connection between the second heat exchanger 5 b and the heater 14.

[0296] H. Fluid connection between the heater 14 and the electrolyser 1

[0297] I. Fluid connection entering the steam supply line 1

[0298] J. Fluid connection between fluid connection I and the second inter generator intermediate 60 preferably comprising the regulator 40.

[0299] K. Fluid connection between the second intermediate generator 60 and the condenser 23

[0300] L. Fluid connection between the condenser 23 and the electric generator 28

[0301] M. Fluid connection between the electric generator 28 and compressor 41

[0302] N. Fluid connection between compressor 41 and the first exchanger 5a of the first heat exchange module 5

[0303] O. Fluid connection between the fluid connection I and the first intermediate generator 50

[0304] P. Fluid connection between the first intermediate generator 50 and the fluid connection N

[0305] 100 Fluid connection between the electrolyser 1 and the second heat exchanger 11b

[0306] 101 Fluid connection between the second heat exchanger 11 b and the first heat exchanger lia

[0307] 102 Fluid connection between the first heat exchanger 1 la and the exchanger in intermediate 9

[0308] 103. Fluid connection between the intermediate exchanger 9 and the inter exchanger median 29

[0309] 104. Heat exchanger outlet fluid connection 29

[0310] 105. Fluid connection between the intermediate exchanger 9 and the inter exchanger median 39

[0311] 106. Fluid connection between the intermediate exchanger 29 and the inter exchanger median 39

[0312] 110 Inlet fluid connection in the compressor 30

[0313] 111 Fluid connection between the compressor 30 and the first heat exchanger lia

[0314] 112 Fluid connection between the first heat exchanger 11a and the second heat exchanger 11b

[0315] 113 Fluid connection between the second heat exchanger 11 b and the re driver 13

[0316] 114 Fluid connection between heater 13 and electrolyser 1

[0317] 200 Fluid connection between the compressor 26 and the condenser 23

[0318] 201 Fluid connection between the condenser 23 and the expansion valve 24

[0319] 202 Fluid connection between the expansion valve 24 and the evaporator 25

[0320] 203 Fluid connection between the evaporator 25 and the compressor 26

[0321] 300. Fluid connection between the electrolyser 1 and the second heat exchanger 5b

[0322] 301. Fluid connection between the second heat exchanger 5 b and the first 5 a heat exchanger

[0323] 302. Fluid connection between the first heat exchanger 5a and the first intermediate exchanger 6

[0324] 303. Fluid connection between the first intermediate exchanger 6 and the second intermediate heat exchanger 7

[0325] 304. Fluid connection between the second intermediate heat exchanger 7 and the air cooler 16

[0326] 305. Fluid connection between the air cooler 16 and the liquid / gas separator 17

[0327] 306. Fluid connection between the liquid / gas separator 17 and the compressor 18

[0328] 307. Fluid connection between the compressor 18 and the fifth inter exchanger median 12

[0329] 308. Fluid connection between the fifth intermediate exchanger 12 and the air cooler 19

[0330] 309. Fluid connection between the air cooler 19 and the liquid / gas separator 20

[0331] 310. Fluid connection between the liquid / gas separator 20 and the compressor 22

[0332] 311. Fluid connection between the compressor 22 and the sixth inter exchanger median 15

[0333] 312. Fluid connection between the sixth intermediate exchanger 15 and the air cooler 31

[0334] 313. Fluid connection between the air cooler 31 and the liquid / gas separator 34

[0335] 314. Fluid connection for the outlet of dihydrogen from the liquid / gas separator 34

[0336] 315. Fluid connection between the first intermediate exchanger 6 and the third intermediate heat exchanger 8

[0337] 316. Fluid connection between the third intermediate heat exchanger 8 and the second intermediate heat exchanger 7

[0338] 317. Fluid connection between the compressor 18 and the eighth inter exchanger median 35

[0339] 318. Fluid connection between the eighth intermediate exchanger 35 and the ninth intermediate interchange 36

[0340] 319. Fluid connection between the ninth intermediate exchanger 36 and the fifth intermediate interchange 12

[0341] 320. Fluid connection between the compressor 22 and the tenth inter exchanger median 37

[0342] 321. Fluid connection between the tenth intermediate exchanger 37 and the eleventh intermediate exchanger 38

[0343] 322. Fluid connection between the eleventh intermediate exchanger 38 and the sixth intermediate exchanger 15

[0344] 400. Fluid connection between the outlet of the second intermediate exchanger 7 and the evaporator 25

[0345] 401. Fluid connection between the evaporator 25 and the inlet of the second exchanger intermediate 7

[0346] 402. Fluid connection between the outlet of the fifth intermediate exchanger 12 and the evaporator 25

[0347] 403. Fluid connection between the evaporator 25 and the inlet of the fifth exchanger intermediate 12

[0348] 404. Fluid connection between the outlet of the sixth intermediate exchanger 15 and the evaporator 25

[0349] 405. Fluid connection between the evaporator 25 and the inlet of the sixth exchanger in intermediate 15

[0350] 406. Fluid connection between the outlet of the seventh intermediate exchanger 29 and the evaporator 25

[0351] 407. Fluid connection between the evaporator 25 and the inlet of the seventh exchanger in intermediate 29

[0352] 410. Main branch of the evaporator 25 towards the intermediate exchanger

[0353] 411. Main branch of the intermediate exchanger to the evaporator 25

[0354] 500. Fluid connection between the outlet of the first intermediate exchanger 6 and the first intermediate generator 50

[0355] 501. Fluid connection between the first intermediate generator 50 and the inlet of the first intermediate interchange 6

[0356] 502. Fluid connection between the outlet of the fourth intermediate exchanger 9 and the first intermediate generator 50

[0357] 503. Fluid connection between the first intermediate generator 50 and the inlet of the fourth intermediate interchange 9

[0358] 504. Fluid connection between the outlet of the eighth intermediate exchanger 35 and the first intermediate generator 50

[0359] 505. Fluid connection between the first intermediate generator 50 and the inlet of the eighth intermediate interchange 35

[0360] 506. Fluid connection between the outlet of the tenth intermediate exchanger 37 and the first intermediate generator 50

[0361] 507. Fluid connection between the first intermediate generator 50 and the inlet of the tenth intermediate interchange 37

[0362] 510. Main branch of the first intermediate generator 50 towards the exchanger in intermediate

[0363] 511. Main branch from the intermediate exchanger to the first generator in intermediate 50

[0364] 600. Fluid connection between the outlet of the third intermediate exchanger 8 and the second intermediate generator 60

[0365] 601. Fluid connection between the second intermediate generator 60 and the inlet of the third intermediate interchange 8

[0366] 602. Fluid connection between the outlet of the twelfth intermediate exchanger 39 and the second intermediate generator 60

[0367] 603. Fluid connection between the second intermediate generator 60 and the inlet of the twelfth intermediate interchange 39

[0368] 604. Fluid connection between the outlet of the ninth intermediate exchanger 36 and the second intermediate generator 60

[0369] 605. Fluid connection between the second intermediate generator 60 and the inlet of the ninth intermediate interchange 36

[0370] 606. Fluid connection between the outlet of the eleventh intermediate exchanger 38 and the second intermediate generator 60

[0371] 607. Fluid connection between the second intermediate generator 60 and the inlet of the eleventh intermediate interchange 38

[0372] 610. Main branch of the second intermediate generator 60 towards the exchanger intermediate

[0373] 611. Main branch of the intermediate exchanger to the second generator in intermediate 60

Claims

1. Claims System comprising - a high temperature electrolyser (1) (EHT), - a first supply line (2) of the electrolyser configured to supply the electrolyser (1) with water vapour, - a first discharge line (4) from the electrolyser configured to discharge di-hydrogen from the electrolyser (1), - a second discharge line (3) from the electrolyser configured to discharge oxygen from the electrolyser (1), - a first heat exchange module (5) configured to ensure a heat exchange between the first water vapor supply line (2) and the first dihydrogen discharge line (4), characterized in that the system comprises a first module for recovering thermal energy from the dihydrogen at the outlet of the first heat exchange module (5) for the benefit of the first water vapor supply line (2), the recovery module comprising - a first intermediate exchanger (6) arranged on the first discharge line (4) downstream of the first heat exchange module (5) and configured to transfer the thermal energy from the dihydrogen to an intermediate fluid, and - a first intermediate steam generator (50) arranged on the first steam supply line (2) configured to transfer thermal energy from the intermediate fluid to the liquid water, - a first intermediate fluid circuit configured to receive an intermediate fluid and ensure the fluid connection between the first intermediate exchanger (6) and the first intermediate steam generator (50), and the system comprises a third module for recovering thermal energy from the dihydrogen at the output of the first module heat exchange module (5) for the benefit of the first water vapor supply line (2), the third recovery module comprising a heat pump and an intermediate circuit, the intermediate circuit comprising - a second intermediate exchanger (7) arranged on the first discharge line (2) downstream of the first heat exchange module (5) and configured to transfer the thermal energy from the dihydrogen to an intermediate fluid, and - a third intermediate fluid circuit (32) configured to receive an intermediate fluid and ensure the fluid connection between the second intermediate exchanger (7) and the heat pump, the heat pump including - a fluid circuit (27) configured to receive a heat transfer fluid, - an evaporator (25) arranged on the intermediate fluid circuit (32) downstream of the second intermediate exchanger (7) and configured to transfer the thermal energy from the intermediate fluid to the heat transfer fluid, - a compressor (26) configured to compress the heat transfer fluid, - a condenser (23) arranged on the first water vapor supply line (2) upstream of the first heat exchange module (5) and configured to transfer the thermal energy from the heat transfer fluid to the liquid water, - an expander (24) configured to expand the heat transfer fluid, - the fluid circuit (27) being configured to fluidly connect the evaporator (25) to the compressor (26), the compressor (26) to the condenser (23), the condenser (23) to the expansion valve (24) and the expansion valve (24) to the evaporator (25), and the system comprises a fifth intermediate exchanger (12) arranged on the first dihydrogen evacuation line (4) downstream of the second intermediate exchanger (7) and in parallel with the second intermediate exchanger (7) on the third intermediate fluid circuit (32) configured to transfer thermal energy from the di-hydrogen to the intermediate fluid.

2. System according to the preceding claim comprising a sixth intermediate exchanger (15) arranged on the first dihydrogen discharge line (4) downstream of the fifth intermediate exchanger (12) and in parallel with the second intermediate exchanger (7) and the fifth heat exchanger (12) on the intermediate fluid circuit (32) configured to transfer the thermal energy from the dihydrogen to the intermediate fluid.

3. System according to any one of the preceding claims comprising an electric steam generator (28) arranged on the first water supply line (2) upstream of the first heat exchange module (5).

4. System according to the preceding claim in which the electric steam generator (28) is arranged downstream of the first steam generator (50).

5. System according to any one of claims 1 to 3 comprising a second module for recovering under vacuum the thermal energy of the dihydrogen at the outlet of the first heat exchange module (5) for the benefit of the first water vapor supply line (2), the depression recovery module comprising a third intermediate exchanger (8) arranged on the first discharge line (4) downstream of the first heat exchange module (5) and configured to transfer the thermal energy of the dihydrogen to an intermediate fluid,an expander (40) and a compressor (41) arranged upstream of the first heat exchange module (5) on the first steam supply line (2) and defining between them a depression section of the first steam supply line (2), a second intermediate steam generator (60) arranged on the depression portion of the first steam supply line (2) configured to transfer the thermal energy from the intermediate fluid to the liquid water, a second intermediate fluid circuit () configured to receive an intermediate fluid and ensure the fluid connection between the third intermediate exchanger (8) and the second steam generator (60).,

6. System according to the preceding claim in which the electric steam generator (28) is arranged on the depression portion downstream of the second steam generator (60).

7. System according to any one of the two preceding claims in which the first steam supply line (2) comprises a main branch on which the steam generator (50) is arranged and a vacuum branch comprising the vacuum section, the main branch and the vacuum branch being arranged in parallel.

8. System according to any one of the preceding claims comprising a second supply line (10) of the electrolyser configured to supply the electrolyser (1) with air.

9. System according to the preceding claim comprising a second heat exchange module (11) configured to ensure a heat exchange between the second air supply line (10) and the second oxygen discharge line (3).

10. System according to any one of the preceding claims comprising a fourth intermediate heat exchanger (9) arranged between the second oxygen discharge line (10) and on the first intermediate fluid circuit (), in parallel with the first intermediate exchanger (6).

11. System according to the preceding claim comprising a seventh intermediate exchanger (29) arranged on the second dioxygen discharge line (10) downstream of the first heat exchanger (9) and in parallel with the second intermediate exchanger (7) on the third intermediate fluid circuit (32) configured to transfer the thermal energy from the dioxygen to the intermediate fluid.

Images