WO2014207279A1 - Method for producing synthesis gas - Google Patents

Abstract

The invention relates to a method for producing synthesis gas (H₂/CO), in a controllable ratio, by means of a catalytic and electrochemical process which uses an electrochemical cell formed by ionic, anionic or cationic conductive solid electrolytes. The H₂/CO ratio is controlled in a single step under constant operating conditions, i.e. at a constant temperature of the electrochemical cell, and constant conditions of composition and concentration of the inflow current. In the present invention, the inflow current is selected from a current of light hydrocarbons and a water vapour current, or a gaseous current containing at least one alcohol (C₁-C₃).

Description

 PROCEDURE TO OBTAIN GAS FROM SYNTHESIS

DESCRIPTION

The present invention relates to a process for obtaining synthesis gas (H ₂ / CO) with a controllable ratio by means of a catalytic and electrochemical process using an electrochemical cell formed by anionic or cationic conductive solid electrolytes. The control of the H ₂ / CO ratio is carried out in a single stage under constant operating conditions, that is, at a constant temperature of the electrochemical cell and constant conditions of composition and concentration of the input current.

Therefore, the present invention is encompassed in the technical field of synthesis gas production and for its use in the petrochemical industry or in the production of fuels.

STATE OF THE PREVIOUS TECHNIQUE

The synthesis gas (mixture of H ₂ / CO) is known to have a wide variety of applications in the petrochemical industry. For example, synthesis gas can be used in the production of ammonia or methanol. In addition, synthesis gas can be used as an intermediate product in the production of synthetic gasolines, for use as fuel or lubricant through the Fischer-Tropsch synthesis. For these applications the required H ₂ / CO ratio is typically 2. However, there are other processes within the petrochemical industry such as oxo-synthesis processes that require lower H ₂ / CO ratios, between 1 and 2, or even pure carbon monoxide (CO), as occurs in carbonylation processes. On the other hand, in the petrochemical industry there are also many processes where hydrogen (H ₂ ) of high purity is required, such processes are for example reactions of hydrogenation, interesting in this case to obtain an H ₂ / CO ratio greater than 2, as high as possible.

The synthesis gas is generally obtained at the industrial level by catalytic processes of reforming or partial oxidation of hydrocarbons, mainly from methane (EP0168892 A2). This type of process allows obtaining a fixed H ₂ / CO ratio and typically of 3. In order to obtain a different H ₂ / CO ratio, additional purification, separation and conversion steps are necessary, such as: water displacement reactions in gaseous state ( denominated in English water gas shift), processes of adsorption under pressure or preferential oxidation of CO. These additional stages, prior to the synthesis process, imply a greater complexity of the process as well as higher production costs of the final product.

Another known possibility of varying the H ₂ / CO ratio in a controlled manner is carried out by the controlled addition of pure oxygen (O ₂ ) to the atmosphere where the synthesis reaction is carried out [Cao, Y. et al. Fuel. 2008, 22, 1720-1730], where a partial oxidation or autothermal reforming occurs that modifies the CO concentration produced. The addition of pure O ₂ in this type of processes implies previous and additional stages of nitrogen separation (N ₂ ) from the air that implies a greater complexity of the process, by adding more stages to the process. On the other hand, the H ₂ / CO ratio can be controlled in these processes by adjusting the operating conditions such as the temperature at which the synthesis is carried out or the relationship between the starting hydrocarbon and the added O ₂ . The complexity and costs of these processes are high because the temperatures used are usually high, greater than 1000 ° C and reactors of two gas inlets and two gas outlets are required to work in double atmosphere [US47993904].

Therefore, to overcome all the technical problems mentioned, it is necessary to develop a new synthesis gas synthesis process. Controllable ratio of H ₂ / CO.

DESCRIPTION OF THE INVENTION

The present invention relates to a process for obtaining synthesis gas (H ₂ / CO) with a controllable ratio by means of a catalytic and electrochemical process using an electrochemical cell formed by ionic, anionic or cationic conductive solid electrolytes. The control of the H ₂ / CO ratio is carried out under constant conditions of operation, that is, at constant temperature of the electrochemical cell and constant conditions of composition and concentration of the input current.

In the present invention, the inlet stream is selected from a gaseous stream of light hydrocarbons together with a stream of water vapor, or a gaseous stream containing at least one (C 1 -C 3) alcohol.

By "light hydrocarbons" is meant those organic chemical compounds formed solely of hydrogen and carbon (C1-C4), including natural gas.

Natural gas is a combustible gas that comes from geological formations, which is why it constitutes a non-renewable energy source. In addition to methane, natural gas can contain carbon dioxide, ethane, propane, butane and nitrogen, among other gases.

Therefore, in the present invention, the light hydrocarbons are selected from the list comprising methane, ethane, propane, butane, natural gas or any combination thereof.

In the case where the solid electrolyte conductor is an anionic conductive material, for example oxygen ion conductor (O ^{2 "} ), in the present invention it comprises at least one electrode selective for the electrolysis of the water and at least one selective counter electrode to the reforming reaction and to the partial oxidation of the input current of the electrochemical cell.

Therefore, in the present invention, when anionic conductors are used, the addition of gaseous streams of humidified hydrocarbons or of alcoholic gas streams, together with or without a stream of water vapor, will allow in addition to the synthesis gas obtained by conventional catalytic reforming in the electrochemical catalyst will produce additional electrocatalytic processes that allow to control the final H2 / CO ratio under constant conditions, that is, at constant temperature of the electrochemical cell and constant conditions of composition and concentration of the input current. These additional processes are mainly the process of water vapor electrolysis (H ₂ O -> H ₂ + O ^{2 "} ) that allows to produce a greater amount of H ₂ and the electrochemical and catalytic oxidation of the hydrocarbon or alcohol that has not reacted and of the CO produced from the O ^{2 "} ions and the O ₂ molecules, both generated in the previous electrolysis process. In this way, the final adjustment of the H ₂ / CO ratio is carried out in a single stage. The additional H ₂ produced in the electrolysis process as well as the oxidation of part of the produced CO to carbon dioxide (CO ₂ ) allows to modify considerably the synthesis gas ratio.

Therefore, when the electrochemical cell is at a temperature between 300 ° C and 980 ° C, and under constant conditions of composition and concentration of the input current, the catalytic process of reforming on the selective counter electrode takes place. process. Additionally, under the application of electric current, the electrolysis reaction occurs with the consequent production of H ₂ . Simultaneously, the O ² ions generated in the electrochemical reaction are transported by the solid electrolyte conductor to the counter electrode that acts as a catalyst for the electrocatalytic oxidation of the inlet current and CO with the consequent production of synthesis gas (H ₂ / CO In addition part of the CO, can be oxidized to CO ₂ by electrochemical oxidation, which allows a net control of the H ₂ / CO ratio of the synthesis gas produced by controlling the speed of each of the processes with the electrical intensity. It is the intensity of applied voltage that allows controlling the electrochemical speed of the mentioned processes.

In the case that the solid electrolyte conductor is a cationic conductive material, for example sodium ion conductor Na ⁺ and potassium K ⁺ , in the present invention it comprises a selective catalyst electrode to the process of reforming the inlet current of the cell electrochemistry and a metallic counter electrode. This configuration allows the process of reforming the input current to be promoted electrochemically, by sending promoter ions from the cationic conductive material to the selective electrode of the reforming process.

In this way, through the known phenomenon of electrochemical promotion of heterogeneous catalysts or NEMCA effect (from the English acronym Non Faradaic Electrochemical Modification of Catalytic Activity), the presence of electro-positive ions for example of Na ⁺ and K ⁺ ions in the catalytic electrode favors chemisorption of electronegative molecules such as water versus hydrocarbon or alcohol that form the input stream. In the present invention, the controllable adsorption of the inlet current is carried out by varying the electric potential that varies the content of the promoter sent to the catalyst electrode, making it possible to control the degree of decomposition of the inlet current and the degree of the reforming process, with it the H ₂ / CO ratio of the resultant synthesis gas obtained.

In the case of using, in the present invention, a solid cationic electrolyte conductor (Na ⁺ or K ⁺ conductor), the final adjustment of the H ₂ / CO ratio is produced by the sending of ionic promoters (Na ⁺ or K ⁺ ) by current electrical to the catalytic electrode that modify the adsorption of water in the active centers and with it the kinetics of the catalytic process. This occurs under a constant concentration of the input current and a specific operating temperature of the electrochemical cell.

Therefore, the main advantages with respect to conventional reforming techniques is, firstly, that it is not necessary to incorporate a pure 0 ₂ current in the electrochemical cell since it is produced in situ during the electrolysis process, avoiding this mode additional pre-stages such as for example the additional preliminary separation of N ₂ from the air.

In the present invention, in addition to the synthesis gas obtained by conventional catalytic reforming in the electrochemical catalyst, additional electrocatalytic processes are produced which allow the H ₂ / CO ratio to be controlled, that is, in a single stage synthesis gas of H ₂ ratio is produced / Controllable CO.

In addition, the electrochemical cell that can be used is simple, does not require complex atmospheric separation chambers. In the present invention, the control of the H ₂ / CO ratio is carried out by means of a variation of the voltage applied to the electrodes that allows the control of the electrochemical processes. The operating conditions are constant, the synthesis is carried out at a constant temperature and at a low temperature in comparison with those used in conventional techniques.

The inlet stream is not only limited to wet gaseous light hydrocarbons, gaseous streams of pure or moist alcohols can also be used.

Therefore, a first aspect of the invention relates to a process for producing synthesis gas, of controllable H ₂ / CO ratio, comprising the passage of an input current selected from a gaseous stream of light hydrocarbons and a stream of water vapor, or a gaseous stream containing at least one (C1-C3) alcohol to an electrochemical cell which is at a temperature between 300 ° C and 980 ° C, characterized in that said electrochemical cell contains a solid electrolyte conductor ion to which a potential between -3 and +3 volts is applied.

By "electrochemical cell" is meant in the present invention a device capable of transforming an electric current into a chemical oxidation-reduction reaction that does not occur spontaneously. The electrochemical cell also refers in the present invention to an electrochemical reactor suitable for industrial use in any configuration known to any person skilled in the art, such as, for example, an electrochemical reactor with a tubular or monolithic configuration.

Preferably the inlet stream does not contain pure O2.

Preferably, the inlet stream is diluted in an inert gas stream, where the inert gas is selected from the list comprising nitrogen (N ₂ ), helium (He), neon (Ne), argon (Ar), krypton (Kr). ) and xenon (Xe). Preferably the inert gas stream is N ₂ . The inlet stream can be diluted up to 98% by volume in said inert gas stream.

In a preferred embodiment, the electrochemical cell is at a temperature between 500 ° C and 900 ° C.

In another preferred embodiment, the applied potential is between -2.5 and +2.5 volts. More preferably, between -2 and +2 volts.

Preferably, in the present invention the gaseous light hydrocarbons are selected from the list comprising methane, ethane, propane, butane, natural gas or any combination thereof. In a more preferred embodiment the light hydrocarbon is a combination of light hydrocarbons comprising at least methane. In another preferred embodiment, the light hydrocarbon is natural gas.

The proportion of light hydrocarbon and water vapor depends on the hydrocarbon used, for example, in case the hydrocarbon is methane, the preferred ratio will be about 1: 3.

Preferably, in the present invention the alcohol is selected from the list comprising methanol, ethanol, propanol or any combination thereof. More preferably, the alcohol is methanol or ethanol.

In the present invention, the alcohols can be bioalcohols obtained by the action of a microorganism or by some other biotechnological process. For example, alcohols can be used from residual streams of alcohols with high graduation, up to 90 ° C.

In another preferred embodiment, in addition to the gas stream containing at least one (C 1 -C 3) alcohol, a stream of water vapor is added.

The gaseous inlet streams of hydrocarbons or of alcohol and water vapor can be mixed before passing into the electrochemical cell or they can pass without previously mixing.

 Preferably the gaseous hydrocarbon or alcohol streams and the water vapor stream are mixed before passing to the electrochemical cell.

On the other hand, in a preferred embodiment, the solid ionic electrolyte conductor is an anionic conductor that conducts oxygen ions (O2 ^" ).

In another preferred embodiment, the anionic conductor comprises a solid electrolyte selected from zirconium oxide, titanium oxides, yttrium oxide stabilized with zirconium oxide, zirconium oxide stabilized with calcium, perovskites with mixed conductivity or any combination thereof .

Furthermore, preferably, the anionic conductor comprises at least one electrode selective to the electrolysis of water and at least one counter-electrode selective to the reforming reaction and to the process of partial oxidation of the Input current.

In another preferred embodiment, the electrode selective to the electrolysis of water is platinum (Pt).

Preferably, the selective counter-electrode to the reforming reaction of the input stream is selected from nickel (Ni), platinum (Pt), palladium (Pd) or any combination thereof.

In another preferred embodiment, the electrochemical cell containing an anionic conductor as described above is at a temperature of between 700 and 900 ° C when the inlet stream is a gaseous stream of light hydrocarbons and a stream of water vapor.

In another preferred embodiment, the electrochemical cell containing an anionic conductor as described above is at a temperature of between 500 and 750 ° C when the inrush current is a gaseous stream containing at least one (C1-C3) alcohol.

On the other hand, in another preferred embodiment, the solid ionic electrolyte conductor is a cationic conductor. The inlet stream in this case is also formed by a gaseous stream of light hydrocarbons and a stream of water vapor, or a gaseous stream containing at least one alcohol (dC 3). However, in the case where the cationic ionic electrolyte conductor is to be used, the gas stream containing at least one (C1-C3) alcohol must also contain a stream of water vapor.

Preferably, the cationic conductor conducts sodium ions Na ⁺ or potassium K ⁺ .

In another preferred embodiment, the cationic electrolyte is selected from Na-β-0 ₂ 0 ₃ , Κ-β-ΑΙ ₂ 0 ₃ , NASICON, LISICON or any combination thereof. In another preferred embodiment, the cationic conductor further comprises at least one metal electrode selective to the process of reforming the inlet stream and at least one metal counter electrode.

Preferably, the metallic electrode selective to the process of reforming the input current is platinum (Pt).

Preferably, the metal counter electrode is gold (Au).

In another preferred embodiment, the electrochemical cell, containing a cationic conductor as described above, is at a temperature between 700 and 900 ° C when the inlet current is a gaseous stream of light hydrocarbons and a stream of water vapor .

In another preferred embodiment, the electrochemical cell, containing a cationic conductor as described above, is at a temperature between 500 and 750 ° C when the inlet current is a gas stream containing at least one (C1-C3) alcohol ) and that adds a stream of water vapor.

The voltage source used to apply the aforementioned voltage to the electrochemical cell can be a conventional source with fossil or nuclear energy origin or a renewable source using, for example, hydraulic, solar, wind, geothermal, marine and / or biomass energy . So, finally, in a preferred embodiment, the method uses a conventional or renewable source for the application of the potential. More significantly, the procedure uses a conventional source.

Throughout the description and the claims the word "comprises" and its variants do not intend to exclude other technical characteristics, additives, components or steps. For those skilled in the art, other objects, advantages and characteristics of the invention will be derived in part from the description and in part of the practice of the invention. The following examples and figures are provided by way of illustration, and are not intended to be limiting of the present invention.

BRIEF DESCRIPTION OF THE FIGURES

FIG. one . Representation of an electrochemical cell that uses an ionic solid electrolyte conductor, which can be both anionic and cationic.

FIG. 2. Schematic representation of a solid electrolyte conductor acting as an anionic conductor comprising an anionic solid electrolyte, an electrode selective to the electrolysis of water and a counter electrode selective to the reforming reaction and to the partial oxidation of the input current.

FIG. 3. Variation of the H2 / CO ratio as a function of the applied potential for different reaction temperatures. Conditions: [CH ₄ ] = 1%, [H ₂ 0] = 3%, [N ₂ ] = 96%, F = 100 ml / min, with anionic conductor.

FIG. 4. Dynamic graph showing the different H ₂ / CO ratios obtained according to the applied potential in a given period of time

FIG. 5. Schematic representation of a solid electrolyte conductor acting as a cationic conductor comprising a cationic solid electrolyte, a metal electrode selective to the process of reforming the input current and a metal counter electrode.

FIG. 6. Variation of the H ₂ / CO ratio as a function of the applied potential for different reaction temperatures. Conditions: [CH] = 1%, [H ₂ 0] = 3%, [N ₂ ] = 96%, F = 100 ml / min, with cationic conductor. FIG. 7. Variation of the H ₂ / CO ratio as a function of the applied potential for different reaction temperatures. Conditions: [CH ₃ OH] = 0.7%, [H ₂ 0] = 2%, [N ₂ ] = 97,3%, F = 100 ml / min, with anionic conductor.

EXAMPLE

FIG. one . shows the configuration of a laboratory electrochemical cell that uses ionic solid electrolyte conductors, both anionic (9) and cationic (10). This cell consists of the following elements:

(1) Working electrode

 (2) Counter electrode

 (3) Gas outlet

 (4) Metal lid

 (5) Cooling coil

 (6) Perforated alumina tube

 (7) Gold threads

 (8) Quartz tube

 (9) Solid anionic electrolyte conductor

 (10) Cationic solid electrolyte conductor

 (1 1) Gas inlet

In the electrochemical cell shown in FIG. 1, the anionic (9) and cationic solid electrolyte conductors (10) are inside the quartz tube (8) that limits the area where the H ₂ / CO controlled synthesis gas is produced and the additional electrocatalytic processes in phase soda. This quartz tube (8) is closed by a metal cover (4) that couples a perforated alumina tube (6). The working electrode (1) and the counter electrode (2) are connected with the anionic (9) or cationic (10) solid electrolyte conductors through this perforated alumina tube (6), the potential is applied to these electrodes (1 ) and (2). The different temperatures that are reached in the cell electrochemistry are achieved by the cooling coil (5) coupled to the metal cover (4) and by gold wires (7) that act as thermal conductors and that are introduced into the cell through the alumina tube. The input current is introduced through the gas inlet (11) and the synthesis gas produced is collected through the gas outlet (3).

Example 1 :

In this first example, to produce control gas of synthesis ratio an electrochemical cell was used as shown in FIG. one . comprising an anionic solid electrolyte conductor such as that shown in FIG. two.

The solid anionic electrolyte conductor shown in FIG. 2. It consists of the following elements:

(12) Selective counter electrode to the reforming process and partial oxidation of the input current (for example CH ₄ → CH ₂ , CO, C0 ₂ ) is platinum (Pt)

(13) Selective electrode for water electrolysis (H ₂ 0 + 2e ^" → H ₂ ) is platinum (Pt)

(14) Anionic solid electrolyte type YSZ (yttrium oxide stabilized with zirconium oxide)

FIG. 2. shows a schematic representation of an anionic conductor comprising an anionic solid electrolyte which acts as a YSZ-type conductor of O ^{2 "} ions and which further comprises a working electrode selective to the electrolysis of water (13) and a selective counter-electrode to the reforming reaction and partial oxidation of the input stream (12).

Both electrodes are connected to a power supply that allows the application of electrical intensity to the system and, therefore, allows the control of the composition of the synthesis gas under fixed conditions of operation (operating temperature of the electrochemical cell) and reaction (composition and concentration of the input current of the electrochemical cell).

The coupling of the electrolysis process to the catalytic reforming process allows to carry out the additional production of H ₂ as well as the partial oxidation of the hydrocarbon (and therefore the adjustment of the ratio) without the need to feed pure oxygen to the electrochemical reactor (avoiding previous stages). of separation of the same from the air). The 0 ₂ is generated in-situ in the process itself, which allows the presence of secondary reactions of total and partial oxidation.

To carry out the production of synthesis gas of variable ratio using this electrochemical cell and the anionic solid electrolyte described, an input stream composed of methane [CH ₄ ] = 1%, water vapor [H ₂ 0] = was introduced 3% and nitrogen as inert gas [N ₂ ] = 96%, the flow rate of this stream being F = 100 ml / min.

In FIG. 3. It can be observed how the H ₂ / CO ratio obtained can be varied depending on the potential and the different reaction temperatures applied. This figure shows that the voltage variation allows control of the H ₂ / CO ratio. The H ₂ / CO ratio values obtained in this electrochemical cell comprising an anionic solid electrolyte conductor range between 1, 5 and 1 1 for a temperature range between 750 ° C and 800 ° C.

On the other hand FIG. 4. shows the ratios of H ₂ , CO and C 0 ₂ versus the time obtained using the configuration of the electrochemical cell described in this example. The word OCP refers to the state of the open circuit in which the electrochemical cell is located when no potential is applied. During the periods of time during which the electrochemical cell is in open circuit, the H ₂ / CO ratio remains practically constant. In the periods of time where a potential of 2.5 volts is applied, an immediate response is observed, less than 5 minutes, which corresponds to the drastic increase in the H2 / CO ratio as a function of the applied voltage.

Example 2:

In this example an electrochemical cell is used as shown in FIG. one . with a solid cationic electrolyte conductor as shown in FIG. 5. to produce synthesis gas.

The cationic solid electrolyte shown in Figure 5 consists of the following elements:

(15) Electrode working platinum selective to the process of reforming the input current (for example CH ₄ + H ₂ 0 → H ₂ , CO, C0 ₂ )

 (16) Au counter electrode

(17) Cationic solid electrolyte type Na-P-AI ₂ 03

FIG. 5. shows a schematic representation of a cationic solid electrolyte (17) which acts as conductive type Na-p-AI ₂ 03 Na ⁺ and comprising a selective electrode reforming process stream inlet (15) and Au counter-electrode (16).

As in example 1, the electrodes are connected to a power supply that allows the application of the electrical intensity to the system and, therefore, allows the control of the composition of the synthesis gas under fixed conditions of operation (temperature of operation of the electrochemical cell) and reaction (composition and concentration of the input current of the electrochemical cell).

To carry out the production of variable ratio synthesis gas using the electrochemical cell and the described anionic solid electrolyte, a input current composed of methane [CH ₄ ] = 1%, water vapor [H ₂ 0] = 3% and nitrogen as inert gas [N ₂ ] = 96%, the flow rate of this stream being F = 100 ml / min.

The control of the quantity of sodium ions Na ⁺ promoters sent to the catalyst electrode is carried out by means of the controlled application of electric current that allows to control the adsorption of the species that participate in the catalytic process and therefore the ratio of synthesis gas produced .

In FIG. 6. The variation of the H ₂ / CO ratio is shown as a function of the applied potential for different reaction temperatures from a humidified methane stream. This figure shows that the voltage variation allows control of the H ₂ / CO ratio. The H ₂ / CO ratio values obtained in this electrochemical cell comprising a solid cationic electrolyte conductor range between 6 and 30 for a temperature range between 450 ° C and 550 ° C.

Example 3:

In this example an electrochemical cell is used as shown in FIG. one . with the solid anionic electrolyte conductor that is described in example 1 and is depicted in FIG. 2 to produce synthesis gas.

To carry out the synthesis gas production with a controllable ratio using this electrochemical cell and the described anionic solid electrolyte, an inlet stream composed of methanol [CH ₃ OH] = 0.7%, water vapor [H _{2] was introduced.} 0] = 2% and nitrogen as inert gas [N ₂ ] = 97.3%, the flow rate of this stream being F = 100 ml / min.

In FIG. 7. It can be observed how the H ₂ / CO ratio obtained can be varied depending on the potential and the different reaction temperatures applied. This figure shows that the voltage variation allows control of the H ₂ / CO ratio. The H ₂ / CO ratio values obtained in this electrochemical cell comprising an anionic solid electrolyte conductor range between 2.4 and 9.13 for a temperature range between 500 ° C and 600 ° C. Examples 1 to 3 provided by way of illustration are not intended to be limiting of the present invention. Although they refer to a laboratory-sized electrochemical cell, this cell could be replaced by tubular configurations or monolithic reactor-type configurations (called Monolithic Electro-promoted reactor) on an industrial scale.

Claims

one . A process for producing synthesis gas, of controllable H ₂ / CO ratio, comprising the passage of an input stream selected from a gaseous stream of light hydrocarbons and a stream of water vapor, or a gaseous stream containing at least an alcohol (C1-C3) to an electrochemical cell which is at a temperature between 300 ° C and 980 ° C, characterized in that said electrochemical cell contains an ionic solid electrolyte conductor to which a potential of between -3 and +3 volts. 2. The process according to claim 1, wherein the inlet stream is diluted in an inert gas stream selected from the list comprising nitrogen, helium, neon, argon, krypton and xenon. 3. The method according to any of claims 1 or 2, wherein the electrochemical cell is at a temperature between 500 ° C and 900 ° C. 4. The method according to any of claims 1 to 3, wherein the applied potential is between -2.5 and +2.5 volts. 5. The method according to claim 4, wherein the applied potential is between -2 and +2 volts. 6. The process according to any of claims 1 to 5, wherein the gaseous light hydrocarbons are selected from the list comprising methane, ethane, propane, butane, natural gas or any combination thereof. The method according to claim 6, wherein the light hydrocarbon is a combination of light hydrocarbons comprising at least methane or natural gas. 8. The process according to any of claims 1 to 5, wherein the alcohol is selected from the list comprising methanol, ethanol, propanol or any combination thereof. 9. The process according to claim 8, wherein the alcohol is methanol or ethanol. 10. The process according to any of claims 1 to 5, 8 or 9, wherein in addition to the gas stream containing at least one (C1-C3) alcohol, a stream of water vapor is added. eleven . The process according to any of claims 1 to 10, wherein the gaseous hydrocarbon or alcohol streams and the water vapor stream are mixed before passing to the electrochemical cell. The method according to any of claims 1 to 11, wherein the ionic solid electrolyte conductor is an anionic conductor that conducts oxygen ions. The method according to claim 12, wherein the anionic conductor comprises a solid electrolyte selected from zirconium oxide, titanium oxides, yttrium oxide stabilized with zirconium oxide, zirconium oxide stabilized with calcium, perovskites with conductivity mixed or any of its combinations. The method according to any of claims 12 or 13, wherein the anionic conductor comprises at least one electrode selective to the electrolysis of the water and at least one selective counter electrode to the reforming reaction and to the partial oxidation of the input stream. 15. The method according to claim 14, wherein the electrode selective to the electrolysis of water is platinum. 16. The process according to any of claims 14 or 15, wherein the porous catalytic counter electrode selective to the reforming reaction and the partial oxidation of the inlet stream is selected from nickel, platinum, palladium or any combination thereof. 17. The method according to any of claims 12 to 16, wherein the electrochemical cell is at a temperature between 700 and 900 ° C when the inlet stream is a gaseous stream of light hydrocarbons and a stream of water vapor. 18. The method according to any of claims 12 to 16, wherein the electrochemical cell is at a temperature between 500 and 750 ° C when the inlet stream is a gaseous stream containing at least one (C1-C3) alcohol . 19. The method according to any of claims 10 or 11, wherein the ionic solid electrolyte conductor is a cationic conductor. 20. The process according to claim 19, wherein the cationic conductor conducts sodium ions Na ⁺ or potassium K ⁺ . twenty-one . The method according to any of claims 19 or 20, wherein the cationic conductor comprises a solid electrolyte that is selected from Na-p-AI ₂ 0 ₃ , Κ-β-ΑΙ ₂ 0 ₃ , NASICON, LISICON or any of its combinations 22. The method according to any of claims 19 to 21, wherein the cationic conductor further comprises at least one metal electrode selective to the process of reforming the inlet stream and at least one metal counter electrode. 23. The method according to claim 22, wherein the metal electrode selective to the process of reforming the input stream is platinum. 24. The method according to any of claims 22 or 23, wherein the metal counter electrode is gold. 25. The method according to any of claims 19 to 24, wherein the electrochemical cell is at a temperature between 700 and 900 ° C when the inlet stream is a gaseous stream of light hydrocarbons and a stream of water vapor. 26. The method according to any of claims 19 to 24, wherein the electrochemical cell is at a temperature between 500 and 750 ° C when the inlet stream is a gaseous stream containing at least one (C1-C3) alcohol and a stream of water vapor. 27. The method according to any of claims 1 to 26, wherein a conventional or renewable source is used for the application of the potential.