FR3086939A1 - SELF-CONTAINED INSTALLATION AND PROCESS FOR RECOVERY AND TRANSFORMATION OF HYDROGEN - Google Patents

Abstract

The invention relates to an industrial installation (1) and an industrial process for the transformation of dihydrogen (H2, also called hydrogen), characterized in that the installation (1) comprises at least one supply line for fluid extracted from the sub- terrestrial soil, typically a gas, containing dihydrogen, said line supplying a device (10) for converting dihydrogen into ammonia (NH3) for the production of ammonia, said produced ammonia being directed to at least one supply line for at least one liquid ammonia storage tank. The invention relates to a method for recovering dihydrogen.

Description

Installation and autonomous process of hydrogen recovery and transformation

The present invention relates to the field of hydrogen development (H ₂ ).

The present invention also relates to the field of hydrogen transformation

More particularly, the present invention relates to the valorization and transformation of sub-terrestrial hydrogen, that is to say extract from the terrestrial subsoil (also called native or natural hydrogen).

Thus the invention relates in particular to an industrial installation and an industrial process for the transformation of hydrogen into ammonia, and in particular using hydrogen and ammonia in gaseous form.

State of the art

It is well known to transform hydrogen into ammonia, for example by the Haber Bosch process. This process requires the reaction of hydrogen with nitrogen for the production of ammonia. However, all industrial facilities to date use synthetic hydrogen.

The applicant proposes to commercially exploit sources of gaseous hydrogen from the underground (sub-terrestrial).

To the knowledge of the inventors, no industrial operation has been described and operates to date on the basis of sub-terrestrial hydrogen. There is therefore a technical and industrial need in this regard.

The gaseous hydrogen produced from such natural sources of gaseous hydrogen, that is to say extracted from the earth's subsoil, has a variable quality and available quantity. This again presents a technical difficulty from an industrial point of view.

In addition, the hydrogen thus available is generally present in isolated territories, that is to say in particular non-industrialized territories, and having no electrical network. This therefore represents a particularly important industrial challenge in order to be able to build an industrial installation for the exploitation of such a sub-terrestrial hydrogen.

Objects of the invention

The present invention proposes to solve these technical problems, and in particular the major technical problem of the exploitation of hydrogen from the earth's subsoil. No solution, in particular industrializable, is proposed to date to the knowledge of the inventors.

The present invention aims to provide an industrial installation and process for the transformation of sub-terrestrial hydrogen.

The present invention aims to provide an industrial installation and process for upgrading sub-terrestrial hydrogen.

The present invention aims to provide such industrial facilities and methods in an economically profitable manner for an industrialist, in particular by taking into account the possible unavailability of the electrical network.

The present invention aims in particular to provide such industrial installations and processes which are autonomous in electricity.

Detailed description of the invention

It has been discovered by the present inventors that it is possible to solve the technical problems mentioned above by the present invention. The invention is described in particular with reference to the figures for convenience, without any limitation solely to the examples of the figures.

The invention therefore relates to an industrial installation 1 for transforming dihydrogen (H ₂ , also called hydrogen), characterized in that the installation 1 comprises at least one supply line for fluid extracted from the earth's subsoil, typically a gas containing dihydrogen, said line supplying a device 10 for converting dihydrogen into ammonia (NH ₃ ) for the production of ammonia, said produced ammonia being directed to at least one supply line for at least one storage tank d ammonia in liquid form.

Preferably, the installation comprises at least one NH ₃ 130 fuel cell producing electricity, and a supply line for the NH ₃ 130 fuel cell from the ammonia tank.

Advantageously, said NH ₃ 130 fuel cell produces electricity and supplies electricity to at least said installation 1.

According to one embodiment, the installation comprises at least one source of electricity which is not generated from hydrocarbon, such as for example from a fuel cell, for example a hydrogen cell, a turbine ammonia gas, a photovoltaic device, a wind turbine, a device using geothermal energy, tidal energy, wave energy, a tidal turbine, or even biomass.

Advantageously, the installation 1 is self-sufficient in electrical consumption by the electricity produced by the NH ₃ 130 fuel cell or cells and / or the source of electricity which is not generated from hydrocarbon.

Typically, the device 10 for converting dihydrogen into ammonia comprises a gas / liquid separator 80, a recycling compressor 90, a reactor 100 for converting dihydrogen to ammonia, an ammonia condenser 110, and preferably a storage tank 120 of the ammonia produced.

Advantageously, the invention allows the storage of ammonia in liquid form. This allows on the one hand to develop a natural source of hydrogen by a product having a local and international market and on the other hand avoids the handling and storage of gas.

The industrial installation comprises several modules operating alone or with other modules.

Dihydrogen gas can be extracted from the earth's subsoil, for example by a wellbore. Such sources are localized in various places of the planet like for example in Mali, in the United States, in Russia, in France, in Australia, in Brazil, in Argentina, in Iceland, in Canada, in Oman, in the Philippines, in Angola . The advantage of such a source is the high hydrogen content, and typically greater than 30% by volume relative to the total volume of the gaseous fraction considered. Advantageously, the hydrogen content is greater than 90% by volume relative to the total volume of the gaseous fraction considered.

The extraction of dihydrogen is carried out according to one embodiment by drilling a well using conventional techniques for drilling and extracting gas from the earth's subsoil. The extraction is carried out taking into account the safety necessary for handling hydrogen.

The transformation of hydrogen into ammonia, and the different variants of the implementation of this transformation, and in particular of the Haber Bosch process, as described in the prior art are an integral part of the present invention.

According to one embodiment, the installation 1 comprises at least one device 30 for extracting a fluid, typically a gas, containing dihydrogen from the earth's subsoil.

Advantageously, the installation 1 and the method according to the present invention are not sensitive to the purity of the hydrogen.

For example, the fluid, typically a gas, containing dihydrogen extracted from the earth's subsoil can comprise one or more other fluids, typically gases, such as for example methane, nitrogen, and helium, in different proportions.

An example of a gaseous fluid mixture feeding the installation 1 or the method according to the invention comprises or consists essentially of dihydrogen, nitrogen and methane, for example in the volume proportions of dihydrogen generally ranging from 10 to 99% (v / v total extracted gaseous fluid), methane generally ranging from 0.5 to 60% (total v / v extracted gaseous fluid), dinitrogen generally ranging from 0.5 to 60% (total v / v extracted gaseous fluid ).

An example of a gaseous fluid mixture comprises or essentially consists of dihydrogen, dinitrogen and methane, for example in the volume proportions of dihydrogen from 5 to 15% (v / v total of the gaseous fluid extracted), of methane generally ranging from 70 90% (total v / v of the extracted gaseous fluid), dinitrogen generally ranging from 0.5 to 5% (total v / v of the extracted gaseous fluid).

An example of a gaseous fluid mixture comprises or essentially consists of dihydrogen, dinitrogen and methane, for example in the volume proportions of dihydrogen from 15 to 40% (v / v total of the gaseous fluid extracted), of methane generally ranging from 10 at 20% (total v / v of the extracted gaseous fluid), dinitrogen generally ranging from 40 to 60% (total v / v of the extracted gaseous fluid).

An example of a gaseous fluid mixture comprises or consists essentially of dihydrogen, dinitrogen and methane, for example in the volume proportions of dihydrogen from 50 to 80% (v / v total of the gaseous fluid extracted), of methane generally ranging from 5 at 15% (total v / v of the extracted gaseous fluid), dinitrogen generally ranging from 10 to 30% (total v / v of the extracted gaseous fluid).

An example of a gaseous fluid mixture comprises or essentially consists of dihydrogen, dinitrogen and methane, for example in the volume proportions of dihydrogen from 90 to 98% (v / v total of the gaseous fluid extracted), of methane generally ranging from 0 , 5 to 2% (total v / v of the extracted gaseous fluid), of dinitrogen generally ranging from 0.5 to 2% (total v / v of the extracted gaseous fluid).

Alternatively, the gas mixture may also include helium.

Typically, the flow rate of the gaseous mixture from an extraction device 30 has a flow rate of 5000 m3 / day to 30,000 m3 / day supplying the ammonia reactor 100.

Advantageously, the installation 1 and the method according to the present invention are not sensitive to the quantity of hydrogen available. For flows greater than 30,000 m3 / day, it will suffice to put several installations in series 1.

Advantageously, the installation 1 and the method according to the present invention avoid the use of excessively expensive hydrogen compression devices.

According to a variant, the installation 1 comprises a device 50 for purifying the dihydrogen extracted from the earth's subsoil upstream from the device for transforming dihydrogen into ammonia, for example the purification device 50 enriching the fluid (gas) purified in dihydrogen relation to the fluid (gas) extracted from the basement.

According to one embodiment, the installation 1 and the method according to the present invention comprise a pressure-modulated adsorption device (APM or PSA “Pressure Swing Adsorption” in English), preferably forming a device 50 for purifying the extracted dihydrogen underground soil, preferably located upstream of the device for converting dihydrogen into ammonia.

According to one embodiment, the installation 1 and the method according to the present invention comprise a compression device 70 (for example of the “skid compressor” type), typically disposed between the purification device 50 and the inlet to the loop with the NH ₃ reactor.

Alternatively, the installation 1 comprises a device for treating the purge gases 150 and in particular purged gaseous ammonia.

According to a variant, the installation 1 comprises a device 60 for purifying the air into nitrogen and supplying purified nitrogen to the device 10 for converting dihydrogen into ammonia, for example nitrogen originating from the fluid extracted from the subsoil or from an air storage tank 40 or ambient air. Alternatively, nitrogen is contained in the same fluid as dihydrogen, typically when the fluid is extracted from the subsoil.

According to one embodiment, the installation 1 comprises a system for purifying and / or transforming one or more compounds other than the dihydrogen contained in the fluid (gas) extracted from the subsoil, for example this other compound is methane and / or helium.

According to one embodiment, the installation 1 and the method according to the present invention comprise a methane vapor reforming device (SMR or “steam methane reforming” in English), if methane is present in sufficient quantity for its vapor reforming. A methane vapor reforming device is typically placed at the outlet of a pressure-modulated adsorption device, for example at the outlet of the device 50 according to FIG. 1.

Alternatively, the fuel cell 130 supplies an electrical network 140 other than the electrical network of the installation and / or one or more electricity storage units 142, for example electricity storage batteries.

Advantageously, the installation 1 is autonomous in electricity.

The invention also relates to an industrial process for producing ammonia and / or electricity, characterized in that it implements an installation 1 according to the invention.

According to a variant, said method comprises the supply of dihydrogen extracted from the earth's subsoil, the supply of dihydrogen to the device for transforming dihydrogen into ammonia (NH ₃ ) for the production of ammonia, the supply of a battery to ammonia fuel 130 produced by the transformation device 10, the production of electricity by the fuel cell 130, the electricity produced supplying at least said installation 1.

The invention also relates to a method for recovering dihydrogen, characterized in that the method comprises the implementation of an installation 1 according to the invention, or of a method according to the invention, or comprises in an industrial installation: the extraction of dihydrogen from the earth's subsoil and the production of ammonia from the extracted dihydrogen, and preferably the production of electricity from the ammonia produced and the supply of electricity produced at least from said industrial installation .

Advantageously, the present invention relates to installations 1 and industrial processes using hydrogen in the form of ammonia and / or electricity. Ammonia is advantageously used for the production of electricity in one or more dedicated fuel cells.

Alternatively, the power of the ammonia fuel cell 130 ranges from 100 to 700 kW.

According to one embodiment, the installation 1 and the method according to the present invention make it possible to produce ammonia in an amount of 1 to 5000 tonnes per year, and typically up to 1000 tonnes per year.

Alternatively, the ammonia can be stored in an ammonia storage tank upstream of the fuel cell. Thus, the ammonia can be stored before being circulated to the fuel cell.

According to a variant, the excess ammonia can be valued by its sale on the market 160. The ammonia can be sold for example on the spot or exported.

Advantageously, the present invention relates to industrial plants and processes which use hydrogen for electricity.

Alternatively, excess electricity can be valued by selling it on the market. Alternatively, excess electricity can power surrounding homes and / or industrial facilities. Thus, the invention is particularly interesting from the point of view of the economy and the development of a human ecosystem close to an installation according to the invention by producing electricity in isolated terrestrial areas, for example where the local people do not have access to electricity. The present invention therefore has an important humanitarian character.

For the purposes of starting the installation 1 and the method according to the invention, an electrical supply will generally be necessary. An electrical supply can be embodied by way of illustration by any source of electricity capable in particular of operating in an isolated environment, without connection to an existing electrical network. We are talking here about an external electrical energy source 170. This source can for example be a source of electricity from renewable energy such as for example photovoltaic modules, wind turbines, or if necessary a heat engine or even a battery with fuel, for example phosphoric acid ("Phosphoric acid fuel cells" (PAFC)).

Advantageously, a phosphoric acid fuel cell which converts hydrogen and air into electricity is not very sensitive to the purity of the hydrogen and can therefore also be used from the sub-terrestrial hydrogen source.

The start-up step of the installation 1 with electricity not generated by the installation is preferably limited in time and preferably implemented only for the time that the installation produces sufficient electricity to be autonomous in electricity, and during a drop in electricity production, if applicable.

According to a variant, when the installation 1 and the method according to the present invention are implemented, the external electrical energy source 170 no longer supplies electricity to the installation 1 and the method of the invention after the start-up step and the electricity required by the installation 1 and the method according to the present invention comes from the electricity generated by the installation 1 itself. Thus, the installation 1 and the method according to the present invention are autonomous or otherwise said to be self-sufficient.

According to a variant, the electrical power required to start the installation 1 is typically less than or equal to 100 kW. The start-up period of the installation 1 is generally less than 48 hours, preferably less than 24 hours and according to a particular embodiment less than 20 hours.

Thus, the present invention makes it possible to exploit and transform the hydrogen extracted from the earth's subsoil, in particular in remote areas, in particular without electrical installations.

According to the invention, the terms "installation", "device", "system" or "apparatus" are used interchangeably. However, the installation generally designates here installation 1 in general.

In the present invention, reference is made independently to the various elements by their reference number in the figures, without any limitation of the scope of the invention. References to an element with several reference numbers mean that the description applies generally and independently, but also in combination, to the element bearing the sign to which it is referred.

The invention will be better understood on reading the description which follows, given solely by way of example, and made with reference to the appended drawings in which:

FIG. 1 represents a general block diagram of an embodiment according to the invention. It is in no way limiting on the various embodiments of the invention.

The general diagram of Figure 1 consists of installation 1 with two blocks called ISBL 10 and OSBL 20 respectively for "Inside Battery Limit" or internal to the battery limits which advantageously allows the production of ammonia from dihydrogen and “Outside Battery Limit” or external to the limits of the battery, which advantageously allows the purification at least of the dihydrogen potentially not sufficiently purified and involved in the transformation according to the invention. To these two blocks 10,20 are added an external electrical energy source 170, an ammonia storage tank 120, a purification and / or recovery system (50,60) of other recoverable gases potentially associated with dihydrogen. (in particular helium and methane) and a fuel cell 130 operating with ammonia. Installation 1 comprises an inlet pipe for the fluid containing dihydrogen, nitrogen and helium, typically supplying the loop containing the NH ₃ reactor between the ammonia condenser 110 and the gas / liquid separator 80.

This fuel cell 130 partially, and preferably completely, replaces the external electrical energy source 170 (for example diesel generator) to supply electrical energy to the installation 1 after start-up. The excess electricity can be sold, for example via an electrical network 140, and / or stored, for example in batteries 142. If no solution is available for the excess electricity, then the ammonia produced is stored upstream of the stack 130 for later use, for example of a storage container 120.

The external electrical energy source 170 supplies the electrical power necessary for starting up the installation 1 which, once in operation, becomes autonomous. The external electrical energy source 170 can then no longer be used to supply electricity to installation 1. This external electrical energy source 170 typically has a power typically of 10 to 200 kW (ideally 100 kW). The external electrical energy source 170 can be for example a diesel generator 170 or a phosphoric acid fuel cell (PAFC), advantageously insensitive to impurities from the hydrogen fuel.

According to one embodiment, the NPO block 20 includes auxiliary gas treatment systems 60 for the separation of nitrogen from the air in the storage tank 40, the nitrogen being advantageously used in the transformation of the hydrogen, typically using the Haber Bosch process.

According to one embodiment, the system for purifying dihydrogen 50 can also comprise a system for separation and / or recovery of any other recoverable gas (helium, methane, nitrogen, etc.).

According to an advantageous embodiment, the ISBL block 10 represents a module for transforming hydrogen into ammonia with nitrogen originating either from the gas mixture originating from the subsoil and separated by the module 50, or typically from air. from the reservoir 40, and preferably coming from the nitrogen generator 60.

According to one embodiment, the ISBL 10 is supplied with one or more fluids containing dihydrogen and nitrogen. For example, the outlet fluids of the purifiers 50 and 60 are brought into contact before supplying the ISBL 10, for example before the compressor 70 in FIG. 1.

Other objects, characteristics and advantages of the invention will become apparent to those skilled in the art after reading the explanatory description which refers to examples which are given only by way of illustration and which cannot be in no way limit the scope of the invention.

The examples form an integral part of the present invention and any characteristic which appears new compared to any prior state of the art from the description taken as a whole, including the examples, forms an integral part of the invention in its function and in its generality.

Thus, each example is general in scope.

On the other hand, in the examples, the temperature is expressed in degrees Celsius unless otherwise indicated, and the pressure is atmospheric pressure, unless otherwise indicated.

Examples

As a reminder, the reaction mainly used for the transformation of dihydrogen into ammonia is as follows:

3H ₂ + N ₂ -> 2NH ₃

Preliminary remarks :

I kg of ammonia is formed from 176 g of H ₂ . (3 moles H ₂ = 6g to give 2 moles NH ₃ = 17 * 2 = 34 g). The ammonia reactor (for example NFuel® from Proton Ventures) is based on the Haber Bosch process. The reaction takes place between 300 ° C and 500 ° C and a pressure of 150 to 250 atmospheres (15-25 MPa). Its typical yield is 25% to 28%.

Energy must be supplied for the compression and heating of the gases. As for the chemical reaction, which is exothermic, this heat can be used to heat the gases in continuous mode.

For example, around 1000 kWh per tonne of ammonia produced (1 kWh per kg) is required. Most of this power is used to compress the gases because the heating consumes shortly after the start of the reaction (exothermic reaction).

Example 1:

In an installation according to FIG. 1, a gaseous mixture from an extraction device 30 is used with a flow rate of 5000 m3 / day to 30,000 m3 / day containing 10% of Hydrogen, 1% of nitrogen, 85 % methane and 4% helium. After PSA (Pressure Swing Adsorption 50) the methane is separated. The outgoing gas mixture is composed of 66.67% H ₂ , 6.66% nitrogen and 26.67% helium. The air 40 is passed into another PSA 60 to separate the nitrogen and to complete the mixture entering the ammonia reactor (3 volumes of hydrogen for one volume of nitrogen). The purified flow is sent to a device for converting H ₂ into NH ₃ 10 comprising an ammonia reactor 100 (for example NFuel®1, 4 or 20 from Proton Ventures with capacities of 120 kg / h, 415 kg / h and 2500 kg / h respectively). We choose the model adapted to the desired amount of ammonia (NFuel®1 for most cases and NFuel®4 in some cases). An electrical energy of 240 kWh, 721 kWh and 1442 kWh is respectively supplied per day of operation for flows of 5,000 to 30,000 m3 / day. The outlet gases are composed of NH ₃ , H ₂ and N ₂ which have not yet reacted and Helium which does not enter the reaction. The ammonia is condensed by cooling to -30 ° C and separated from the mixture. The gases are reinjected into the ammonia reactor 100 for a new reaction loop. Using a Proton Ventures NFuel®1 reactor which can produce up to 120 kg / h of ammonia, all of the hydrogen available in the first case of this example is consumed in 2 hours.

A 120 kW 170 diesel generator provides 240 kWh in 2 hours, for example, to consume all of the hydrogen and produce 240 kg of ammonia used in a 5 to 50 kW ammonia fuel cell operating continuously.

The energy value of ammonia is between 5.17 kWh / kg ("Low Heat Value") and 37.83 kWh / kg ("High Heat Value"). A 51.7 kW NH ₃ fuel cell in theory consumes 10 kg per hour with an efficiency of 100% and 20 kg / hour with an efficiency of 50% (Considering the low energy value).

The values are detailed in Table 1.

Example 2

In the same way as in Example 1, a gas mixture from an extraction device 30 is used with a flow rate of 5000 m3 / day to 30,000 m3 / day containing 30% hydrogen, 50% nitrogen , 15% methane and 5% helium. After PSA (Pressure Swing Adsorption 50) the methane is separated. The outgoing gas mixture is composed of 35.30% H ₂ , 58.82% nitrogen and 5.88% helium. The air 40 is passed into another PSA 60 to separate the nitrogen and complete the mixture entering the ammonia reactor 100. An electrical energy of 721 kWh, 2163 kWh and 4327 kWh per operating day is provided for the flow rates of 5,000 to 30,000 m3 / day.

The values are detailed in Table 2.

Example 3

In the same way as in Example 1, a gas mixture from an extraction device 30 is used with a flow rate of 5000 m3 / day to 30,000 m3 / day containing 70% hydrogen, 20% nitrogen , 8% methane and 2% helium. After PSA (Pressure Swing Adsorption 50) the methane is separated. The outgoing gas mixture is composed of 76.08% H ₂ , 21.74% nitrogen and 2.17% helium. The air 40 is passed through another PSA 60 to separate the nitrogen and complete the mixture entering the ammonia reactor 100. An electrical energy of 1683 kWh, 5048 kWh and 10096 kWh per operating day is provided for the flow rates of 5,000 to 30,000 m3 / day.

The values are detailed in Table 3.

Example 4

In the same way as in Example 1, a gas mixture from an extraction device 30 is used with a flow rate of 5000 m3 / day to 30,000 m3 / day contains 97% of Hydrogen, 1% of nitrogen , 1% methane and 1% helium. In this example, we can use the mixture as it is and add nitrogen 40 with PSA 60 from the air (3 volumes of hydrogen for one volume of nitrogen. We provide an electrical energy of 2332 kWh, 6995 kWh and 13,990 kWh per day of operation for flows from 5,000 to 30,000 m3 / day.

We use a more powerful 170 diesel generator in this case (or the cases with even more hydrogen). The most powerful commercial diesel generators deliver 1500 kW. The ammonia produced in this case would be 14,550 kg / day feeding a 1 MW fuel cell for approximately 38 hours.

The values are detailed in Table 4.

The installations and methods according to examples 1 to 4 therefore make it possible to convert H ₂ into NH ₃ with the advantages linked to NH ₃ , in particular in terms of energy density and storage, and to supply electricity to the installation in order to make electricity autonomous, especially if it is installed in an isolated environment.

CD m

GJ σι

NJ ω <D

WHERE £ *

C »ί»

CO w NS cc

M

m x <D 3

NJ On

w £ sJ O ® W Q w © S

O tf 'tn o o

Table 1 Flow rates (m3 / day ')

ΓΌ

CJ

O ω GJ co gj IXS <Al cc

O

FO ω

M jO ω s o

tn

C "<s

NJ ~ cn ® cn o

®s

ΓΟ in - »co in CÎ5 £ · “· ω 'ώ in

.fs Ο ω in m ο Γ0 ED 0Φ es e ^ j in <D

¢ 3 iis in

X · * ’> Λ? '3 ^ 4 · very Ο .. Q. αχ αχ £ Γ ÇT S ' s s VS .Γ7-. ! Free 2 Composition aaz î Table 2 | Ν8 S3 ο _Α _ω W Ο Η Ο · Α ο Ο '' X ro in o O o o (D. σ ω '3 ω CL Μ ... _t . fo en.-s en o XO O O ' Z rc "DD CT > "* F **, x ^ p O I „ _T. hj CT V. in ig · <Ο: O ' OJ SL Μ æ ο ο ... .s & ω © ago œ ο S ' X ΤΌ U, in s o S en ο ... O xp V-, _oo x Z ro ΓΟ _L s & 5 o G ' O X "Σ! S O o ^v 03 $ 5 Μ e © Ô3 Ο g 8 § 3? X N> CO o o o 5 en en h h5 ο θ \ jT o * · * ΓΌ KS os è w; ç: o -.c - ¹ 'o o' o X .Ai. o in 4? "O '? o ° CO sa

Γ-û

o cn o 8 to CD o io

in

0'1

CO in σ>

a ο sî ω

σι ω

CD co

ΓΟ Μ σι σι

Q. χ Q. CT :; τ £ Χ Q. Ο φ 'gr çr 3 3 ο.ο 00 __ * ^ ν 1 Example 4 Composition qaz | —I ® CF Φ ω c 4 " φ φ ... ί. φ ». Ν CO g CO * X ϋΐ, ρ 0 0 X M tn s 0 at CT " 3 ω Q. fO S 3 Z FC 1 \ Ύ M g 5 δ ** 0 X FO S-! k-ί ç ^ S. w Bt 2553 1 κ> '.JûèA. ·. · h5 in 0 0 0 • \ ' Φ jÿj φ δν Γ’3 '• χί ·.  & we ’. ^, X O X  - às-w 3. _s 0 œ BL 'V' φ φ ϊίΐ "3S <ο 'X ** 'C * φΓ s ïj '0 § °; X to ω § e »e> - U 'W' ^ * · ' ΛΑ g Z ro „<O> 'X '. O ’o> S JS O X <ϊ ^: · · ^ΙΓ \ Cfljw 8 3S: CJJ SL

σι

Claims (16)

1. -Industrial installation (1) for transformation of dihydrogen (H ₂ , also called hydrogen), characterized in that the installation (1) comprises at least one supply pipe for fluid extracted from the earth's subsoil, typically a gas containing dihydrogen, said line supplying a device for converting (10) dihydrogen into ammonia (NH ₃ ) for the production of ammonia, said produced ammonia being directed to at least one supply line for at least one reservoir storage of ammonia in liquid form. 2. - Installation according to claim 1, characterized in that the installation comprises at least one NH ₃ 130 fuel cell producing electricity, and a supply line for the NH ₃ 130 fuel cell from the tank ammonia. 3. - Installation according to claim 2, characterized in that said NH ₃ fuel cell (130) produces electricity and supplies electricity to at least said installation 1. 4. - Installation according to claim 1, characterized in that the installation comprises at least one source of electricity which is not generated from hydrocarbon, such as for example from a fuel cell, for example a hydrogen fuel cell, an ammonia gas turbine, a photovoltaic device, a wind turbine, a device using geothermal energy, tidal power, wave energy, a tidal turbine, or even biomass. 5. - Installation according to claim 2, 3 or 4, characterized in that the installation (1) is self-sufficient in electrical consumption by the electricity produced by the NH ₃ fuel cell (s) (130) and / or the source electricity that is not generated from hydrocarbon. 6. - Installation according to any one of claims 1 to 5, characterized in that the device (10) for converting dihydrogen into ammonia comprises a gas / liquid separator (80), a recycling compressor (90), a reactor transformation 100 of dihydrogen into ammonia, an ammonia condenser (110), and preferably a storage tank (120) of the ammonia produced. 7. - Installation according to any one of claims 1 to 6, characterized in that the installation (1) comprises at least one extraction device (30) of a fluid, typically a gas, containing dihydrogen from under - ground floor. 8. - Installation according to any one of claims 1 to 7, characterized in that the installation (1) comprises a device for treating the purge gases 150 and in particular purged gaseous ammonia. 9. - Installation according to any one of claims 1 to 8, characterized in that the installation (1) comprises a device for purifying (50) of the dihydrogen extracted from the ground underground upstream of the device for transforming dihydrogen into ammonia, for example the purification device (50) enriching the fluid (gas) purified in dihydrogen relative to the fluid (gas) extracted from the subsoil. 10. - Installation according to any one of claims 1 to 9, characterized in that the installation (1) comprises a device for purifying (60) the air into nitrogen and supplying the device (10) with purified nitrogen transformation of dihydrogen into ammonia, for example nitrogen coming from the fluid extracted from the basement or from an air storage tank (40) or from ambient air. 11. - Installation according to any one of claims 1 to 10, characterized in that the installation (1) comprises a system for purifying and / or transforming one or more compounds other than the dihydrogen contained in the fluid ( gas) extracted from the subsoil, for example this other compound is methane and / or helium. 12. - Installation according to any one of claims 2 to 11, characterized in that the fuel cell (130) supplies an electrical network (140) other than the electrical network of the installation and / or one or more units of electricity storage (142), for example electricity storage batteries. 13. - Installation according to any one of claims 1 to 12, characterized in that the installation (1) is autonomous in electricity. 14, - Industrial process for producing ammonia and / or electricity, characterized in that it implements an installation (1) as defined in any one of claims 1 to 13. 5 15. Industrial process for the production of ammonia and / or electricity according to claim 14, characterized in that said process comprises the supply of dihydrogen extracted from the earth's subsoil, the supply of dihydrogen to the dihydrogen transformation device in ammonia (NH ₃ ) for the production of ammonia, the supply of a fuel cell with ammonia (130) produced by the transformation device (10), the production of electricity by the fuel cell (130 ), the electricity produced supplying at least said installation 1. 16.- Method for upgrading dihydrogen, characterized in that the method comprises the use of an installation (1) as defined in any one of Claims 1 to 13, or of a method according to Claim 14 or 15, or includes in an industrial installation: the extraction of dihydrogen from the earth's subsoil and the production of ammonia from the extracted hydrogen, and preferably the production of electricity from the ammonia produced and l electricity supply produced at least from said industrial installation.