FR3161690A1 - System and process for the co-production of dihydrogen, dioxygen and a hydrogenated or oxidized product - Google Patents

Abstract

Coupling of a hydrogenation or oxidation plant (2) and a dihydrogen production plant (3) to transfer (4) heat produced by the hydrogenation or oxidation plant (2) to an inlet stream of an electrochemical device in the dihydrogen production plant (3) and/or to convey (100) to the hydrogenation or oxidation plant (2) one or more fluids formed by the electrochemical device. Figure for the abstract: Fig. 6

Description

System and process for the co-production of dihydrogen, dioxygen and a hydrogenated or oxidized product

The present invention relates to the field of electrochemical devices and finds applications in particular in the sectors of renewable energy production, especially dihydrogen, as well as in the chemical and petrochemical industries.

The invention is of particular interest, but not limited to, solid oxide electrochemical devices, especially high-temperature electrolyzers.

State of the art

Conventional hydrogenation and oxidation techniques on the one hand, and dihydrogen production on the other, have an ecological impact that needs to be reduced.

The present invention aims to reduce such an impact in the field of dihydrogen production and/or in the field of hydrogenated product production and/or in the field of oxidized product production.

A particular, but not limiting, objective of the invention is to reduce the energy consumption of a conventional dihydrogen production facility.

• une installation de traitement d’un ou plusieurs produits, configurée pour traiter ce ou ces produits par hydrogénation et/ou par oxydation,
• une installation de production de dihydrogène et/ou de dioxygène comprenant un dispositif électrochimique tel qu’un électrolyseur en phase vapeur, le dispositif électrochimique étant configuré pour former, à partir d’un flux d’un fluide d’entrée, un flux de sortie comprenant du dihydrogène et/ou un flux de sortie comprenant du dioxygène.

The invention relates to an industrial system comprising:

• a treatment plant for one or more products, configured to treat this product or these products by hydrogenation and/or oxidation,
• a hydrogen and/or oxygen production installation comprising an electrochemical device such as a vapor phase electrolyzer, the electrochemical device being configured to form, from an input fluid stream, an output stream comprising hydrogen and/or an output stream comprising oxygen.

According to a first aspect, the system of the invention may include a heat transfer device configured to recover heat produced by the processing installation and transfer it to said inlet stream.

In one embodiment, the treatment plant includes a hydrogenation device configured to treat one of said products by hydrogenation, the heat transfer device being configured to recover heat produced by the hydrogenation device and transfer it to said inlet stream.

Without limitation, the hydrogenation device may include one or more pieces of equipment chosen from a list including a heater, a condenser and a cooler.

The heat transfer device can be configured to recover heat produced by one or more of these devices.

In one embodiment, the treatment installation includes an oxidation device configured to treat one of said products by oxidation, the heat transfer device being configured to recover heat produced by the oxidation device and transfer it to said inlet stream.

These embodiments can be combined, the treatment installation being able, for example, to include both a hydrogenation device and an oxidation device.

The invention thus makes it possible to utilize waste heat from various heat sources within the treatment plant and, without limitation, to use this heat to produce steam. This reduces the electrical energy required to produce hydrogen, thereby improving the energy efficiency of the electrochemical device.

According to a second aspect which is independent of said first aspect, the system of the invention may include a transport element configured to convey to said treatment installation all or part of said output stream comprising dihydrogen and/or said output stream comprising dioxygen.

The transport unit may include one or more conduits and/or one or more pieces of equipment to ensure or optimize this fluid transport function.

In an embodiment in which the treatment installation includes a hydrogenation device configured to treat one of said products by hydrogenation, the transport element can be configured to convey to the hydrogenation device said output stream comprising dihydrogen which is formed by the electrochemical device, the hydrogenation device being configured to bring this stream into contact with said product treated by the hydrogenation device in order to form a hydrogenated output product.

In an embodiment in which the treatment installation includes an oxidation device configured to treat one of said products by oxidation, the transport member can be configured to convey to the oxidation device said output stream comprising dioxygen which is formed by the electrochemical device, the oxidation device being configured to bring this stream into contact with said product treated by the oxidation device in order to form an oxidized output product.

Such coupling makes it possible to reduce the carbon footprint of the treatment facility by using low-carbon dioxygen and/or dihydrogen as a reagent, especially compared with dihydrogen obtained from fossil fuels such as natural gas or coal.

The system may include one or more heat transfer devices according to said first aspect and/or one or more transport elements according to said second aspect, or only one or more heat transfer devices according to said first aspect, or only one or more transport elements according to said second aspect.

In one embodiment, the heat transfer device is configured to change said inlet flow from the liquid state to the gaseous state.

This embodiment is of particular interest when the electrochemical device is a vapor phase electrolyzer, it being understood that the dihydrogen production installation of the system of the invention may include another type of electrochemical device, for example a liquid phase electrolyzer.

In one embodiment, the system includes one or more purification and/or compression components for one or more of said output streams formed by the electrochemical device.

When the system includes a transport element as defined above, the purification and/or compression element(s) may be configured to purify and/or compress one or more of said output streams formed by the electrochemical device before their introduction into the treatment plant.

The invention also relates to an industrial process implementing a system as defined above.

• un traitement d’un ou plusieurs produits à l’aide de l’installation de traitement dudit système,
• la formation, à l’aide du dispositif électrochimique dudit système, d’un flux de sortie comprenant du dihydrogène et/ou d’un flux de sortie comprenant du dioxygène.

The process includes, in particular:

• the processing of one or more products using the processing installation of said system,
• the formation, using the electrochemical device of said system, of an output stream comprising dihydrogen and/or an output stream comprising dioxygen.

• une mise en œuvre du dispositif de transfert thermique dudit système de manière à récupérer de la chaleur produite par l’installation de traitement, et/ou
• une mise en œuvre dudit dispositif de transfert thermique de manière à transférer la chaleur ainsi récupérée audit flux d’entrée, et/ou
• une mise en œuvre dudit organe de transport de manière à acheminer un ou plusieurs desdits flux de sortie formés par le dispositif électrochimique vers l’installation de traitement, et/ou
• un traitement d’un ou plusieurs desdits flux de sortie formés par le dispositif électrochimique à l’aide d’un ou plusieurs desdits organes de purification et/ou de compression, afin de purifier et/ou comprimer un ou plusieurs de ces flux de sortie, par exemple avant leur introduction dans l’installation de traitement.

Depending on the system architecture and the aforementioned characteristics it includes, the process may include:

• an implementation of the heat transfer device of said system so as to recover heat produced by the treatment plant, and/or
• an implementation of said heat transfer device so as to transfer the heat thus recovered to said inlet flow, and/or
• an implementation of said transport element so as to convey one or more of said output flows formed by the electrochemical device to the treatment installation, and/or
• a treatment of one or more of said output streams formed by the electrochemical device using one or more of said purification and/or compression devices, in order to purify and/or compress one or more of these output streams, for example before their introduction into the treatment plant.

Without limitation, one or more of the said products treated by the treatment facility are chosen from a list including an oil, a grease, an alcohol, an aromatic hydrocarbon, a heteroatomic hydrocarbon, a heterocyclic hydrocarbon, an unsaturated hydrocarbon and a gas.

Other advantages and features of the invention will become apparent from the detailed, non-limiting description that follows.

Brief description of the figures

• laFIG. 1est une vue schématique d’un système industriel comprenant une installation d’hydrogénation et/ou d’oxydation, une installation de production de dihydrogène et de dioxygène, ainsi qu’un dispositif configuré pour transférer de la chaleur de l’installation d’hydrogénation et/ou d’oxydation vers l’installation de production de dihydrogène et de dioxygène ;
• laFIG. 2est une vue schématique d’une installation d’hydrogénation équipée d’unités de récupération de chaleur ;
• laFIG. 3est une vue schématique d’un système industriel comprenant une installation d’hydrogénation et/ou d’oxydation, une installation de production de dihydrogène et de dioxygène, ainsi qu’un dispositif configuré pour acheminer un ou plusieurs fluides produits par l’installation de production de dihydrogène et de dioxygène vers l’installation d’hydrogénation et/ou d’oxydation ;
• laFIG. 4est une vue schématique d’une variante de réalisation du système de laFIG. 3;
• laFIG. 5est une vue schématique d’une autre variante de réalisation du système de laFIG. 3;
• laFIG. 6est une vue schématique d’un système industriel comprenant une installation d’hydrogénation et/ou d’oxydation, une installation de production de dihydrogène et de dioxygène, un dispositif configuré pour transférer de la chaleur de l’installation d’hydrogénation et/ou d’oxydation vers l’installation de production de dihydrogène et de dioxygène, ainsi qu’un dispositif configuré pour acheminer un ou plusieurs fluides produits par l’installation de production de dihydrogène et de dioxygène vers l’installation d’hydrogénation et/ou d’oxydation.

The detailed description that follows refers to the attached drawings on which:

• there FIG. 1 is a schematic view of an industrial system comprising a hydrogenation and/or oxidation plant, a hydrogen and oxygen production plant, and a device configured to transfer heat from the hydrogenation and/or oxidation plant to the hydrogen and oxygen production plant;
• there FIG. 2 is a schematic view of a hydrogenation plant equipped with heat recovery units;
• there FIG. 3 is a schematic view of an industrial system comprising a hydrogenation and/or oxidation plant, a dihydrogen and dioxygen production plant, and a device configured to convey one or more fluids produced by the dihydrogen and dioxygen production plant to the hydrogenation and/or oxidation plant;
• there FIG. 4 is a schematic view of a variant implementation of the system of the FIG. 3 ;
• there FIG. 5 is a schematic view of another variant implementation of the system of the FIG. 3 ;
• there FIG. 6 is a schematic view of an industrial system comprising a hydrogenation and/or oxidation plant, a hydrogen and oxygen production plant, a device configured to transfer heat from the hydrogenation and/or oxidation plant to the hydrogen and oxygen production plant, and a device configured to convey one or more fluids produced by the hydrogen and oxygen production plant to the hydrogenation and/or oxidation plant.

Common references are used across the different figures to designate identical or analogous elements.

Detailed description of implementation methods

There FIG. 1 schematically represents an industrial system 1 according to a first embodiment.

System 1 in this example is intended for the co-production of a hydrogenated product or an oxidized product on the one hand and, on the other hand, of dihydrogen and dioxygen.

In the implementation of the FIG. 1 , system 1 includes an installation 2 for processing a product called "to be treated", an installation 3 for producing dihydrogen and dioxygen, and a device 4 performing a coupling, or an interface, between installations 2 and 3.

In this embodiment, device 4 is a heat transfer device which is configured to recover heat produced by installation 2 and to use the heat thus recovered in installation 3 for the production of dihydrogen and dioxygen.

Installation 3 includes an electrochemical device for producing dihydrogen and dioxygen from a flow of an input fluid.

In this non-limiting example, the electrochemical device is an electrolyzer comprising solid oxide electrolytic cells that perform vapor-phase electrolysis. This electrochemical device constitutes a technology known by the English name "Solid Oxide Electrolysis Cell" (SOEC).

In a manner known per se, such an electrolyzer comprises one or more stacks of cells, each forming a cathode, an anode and an electrolyte, so as to constitute a reaction zone.

The electrochemical device of installation 3 is in this example configured to carry out a high temperature electrolysis, so as to form, on the one hand, a first output flow of a fluid which includes dihydrogen and, on the other hand, a second output flow of a fluid which includes dioxygen, from the said input flow which in this example includes water vapor having a temperature which can typically be between 100°C and 850°C.

There FIG. 2 shows an installation 2 that can be implemented in system 1 of the FIG. 1 .

In this example, installation 2 forms a hydrogenation device.

By way of non-exhaustive list, device 2 of the FIG. 2 includes a heater 11, an autoclave-type reactor 12, a condenser 13, a cooler 14 and filtration equipment 15.

Device 2 is configured to process said product successively in equipment 11, 12, 14 and 15, the FIG. 2 illustrating with dashed arrows the path taken by the product to be treated within device 2.

In this particular example, the product to be treated which is introduced into device 2 includes an oil.

Device 2 of the FIG. 2 includes a fluidic network including conduits 21 and 22 which are configured to introduce into reactor 12 respectively a catalyst and a reactant comprising dihydrogen.

The fluidic network includes a conduit 24 configured to introduce into the heater 11 a so-called heating flow in the form of steam, and a conduit 25 to extract the heating flow from the heater 11.

The fluidic network also includes conduits 27 and 28 forming a circuit configured to circulate a fluid between the condenser 13 and a heating and cooling unit (not shown) of the reactor 12.

The fluidic network includes a conduit 31 configured to introduce a flow of refrigerant fluid into the condenser 13, and a conduit 32 to extract the refrigerant flow from the condenser 13.

The fluidic network further includes a conduit 34 configured to introduce into the cooler 14 a so-called cooling flow, for example water, and a conduit 35 to extract this cooling flow from the cooler 14.

In this example, device 2 of the FIG. 2 is equipped with heat recovery units 41, 42 and 43 which are configured to recover heat carried by, respectively, said heating flow exiting heater 11 through conduit 25, said refrigerant flow exiting condenser 13 through conduit 32 and said cooling flow exiting cooler 14 through conduit 35.

An example of the implementation of device 2 of the will now be briefly described. FIG. 2 , it being understood that the operation of such a device is known as such, that is to say independently of its implementation in a system according to the invention, in particular independently of the heat recovery carried out here using units 41, 42 and 43.

The product to be treated passes through the heater 11 in which it recovers part of the heat carried by the heating flow, so as to reach a temperature which can typically be between 130°C and 150°C.

The product thus heated is introduced into reactor 12, in which it is brought into contact on the one hand with the dihydrogen reagent which is introduced into reactor 12 through conduit 22, for example in the form of bubbles using an agitator (not shown) and, on the other hand, with the catalyst which is introduced into reactor 12 through conduit 21, in order to produce a hydrogenation reaction.

The condenser 13 typically allows the reactor 12 to be cooled with the fluid circulating in the circuit formed by the conduits 27 and 28, so as not to exceed a predetermined maximum temperature, for example 200°C.

In this example, the hydrogenated product is then cooled by the cooler 14 using the cooling fluid, and then filtered using the equipment 15 to remove the residual catalyst, the equipment 15 being able, for example, to include a pressure vessel equipped with metallic gauze or filter candles.

With reference to figures 1 and 2, units 41, 42 and 43, which in this example form device 4, thus make it possible to recover heat produced by installation 2 and to use the heat thus recovered in installation 3 for the production of dihydrogen and dioxygen.

More specifically, the heat recovered by device 4 is used here to increase the temperature of said input stream before its introduction into the electrochemical device, in this example to change this input stream from the liquid state to the gaseous state.

The heat transfer device 4 and, in this particular example, the heat recovery units 41, 42 and 43, thus make it possible to produce superheated steam from the fluid forming the inlet flow.

Of course, electrical energy can be used as an alternative or complementary method to increase the temperature of this inlet flow.

In general, the heat transfer device 4 and/or one or more of said heat recovery units 41, 42 and 43 may comprise one or more pieces of equipment, each of which may be selected from a non-exhaustive list including an economizer, a recuperator, a heat exchanger, an electric heater, a degasser, a vaporizer, a superheater, a heat storage device, an electrical energy storage device and a heat pump.

Of course, the heat transfer device 4 can be configured to transfer the heat thus recovered to the inlet stream via a transfer fluid such as water or thermal oil.

Installation 2 of system 1 of the FIG. 1 may include a hydrogenation device different from that of the FIG. 2 For example, device 2 described above with reference to the FIG. 2 may include one or more additional pieces of equipment (not shown), such as equipment for drying the product to be treated, installed upstream or downstream of reactor 12.

In an alternative embodiment, not shown, installation 2 of system 1 of the FIG. 1 includes a hydrogenation device carrying out a cyclohexane synthesis process. In a manner known per se, such a device may include a mixing element for a benzene stream and a dihydrogen stream, as well as various heat-producing equipment, to form a cyclohexane stream in liquid form, thus facilitating its transport to a delivery point where the cyclohexane can be dehydrogenated so as to release the dihydrogen and regenerate the benzene.

• un ou plusieurs réchauffeurs configurés pour réchauffer du benzène et du dihydrogène mélangés par ledit organe de mélange,
• un réacteur, par exemple un réacteur catalytique en lit fixe, configuré pour recevoir un flux d’entrée comprenant le mélange de benzène et de dihydrogène afin de produire une réaction d’hydrogénation, un ou plusieurs desdits réchauffeurs pouvant être configurés pour recevoir un flux de sortie du réacteur d’hydrogénation et pour transférer de la chaleur de ce flux de sortie audit flux d’entrée de sorte que celui-ci atteigne une température qui peut être de 150°C,
• un ou plusieurs refroidisseurs configurés pour abaisser la température du flux de sortie du réacteur d’hydrogénation, ce flux de sortie pouvant plus particulièrement comprendre des produits de réaction ainsi que du benzène et du dihydrogène n’ayant pas réagi ou en excès, par exemple jusqu’à une température de l’ordre de 50°C, un ou plusieurs de ces refroidisseurs pouvant être configurés pour transférer de la chaleur ainsi récupérée audit flux d’entrée,
• un séparateur, par exemple un séparateur flash gaz-liquide, configuré pour séparer des produits de réaction et du dihydrogène résiduel, le dispositif pouvant éventuellement être configuré pour recycler en entrée du réacteur d’hydrogénation du dihydrogène gazeux et des coproduits légers tels que du méthane obtenues en tête du séparateur,
• un système comprenant un réchauffeur configuré pour augmenter la température d’un flux de produit lourd, par exemple jusqu’à une température de l’ordre de 120°C, et un organe de distillation configuré pour traiter le flux ainsi réchauffé de manière à obtenir du cyclohexane en pied de colonne.

By way of example, such a hydrogenation device may include various combinations of the following components:

• one or more heaters configured to heat benzene and dihydrogen mixed by said mixing device,
• a reactor, for example a fixed-bed catalytic reactor, configured to receive an inlet stream comprising a mixture of benzene and dihydrogen in order to produce a hydrogenation reaction, one or more of said heaters being able to be configured to receive an outlet stream from the hydrogenation reactor and to transfer heat from this outlet stream to said inlet stream so that the latter reaches a temperature which may be 150°C,
• one or more coolers configured to lower the temperature of the outlet stream from the hydrogenation reactor, this outlet stream possibly including reaction products as well as unreacted or excess benzene and dihydrogen, for example down to a temperature of around 50°C, one or more of these coolers being able to be configured to transfer heat thus recovered to said inlet stream,
• a separator, for example a flash gas-liquid separator, configured to separate reaction products and residual dihydrogen, the device possibly being configured to recycle gaseous dihydrogen and light co-products such as methane obtained at the top of the separator back into the hydrogenation reactor,
• a system comprising a heater configured to increase the temperature of a heavy product stream, for example up to a temperature of around 120°C, and a distillation unit configured to treat the stream thus heated in order to obtain cyclohexane at the bottom of the column.

One or more heat recovery units, similar to units 41, 42 and 43 described above with reference to the FIG. 2 , can be used to recover heat in such a hydrogenation device, for example at one or more of said heaters and/or one or more of said coolers.

More generally, the installation 2 of the system 1 of the invention may include at least one hydrogenation device for a product which may not be limited to being selected from a list including oils, fats and their oleochemical derivatives, in particular fatty acids, fatty acid esters, fatty nitriles, alcohols, aromatic hydrocarbons, heteroatomic hydrocarbons, heterocyclic hydrocarbons, and unsaturated hydrocarbons.

In general, a hydrogenation device is typically configured to add dihydrogen to unsaturated hydrocarbon molecules (e.g. aromatic compounds, olefins, diolefins, fatty acids, etc.) or heteroatomic hydrocarbon molecules, i.e. hydrocarbons containing heteroatoms such as oxygen, sulfur, or nitrogen, for example, to convert a liquid oil into a solid fat, to change the consistency of a fat, to stabilize an oil or fat, or to expand the availability of edible oils or fats.

According to another embodiment, not shown, installation 2 of system 1 of the FIG. 1 includes a device for treating a product by oxidation, using dioxygen in this example as the oxidizing reagent. The preceding description applies by analogy to this variant of the embodiment, it being understood that such an oxidation device may be equipped with one or more heat recovery units, analogous to units 41, 42 and 43 described above with reference to the FIG. 2 , to form the coupling device 4 of system 1.

Thus, system 1 of the FIG. 1 can also be used for the co-production of an oxidized product on the one hand and, on the other hand, of dihydrogen and dioxygen.

The different variants described above can be combined, the installation 2 of system 1 of the invention generally comprising one or more hydrogenation devices and/or one or more oxidation devices, as well as a coupling device comprising one or more units configured to recover heat from such devices.

There FIG. 3 schematically represents an industrial system 1 according to a second embodiment, which is described solely according to its differences from the embodiment of the FIG. 1 The preceding description applies by analogy to this second embodiment, in particular the description of installation 2 according to its different variants.

System 1 of the FIG. 3 differs from that of the FIG. 1 in that it includes another type of coupling device for installations 2 and 3.

In particular, system 1 of the FIG. 3 includes in this example a device 100 which does not form a heat transfer device as described above but which forms a transport component, configured to convey one or more of said output flows formed by the electrochemical device of installation 3 to installation 2.

A first variant of the implementation method of the FIG. 3 is illustrated at the FIG. 4

In this example, installation 2 forms a hydrogenation device as illustrated in the FIG. 2 , it being understood that this description applies by analogy to a different installation 2.

In this non-limiting example, installation 3 is similar to that described above and the preceding description applies by analogy to what follows.

• un conduit 120 relié à une entrée du dispositif de chauffage 110 afin d’y introduire ledit flux d’entrée,
• un conduit 122 reliant une sortie du dispositif 110 à une entrée du dispositif électrochimique de l’installation 3 afin d’introduire dans le dispositif électrochimique tout ou partie dudit flux d’entrée sortant du dispositif 110,
• un conduit 124 reliant une première sortie du dispositif électrochimique de l’installation 3 à une entrée du dispositif de traitement 112 afin d’introduire dans le dispositif 112 tout ou partie dudit premier flux de sortie formé par le dispositif électrochimique, c’est-à-dire le flux de sortie comprenant du dihydrogène,
• un conduit 126 reliant une deuxième sortie du dispositif électrochimique de l’installation 3 à une entrée du dispositif de traitement 114 afin d’introduire dans le dispositif 114 tout ou partie dudit deuxième flux de sortie formé par le dispositif électrochimique, c’est-à-dire le flux de sortie comprenant du dioxygène,
• un conduit 128 qui relie une sortie du dispositif 112 à l’installation 2 afin d’introduire dans l’installation 2 tout ou partie dudit premier flux de sortie traité par le dispositif 112, le conduit 128 correspondant dans cet exemple au conduit 22 de laFIG. 2,
• un conduit 130 relié à une sortie du dispositif 114 afin d’en extraire tout ou partie dudit deuxième flux de sortie traité par le dispositif 114.

In the example of the FIG. 4 System 1 comprises, in addition to installations 2 and 3, a heating device 110, devices 112 and 114 for treating the outlet flows formed by installation 3, and a fluid network comprising, but not limited to:

• a conduit 120 connected to an inlet of the heating device 110 in order to introduce said inlet flow,
• a conduit 122 connecting an output of the device 110 to an input of the electrochemical device of the installation 3 in order to introduce into the electrochemical device all or part of said inlet flow exiting the device 110,
• a conduit 124 connecting a first outlet of the electrochemical device of the installation 3 to an inlet of the treatment device 112 in order to introduce into the device 112 all or part of said first outlet flow formed by the electrochemical device, i.e. the outlet flow comprising dihydrogen,
• a conduit 126 connecting a second outlet of the electrochemical device of the installation 3 to an inlet of the treatment device 114 in order to introduce into the device 114 all or part of said second outlet stream formed by the electrochemical device, i.e. the outlet stream comprising dioxygen,
• a conduit 128 which connects an outlet of the device 112 to the installation 2 in order to introduce into the installation 2 all or part of said first outlet flow treated by the device 112, the conduit 128 corresponding in this example to the conduit 22 of the FIG. 2 ,
• a conduit 130 connected to an output of the device 114 in order to extract all or part of said second output stream processed by the device 114.

In this example, the inlet flow arriving at device 110 through conduit 120 includes purified water and the heating device 110 is configured to change this inlet flow from a liquid to a gaseous state.

More specifically, the heating device 110 is configured in this example to form a superheated steam stream from the purified inlet stream.

To do this, the device 110 can recover heat from an energy carrier formed from an external heat source, for example in the form of a flow of a hot fluid in a gaseous or liquid state.

Alternatively or in addition, device 110 can recover heat using electrical energy supplied by an electrical network and/or an electrical energy storage device.

Device 110 can therefore form a heat recovery device and for this purpose may include one or more pieces of equipment which may be chosen from a non-exhaustive list including an economizer, a recuperator, a heat exchanger, an electric heater, a degasser, a vaporizer, a superheater, a heat storage device, an electrical energy storage device and a heat pump.

Regarding devices 112 and 114, these can generally be configured to perform cooling and/or compression and/or purification operations on the flows they receive, carried out by one or more corresponding processing units.

For example, each of devices 112 and 114 may include a purification unit (not shown) comprising one or more technologies selected from adsorption, absorption, membrane, distillation, and conversion technologies. Purification of the first output stream, i.e., the fluid stream containing dihydrogen, notably removes impurities such as water and/or dioxygen and/or nitrogen and/or argon and/or carbon monoxide and/or carbon dioxide from this stream. Purification of the second output stream, i.e., the fluid stream containing dioxygen, notably removes impurities such as water and/or nitrogen and/or argon and/or carbon monoxide and/or carbon dioxide from this stream.

Each of the devices 112 and 114 may also include a compression unit, in order to compress the purified stream from the corresponding purification unit, for example for storage in a storage device (not shown).

With reference to Figures 3 and 4, said transport element 100 of system 1 is, within the framework of the embodiment variant of the FIG. 4 formed by conduits 22/128 and 124.

A second variant of the implementation method of the FIG. 3 is illustrated at the FIG. 5 which is described solely according to its differences from the variant of the FIG. 4 The preceding description applies by analogy.

In the example of the FIG. 5 , installation 2 includes at least one oxidation device as described above and the transport element 100 of system 1 is formed by the conduit 130 which connects the outlet of device 114 to installation 2 in order to introduce into installation 2 all or part of said second outlet stream treated by device 114.

Conduit 128 of system 1 of the FIG. 5 is not connected to installation 2 in this example.

• un équipement (non représenté) configuré pour introduire dans le dispositif électrochimique de l’installation 3 un gaz de balayage, et/ou
• un dispositif (non représenté) configuré pour purifier ledit flux d’entrée avant son arrivée dans le conduit 120 et/ou pour former ledit flux d’entrée en utilisant de l’eau résiduelle formée par l’installation 3 et/ou de l’eau extraite desdits flux de sortie par les dispositifs 112 et/ou 114 et/ou de l’eau provenant d’une source externe (non représentée).

In each of the non-limiting variants of Figures 4 and 5, system 1 may include one or more additional pieces of equipment, for example:

• equipment (not shown) configured to introduce a sweeping gas, and/or into the electrochemical device of installation 3
• a device (not shown) configured to purify said inlet stream before it enters conduit 120 and/or to form said inlet stream using residual water formed by installation 3 and/or water extracted from said outlet streams by devices 112 and/or 114 and/or water from an external source (not shown).

System 1 of the invention may also be devoid of some of the equipment described above with reference to Figures 4 and 5, for example be devoid of one or more of the processing devices 112 and 114.

For example, in an unrepresented variant of the FIG. 4 System 1 does not include a treatment device 112, so as to convey said first output stream from installation 3 to installation 2 without intermediate treatment. In an unshown variant of the FIG. 5 , system 1 does not include a processing device 114, so as to convey said second output stream from installation 3 to installation 2 without intermediate processing.

In addition, part of the first output stream and/or part of the second output stream formed by installation 3 can be used, alternatively or complementaryly, to form respectively a fuel and/or an oxidizer in one or more devices which may or may not belong to installation 2.

The variants of figures 4 and 5 can of course be combined, for example to form a system 1 in which the installation 2 includes at least one hydrogenation device and at least one oxidation device.

There FIG. 6 schematically represents an industrial system 1 according to a third embodiment which combines the principles of the embodiments of figures 1 and 3.

Thus, in this example, system 1 of the FIG. 6 includes, on the one hand, a heat transfer device 4 such as in the system of the FIG. 1 , according to any one of the variants described above (for example, the variant of the FIG. 2 ) and, on the other hand, a transport organ 100 such as in the system of the FIG. 3 , according to any one of the variants described above (in particular with reference to figures 4 and 5).

The preceding description applies by analogy to this third mode of embodiment.

The invention is not limited to the examples just described, the system may in particular implement one or more of the following non-limiting variants.

Regarding, for example, the installation for the production of dihydrogen and dioxygen, this may include one or more electrochemical devices different from the one described above, for example a device configured to carry out an alkaline electrolysis or a proton exchange membrane electrolysis.

As another example, the system of the invention may include a heat transfer device comprising one or more heat recovery units such as those illustrated in the FIG. 2 and/or one or more other heat recovery units (not shown), depending in particular on the architecture of installation 2 and the available heat sources.

Of course, the system of the invention and in particular the installation for the production of dihydrogen and dioxygen may include many conventional pieces of equipment which are not described above, for example one or more pumps, one or more compressors, one or more fans, one or more flow control valves, one or more ejectors, etc.

Claims (10)

Industrial system (1) comprising:

• an installation (2) for the treatment of one or more products, configured to treat this or these products by hydrogenation and/or by oxidation,
• an installation (3) for the production of dihydrogen and/or dioxygen comprising an electrochemical device such as a vapor phase electrolyzer, the electrochemical device being configured to form, from an input fluid stream, an output stream comprising dihydrogen and/or an output stream comprising dioxygen,
• a heat transfer device (4) configured to recover heat produced by the processing plant (2) and transfer it to said inlet stream.

System (1) according to claim 1, wherein the processing plant (2) comprises a hydrogenation device configured to process one of said products by hydrogenation, the heat transfer device (4) being configured to recover heat produced by the hydrogenation device (2) and transfer it to said inlet stream. System (1) according to claim 2, wherein the hydrogenation device (2) comprises one or more pieces of equipment selected from a list including a heater (11), a condenser (13) and a cooler (14), the heat transfer device (4, 41, 42, 43) being configured to recover heat produced by one or more of these pieces of equipment (11, 13, 14). System (1) according to claim 2 or 3, comprising a transport element (100) configured to convey to the hydrogenation device (2) said output stream comprising dihydrogen which is formed by the electrochemical device, the hydrogenation device (2) being configured to bring this stream into contact with said product treated by the hydrogenation device (2) in order to form a hydrogenated output product. System (1) according to any one of claims 1 to 4, wherein the processing plant (2) comprises an oxidation device configured to process one of said products by oxidation, the heat transfer device (4) being configured to recover heat produced by the oxidation device and transfer it to said inlet stream. System (1) according to claim 5, comprising a transport member (100) configured to convey to the oxidation device (2) said output stream comprising dioxygen which is formed by the electrochemical device (3), the oxidation device (2) being configured to bring this stream into contact with said product treated by the oxidation device (2) in order to form an oxidized output product. System (1) according to any one of claims 1 to 6, wherein the heat transfer device (4) is configured to change said inlet flow from the liquid state to the gaseous state. System (1) according to any one of claims 1 to 7, comprising one or more purification and/or compression elements (112, 114) for one or more of said output streams formed by the electrochemical device (3). An industrial process implementing a system (1) according to any one of claims 1 to 8, the process comprising:

• the processing of one or more products using the processing installation (2) of said system (1),
• the formation, using the electrochemical device (3) of said system (1), of an output stream comprising dihydrogen and/or an output stream comprising dioxygen,
• an implementation of the heat transfer device (4) of said system (1) so as to recover heat produced by the processing installation (2) and transfer it to said inlet flow.

A process according to claim 9, wherein one or more of said products treated by the treatment plant (2) are selected from a list including an oil, a grease, an alcohol, an aromatic hydrocarbon, a heteroatomic hydrocarbon, a heterocyclic hydrocarbon, an unsaturated hydrocarbon and a gas.