TECHNICAL FIELD
[0001] The present invention relates to a method for producing sodium hydroxide and/or chlorine,
and a two-chamber type electrolytic cell for saltwater.
BACKGROUND ART
[0002] Sodium hydrate and chlorine are essential as industrial materials. They have conventionally
been produced by a method using an ion exchange membrane electrolytic cell to electrolyze
saltwater, in which a metal electrode is used as a cathode and the saltwater is electrolyzed
according to the reaction given by the following equation (1).
2NaCl + 2H
2O → Cl
2 + 2NaOH + H
2 (1)
[0003] However, since the electrolysis of saltwater according to the above equation (1)
requires huge amounts of electric power, a method in which a gas-diffusion electrode
is used as a cathode to reduce oxygen (hereinafter, referred to as oxygen cathode
method) has been addressed in hope of significant energy saving in recent years. In
the oxygen cathode method, a reaction at the anode is oxidation of chlorine ion, which
is the same as in the conventional method, and as a whole, the reaction is given by
the following equation (2).
2NaCl + 1/2O
2 + H
2O → Cl
2 + 2NaOH (2)
[0004] In the oxygen cathode method, a three-chamber type method, in which an electrolytic
cell is divided into an anode chamber, a catholyte chamber, and a cathode gas chamber,
has been employed. However, in recent years, as described in Patent Document 1, for
example, a two-chamber type method has been investigated, in which an electrolytic
cell is divided into an anode chamber and a cathode gas chamber by making an anode,
an ion exchange membrane, and a gas-diffusion cathode attached firmly to each other
to eliminate a catholyte chamber substantially. As shown in the above chemical equations,
water is required for electrolyzing saltwater, and at the same time, water is also
required for keeping the concentration of the generated sodium hydroxide from being
too high. In the three-chamber type method, the cathode chamber has a liquid chamber
to circulate aqueous sodium hydroxide, from which sufficient water is supplied. On
the other hand, in the two-chamber type method, since the cathode chamber does not
have a liquid chamber, water is supplied through the ion exchange membrane from the
anode chamber as electro-osmosis water, which is not sufficient, and water is needed
to be supplied to the cathode in some way. The Patent Document 1 discloses that the
shortage of water is compensated by supplying water through the gas chamber, and specifically
discloses that water is heated beforehand to 90°C and then introduced through an inlet
for oxygen gas. Patent Document 2 also discloses that humidified oxygen-containing
gas is supplied to the cathode chamber, and specifically discloses that the humidified
oxygen-containing gas has been prepared by bubbling oxygen into water heated to 80°C
and then is introduced to the cathode chamber.
RELATED ART DOCUMENTS
PATENT DOCUMENTS
SUMMARY OF THE INVENTION
PROBLEMS TO BE SOLVED BY THE INVENTION
[0006] However, the method for supplying water disclosed in the Patent Document 1 and 2
requires energy to heat water to 80°C or 90°C. In addition, in the method disclosed
in the Patent Document 1, when the temperature of the electrolytic cell becomes too
high, the anolyte temperature is decreased by circulating the anolyte in an external
heat exchanger and using cooling water and the like, which further requires energy
for preparing the cooling water.
[0007] Considering the above, the purpose of the present invention is to offer a method
capable of efficiently producing sodium hydroxide and/or chlorine in such a way that
water is supplied to the cathode chamber and overheating of the electrolytic cell
is suppressed without extra energy other than the energy for electrolytic reaction.
MEANS FOR SOLVING THE PROBLEMS
[0008] The present invention includes the following:
- [1] A method for producing sodium hydroxide and/or chlorine by electrolyzing saltwater,
comprising using a two-chamber type electrolytic cell for saltwater comprising one
or more unit cells equipped with an anode chamber including an anode, a cathode chamber
including a gas-diffusion cathode, and an ion exchange membrane sandwiched by the
anode chamber and the cathode chamber, supplying saltwater to the anode chamber, and
supplying humidified oxygen-containing gas to the cathode chamber, wherein each of
the unit cells further comprises a humidifying chamber generating the humidified oxygen-containing
gas that is to be supplied to the cathode chamber, the humidifying chamber is adjoined
to and in heat exchange relation with the anode chamber or the cathode chamber in
one of the unit cells, or the anode chamber or the cathode chamber in another of the
unit cells adjacent to the one of the unit cells, and the oxygen-containing gas is
humidified by generating water vapor with heat from the anode chamber or the cathode
chamber.
- [2] The method according to [1], wherein the humidifying chamber is adjoined to the
cathode chamber, and the humidified oxygen-containing gas generated in the humidifying
chamber is supplied from the humidifying chamber to the cathode chamber through at
least one opening located at a partition between the humidifying chamber and the cathode
chamber.
- [3] The method according to [2], wherein the at least one opening located at the partition
between the humidifying chamber and the cathode chamber comprises a single opening.
- [4] The method according to [2], wherein the at least one opening located at the partition
between the humidifying chamber and the cathode chamber comprises a plurality of openings.
- [5] The method according to [1], wherein the humidified oxygen-containing gas generated
in the humidifying chamber is supplied from the humidifying chamber to the cathode
chamber through at least one flow path located outside the humidifying chamber and
the cathode chamber.
- [6] The method according to [5], wherein the at least one flow path located outside
the humidifying chamber and the cathode chamber comprises a single flow path.
- [7] The method according to [5], wherein the at least one flow path located outside
the humidifying chamber and the cathode chamber comprises a plurality of flow paths.
- [8] The method according to any one of [1] to [7], wherein the unit cells are connected
with each other in the electrolytic cell, and the unit cells are arranged such that
the sequence of the anode chamber, the cathode chamber, and the humidifying chamber
is repeated.
- [9] A two-chamber type electrolytic cell for saltwater, comprising one or more unit
cells equipped with an anode chamber, a cathode chamber, and an ion exchange membrane
sandwiched by the anode chamber and the cathode chamber, wherein the anode chamber
includes an anode, and is equipped with an inlet for saltwater as a starting material,
an outlet for electrolyzed saltwater, and an outlet for chlorine, the cathode chamber
includes a gas-diffusion cathode, and is equipped with an inlet for humidified oxygen-containing
gas and an outlet for electrolytic reactant, each of the unit cells further comprises
a humidifying chamber generating oxygen-containing gas that is to be supplied to the
cathode chamber, and the humidifying chamber is adjoined to and in heat exchange relation
with the anode chamber or the cathode chamber in one of the unit cells, or the anode
chamber or the cathode chamber in another of the unit cells adjacent to the one of
the unit cells, and is equipped with an inlet for the oxygen-containing gas.
- [10] The electrolytic cell according to [9], wherein the unit cells are connected
with each other in the electrolytic cell, and the unit cells are arranged such that
the sequence of the anode chamber, the cathode chamber, and the humidifying chamber
is repeated.
EFFECTS OF THE INVENTION
[0009] According to the present invention, since the humidifying chamber is adjoined to
and in heat exchange relation with the anode chamber or the cathode chamber, the oxygen-containing
gas can be humidified with heat from the anode chamber or the cathode chamber, and
overheating of the electrolytic cell can be suppressed.
BRIEF DESCRIPTION OF THE DRAWINGS
[0010]
FIG. 1 is a schematic cross-section view of an example of one of unit cells.
FIGs. 2(a) and 2(b) are schematic cross-section views of examples of the shape of
an opening for supplying humidified oxygen-containing gas.
FIG. 3 is a schematic cross-section view of an example of one of unit cells equipped
with a connecting pipe supplying humidified oxygen-containing gas.
FIG. 4 is a schematic cross-section view of an example of a monopolar electrolytic
cell.
FIG. 5 is a schematic cross-section view of an example of a bipolar electrolytic cell.
MODE FOR CARRYING OUT THE INVENTION
[0011] Hereinafter, a two-chamber type electrolytic cell for saltwater and a method for
producing sodium hydroxide and/or chlorine using the electrolytic cell according to
the present invention will be described with reference to the drawings. The present
invention, however, is not limited by the following drawings and can be altered in
design within a scope in compliance with the intent described above and below.
[0012] FIG. 1 shows an example of one of unit cells in an electrolytic cell of the present
invention. Unit cell 1 has an anode chamber 3, a cathode chamber 4, and an ion exchange
membrane 2 sandwiched by the anode chamber 3 and the cathode chamber 4. The anode
chamber 3 includes an anode 3a closely adjoining the anode side of the ion exchange
membrane 2. The anode chamber 3 is also equipped with an inlet 3b for saltwater as
a starting material at a lower part and equipped with an outlet 3c for electrolyzed
saltwater and chlorine at an upper part. The cathode chamber 4 is equipped with a
liquid retention layer 4b adjoining the cathode side of the ion exchange membrane
2, a gas-diffusion cathode 4a, and if necessary, a gas-diffusion cathode support 4c
and a cushion material 4d in this order.
[0013] The unit cell 1 of the present invention is equipped with a humidifying chamber 5
separated from the cathode chamber 4 by a partition 6, and the humidifying chamber
5 is in heat exchange relation with the cathode chamber 4. The partition 6 exemplified
in the drawing has a planar shape as shown in FIG. 2(a), and the space above the partition
6 in whole performs as an opening 7, which enable humidified oxygen-containing gas
to be supplied from the humidifying chamber 5 to the cathode chamber 4. In addition,
the cathode chamber 4 is also equipped with a pressure equalizing line 4e to keep
water level in the humidifying chamber 5 constant. However, in the present invention,
if another measure can keep the water level in the humidifying chamber 5 constant,
the pressure equalizing line 4e is not required.
[0014] Water in the humidifying chamber may be in communication with the outside, or may
not be in communication with the outside. In cases where the water is in communication
with the outside, a line can be further provided to introduce water from the outside
to the humidifying chamber and to discharge heated water to the outside (not shown
in the figures). In the case where the water is introduced from the outside, the flow
rate and the temperature of the water can be accordingly determined such that the
water temperature in the humidifying chamber satisfies the predetermined condition
(for example, 80°C or higher). However, in either case, whether the water is introduced
or not introduced from the outside, it is preferable that the only heat produced by
electrolytic reaction is used to heat the water up to the predetermined temperature
in view of energy efficiency.
[0015] In the above unit cell 1, saltwater as a starting material is supplied from the inlet
3b for saltwater to the anode chamber 3, and at the same time, oxygen-containing gas
is bubbled from an inlet 5a for oxygen-containing gas into water stored in the humidifying
chamber 5 to generate the humidified oxygen-containing gas (oxygen concentration may
be, for example, 90 % or more, preferably 93 % or more). By supplying the humidified
oxygen-containing gas to the cathode chamber 4 and applying an electrical current,
chlorine is generated at the anode 3a and sodium hydroxide is generated at the gas-diffusion
cathode 4a. With progression of the electrolytic reaction of saltwater, heat generated
at the cathode is conducted to the humidifying chamber 5, which can heat the water
stored in the humidifying chamber 5 and facilitate vaporization of the water in the
humidifying chamber. The following supply of the oxygen-containing gas to the humidifying
chamber by means like bubbling can generate oxygen-containing gas including water
vapor with an amount approximately equal to the saturation amount at the water temperature
in the humidifying chamber. Therefore, without using extra energy other than the energy
for electrolytic reaction, the efficiency of humidifying the oxygen-containing gas
can be improved. Moreover, in the case where oxygen-containing gas that contains highly
concentrated water vapor is supplied from a humidifier located outside the electrolytic
cell, which is disclosed in the Patent Document 1, enough amount of water vapor cannot
be supplied because of water condensation in a pipe during being supplied. Additionally,
especially in an electrolytic cell having some unit cells, each of the unit cells
may be supplied with a different amount of water because the degree of water condensation
may vary in each of the unit cells. On the contrary, in the present invention, since
each of the unit cells is equipped with the humidifying chamber, enough amount of
water can be supplied to each of the unit cells without variation of the water amount.
Furthermore, by conducting heat of the cathode chamber to the humidifying chamber,
overheating of the unit cells, that is, overheating of the electrolytic cell, can
be prevented without extra energy for cooling.
[0016] In the example of FIG. 1 described above, the humidifying chamber 5 is adjoined to
the cathode chamber 4 in the unit cell 1. However, the humidifying chamber 5 may be
adjoined to the anode chamber 3 (as described, the unit cell equipped with the chambers
in the sequence of the humidifying chamber 5, the anode chamber 3, and the cathode
chamber 4 is hereinafter referred to as a B-type unit cell; the unit cell equipped
with the chambers in the sequence of the anode chamber 3, the cathode chamber 4, and
the humidifying chamber 5 is hereinafter referred to as a A-type unit cell.). Even
in the case of the B-type unit cell, since the electrolytic reaction at the anode
chamber 3 is an exothermal reaction, heat generated by the exothermal reaction can
be used to heat the humidifying chamber 5 to improve the efficiency of generating
water vapor. In addition, as described later, more than one B-type unit cells can
be placed next to each other, and in such a case, the humidifying chamber 5 may be
adjoined to the cathode chamber 4 of the adjacent unit cell. In this case, the exothermal
reaction in the cathode chamber 4 in the adjacent unit cell can improve the efficiency
of generating water vapor in the humidifying chamber 5.
[0017] Chlorine generated in the anode chamber 3 is discharged from the outlet 3c along
with saltwater after electrolyzation. Sodium hydroxide generated in the cathode chamber
4 is transformed into aqueous sodium hydroxide having a concentration of about 32.0
% to 34.0 % with electro-osmotic water from the anode chamber 3 or moisture in the
oxygen-containing gas transferred to the cathode chamber, which runs down the cathode
chamber under its weight and is discharged along with exhaust gas of the oxygen-containing
gas from an outlet 4g for electrolytic reactant. As described above, since enough
amount of water can be supplied to the cathode in the present invention, the concentration
of the aqueous sodium hydroxide can be kept from being too high, and as a result,
damage of the gas-diffusion cathode 4a and the ion exchange membrane 2 can be prevented.
[0018] The partition 6 in the unit cell 1 may have at least one opening 7 having various
shapes, as long as the partition 6 allows the humidified oxygen-containing gas to
be communicated from the humidifying chamber 5 to the cathode chamber 4 through an
upper side of the partition 6. For example, as shown in FIG. 2(b), the partition 6
may have a plurality of openings 7 on its upper side. The at least one opening 7 located
at the upper side of the partition 6 may occupy the entire upper side of the partition
6 as shown in FIG. 2(a), or may occupy a part of the upper side of the partition 6
as shown in FIG. 2(b). Furthermore, the number of the at least one opening 7 is not
particularly limited and may be one or more. Further, the shape of the at least one
opening 7 is not particularly limited.
[0019] Moreover, the partition 6 may not have the at least one opening 7, as long as the
humidified oxygen-containing gas is allowed to be communicated from the humidifying
chamber 5 to the cathode chamber 4. For example, the humidified oxygen-containing
gas may be supplied to the cathode chamber 4 through an external flow path such as
a connecting pipe 8 as shown in FIG. 3. The unit cell 1 in FIG. 3 is the same as the
unit cell in FIG. 1 except that the unit cell 1 in FIG. 3 is equipped with the connecting
pipe 8 instead of the opening 7 shown in FIG. 1.
[0020] In the case where the aforementioned B-type unit cell is used, connecting the humidifying
chamber 5 and the cathode chamber 4 by the connecting pipe 8 as described above enables
the humidified oxygen-containing gas to be supplied from the humidifying chamber 5
to the cathode chamber 4. In addition, in the case where more than one B-type cell
is placed next to each other, to enable the oxygen-containing gas to be supplied from
the humidifying chamber 5 to the cathode chamber 4 of the adjacent unit cell, the
opening 7 may be formed at the boundary of the humidifying chamber 5 and the cathode
chamber 4 of the adjacent unit cell, or the connecting pipe 8 may be connected to
the humidifying chamber 5 and the cathode chamber 4 of the adjacent unit cell.
[0021] In the unit cell as described above (including both the A-type unit cell and the
B-type unit cell; the same applies hereafter), the anode 3a is not particularly limited,
as long as it is an insoluble anode used for electrolysis of saltwater. For example,
the anode may be such that coating of metal oxide including ruthenium oxide, titanium
oxide, iridium oxide, or platinum-group metal oxides is applied on a base substance
having a mesh structure such as expanded metal or fine mesh composed of metal including
titanium.
[0022] The ion exchange membrane 2 is not particularly limited as long as it can be used
for electrolysis of saltwater, and for example, it can be exemplified by a cation
exchange membrane of perfluorocarbon-type, in which the ion exchange group is carboxyl
acid and/or sulfonic acid.
[0023] The gas-diffusion cathode 4a is not particularly limited as long as it can be used
for electrolysis of saltwater by the oxygen cathode method, and it is exemplified
by a sheet-like triple-layer electrode in which a base material such as metal mesh-like
material, carbon cloth, and/or hydrophobic resin is used, a reactive layer supported
by a hydrophile catalyst is jointed on one side of the base material, and a water-shedding
gas-diffusion layer is jointed on the other side of the base material. The catalyst
can be exemplified by silver, platinum, gold, metal oxides, and carbon. The gas-diffusion
cathode may be permeable to liquid, or may not permeable to liquid.
[0024] In the cathode chamber 4, absence of liquid between the ion exchange membrane 2 and
the gas-diffusion cathode 4a makes it impossible for current to flow therebetween.
While liquid can be retained between the ion exchange membrane 2 and the gas-diffusion
cathode 4 by capillary action if the ion exchange membrane 2 and the gas-diffusion
cathode 4 are closely attached to each other, it is preferable that the liquid retention
layer 4b is placed between the ion exchange membrane 2 and the gas-diffusion cathode
4a to retain liquid more certainly. The liquid retention layer 4b enables liquid such
as aqueous sodium hydroxide to be uniformly retained between the ion exchange membrane
2 and the gas-diffusion cathode 4a to prevent an increase in current density and voltage.
Hydrophilicity and corrosion resistance are required for the liquid retention layer
because the liquid retention layer needs to retain aqueous sodium hydroxide (having
a concentration of about 30 % and temperature of about 80°C to 90°C) generated by
electrolytic reaction. Therefore, carbon materials such as carbon fibers and a porous
structure composed of resin are preferably used.
[0025] An advantage of the two-chamber type method is that voltage can be made small due
to small electric resistance between the electrodes since the anode, the ion exchange
membrane, and the cathode are adjoined to each other. To closely attach the gas-diffusion
cathode 4a to the ion exchange membrane 2 (if necessary, through the liquid retention
layer 4b), it is preferable that the cushion material 4d is placed in a compressed
state to generate reactive force, which is utilized to closely attach the gas-diffusion
cathode 4a to the ion exchange membrane 2. In the two-chamber type method, separated
by the ion exchange membrane, liquid pressure exerted by saltwater is applied to the
anode chamber, and gas pressure is applied to the cathode chamber. The reactive force
of the cushion material 4d is designed in conformity with the difference between the
liquid pressure and the gas pressure. Since the deeper the depth of the saltwater
is, the larger the liquid pressure is, making the reactive force of the cushion material
at the lower side larger than at the upper side of the cathode chamber enables pressure
applied to the ion exchange membrane or the anode electrode to be uniform. As such
a cushion material 4d, a coiled material or a waved mat material can be used. Since
the coiled material has elasticity in the diametrical direction and generates the
reactive force in the diametrical direction, the coil axis can be placed parallel
to the back board of the cathode gas chamber, and the reactive force of the cushion
material can be designed to be larger at the lower side than at the upper side by
selecting the wire diameter of the coil, the diameter of the coil material, and the
laying density of the coil. As to the waved mat material, waved demister mesh in which
metal wires are stocking stitched can be used, and the reactive force of the cushion
material can be designed to be larger at the lower side than at the upper side by
selecting the diameter of the wires, the number of the wires, and the number of the
lamination layers of the mat material.
[0026] The gas-diffusion cathode support 4c can be placed between the cushion material 4d
and the gas-diffusion cathode 4a, if necessary. The gas-diffusion cathode support
4c receives the reactive force of the cushion material 4d to allow the force to be
uniformed and transmits the uniformed force to the gas-diffusion cathode 4a and the
liquid retention layer 4b, and farther, the ion exchange membrane 2. As the gas-diffusion
cathode support 4c, mesh materials such as a woven metal wire can be used.
[0027] Since both the cushion material 4d and the gas-diffusion cathode support 4c are placed
in the cathode chamber, which is in a high corrosive environment because of high temperatures
and the existence of highly concentrated oxygen and highly concentrated sodium hydroxide,
it is preferable that nickel or nickel alloy whose nickel content is 20 % by weight
or more, and silver plating thereof is used.
[0028] As the material for the walls constituting the anode chamber 3, titanium or titanium
alloy whose titanium content is 20 % by weight or more is preferably used. As the
material for the walls constituting the cathode chamber 4 and the humidifying chamber
5, nickel or nickel alloy whose nickel content is 20 % by weight or more, and silver
plating thereof is preferably used.
[0029] In the present invention, more than one of the aforementioned unit cells (the A-type
unit cells or the B-type unit cells, preferably the A-type unit cells) may be placed
next to each other to compose the electrolytic cell. In this case, each of the unit
cells may be connected in parallel electrically to compose a monopolar electrolytic
cell, or each of the unit cells may be connected in series electrically to compose
a bipolar electrolytic cell, and the bipolar electrolytic cell is preferable. Hereinafter,
the monopolar electrolytic cell and the bipolar electrolytic cell will be explained
referring to an example in which more than one of the A-type unit cells having the
aforementioned opening 7 for the means of communication of the oxygen-containing gas
between the humidifying chamber 5 and the cathode chamber 4 are placed next to each
other. The following example may be applied to another example in which the connecting
pipe 8 is used or in which more than one of the B-type cells are placed next to each
other.
[0030] FIG. 4 is a schematic cross-section view of an example of a monopolar electrolytic
cell, in which three of the A-type unit cells having the opening 7 are placed next
to each other. In the monopolar electrolytic cell 10 shown in FIG. 4, more than one
of the A-type unit cells (three of the A-type unit cells in the example of the figure),
in which the aforementioned anode chamber 3, the cathode chamber 4, and the humidifying
chamber 5 are placed in this sequence, can be arranged such that the sequence in each
of the unit cells may be alternately reversed, such as the regular sequence (the anode
chamber 3, the cathode chamber 4, and the humidifying chamber 5 are placed in this
sequence), the reverse sequence (the humidifying chamber 5, the cathode chamber 4,
and the anode chamber 3 are placed in this sequence), the regular sequence, and the
reverse sequence. The anode electrodes of each of the unit cells are connected to
an external electric source in parallel electrically respectively, and the cathode
electrodes of each of the unit cells are also connected to the external electric source
in parallel electrically respectively. The reference sign 9 shows a water storage
tank for adjusting water level in the humidifying chamber. This example also allows
heat of the cathode chamber 4 to be transmitted to the humidifying chamber 5 to humidify
the oxygen-containing gas efficiently. In such an aforementioned example, in which
more than one of the unit cells are placed next to each other such that the sequence
in each of the unit cells may be alternately reversed, the humidifying chamber 5 of
one of the unit cell (1) may be adjoined to the humidifying chamber 5 of the next
unit cell (2). In this case, one humidifying chamber 5 may be shared by both the unit
cell (1) and the unit cell (2).
[0031] FIG. 5 is a schematic cross-section view of an example of a bipolar electrolytic
cell, in which four of the A-type unit cells having the opening 7 are placed next
to each other. In the bipolar electrolytic cell 20 shown in FIG. 5, more than one
of the unit cells 1 (four of the unit cells 1 in the example of the figure), each
of which has the anode chamber 3 and the cathode chamber 4 internally having the humidifying
chamber 5, are arranged such that the sequence of the anode chamber 3, the cathode
chamber 4, and the humidifying chamber 5 is repeated. In the bipolar electrolytic
cell 20, the anode electrode 3a in one unit cell (1) is capable of being electrically
conducted to the cathode electrode 4a in the next unit cell (2) (not shown in the
figure), and the cathode electrode 4a at one end and the anode electrode 3a at the
other end are connected to an external electric source respectively to connect each
of the unit cells in series electrically. Each of the inlets 3b for saltwater of the
unit cells, each of the outlets 3c for electrolyzed saltwater and chlorine of the
unit cells, each of the inlets 5a for oxygen-containing gas of the unit cells, each
of water inlets 5b of the unit cells, each of the outlets 4g for electrolytic reactant
of the unit cells, and each of the pressure equalizing lines 4e of the unit cells
are respectively connected to each other by pipes, and the water inlets 5b and the
pressure equalizing lines 4e are connected to the water storage tank 9. The mechanism
of the electrolytic reaction in each of the unit cells of the bipolar electrolytic
cell 20 is the same as in the aforementioned unit cells. However, because of the arrangement
of the unit cells, each of the humidifying chambers 5 is adjoined not only to the
cathode chamber 4 in the same unit cell but also to the anode chamber 3 in the next
unit cell. Therefore, the humidifying chamber 5 can use heat generated by electrolytic
reaction in both the anode chamber 3 and the cathode chamber 4 for humidification,
which results in the increase of the heat efficiency in humidification. In addition,
since the heat generated in the anode chamber 3 is transferred to the humidifying
chamber 5, the anode chamber 3 can be cooled at the same time.
[0032] Moreover, in the case where more than one of the B-type unit cells (having the sequence
of the humidifying chamber, the anode chamber, and the cathode chamber) are arranged
regularly without alternately reversing the sequence of each of the unit cells to
compose a bipolar electrolytic cell such as the example shown in FIG. 5, the humidifying
chamber 5 is sandwiched by the anode chamber 3 and the cathode chamber 4. In this
case, the humidifying chamber 5 can also use heat generated in both the anode chamber
3 and the cathode chamber 4 during humidification.
EXAMPLES
[0034] Hereinafter, the present invention is more specifically described with reference
to examples. The present invention, however, is not limited by the following examples
but can also be absolutely carried out with appropriate changes to the examples within
a scope in compliance with the intent described above and later, and all the changes
are to be encompassed within a technical scope of the present invention.
Example 1
[0035] Five of the unit cells shown in FIG. 1 (except not having a gas-diffusion cathode
support) were arranged such that the sequence of an anode chamber, a cathode chamber,
and a humidifying chamber was repeated in this sequence, and were connected to each
other in series electrically to compose a bipolar two-chamber type electrolytic cell
for saltwater. DSE manufactured by De Nora Permelec Ltd. (insoluble metal in which
metal base substance is coated with platinum-group metal or oxides thereof as a main
component) was used as an anode electrode; gas-liquid transmissive carbon-silver electrode
(GDE2013) manufactured by De Nora Permelec Ltd. was used as an cathode electrode;
4403D manufactured by Asahi Kasei Chemicals Corporation was used as an ion exchange
membrane; carbon fiber woven fabric, the thickness of which is 0.45 mm, was used as
a liquid retention layer; and silver-plated nickel wire in spiral shape was used as
a cushion material.
[0036] Saltwater having a concentration of 218 g/L and a temperature of 53.8°C was supplied
to the anode chamber at the rate of 183 L/m
2/h. Water was stored in the humidifying chamber, to which 1.5 times the theoretical
requisite moles of oxygen-containing gas (corresponds to "oxygen-containing gas supplied
to electrolytic cell" shown in the below table 1) having a temperature of 25°C and
a concentration of 93.0 % was supplied by bubbling. The temperature of the humidifying
chamber was 84.0 °C, and therefore, at the time when being supplied to the cathode
chamber, the temperature of the humidified oxygen-containing gas was about 84.0°C.
The saltwater was electrolyzed at the current density of 5.65 kA/m
2, and each value was measured after ten days of the electrolyzation.
Comparative Example 1
[0037] Except not having the humidifying chamber in a unit cell, five of the same unit cells
as Example 1 having the same material of the anode electrode, the cathode electrode,
the ion exchange membrane, etc. and the same size of the cathode chamber, the anode
chamber, etc. were arranged such that the sequence of the anode chamber, and the cathode
chamber is repeated in this sequence, and were connected to each other in series electrically
to compose a conventional bipolar two-chamber type electrolytic cell for saltwater
(not shown in the figures).
[0038] Saltwater having a concentration of 219 g/L and a temperature of 51.4°C was supplied
to the anode chamber at the rate of 183 L/m
2/h. The cathode chamber of each of the unit cells was connected to a humidifier prepared
outside the electrolytic cell. In the humidifier, 1.5 times the theoretical requisite
moles of oxygen-containing gas having a concentration of 93.0 % was bubbled into the
water (25°C) in the humidifier to generate humidified oxygen-containing gas having
a temperature of 25°C, which was supplied to the cathode chamber at the same temperature.
The saltwater was electrolyzed at the current density of 5.65 kA/m
2, and each value was measured after ten days of the electrolyzation. Being different
from Example 1, Comparative Example 1 did not have the humidifying chamber in the
unit cell and the humidified oxygen-containing gas was supplied from the external
humidifier, and therefore, the meaning of "oxygen-containing gas supplied to electrolytic
cell" and "oxygen-containing gas supplied to cathode chamber" shown in the below table
1 are identical in meaning (the same applies to the following Comparative Examples
2 to 4).
Comparative Example 2
[0039] In the same manner as in Comparative Example 1 except that the water temperature
of the external humidifier in Comparative Example 1 was altered to 84°C, and that
humidified oxygen-containing gas generated at 84°C was supplied to the cathode chamber
at the same temperature (heat input rate to the humidifier was about 5.2 MJ/m
2/h), each value was measured after ten days of the electrolyzation.
Comparative Example 3
[0040] With the same composition as in Comparative Example 2, additionally, heat-retention
around the pipe connecting the humidifier and the anode chamber of each of the unit
cells was improved to prevent the temperature of the humidified oxygen-containing
gas from decreasing, and each value was measured after ten days of the electrolyzation.
The heat input rate to the humidifier was about 5.2 MJ/m
2/h, which was the same as in Comparative Example 2.
Example 2
[0041] The same electrolytic cell as in Example 1 was operated for 300 days, after which
each value was measured.
Comparative Example 4
[0042] The same electrolytic cell as in Comparative Example 1 was operated for 300 days,
after which each value was measured.
[0043] The measurement results of the Examples and the Comparative Examples are shown in
Table 1 and Table 2. Table 2 shows both the average value of five of the unit cells
and the difference between the average value and each value of five of the unit cells
in the concentration of generated sodium hydroxide and current efficiency.
[Table 1]
|
Current density (kA/m2) |
Supplied Saline water |
Liquid in anode compartment |
Oxygen-containing gas supllied to electrolysis cell |
Oxygen-containing gas supplied to cathode compartment |
Cell voltage (V) |
Temperature in humidifying compartment (°C) |
Tempera -ture of catode (°C) |
Tempera -ture of exhaust gas (°C) |
Average concentration of generated NaOH (%) |
Current efficiency (%) |
Amount (L/m2/h) |
Concent -ration (g/L) |
Temperature (°C) |
Concentration (g/L) |
Temperature (°C) |
Concentration (%) |
Multiple of theoretical amount |
Temperature (°C) |
Temperature (°C) |
Example 1 |
5.65 |
183 |
218 |
53.8 |
173 |
84.0 |
93.0 |
×1.5 |
25.0 |
84.0 |
2.30 |
84.0 |
82.0 |
82.0 |
32.2 |
96.5 |
Comparative Example 1 |
5.65 |
183 |
219 |
51.4 |
174 |
84.0 |
93.0 |
×1.5 |
25.0 |
25.0 |
2.32 |
- |
75.0 |
75.0 |
34.6 |
96.5 |
Comparative Example 2 |
5.65 |
183 |
219 |
47.0 |
174 |
84.0 |
93.0 |
×1.5 |
84.0 |
84.0 |
2.30 |
- |
82.0 |
82.0 |
32.2 |
96.4 |
Comparative Example 3 |
5.65 |
183 |
219 |
47.0 |
174 |
84.0 |
93.0 |
×1.5 |
84.0 |
84.0 |
2.30 |
- |
82.0 |
82.0 |
32.2 |
96.5 |
Example 2 |
5.65 |
183 |
218 |
53.3 |
173 |
84.0 |
93.0 |
×1.5 |
25.0 |
84.0 |
2.35 |
84.0 |
82.0 |
82.0 |
32.2 |
96.3 |
Comparative Example 4 |
5.65 |
183 |
219 |
51.0 |
174 |
84.0 |
93.0 |
×1.5 |
25.0 |
25.0 |
2.43 |
- |
75.0 |
75.0 |
34.6 |
96.0 |
[Table 2]
|
Concentration of generated NaOH |
Current efficiency |
Average (%) |
#1 |
#2 |
#3 |
#4 |
#5 |
Average (%) |
#1 |
#2 |
#3 |
#4 |
#5 |
Example 1 |
32.2 |
-0.2% |
+0.1% |
+0.1% |
+0.2% |
-0.2% |
96.5 |
-0.2% |
+0.1% |
0% |
+0.2% |
-0.1% |
Comparative Example 1 |
34.6 |
-0.2% |
+0.2% |
+0.1% |
+0.1% |
-0.2% |
96.5 |
-0.3% |
+0.1% |
+0.1% |
0% |
+0.1% |
Comparative Example 2 |
32.2 |
+0.5% |
-0.2% |
-0.4% |
-0.2% |
+0.3% |
96.4 |
-0.4% |
+0.2% |
+0.3% |
+0.2% |
-0.3% |
Comparative Example 3 |
32.2 |
-0.1% |
+0.2% |
+0.2% |
0% |
-0.3% |
96.5 |
-0.2% |
+0.2% |
+0.1% |
0% |
-0.1% |
Example 2 |
32.2 |
-0.1% |
+0.1% |
0% |
+0.2% |
-0.2% |
96.3 |
-0.2% |
+0.1% |
0% |
+0.2% |
-0.1% |
Comparative Example 4 |
34.6 |
0% |
+0.2% |
+0.1% |
-0.1% |
-0.2% |
96.0 |
-0.3% |
+0% |
+0.2% |
+0.2% |
-0.1% |
[0044] In Example 1, due to the reaction heat, the temperature of the humidifying chamber
was equivalent to the temperature of the anode chamber, and the concentration of generated
sodium hydroxide was 32.2 %, not too high, which shows that enough amount of water
vapor was supplied (Table 1). In addition, variation in the concentration of generated
sodium hydroxide and in current efficiency in each of five unit cells could be made
small, which shows that the variation in the amount of the water vapor supplied to
the anode chamber of each of the unit cells was small (Table 2). Moreover, Example
2, in which the electrolyzation was operated longer than in Example 1, showed good
current efficiency of 96.3 % even after 300 days, as well as good results in other
values almost the same as in Example 1. Since enough amount of water vapor could be
supplied in Example 2, low concentration of generated sodium hydroxide could be maintained,
and since damage of the gas-diffusion cathode was prevented in Example 2, the difference
in voltage of the gas-diffusion cathode after 300 days of electryzation was as small
as 45 mV on average. The differences in voltage of the gas-diffusion cathode in each
of the unit sells were 78 mV, 15 mV, 45 mV, 33 mV, and 54 mV respectively.
[0045] On the other hand, in Comparative Example 1, in which humidified oxygen-containing
gas was supplied from the external humidifier, since the temperature of the external
humidifier was 25.0°C, the pressure of water vapor in the gas was low, and the concentration
of generated sodium hydroxide was as high as 34.6 %, which shows that the supplied
amount of water vapor was insufficient (Table 1).
[0046] Comparative Example 2 was an example in which the temperature of the external humidifier
was altered to 84°C to increase the water vapor pressure in the oxygen-containing
gas, which required energy to raise water temperature in the external humidifier.
The average concentration of generated sodium hydroxide was 32.2 %, which means that
enough amount of water vapor could be supplied on the average, however, as shown in
Table 2, the variation in both the concentration of sodium hydroxide and current efficiency
of each unit cell became large. The reason of this is considered that water was condensed
in the process where the oxygen-containing gas was supplied from the external humidifier
to the cathode chamber of each of the unit cells, and the degree of the condensation
was different in each of the unit cells. In addition, since the oxygen-containing
gas of high temperature was supplied from outside the electrolytic cell, the saltwater
supplied to the anode electrode was required to have a low temperature to prevent
the electrolytic cell from overheating (while the temperature of the supplied saltwater
in Example 1 was 53.8°C, which is within the usual range of the temperature in saltwater
electrolysis plants, the temperature of the supplied saltwater in Comparative Example
2 was 47.0°C.), and thus, extra energy was required for cooling the supplied saltwater.
[0047] Comparative Example 3 was an example in which heat-retention of the pipe from the
external humidifier in Comparative Example 2 was improved, and required extra energy
for heating in the external humidifier, which is the same as in Comparative Example
2. In Comparative Example 3, water condensation was suppressed in the pipes, and as
a result, the variations in the concentration of the generated sodium hydroxide and
the current efficiency of each of the unit cells could be made small, however, extra
energy for cooling the supplied saltwater was required in the same manner as in Comparative
Example 2.
[0048] Comparative Example 4 was an example in which the electrolytic cell was operated
for 300 days in the same condition as in Comparative Example 1, and the difference
in the voltage of the gas-diffusion cathode after 300 days of electrolyzation was
108 mV on average of five of the unit cells, which was much higher than in Example
2, and current efficiency was 96.0 %, which was lower than in Example 2. The reason
of this is considered that as the same as in Comparative Example 1, the concentration
of generated sodium hydroxide was 34.6 % in Comparative Example 4, which was 2 % or
higher than the concentration of sodium hydroxide of 32.2 % in Examples 1 and 2, and
as a result, the gas-diffusion cathode was damaged. The differences in voltage of
the gas-diffusion cathode in each of the unit sells were 123 mV, 66 mV, 114 mV, 108
mV, and 129 mV respectively.
DESCRIPTION OF REFERENCE SIGNS
[0049]
- 1:
- unit cell
- 2:
- ion exchange membrane
- 3:
- anode chamber
- 3a:
- anode electrode
- 4:
- cathode chamber
- 4a:
- gas-diffusion cathode
- 5:
- humidifying chamber
- 6:
- partition
- 7:
- opening
- 8:
- connecting pipe
- 10:
- monopolar electrolytic cell
- 20:
- bipolar electrolytic cell
1. A method for producing sodium hydroxide and/or chlorine by electrolyzing saltwater,
the method comprising
using a two-chamber type electrolytic cell for saltwater comprising one or more unit
cells equipped with an anode chamber including an anode, a cathode chamber including
a gas-diffusion cathode, and an ion exchange membrane sandwiched by the anode chamber
and the cathode chamber,
supplying saltwater to the anode chamber, and
supplying humidified oxygen-containing gas to the cathode chamber, wherein
each of the unit cells further comprises a humidifying chamber generating the humidified
oxygen-containing gas that is to be supplied to the cathode chamber,
the humidifying chamber is adjoined to and in heat exchange relation with the anode
chamber or the cathode chamber in one of the unit cells, or is adjoined to and in
heat exchange relation with the anode chamber or the cathode chamber in another of
the unit cells adjacent to the one of the unit cells, and
the oxygen-containing gas is humidified by generating water vapor with heat from the
anode chamber or the cathode chamber.
2. The method according to claim 1, wherein the humidifying chamber is adjoined to the
cathode chamber, and the humidified oxygen-containing gas generated in the humidifying
chamber is supplied from the humidifying chamber to the cathode chamber through at
least one opening located at a partition between the humidifying chamber and the cathode
chamber.
3. The method according to claim 2, wherein the at least one opening located at the partition
between the humidifying chamber and the cathode chamber comprises a single opening.
4. The method according to claim 2, wherein the at least one opening located at the partition
between the humidifying chamber and the cathode chamber comprises a plurality of openings.
5. The method according to claim 1, wherein the humidified oxygen-containing gas generated
in the humidifying chamber is supplied from the humidifying chamber to the cathode
chamber through at least one flow path located outside the humidifying chamber and
the cathode chamber.
6. The method according to claim 5, wherein the at least one flow path located outside
the humidifying chamber and the cathode chamber comprises a single flow path.
7. The method according to claim 5, wherein the at least one flow path located outside
the humidifying chamber and the cathode chamber comprises a plurality of flow paths.
8. The method according to any one of claims 1 to 7, wherein the unit cells are connected
with each other in the electrolytic cell, and the unit cells are arranged such that
the sequence of the anode chamber, the cathode chamber, and the humidifying chamber
is repeated.
9. A two-chamber type electrolytic cell for saltwater, comprising one or more unit cells
equipped with an anode chamber, a cathode chamber, and an ion exchange membrane sandwiched
by the anode chamber and the cathode chamber, wherein
the anode chamber includes an anode, and is equipped with an inlet for saltwater as
a starting material, an outlet for electrolyzed saltwater, and an outlet for chlorine,
the cathode chamber includes a gas-diffusion cathode, and is equipped with an inlet
for humidified oxygen-containing gas and an outlet for electrolytic reactant,
each of the unit cells further comprises a humidifying chamber generating oxygen-containing
gas that is to be supplied to the cathode chamber, and
the humidifying chamber is adjoined to and in heat exchange relation with the anode
chamber or the cathode chamber in one of the unit cells, or is adjoined to and in
heat exchange relation with the anode chamber or the cathode chamber in another of
the unit cells adjacent to the one of the unit cells, and is equipped with an inlet
for the oxygen-containing gas.
10. The electrolytic cell according to claim 9, wherein the unit cells are connected with
each other in the electrolytic cell, and the unit cells are arranged such that the
sequence of the anode chamber, the cathode chamber, and the humidifying chamber is
repeated.