JPWO2013145782A1 - Electrochemical reduction apparatus and method for producing hydrogenated product of aromatic hydrocarbon compound or nitrogen-containing heterocyclic aromatic compound - Google Patents

Abstract

The electrochemical reduction device 10 includes an electrode unit 100, a power control unit 20, an organic matter storage tank 30, a water storage tank 40, a steam / water separation unit 50, and a control unit 60. The electrode unit 100 includes an electrolyte membrane 110, a reduction electrode 120, and an oxygen generation electrode 130. The electrolyte membrane 110 is formed of an ionomer. The reduction catalyst used for the reduction electrode 120 contains at least one of Pt and Pd. The oxygen generating electrode 130 includes a noble metal oxide-based catalyst such as RuO 2 or IrO 2. When the control unit 60 represents the potential at the reversible hydrogen electrode as VHER, the standard oxidation-reduction potential of the aromatic hydrocarbon compound or the nitrogen-containing heterocyclic aromatic compound as VTRR, and the potential of the reduction electrode 120 as VCA, VHER-20 mV. The power control unit 20 is controlled so as to satisfy the relationship of ≦ VCA ≦ VTRR.

Description

  The present invention relates to an apparatus and method for electrochemical hydrogenation of an aromatic hydrocarbon compound or a nitrogen-containing heterocyclic aromatic compound.

  Cyclic organic compounds such as cyclohexane and decalin are known to be obtained efficiently by hydrogenating the corresponding aromatic hydrocarbon compounds (benzene, naphthalene) using hydrogen gas. Since this reaction requires high-temperature and high-pressure reaction conditions, it is not suitable for small- to medium-scale production. On the other hand, the electrochemical reaction using an electrolytic cell does not need to handle gaseous hydrogen because water can be used as a hydrogen source, and the reaction conditions are relatively mild (normal temperature to about 200 ° C., normal pressure). ) Is known to proceed.

JP 2003-045449 A JP 2005-126288 A JP 2005-239479 A

Masaru Ichikawa, J.H. Jpn. Inst. Energy, 85, 517 (2006)

  As an example of electrochemical nuclear hydrogenation of aromatic hydrocarbon compounds such as toluene, toluene vaporized in the form of gas is sent to the reduction electrode side, and the configuration is similar to water electrolysis, without passing through the state of hydrogen gas In addition, a method for obtaining methylcyclohexane, which is a nuclear hydride, has also been reported (see Non-Patent Document 1), but the amount of material (current density) that can be converted per electrode area and time is not large, and industrially aromatic carbonization. It was difficult to nucleate hydrogen compounds.

  The present invention has been made in view of these problems, and an object thereof is to provide a technique capable of electrochemically nuclear hydrogenating an aromatic hydrocarbon compound or a nitrogen-containing heterocyclic aromatic compound with high efficiency. It is in.

One embodiment of the present invention is an electrochemical reduction device. The electrochemical reduction apparatus includes an electrolyte membrane having ionic conductivity, a reduction electrode provided on one side of the electrolyte membrane and including a reduction catalyst for nuclear hydrogenation of an aromatic hydrocarbon compound, and the other of the electrolyte membrane An electrode unit including an oxygen generation electrode provided on the side of the electrode, a power control unit that applies a voltage Va between the reduction electrode and the oxygen generation electrode, and a potential at the reversible hydrogen electrode V _HER , when the standard oxidation-reduction potential of an aromatic hydrocarbon compound is expressed as V _TRR and the potential of the reduction electrode is expressed as V _CA , power control is performed so as to satisfy the relationship of V _{HER −arbitrary} allowable potential ≦ V _CA ≦ V _TRR And a control unit for controlling the unit. The potential in the present invention means a true electrode potential with respect to the reference electrode potential. Therefore, for example, when there is electrolyte membrane resistance, resistance of the electrode catalyst layer, ohmic loss due to various electrical connections, etc., it is necessary to calculate and correct the true electrode potential in consideration of them as described later. There is.

In the electrochemical reduction device of the above aspect, the arbitrarily determined allowable potential may be 20 mV. Further, a reference electrode disposed in contact with the electrolyte membrane and electrically isolated from the reduction electrode and the oxygen generation electrode and held at the reference electrode potential V _Ref , and a potential difference ΔV _CA between the reference electrode and the reduction electrode And a voltage detection unit for detecting, and the control unit may acquire the potential V _{CA of the} reduction electrode based on the potential difference ΔV _CA and the reference electrode potential V _Ref . Control unit varies the voltages Va, the potential V _CA of reduction electrode may be controlled so that the potential of the predetermined range. The control unit may control the power control unit so as to satisfy Va ≧ (V _OER −V _CA ) when the oxygen generation equilibrium potential in the electrolysis of water is expressed as V _OER . The reference electrode may be disposed on the electrolyte membrane on the side where the reduction electrode is provided.

Another aspect of the present invention is an electrochemical reduction device. The electrochemical reduction apparatus includes an electrolyte membrane having ionic conductivity, a reduction electrode provided on one side of the electrolyte membrane and including a reduction catalyst for nuclear hydrogenation of an aromatic hydrocarbon compound, and an electrolyte membrane An electrode unit assembly in which a plurality of electrode units including an oxygen generation electrode provided on the other side are electrically connected in series with each other; a positive electrode terminal and a negative electrode terminal of the electrode unit assembly; A power control unit that applies a voltage VA between the two, a potential at the reversible hydrogen electrode is V _HER , a standard oxidation-reduction potential of the aromatic hydrocarbon compound is V _TRR , and a potential of the reduction electrode of each electrode unit is V _CA And a control unit that controls the power control unit so as to satisfy a relationship of V _{HER -arbitrary} allowable potential ≦ V _CA ≦ V _TRR .

In the electrochemical reduction device of the above aspect, the arbitrarily determined allowable potential may be 20 mV. A reference electrode that is in contact with the electrolyte membrane of any one of the electrolyte layers included in the electrode unit assembly and is electrically isolated from the reduction electrode and the oxygen generation electrode, and a potential difference between the reference electrode and the reduction electrode A voltage detection unit that detects ΔV _CA , and the control unit may acquire the potential V _CA of the return electrode based on the potential difference ΔV _CA and the reference electrode potential V _Ref . Control unit varies the voltage VA, the potential V _CA of the reduction electrode of each electrode unit may be controlled so that the potential of the predetermined range. Further, when the control unit expresses the oxygen generation equilibrium potential in the electrolysis of water as V _OER , VA ≧ (V _OER −V _CA ) × N [N (2 or more) is the number of electrode units connected in series. ] May be controlled so as to satisfy. The reference electrode may be disposed on the side of the electrolyte membrane where the reduction electrode is provided. The reference electrode may be disposed on the electrolyte membrane on the side where the reduction electrode is provided.

  Another embodiment of the present invention is a method for producing a hydrogenated product of an aromatic hydrocarbon compound or a nitrogen-containing heterocyclic aromatic compound. The method for producing a hydrogenated product of the aromatic hydrocarbon compound or the nitrogen-containing heterocyclic aromatic compound uses the electrochemical reduction device according to any one of the above-described aspects, and the aromatic hydrocarbon compound on the reduction electrode side of the electrode unit Alternatively, a nitrogen-containing heterocyclic aromatic compound is introduced, water or a humidified gas is circulated to the oxygen generating electrode side, and the aromatic hydrocarbon compound or nitrogen-containing heterocyclic aromatic compound introduced to the reduction electrode side It is characterized by nuclear hydrogenation. In the production method of this embodiment, the aromatic hydrocarbon compound or nitrogen-containing heterocyclic aromatic compound to be introduced to the reduction electrode side may be introduced to the reduction electrode side in a liquid state at the reaction temperature.

A combination of the above-described elements as appropriate can also be included in the scope of the invention for which patent protection is sought by this patent application.

  According to the present invention, an aromatic hydrocarbon compound or a nitrogen-containing heterocyclic aromatic compound can be electrochemically nuclear hydrogenated with high efficiency.

1 is a schematic diagram illustrating a schematic configuration of an electrochemical reduction device according to Embodiment 1. FIG. 2 is a diagram showing a schematic configuration of an electrode unit included in the electrochemical reduction device according to Embodiment 1. FIG. It is a flowchart which shows an example of the electric potential control of the reduction electrode by a control part. It is a graph which shows the relationship between the electric potential of a reduction electrode, and various current densities. 4 is a schematic diagram showing a schematic configuration of an electrochemical reduction device according to Embodiment 2. FIG. 6 is a schematic diagram illustrating a schematic configuration of an electrochemical reduction device according to Embodiment 3. FIG.

  Hereinafter, embodiments of the present invention will be described with reference to the drawings. In all the drawings, the same reference numerals are given to the same components, and the description will be omitted as appropriate.

(Embodiment 1)
FIG. 1 is a schematic diagram illustrating a schematic configuration of an electrochemical reduction device 10 according to an embodiment. FIG. 2 is a diagram illustrating a schematic configuration of an electrode unit included in the electrochemical reduction device 10 according to the embodiment. As shown in FIG. 1, the electrochemical reduction device 10 includes an electrode unit 100, a power control unit 20, an organic substance storage tank 30, a water storage tank 40, a steam / water separation unit 50, and a control unit 60.

  The power control unit 20 is, for example, a DC / DC converter that converts the output voltage of the power source into a predetermined voltage. The positive output terminal of the power control unit 20 is connected to the positive electrode of the electrode unit 100. The negative output terminal of the power control unit 20 is connected to the negative electrode of the electrode unit 100. As a result, a predetermined voltage is applied between the oxygen generation electrode (positive electrode) 130 and the reduction electrode (negative electrode) 120 of the electrode unit 100. Note that the reference electrode input terminal of the power control unit 20 is connected to a reference electrode 112 provided on the electrolyte membrane 110 to be described later. The potential and the potential of the negative output terminal are determined. In addition, as an electric power source, electric power derived from natural energy such as sunlight or wind power can be used. A mode of potential control of the positive output terminal and the negative output terminal by the control unit 60 will be described later.

  An aromatic compound is stored in the organic matter storage tank 30. The aromatic compound used in the present embodiment is an aromatic hydrocarbon compound containing at least one aromatic ring or a nitrogen-containing heterocyclic aromatic compound, and includes benzene, naphthalene, anthracene, diphenylethane, pyridine, pyrimidine, Pyrazine, quinoline, isoquinoline, N-alkylpyrrole, N-alkylindole, N-alkyldibenzopyrrole and the like can be mentioned. In addition, 1 to 4 hydrogen atoms of the aromatic rings of the above aromatic hydrocarbon and nitrogen-containing heterocyclic aromatic compound may be substituted with an alkyl group. However, “alkyl” in the aromatic compound is a linear alkyl group or branched alkyl group having 1 to 6 carbon atoms. For example, examples of the alkylbenzene include toluene and ethylbenzene, examples of the dialkylbenzene include xylene and diethylbenzene, and examples of the trialkylbenzene include mesitylene. Examples of the alkyl naphthalene include methyl naphthalene. Moreover, the aromatic ring of the above-mentioned aromatic hydrocarbon and nitrogen-containing heterocyclic aromatic compound may have 1 to 3 substituents. In the following description, the aromatic hydrocarbon compound and the nitrogen-containing heterocyclic aromatic compound used in the present invention may be referred to as “aromatic compound”. The aromatic compound is preferably liquid at normal temperature. Moreover, what is necessary is just to be a liquid as a mixture, when using what mixed two or more among the above-mentioned aromatic compounds. According to this, since the aromatic compound can be supplied to the electrode unit 100 in a liquid state without performing processing such as heating and pressurization, the configuration of the electrochemical reduction device 10 can be simplified. it can. The concentration of the aromatic carbide compound in the liquid state is 0.1% or more, preferably 0.3% or more, more preferably 0.5% or more.

  The aromatic compound stored in the organic substance storage tank 30 is supplied to the reduction electrode 120 of the electrode unit 100 by the first liquid supply device 32. As the first liquid supply device 32, for example, various pumps such as a gear pump or a cylinder pump, a natural flow-down device, or the like can be used. In addition, it may replace with an aromatic compound and may use the N-substituted body of the aromatic compound mentioned above. A circulation path is provided between the organic substance storage tank 30 and the reduction electrode of the electrode unit 100, and the aromatic compound and the unreacted aromatic compound nuclear-hydrogenated by the electrode unit 100 are stored in the organic substance via the circulation path. It is stored in the tank 30. In the main reaction that proceeds at the reduction electrode 120 of the electrode unit 100, no gas is generated, but when hydrogen is by-produced, a gas-liquid separation means may be provided in the middle of the circulation path.

  The water storage tank 40 stores ion-exchanged water, pure water, etc. (hereinafter simply referred to as “water”). The water stored in the water storage tank 40 is supplied to the oxygen generating electrode 130 of the electrode unit 100 by the second liquid supply device 42. Similar to the first liquid supply device 32, for example, various pumps such as a gear pump or a cylinder pump, a natural flow-down device, or the like can be used for the second liquid supply device 42. A circulation path is provided between the water storage tank 40 and the oxygen generating electrode of the electrode unit 100, and unreacted water in the electrode unit 100 is stored in the water storage tank 40 through the circulation path. A steam / water separator 50 is provided in the middle of a path for returning unreacted water from the electrode unit 100 to the water storage tank 40. The oxygen generated by the electrolysis of water in the electrode unit 100 is separated from the water by the steam / water separator 50 and discharged out of the system.

  As shown in FIG. 2, the electrode unit 100 includes an electrolyte membrane 110, a reduction electrode 120, an oxygen generation electrode 130, liquid diffusion layers 140a and 140b, and separators 150a and 150b. In FIG. 1, the electrode unit 100 is illustrated in a simplified manner, and the liquid diffusion layers 140a and 140b and the separators 150a and 150 are omitted.

  The electrolyte membrane 110 is formed of a material having proton conductivity (ionomer), and selectively conducts protons while mixing and diffusing substances between the reduction electrode 120 and the oxygen generating electrode 130. To suppress that. The thickness of the electrolyte membrane 110 is preferably 5 to 300 μm, more preferably 10 to 150 μm, and most preferably 20 to 100 μm. When the thickness of the electrolyte membrane 110 is less than 5 μm, the barrier property of the electrolyte membrane 110 is lowered, and cross leakage is likely to occur. On the other hand, if the thickness of the electrolyte membrane 110 is greater than 300 μm, the ion migration resistance becomes excessive, which is not preferable.

Sheet resistance of the electrolyte membrane 110, i.e., ion transfer resistance per geometric area, preferably 2000mΩ · cm ² or less, more preferably 1000M · cm ² or less, and most preferably 500mΩ · cm ² or less. When the area resistance of the electrolyte membrane 110 is higher than 2000 mΩ · cm ² , proton conductivity is insufficient. Examples of the material having proton conductivity (cation exchange type ionomer) include perfluorosulfonic acid polymers such as Nafion (registered trademark) and Flemion (registered trademark). The ion exchange capacity (IEC) of the cation exchange ionomer is preferably 0.7 to 2 meq / g, more preferably 1 to 1.2 meq / g. When the ion exchange capacity of the cation exchange ionomer is less than 0.7 meq / g, the ion conductivity is insufficient. On the other hand, when the ion exchange capacity of the cation exchange ionomer is higher than 2 meq / g, the solubility of the ionomer in water increases, so that the strength of the electrolyte membrane 110 becomes insufficient.

The electrolyte membrane 110 is provided with a reference electrode 112 in contact with the electrolyte membrane 110 in a region separated from the reduction electrode 120 and the oxygen generation electrode 130. That is, the reference electrode 112 is electrically isolated from the reduction electrode 120 and the oxygen generation electrode 130. The reference electrode 112 is held at the reference electrode potential V _Ref . Examples of the reference electrode 112 include a standard hydrogen reduction electrode (reference electrode potential V _Ref = 0V) and an Ag / AgCl electrode (reference electrode potential V _Ref = 0.199 V), but the reference electrode 112 is not limited to these. The reference electrode 112 is preferably installed on the surface of the electrolyte membrane 110 on the reduction electrode 120 side.

The potential difference ΔV _CA between the reference electrode 112 and the reduction electrode 120 is detected by the voltage detection unit 114. The value of the potential difference ΔV _CA detected by the voltage detection unit 114 is input to the control unit 60.

  The reduction electrode 120 is provided on one side of the electrolyte membrane 110. The reduction electrode 120 is a reduction electrode catalyst layer including a reduction catalyst for nuclear hydrogenation of an aromatic compound. The reduction catalyst used for the reduction electrode 120 is not particularly limited. For example, the first catalyst metal (noble metal) containing at least one of Pt and Pd, and Cr, Mn, Fe, Co, Ni, Cu, Zn, Mo , Ru, Sn, W, Re, Pb, Bi, and a metal composition containing one or more second catalytic metals. The form of the metal composition is an alloy of the first catalyst metal and the second catalyst metal, or an intermetallic compound composed of the first catalyst metal and the second catalyst metal. The ratio of the first catalyst metal to the total mass of the first catalyst metal and the second catalyst metal is preferably 10 to 95 wt%, more preferably 20 to 90 wt%, and most preferably 25 to 80 wt%. When the ratio of the first catalyst metal is lower than 10 wt%, durability may be lowered in terms of dissolution resistance. On the other hand, if the ratio of the first catalyst metal is higher than 95 wt%, the electrode activity becomes insufficient because the properties of the reduction catalyst approach the properties of the noble metal alone. In the following description, the first catalyst metal and the second catalyst metal may be collectively referred to as “catalyst metal”.

The catalyst metal described above may be supported on a conductive material (support). The electric conductivity of the conductive material is preferably 1.0 × 10 ⁻² S / cm or more, more preferably 3.0 × 10 ⁻² S / cm or more, and 1.0 × 10 ⁻¹ S / cm or more. Most preferred. When the electrical conductivity of the conductive material is less than 1.0 × 10 ⁻² S / cm, sufficient conductivity cannot be imparted. Examples of the conductive material include a conductive material containing any one of porous carbon, porous metal, and porous metal oxide as a main component. Examples of the porous carbon include carbon black such as ketjen black (registered trademark), acetylene black, and Vulcan (registered trademark). The BET specific surface area of the porous carbon measured by the nitrogen adsorption method is preferably 100 m ² / g or more, more preferably 150 m ² / g or more, and most preferably 200 m ² / g or more. When the BET specific surface area of the porous carbon is smaller than 100 m ² / g, it becomes difficult to uniformly support the catalyst metal. For this reason, the utilization factor of the catalytic metal surface is lowered, and the catalytic performance is lowered. Examples of the porous metal include Pt black, Pd black, and Pt metal deposited in a fractal shape. Examples of the porous metal oxide include oxides of Ti, Zr, Nb, Mo, Hf, Ta, and W. In addition, as a porous conductive material for supporting a catalytic metal, nitrides, carbides, oxynitrides, carbonitrides, partial oxidations of metals such as Ti, Zr, Nb, Mo, Hf, Ta, W, etc. Carbonitrides (hereinafter collectively referred to as porous metal carbonitrides and the like). The BET specific surface area of the porous metal, porous metal oxide, porous metal carbonitride and the like measured by the nitrogen adsorption method is preferably 1 m ² / g or more, more preferably 3 m ² / g or more, and 10 m ² / g. The above is most preferable. If the BET specific surface area of the porous metal, the porous metal oxide, the porous metal carbonitride, or the like is smaller than 1 m ² / g, it becomes difficult to uniformly support the catalyst metal. For this reason, the utilization factor of the catalytic metal surface is lowered, and the catalytic performance is lowered.

  The method of supporting the catalyst metal on the support depends on the type and composition of the first catalyst metal and the second catalyst metal, but the impregnation of the support with the first catalyst metal and the second catalyst metal is performed simultaneously. Or a sequential impregnation method in which the support is impregnated with the second catalyst metal after the support is impregnated with the first catalyst metal. In the case of the sequential impregnation method, after the first catalyst metal is supported on the support, heat treatment or the like may be once applied, and then the second catalyst metal may be supported on the support. After the impregnation of both the first catalytic metal and the second catalytic metal is completed, alloying of the first catalytic metal and the second catalytic metal or the first catalytic metal and the second catalytic metal is performed by a heat treatment step. Formation of an intermetallic compound consisting of

  A conductive material such as the above-described conductive oxide or carbon black may be added to the reduction electrode 120 separately from the conductive compound carrying the catalyst metal. Thereby, the electron conduction path between the reduction catalyst particles can be increased, and the resistance per geometric area of the reduction catalyst layer can be lowered in some cases.

  The reduction electrode 120 may include a fluorine-based resin such as polytetrafluoroethylene (PTFE) as an additive.

  The reduction electrode 120 may include an ionomer having proton conductivity. The reduction electrode 120 preferably contains an ion conductive substance (ionomer) having the same or similar structure as the electrolyte membrane 110 described above at a predetermined mass ratio. According to this, the ion conductivity in the reduction electrode 120 can be improved. In particular, when the catalyst support is porous, the reduction electrode 120 contains an ionomer having proton conductivity, which greatly contributes to improvement of ion conductivity. Examples of ionomers having proton conductivity (cation exchange ionomers) include perfluorosulfonic acid polymers such as Nafion (registered trademark) and Flemion (registered trademark). The ion exchange capacity (IEC) of the cation exchange ionomer is preferably 0.7 to 3 meq / g, more preferably 1 to 2.5 meq / g, and most preferably 1.2 to 2 meq / g. When the catalyst metal is supported on porous carbon (carbon support), the cation exchange ionomer (I) / carbon support (C) mass ratio I / C is preferably 0.1 to 2, and 0 .2 to 1.5 is more preferable, and 0.3 to 1.1 is most preferable. When the mass ratio I / C is lower than 0.1, it is difficult to obtain sufficient ionic conductivity. On the other hand, if the mass ratio I / C is greater than 2, the coating thickness of the ionomer on the catalytic metal increases, which prevents the aromatic compound as a reactant from contacting the catalytic active point or decreases the electronic conductivity. As a result, the electrode activity decreases.

  Moreover, it is preferable that the ionomer contained in the reduction electrode 120 partially covers the reduction catalyst. According to this, three elements (aromatic compound, proton, electron) necessary for the electrochemical reaction in the reduction electrode 120 can be efficiently supplied to the reaction field.

  The liquid diffusion layer 140 a is laminated on the surface of the reduction electrode 120 on the side opposite to the electrolyte membrane 110. The liquid diffusion layer 140a has a function of uniformly diffusing a liquid aromatic compound supplied from a separator 150a described later to the reduction electrode 120. For example, carbon paper or carbon cloth is used as the liquid diffusion layer 140a.

  The separator 150a is laminated on the surface of the liquid diffusion layer 140a opposite to the electrolyte membrane 110. The separator 150a is formed of a corrosion-resistant alloy such as carbon resin, Cr—Ni—Fe, Cr—Ni—Mo—Fe, Cr—Mo—Nb—Ni, Cr—Mo—Fe—W—Ni. . On the surface of the separator 150a on the liquid diffusion layer 140a side, one or a plurality of groove-shaped flow paths 152a are provided. The liquid aromatic compound supplied from the organic substance storage tank 30 circulates in the flow path 152a, and the liquid aromatic compound soaks into the liquid diffusion layer 140a from the flow path 152a. Although the form of the flow path 152a is not specifically limited, For example, a linear flow path and a serpentine flow path can be adopted. When a metal material is used for the separator 150a, the separator 150a may be a structure obtained by sintering spherical or pellet-shaped metal fine powder.

The oxygen generating electrode 130 is provided on the other side of the electrolyte membrane 110. As the oxygen generating electrode 130, one containing a noble metal oxide catalyst such as RuO ₂ or IrO ₂ is preferably used. These catalysts are dispersed in metals such as Cr, Mn, Fe, Co, Ni, Cu, Zn, Nb, Mo, Ta, W or metal wires such as alloys containing them as a main component, and metal substrates such as meshes. It may be supported or coated. In particular, since IrO ₂ is expensive, in the case of using IrO ₂ as a catalyst, by thin film coating to a metal substrate, it is possible to reduce the manufacturing cost.

  The liquid diffusion layer 140b is laminated on the surface of the oxygen generation electrode 130 opposite to the electrolyte membrane 110. The liquid diffusion layer 140b has a function of uniformly diffusing water supplied from a separator 150b described later to the oxygen generation electrode 130. For example, carbon paper or carbon cloth is used as the liquid diffusion layer 140b.

  The separator 150b is laminated on the surface of the liquid diffusion layer 140b opposite to the electrolyte membrane 110. The separator 150b is made of a corrosion resistant alloy such as Cr / Ni / Fe, Cr / Ni / Mo / Fe, Cr / Mo / Nb / Ni, Cr / Mo / Fe / W / Ni, or the surface of these metals. Is formed of a material coated with an oxide layer. One or a plurality of groove-shaped flow paths 152b are provided on the surface of the separator 150b on the liquid diffusion layer 140b side. The water supplied from the water storage tank 40 circulates in the flow path 152b, and the water soaks into the liquid diffusion layer 140b from the flow path 152b. Although the form of the flow path 152b is not specifically limited, For example, a linear flow path and a serpentine flow path can be adopted. When a metal material is used for the separator 150b, the separator 150b may be a structure obtained by sintering spherical or pellet-shaped metal fine powder.

  In the present embodiment, liquid water is supplied to the oxygen generating electrode 130, but humidified gas (for example, air) may be used instead of liquid water. In this case, the dew point temperature of the humidified gas is preferably room temperature to 100 ° C, more preferably 50 to 100 ° C.

The reaction in the electrode unit 100 when toluene is used as the aromatic compound is as follows.
<Electrode reaction at the electrode for oxygen generation>
3H ₂ O → 1.5 O ₂ + 6H ⁺ + 6e ⁻ : E ₀ = 1.23V
<Electrode reaction at the reduction electrode>
Toluene + 6H ⁺ + 6e ⁻ → methylcyclohexane: E ₀ = 0.153 V (vs RHE)
That is, the electrode reaction at the oxygen generating electrode and the electrode reaction at the reduction electrode proceed in parallel, and protons generated by the electrolysis of water through the electrolyte membrane 110 due to the electrode reaction at the oxygen generating electrode. And supplied to the reduction electrode, and used for nuclear hydrogenation of aromatic compounds in the electrode reaction at the reduction electrode.

Returning to FIG. 1, when the potential at the reversible hydrogen electrode is expressed as V _HER , the standard oxidation-reduction potential of the aromatic compound is expressed as V _TRR , and the potential of the reduction electrode 120 is expressed as V _CA , V _HER −20 mV ≦ V _The power control unit 20 is controlled so as to satisfy the relationship _CA ≦ _VTRR . When the potential V _CA is lower than V _HER -20 mV, it is not preferable because competition with the hydrogen generation reaction occurs and the reduction selectivity of the aromatic compound becomes insufficient. On the other hand, when the potential V _CA is higher than the standard redox potential V _TRR , the aromatic hydrogenation reaction does not proceed at a practically sufficient reaction rate, which is not preferable. In other words, by setting the potential V _CA within a range that satisfies the above relational expression, the electrochemical reaction can proceed in both electrodes, and the nuclear hydrogenation of the aromatic compound can be carried out industrially.

In addition, the following may be mentioned as reaction conditions when the aromatic compound is nuclear hydrogenated using the electrochemical reduction device 10. The temperature of the electrode unit 100 is preferably room temperature to 100 ° C, more preferably 40 to 80 ° C. If the temperature of the electrode unit 100 is lower than room temperature, the progress of the electrolytic reaction may be delayed, or a large amount of energy is required to remove the heat generated with the progress of the reaction, which is not preferable. On the other hand, when the temperature of the electrode unit 100 is higher than 100 ° C., water is boiled in the oxygen generating electrode 130, and the vapor pressure of the organic substance is increased in the reduction electrode 120. The chemical reduction apparatus 10 is not preferable. Note that since the reduction electrode potential V _CA is a true electrode potential, it may be different from the actually observed potential V _{CA_actual} . Of the various resistance components present in the electrolytic cell used in the present invention, when there is a portion corresponding to the ohmic resistance, the resistance value per electrode area of these aggregates is defined as the total ohmic resistance _{Rohmic according} to the following formula: A true electrode potential V _CA is calculated.
VCA = VCA_actual + Romic × J (current density)
Examples of the ohmic resistance include proton transfer resistance of an electrolyte membrane, electron transfer resistance of an electrode catalyst layer, and other contact resistance on an electric circuit.
Here, _Rohm can be obtained as an actual resistance component on the equivalent circuit by using an AC impedance method or an AC resistance measurement at a fixed frequency, but once the configuration of the electrolytic cell and the material system to be used are determined, A method that is regarded as a steady value and is used for the following control can be preferably taken.

FIG. 3 is a flowchart illustrating an example of potential control of the reduction electrode 120 by the control unit 60. Hereinafter, the mode of potential control of the reduction electrode 120 will be described by taking an example of using an Ag / AgCl electrode (reference electrode potential V _Ref = 0.199 V) as the reference electrode 112.

First, a potential V _CA (target value) that satisfies V _HER −20 mV ≦ V _CA ≦ V _TRR is set (S10). In one embodiment, the potential V _CA (target value) is a value stored in advance in a memory such as a ROM. In another aspect, the potential V _CA (target value) is set by the user.

Next, the voltage detector 114 detects the potential difference ΔV _CA between the reference electrode 112 and the reduction electrode 120 (S20).

Next, the control unit 60 calculates the potential V _CA (measured value) of the reduction electrode 120 using (Expression) V _CA = ΔV _CA −V _Ref = ΔV _CA −0.199 V (S30).

Next, it is determined whether or not the potential V _CA (actually measured value) satisfies the following formula (1) and the following formula (2) (S40).
| Potential V _CA (actual value) −potential V _CA (target value) | ≦ allowable value (1)
V _HER −20 mV ≦ V _CA (actual value) ≦ V _TRR (2)
In the above formula, the allowable value is, for example, 1 mV.

When the potential V _CA (actually measured value) satisfies the expressions (1) and (2), the process proceeds to “yes” in S40, and the process here ends. On the other hand, if the potential V _CA (actually measured value) does not satisfy both the expressions (1) and (2), the process proceeds to no in S40 and is applied between the reduction electrode 120 and the oxygen generation electrode 130. The voltage Va to be adjusted is adjusted (S50). After adjusting the voltage Va, the process returns to the above-described process (S10).

Here, an example of adjustment of the voltage Va will be described. For example,
If the potential V _CA (actual value) −potential V _CA (target value)> allowable value, the control unit 60 sends an instruction to the power control unit 20 to increase the voltage Va by 1 mV. Note that as a result of increasing the voltage Va, even when | potential V _CA (actual value) −potential V _CA (target value) | ≦ allowable value is satisfied, V _CA (actual value) <V _HER −V _allow In this case, since the expression (2) is not satisfied, in the next process, the control unit 60 decreases the voltage Va by 1 mV.

On the other hand, when potential V _CA (actual value) −potential V _CA (target value) <− allowable value, control unit 60 sends an instruction to power control unit 20 to decrease voltage Va by 1 mV. In addition, as a result of lowering the voltage Va, even if the case of satisfying | potential V _CA (actual value) −potential V _CA (target value) | ≦ allowable value, V _CA (actual value)> V _TRR is satisfied. Since the expression (2) is not satisfied, in the next process, the control unit 60 increases the voltage Va by 1 mV. In this way, the control unit 60 adjusts the voltage Va until the expressions (1) and (2) are finally satisfied.

Note that the value (adjustment range) for raising and lowering the voltage Va is not limited to 1 mV. For example, in the first adjustment of the voltage Va, the adjustment width of the voltage Va is equal to the above-described allowable value, and in the second and subsequent adjustments of the voltage Va, the adjustment width of the voltage Va is, for example, 1/4 of the above-described allowable value. It is good. According to this, the potential V _CA (actually measured value) can be quickly adjusted to a range that satisfies the expressions (1) and (2).

When the oxygen generation equilibrium potential in the electrolysis of water is expressed as V _OER , the control unit 60 controls the power control unit 20 to satisfy Va ≧ (V _OER −V _CA ). Thus, the potential _{V AN} oxygen generating electrode 130 is maintained to be equal to or greater than the oxygen generating equilibrium potential _{V OER.}

図４に示す電流密度Ａ、電流密度Ｂおよび電流密度Ｃはそれぞれ以下のとおりである。
電流密度Ａ：電極セルに流れる全電流密度
電流密度Ｂ：ガスクロマトグラフィーなどから定量したメチルシクロヘキサンの生成量から逆算した、トルエンの還元に用いられた電流密度
電流密度Ｃ：電流密度Ａ−電流密度Ｂ（トルエンの還元に用いられず、主として水素の発生に用いられた電流密度）
また、図４に示すファラデー効率は、電流密度Ｂ／電流密度Ａ×１００（％）により算出される。(Relationship between toluene reduction characteristics and reduction electrode potential)
Using the electrode cell having the configuration shown in Table 1, the nuclear hydrogenation reaction of toluene was performed by changing the potential of the reduction electrode. FIG. 4 is a graph showing the relationship between the potential of the reduction electrode and various current densities. The mass of the reduction catalyst metal is 0.5 mg / cm ² .

The current density A, current density B, and current density C shown in FIG. 4 are as follows.
Current density A: Total current density flowing in the electrode cell Current density B: Current density used for reduction of toluene, calculated from the amount of methylcyclohexane determined by gas chromatography, etc. Current density C: Current density A-Current density B (current density not mainly used for reducing toluene but mainly for generating hydrogen)
Further, the Faraday efficiency shown in FIG. 4 is calculated by current density B / current density A × 100 (%).

As shown in FIG. 4, it was confirmed that when the potential of the reduction electrode becomes lower than the potential V _HER -20 mV, that is, -20 mV, the amount of hydrogen generation increases and the Faraday efficiency is less than 50%, which is not preferable.

(Embodiment 2)
FIG. 5 is a schematic diagram illustrating a schematic configuration of the electrochemical reduction device according to the second embodiment. As shown in FIG. 5, the electrochemical reduction device 10 includes an electrode unit assembly 200, a power control unit 20, an organic matter storage tank 30, a water storage tank 40, a steam / water separation unit 50, and a control unit 60. The electrode unit assembly 200 has a stacked structure in which a plurality of electrode units 100 are connected in series. In the present embodiment, the number N of electrode units 100 is five. The configuration of each electrode unit 100 is the same as that of the first embodiment. In FIG. 5, the electrode unit 100 is illustrated in a simplified manner, and the liquid diffusion layers 140a and 140b and the separators 150a and 150 are omitted.

  The positive output terminal of the power control unit 20 of the present embodiment is connected to the positive terminal of the electrode unit assembly 200. On the other hand, the negative output terminal of the power control unit 20 is connected to the negative terminal of the electrode unit assembly 200. Thereby, a predetermined voltage VA is applied between the positive electrode terminal and the negative electrode terminal of the electrode unit assembly 200. Note that the reference electrode input terminal of the power control unit 20 is connected to a reference electrode 112 provided on an electrolyte membrane 110 of a specific electrode unit 100 described later, and the potential of the positive electrode output terminal is based on the potential of the reference electrode 112. The potential and the potential of the negative output terminal are determined.

  A first circulation path is provided between the organic substance storage tank 30 and the reduction electrode 120 of each electrode unit 100. The aromatic compound stored in the organic substance storage tank 30 is supplied to the reduction electrode 120 of each electrode unit 100 by the first liquid supply device 32. Specifically, the piping constituting the first circulation path is branched on the downstream side of the first liquid supply device 32, and the aromatic compound is distributed and supplied to the reduction electrodes 120 of each electrode unit 100. The aromatic compound nuclear-hydrogenated by each electrode unit 100 and the unreacted aromatic compound merge into a pipe communicating with the organic substance storage tank 30, and then stored in the organic substance storage tank 30 through the pipe.

  A second circulation path is provided between the water storage tank 40 and the oxygen generating electrode 130 of each electrode unit 100. The water stored in the water storage tank 40 is supplied to the oxygen generation electrode 130 of each electrode unit 100 by the second liquid supply device 42. Specifically, a pipe constituting the second circulation path is branched on the downstream side of the second liquid supply device 42, and water is distributed and supplied to the oxygen generation electrode 130 of each electrode unit 100. In each electrode unit 100, unreacted water joins a pipe communicating with the water storage tank 40, and then is stored in the water storage tank 40 through the pipe.

  As in the first embodiment, the reference electrode 112 is provided on the electrolyte membrane 110 of the specific electrode unit 100 so as to be in contact with the electrolyte membrane 110 in a region separated from the reduction electrode 120 and the oxygen generation electrode 130. The specific electrode unit 100 may be any one of the plurality of electrode units 100.

The potential difference ΔV _CA between the reference electrode 112 and the reduction electrode 120 is detected by the voltage detection unit 114. The value of the potential difference ΔV _CA detected by the voltage detection unit 114 is input to the control unit 60.

When the potential at the reversible hydrogen electrode is expressed as V _HER , the standard oxidation-reduction potential of the aromatic compound is expressed as V _TRR , and the potential of the reduction electrode 120 of each electrode unit 100 is expressed as V _CA , the control unit 60 has V _HER −20 mV ≦ V _The power control unit 20 is controlled so as to satisfy the relationship _CA ≦ _VTRR .

  The manner of controlling the potential of the reduction electrode 120 by the control unit 60 is the same as in the first embodiment. However, in the first embodiment, the applied voltage Va is adjusted by the control unit 60, whereas in the present embodiment, the control unit 60 places the positive voltage terminal between the positive electrode terminal and the negative electrode terminal of the electrode unit assembly 200. The applied voltage VA is adjusted.

The control unit 60 controls the power control unit 20 so that VA ≧ (V _OER −V _CA ) × N [N (2 or more) is the number of electrode units: 5 in the present embodiment]. As a result, the potential V _AN is maintained so as to be _{equal to} or higher than the oxygen generation equilibrium potential V _OER .

  According to the present embodiment, since the nuclear hydrogenation of the aromatic compound can proceed in parallel in the plurality of electrode units, the nuclear hydrogenation amount of the aromatic compound per unit time is dramatically increased. be able to. Therefore, it is possible to industrially carry out the nuclear hydrogenation of aromatic compounds.

(Embodiment 3)
FIG. 6 is a schematic diagram illustrating a schematic configuration of the electrochemical reduction device according to the third embodiment. The basic configuration of the electrochemical reduction device 10 according to the present embodiment is the same as that of the second embodiment. In the present embodiment, electrode unit assembly 200 is housed in electrolytic cell 300. A second circulation path is provided between the electrolytic tank 300 and the water storage tank 40, and the electrolytic tank 300 is filled with water supplied from the water storage tank 40. Water filled in the electrolytic cell 300 can flow through the oxygen generating electrode 130 of each electrode unit 100.

  In addition to the effects obtained in the second embodiment, the electrochemical reduction apparatus 10 according to the present embodiment increases the heat capacity of the water tank in the electrolytic cell, thereby increasing the in-plane temperature difference of the oxygen generating electrode 130 and the electrode unit. The temperature difference between them and the temperature difference between the electrodes with the reduction electrode 120 can be reduced.

  The present invention is not limited to the above-described embodiments, and various modifications such as design changes can be added based on the knowledge of those skilled in the art. Embodiments to which such modifications are added Can also be included in the scope of the present invention. For example, in each of the embodiments described above, the aromatic compound and water are configured to circulate in the circulation path, but are connected to the storage tank connected to the inlet side of the electrolysis unit and the outlet side of the electrolysis unit. You may provide a storage tank separately.

  In each of the embodiments described above, the reduction electrode 120 includes an ionomer having proton conductivity, but the reduction electrode 120 may include an ionomer having hydroxy ion conductivity.

In Embodiments 2 and 3, the reference electrode 112 is installed on the electrolyte membrane 110 of one electrode unit 100, but the reference electrode 112 may be installed on the electrolyte membrane 110 of the plurality of electrode units 100. In this case, the voltage detection unit 114, by using the potential difference [Delta] V _CA is detected, the detected average value of a plurality of the potential difference [Delta] V _CA between the reduction electrode 120 corresponding to the respective reference electrode 112, the potential V _CA Is calculated. According to this, when potential variation occurs between the electrode units 100, the voltage VA can be adjusted to a more appropriate range.

DESCRIPTION OF SYMBOLS 10 Electrochemical reduction apparatus, 20 Electric power control part, 30 Organic substance storage tank, 40 Water storage tank, 50 Air-water separation part, 100 Electrode unit, 112, Reference electrode, 114 Voltage detection part, 110 Electrolyte membrane, 120 Reduction electrode, 130 Electrode for oxygen generation, 140a, 140b liquid diffusion layer, 150a, 150b separator, 200 electrode unit assembly, 300 electrolytic cell

  INDUSTRIAL APPLICABILITY The present invention can be used in a technique for electrochemically hydrogenating an aromatic hydrocarbon compound or a nitrogen-containing heterocyclic aromatic compound.

Claims (14)

An electrolyte membrane having ionic conductivity; a reduction electrode provided on one side of the electrolyte membrane and including a reduction catalyst for nuclear hydrogenation of an aromatic hydrocarbon compound or a nitrogen-containing heterocyclic aromatic compound; and An electrode unit comprising an electrode for oxygen generation provided on the other side of the electrolyte membrane;
A power control unit that applies a voltage Va between the reduction electrode and the oxygen generation electrode;
When the potential at the reversible hydrogen electrode is expressed as V _HER , the standard oxidation-reduction potential of the aromatic hydrocarbon compound or the nitrogen-containing heterocyclic aromatic compound is expressed as V _TRR , and the potential of the reduction electrode is expressed as V _CA ,
V _HER -Arbitrary allowable potential ≤ V _CA ≤ V _TRR
A control unit that controls the power control unit to satisfy the relationship:
An electrochemical reduction device comprising:   The electrochemical reduction device according to claim 1, wherein the arbitrarily determined allowable potential is 20 mV. A reference electrode that is in contact with the electrolyte membrane and is electrically isolated from the reduction electrode and the oxygen generation electrode, and is maintained at a reference electrode potential V _Ref ;
A voltage detector that detects a potential difference ΔV _CA between the reference electrode and the reduction electrode;
Further comprising
3. The electrochemical reduction apparatus according to claim 1, wherein the control unit acquires the potential V _{CA of the} reduction electrode based on the potential difference ΔV _CA and the reference electrode potential V _Ref . 4. The electrochemical reduction device according to claim 3, wherein the control unit changes the voltage Va so as to control the potential V _{CA of the} reduction electrode to be in a predetermined range. 5. When the control unit represents the oxygen generation equilibrium potential in water electrolysis as V _OER ,
Va ≧ (V _OER −V _CA )
The electrochemical reduction device according to claim 4, wherein the power control unit is controlled so as to satisfy the above condition.   6. The electrochemical reduction device according to claim 3, wherein the reference electrode is disposed on a side of the electrolyte membrane on which the reduction electrode is provided. 6. An electrolyte membrane having ionic conductivity; a reduction electrode provided on one side of the electrolyte membrane and including a reduction catalyst for nuclear hydrogenation of an aromatic hydrocarbon compound or a nitrogen-containing heterocyclic aromatic compound; and An electrode unit assembly in which a plurality of electrode units including an electrode for oxygen generation provided on the other side of the electrolyte membrane are electrically connected in series with each other;
A power control unit that applies a voltage VA between a positive terminal and a negative terminal of the electrode unit assembly;
When the potential at the reversible hydrogen electrode is expressed as V _HER , the standard redox potential of the aromatic hydrocarbon compound or the nitrogen-containing heterocyclic aromatic compound is expressed as V _TRR , and the potential of the reduction electrode of each electrode unit is expressed as V _CA ,
V _HER -Arbitrary allowable potential ≤ V _CA ≤ V _TRR
A control unit that controls the power control unit to satisfy the relationship:
An electrochemical reduction device comprising:   The electrochemical reduction apparatus according to claim 7, wherein the arbitrarily determined allowable potential is 20 mV. A reference electrode disposed in contact with the electrolyte membrane of any one of the electrolyte layers included in the electrode unit assembly and electrically isolated from the reduction electrode and the oxygen generation electrode;
A voltage detector that detects a potential difference ΔV _CA between the reference electrode and the reduction electrode;
Further comprising
9. The electrochemical reduction device according to claim 7, wherein the control unit acquires the potential V _{CA of the} reduction electrode based on the potential difference ΔV _CA and the reference electrode potential V _Ref . 10. The electrochemical reduction device according to claim 9, wherein the control unit controls the potential V _{CA of the} reduction electrode of each electrode unit to be in a predetermined range by changing the voltage VA. . When the control unit represents the oxygen generation equilibrium potential in water electrolysis as V _OER ,
VA ≧ (V _OER −V _CA ) × N [N (2 or more) is the number of electrode units connected in series]
The electrochemical reduction device according to claim 10, wherein the power control unit is controlled so as to satisfy the condition.   12. The electrochemical reduction device according to claim 9, wherein the reference electrode is disposed on a side of the electrolyte membrane on which the reduction electrode is provided. Using the electrochemical reduction device according to any one of claims 1 to 12,
An aromatic hydrocarbon compound or a nitrogen-containing heterocyclic aromatic compound is introduced to the reduction electrode side of the electrode unit, water or a humidified gas is circulated to the oxygen generation electrode side, and is introduced to the reduction electrode side. A method for producing a hydrogenated product of an aromatic hydrocarbon compound or a nitrogen-containing heterocyclic aromatic compound, wherein the aromatic hydrocarbon compound or the nitrogen-containing heterocyclic aromatic compound is subjected to nuclear hydrogenation.   The aromatic hydrocarbon compound or the aromatic hydrocarbon compound according to claim 13, wherein the aromatic hydrocarbon compound or nitrogen-containing heterocyclic aromatic compound to be introduced to the reduction electrode side is introduced to the reduction electrode side in a liquid state at a reaction temperature. A method for producing a hydrogenated product of a nitrogen-containing heterocyclic aromatic compound.

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