U.S. patent number 3,779,875 [Application Number 05/281,741] was granted by the patent office on 1973-12-18 for preparation of glyoxylic acid.
This patent grant is currently assigned to Rhone-Poulenc S.A.. Invention is credited to Daniel Michelet.
United States Patent |
3,779,875 |
Michelet |
December 18, 1973 |
PREPARATION OF GLYOXYLIC ACID
Abstract
In the cathodic reduction of oxalic acid to glyoxylic acid
production of hydrogen is reduced when the catholyte contains
oxalic acid and 0.001 percent - 1 percent of an adjuvant which is a
tertiary amine or quaternary ammonium derivative having more than
11 carbon atoms and, the nitrogen of which is not part of an
unsaturated heterocyclic ring, or a heterocyclic tertiary amine or
quaternary ammonium derivative thereof, the heterocyclic ring being
unsaturated, containing a nitrogen atom and at least five carbon
atoms.
Inventors: |
Michelet; Daniel
(Sainte-Foy-Les-Lyon, FR) |
Assignee: |
Rhone-Poulenc S.A. (Paris,
FR)
|
Family
ID: |
9082085 |
Appl.
No.: |
05/281,741 |
Filed: |
August 18, 1972 |
Foreign Application Priority Data
|
|
|
|
|
Aug 20, 1971 [FR] |
|
|
7130396 |
|
Current U.S.
Class: |
205/443;
204/296 |
Current CPC
Class: |
C25B
3/25 (20210101) |
Current International
Class: |
C25B
3/04 (20060101); C25B 3/00 (20060101); C07b
029/06 (); C07c 051/40 (); C07c 053/08 () |
Field of
Search: |
;204/75-77 |
References Cited
[Referenced By]
U.S. Patent Documents
|
|
|
798920 |
September 1905 |
Von Portheim |
1013502 |
January 1912 |
Liebknecht |
|
Primary Examiner: Edmundson; F. C.
Claims
I claim:
1. A process for the preparation of glyoxylic acid by the cathodic
reduction of oxalic acid which consists of carrying out an
electrolysis in an electrolysis cell comprising a cathode, a
cathode compartment, a separating diaphragm, an anode compartment
and an anode, the said cathode compartment containing a catholyte
comprising an aqueous solution of oxalic acid, and 0.00005 to 1
percent by weight of an adjuvant which is:
a. a tertiary amine or quaternary ammonium compound which has a
total of more than 11 carbon atoms and the nitrogen atom of which
is not part of an unsaturated heterocyclic ring
b. a heterocyclic tertiary amine or quaternary ammonium compound
derived therefrom; the heterocyclic ring structure of which is
unsaturated, contains nitrogen and possesses at least 5 carbon
atoms.
2. A process according to claim 1, wherein the adjuvant is of the
formula ##SPC6##
wherein each of R.sub.1, R.sub.2, R.sub.3, R.sub.4, R.sub.5,
R.sub.6 and R.sub.7 independently represents a saturated or
unsaturated, linear or branched, aliphatic hydrocarbon radical, or
any pair from R.sub.1, R.sub.2, R.sub.3 and R.sub.4, or any pair
from R.sub.5, R.sub.6 and R.sub.7 together forms a saturated
alkylene or an oxydialkylene radical, or a radical containing at
least two oxyalkylene groups
.alpha. represents a hydrogen atom, or an alkyl radical of up to 20
carbon atoms, or a radical of the formula ##SPC7##
or two adjacent .alpha. symbols together form a radical of the
formula ##SPC8##
the number of unsaturated rings in the compound of the formula III
or V being at most equal to 3;
R.sub.8 represents an alkyl radical of up to 20 carbon atoms.
y is equal to 1, 2 or 3
A.sup.y.sup..theta. is the hydroxyl radical or an anion such that
AH.sub.y represents an inorganic or organic acid.
3. A process according to claim 1, wherein the adjuvant is present
in the catholyte in solution.
4. A process according to claim 2 wherein the adjuvant is selected
from the group consisting of tetrabutyl-ammonium,
tributyl-lauryl-ammonium, trimethyl-lauryl-ammonium,
trimethyl-myristyl-ammonium, trimethyl-palmityl-ammonium,
trimethyl-stearyl-ammonium, trimethyl-oleyl-ammonium,
trimethyl-linoleyl-ammonium, trimethyl-linolenyl-ammonium,
trimethyl-arachidyl-ammonium, trimethyl-behenyl-ammonium,
trimethyl-erucyl-ammonium, triethyl-stearyl-ammonium and
triethyl-hexyl-ammonium salt and hydroxide, pyridine, quinoline and
2,2'-dipyridyl.
5. A process according to claim 1, wherein at least one of the
catholyte and anolyte are circulated outside the cathode and anode
compartments respectively.
6. A process according to claim 5, wherein the catholyte is
circulated, oxalic acid is continuously added to the catholyte and
catholyte is withdrawn to extract the glyoxylic acid produced
therein.
7. A process according to claim 1 wherein the cathode and anode are
made of lead, the diaphragm is a crosslinked sulphonated
styrene-divinylbenzene copolymer dispersed in a polyvinyl chloride
matrix, the catholyte and anolyte are separately circulated outside
the cathode and anode compartments respectively, the catholyte is
degassed with nitrogen and contains 2.9 .times.10.sup.-.sup.3 to
0.01 mol/l of an adjuvant selected from tetra-n-butylammonium,
tributyl lauryl ammonium, triethyl-n-stearyl ammonium hydroxides,
triethyl-n-hexylammonium bicarbonate, trimethyl-n-stearyl ammonium
chloride, pyridine, quinoline and 2,2'-dipyridyl.
Description
The present invention relates to a new process for the preparation
of glyoxylic acid by the cathodic reduction of oxalic acid.
The preparation of glyoxylic acid by the cathodic reduction of
oxalic acid is described in German Patent Specifications Nos.
163,842, 194,038 and 204,787 and Belgian Patent Specification No.
757,106; according to these processes, the oxalic acid, which is
electrolysed, is in the form of an aqueous solution which may
contain sulphuric acid. The majority of the processes described in
the prior art do not state the results obtained during prolonged
electrolyses; two main documents, however, mention this
problem.
H. D. C. Rapson et al. (J. Appl. Chem., 13th June 1963, p 233)
state that the current yield changes from 90 percent at the start
of electrolysis to 30 percent at the end of electrolysis, but he
makes no comment on the causes of this phenomenon.
German Patent Specification No. 347,605 also discloses that a
decrease in yields, and especially in the current yield, is found
after a few hours of electrolysis. In practice, the lowering of the
current yield shows itself by an increase in the production of
hydrogen at the cathode.
The reason for this increase in the production of hydrogen at the
cathode is not completely clear; it probably originates, wholly or
partially, from impurities present in the oxalic acid. Thus
according to German Patent Specification No. 347,605, contamination
of the cathode would occur, but the nature of the impurities
responsible for this contamination is not stated, nor is the origin
or the degree of purity of the oxalic acid employed.
We have now found that the production of hydrogen is greatly
decreased if oxalic acid, which has been recrystallised several
times is used, and that the production of hydrogen is particularly
high if commercial oxalic acid is used, whether it is prepared from
formates (Encyclopaedia of Chemical Technology, Kirk-Othmer, 2nd
edition, 14, p 362-364) or whether it is prepared by the nitric
acid oxidation of propylene (German Patent Specification No.
742,053 and French Patent Specifications Nos. 1,487,446, 1,501,725,
1,528,569 and 2,031,833). Though we do not intend to be bound to
any particular theory, we consider that one of the factors to which
the formation of hydrogen, and thereby the decrease in the electric
current yields, can be attributed, could be the presence of
transition metal ions (especially iron), it being possible for
these ions to originate either from the starting reagents
(especially oxalic acid), or, if these reagents do not contain any
(i.e. the oxalic acid employed being pure acid),from the apparatus
used for the electrolysis.
We have also found that with commercial acid, the current yields
become insufficient after rather short periods of time, e.g.
considerably less than 5 days (an Example of German Patent
Specification No. 347,605). Even if the particular cathodes
disclosed in German Patent Specification No. 347,605 are used, the
advantages achieved with these cathodes (i.e. decrease in the
production of hydrogen) disappear in experiments of long duration
when commercial oxalic acid is reduced electrolytically. The
current yields vary with the batches of commercial oxalic acid
used.
The present invention provides a process for the preparation of
glyoxylic acid by the cathodic reduction of oxalic acid which
consists of carrying out an electrolysis in an electrolysis cell
comprising a cathode, a cathode compartment, a separating
diaphragm, an anode compartment, and an anode, the said cathode
compartment containing a catholyte comprising an aqueous solution
of oxalic acid, and 0.00005 to 1 percent by weight of an adjuvant
which is:
a. a tertiary amine or quaternary ammonium compound which has a
total of more than 11 carbon atoms and the nitrogen atom of which
is not part of an unsaturated heterocyclic ring.
b. a heterocyclic tertiary amine or quaternary ammonium compound
derived therefrom, the heterocyclic ring structure of which is
unsaturated,contains nitrogen and possesses at least five carbon
atoms.
The adjuvants defined above generally have less than 40 carbon
atoms in all.
Preferred adjuvants are those having the formulae: ##SPC1##
wherein each of R.sub.1, R.sub.2, R.sub.3, R.sub.4, R.sub.5,
R.sub.6 and R.sub.7, which may be the same or different, represents
a saturated or unsaturated, linear or branched, aliphatic
hydrocarbon radical, or any pair from R.sub.1, R.sub.2,R.sub.3 and
R.sub.4, or any pair from R.sub.5, R.sub.6 and R.sub.7 together
forms a saturated alkylene or oxydialkylene radical, or a radical
containing at least 2 oxyalkylene groups, for example, a radical of
the formula --(CH.sub.2).sub.n --[--O--(CH.sub.2).sub.n --].sub.m
--OH wherein n = 2 or 3 and m is an integer of 1 to 10,
.alpha. represents a hydrogen atom, or an alkyl radical of up to 20
carbon atoms, or a radical of the formula ##SPC2##
or two adjacent .alpha. symbols together form a radical of the
formula: ##SPC3##
the number of unsaturated rings in the compound of the formula III
or V being at most equal to 3; the preferred amines of the formula
III or IV are pyridine, dipyridyl, quinoline, phenanthroline and
their derivatives carrying alkyl substituents, especially picolines
and lutidines.
R.sub.8 represents an alkyl radical of up to 20 carbon atoms.
y is equal to 1, 2 or 3.
A.sup.y .sup..theta. is the hydroxyl radical or an anion such that
AH.sub.y represents an inorganic or organic acid.
The nature of A.sup.y .sup..theta. can be varied widely and any
particular anion can be replaced by another according to the
conventional techniques of ion exchange; examples of anions
represented by A.sup.y .sup..theta. in addition to the hydroxyl
radical, are nitrate, sulphate, phosphate, sulphonate, bicarbonate
and oxalate.
The adjuvants used in the invention are preferably those which are
soluble in water at the concentration considered, and in particular
it is preferred to choose A.sup.y .sup..theta. so that the salts
have this solubility.
Examples of preferred adjuvants are tetrabutyl-ammonium,
tributyl-lauryl-ammonium, trimethyl-lauryl-ammonium,
trimethyl-myristyl-ammonium, trimethyl-palmityl-ammonium,
trimethyl-stearyl-ammonium, trimethyl-oleyl-ammonium,
trimethyl-linoleyl-ammonium, trimethyl-linolenyl-ammonium,
trimethyl-arachidyl-ammonium, trimethyl-behenyl-ammonium,
trimethyl-erucyl-ammonium, triethyl-stearyl-ammonium and
triethyl-hexyl-ammonium salts, especially the halides and
bicarbonates and the hydroxides; pyridine, quinoline and
2,2'-dipyridyl.
The temperature of the catholyte is generally between 0.degree. and
70.degree.C., and preferably between 5.degree. and 35.degree.C.
Examples of metallic materials which are capable of forming the
cathodes used in the process of the invention, are lead, cadmium,
mercury and amalgams, as well as the alloys of these metals,
particularly with silver, tin or antimony.
The anode of the electrolysis cells consists of an electrically
conducting material which is electrochemically stable in the
anolyte and under the operating conditions considered. Examples of
such materials are metals and metalloids such as platinum,
platinised titanium, graphite, lead and its alloys, particularly
with silver, antimony or tin.
The separating diaphragm of the anode and cathode compartments is
preferably a cation exchange membrane. Any known membrane can be
used, but membranes of the homogeneous type and membranes of the
heterogeneous type are preferred. These membranes can optionally be
reinforced with a screen. For carrying out electrolysis operations
over a long period, it is naturally preferred to use membranes,
which do not swell and which are stable to the action of the
various constituents of the catholyte and the anolyte. Examples of
such membranes are those described in the following specifications.
United States Patent No. 2,681,320 and French Patent Nos.
1,568,994, 1,575,782, 1,578,019, 1,583,089, 1,584,187 and
2,040,950.
The permeation selectivity of the membranes used (defined in and
measured as in French Patent Specification No. 1,584,187) is
preferably greater than 60%.
The catholyte used in the process according to the invention can
comprise water, oxalic acid,glyoxylic acid, one or more adjuvants
having one of the formulae I to V and, optionally, a strong
inorganic acid such as sulphuric acid; however, the strong acid is
preferably absent.
The catholyte can contain oxalic acid without glyoxylic acid only
at the start of electrolysis; in the same way, the catholyte can
contain glyoxylic acid without oxalic acid only at the end of
electrolysis. The concentrations of the oxalic and glyoxylic acid
can be either constant when the reaction is carried out
continuously, or variable when the reaction is carried out
discontinuously or at the start of a continuous operation. In all
cases, the concentration of oxalic acid is less then the saturation
value at the temperature of electrolysis; generally, this
concentration is greater than 2 percent by weight, this value
relating particularly to the constant concentration when the
reaction is carried out continuously and to the final concentration
when the reaction is carried out discontinuously. The concentration
of glyoxylic acid is usually between 3 and 25 percent by weight,
and preferably between 5 and 15 percent by weight, these values
relating particularly to the constant concentration of glyoxylic
acid when the reaction is carried out continuously and to the final
concentration of this acid when the reaction is carried out
discontinuously.
The oxalic acid can be the commercially available material, or if
preferred the acid recrystallised from this can be used. Oxalic
acid produced by any known process can be used with apparatus in
which no special precautions are necessary to remove harmful
ions.
As has been stated above, the concentration of adjuvant in the
catholyte is usually 0.00005 to 1 percent by weight. This
concentration is preferably between 0.0001 and 0.5 percent; the use
of these small amounts has the value of avoiding the need to remove
the adjuvant from the glyoxylic acid produced, as the adjuvant in
these amounts hardly exerts any harmful effect on the properties of
the acid.
The adjuvant helps to reduce the amount of hydrogen produced at the
cathode and improves the electrical yield.
The catholyte can also contain reaction byproducts in small
amounts, e.g. generally less than 1 percent.
An aqueous acid solution is preferably used as the anolyte, though
any other anolyte capable of providing electrical conductivity
between the two electrodes can be used. Aqueous solutions of
sulphuric or phosphoric acids are usually employed in a
concentration generally of 0.1 to 5 mols/litre, and preferably 0.5
to 2 mols/litre.
The current density at the cathode is preferably 3 to 50
A/dm.sup.2, and especially 10 to 35 A/dm.sup.2.
In order to carry out the invention, electrolysis cells of any
known type can be used, for example, those disclosed in the patent
specifications mentioned above and especially Belgian Patent
Specification No. 757,106.
However, it is preferred to use electrolysis cells with solid
electrodes, which makes it possible to produce a compact apparatus,
especially of the filter press type. The electrodes and the
separating diaphragm are advantageously located in parallel
planes.
Also advantageously, either or both of the catholyte and the
anolyte can be circulated in their respective compartments, which
makes it possible to achieve better results.
Finally, spacers, for example, woven fabrics or grids, can be
located between the electrodes and the separating diaphragm.
The following Examples illustrate the invention.
The concentrations of solutions expressed as a percentage denote,
unless otherwise stated, the number of grams of solute per 100
cm.sup.3 of solution; however, these concentrations in g/100
cm.sup.3 differ only slightly from concentrations in %
(weight/weight) because the solutions employed in the Examples
generally have a density of about 1.
The "commercial" oxalic acid used in the Examples is an acid
prepared according to the techniques described in French Patent
Specification No. 331,498 and British Patent Specification No.
11,487/1915, the various reactions carried out leading to an oxalic
acid solution which is dried in vacuo and then crystals separated
from mother liquor. The product is an oxalic acid dihydrate with a
degree of purity of about 99.2 percent. The recrystallizations
mentioned in the Examples were carried out from water.
EXAMPLE 1
The reduction of commercial oxalic acid is carried out in a cell
possessing the following characteristics:
Both the electrodes are rectangular plates of lead with a usable
surface area of these electrodes being 2.5 dm.sup.2.
The cation exchange membrane is of the heterogeneous type
consisting of a crosslinked sulphonated styrene/divinylbenzene
copolymer dispersed in a polyvinyl chloride matrix, and is
reinforced with a screen in the form of a woven fabric.
Permeation selectivity measured in 0.6 M KCl solution: 77.5
percent
Substitution resistance measured in 0.6 M KCl solution: 7
.OMEGA..cm.sup.2.
Electrodes-membranes distance: 3mm.
Two pumps cause the catholyte and the anolyte to flow in the
corresponding compartments of the cell.
The circuits where the anolyte and the catholyte flow each contain
an expansion vessel equipped with supply and removal pipelines.
The circuit of the catholyte also contains a heat exchanger.
The electrolysis conditions are as follows:
current density: -- 14 A/dm.sup.2
voltage: -- 4.45 V
temperature -- 20.degree.C.
speed of flow of the electrolytes over the electrodes: -- 1
m/second.
The catholyte is degassed with a stream of nitrogen of 300 1/hour
and the hydrogen formed is measured by gas phase chromatography, in
the gas coming from the expansion vessel of the catholyte
circuit.
Catholyte introduced initially: 7 l of a 3.28% oxalic acid
solution.
This solution is electrolysed for 7 hours 15 minutes, supplying
0.510 l/hour of a 15.6 percent strength aqueous solution of oxalic
acid and removing the catholyte so as to keep its volume constant;
in a second stage, electrolysis is carried out continuously at
constant concentration for 21 hours, supplying the catholyte with
0.825 l/hour of a solution containing 10.5 percent of oxalic acid.
During this entire period, the volume of the catholyte is kept
constant at 7 l.
At the end of this period, which has lasted for a total of 28 hours
15 minutes, the rate of production of hydrogen is measured; from
this rate, an instantaneous current yield of 18.25 percent (yield
for the production of hydrogen) is deduced.
The catholyte was found to contain 4.4 percent glyoxylic acid and
4.2 percent oxalic acid.
50 cm.sup.3 of a 40 percent (weight/weight) solution of
tetra-(n-butyl)-ammonium hydroxide are then added, as an adjuvant,
and electrolysis is continued, supplying 0.815 l/hour of a 10.5
percent solution of oxalic acid until the end of the experiment
(with corresponding removal of catholyte to constant volume).
Because of the continuous removal of the catholyte solution, the
content of adjuvant decreases at the end of the experiment.
Table I shows the development of the instantaneous current yield
(yield for the production of hydrogen) during the various time
intervals studied. ##SPC4##
Yields for the production of glyoxylic acid:
The average yields during the period of the experiment which
extends from 39 hours 15 minutes to 79 hours 15 minutes, namely 40
hours, were evaluated The catholyte removed during the 40 hours
represents 33.990 l. The material balance for the 40 hour period
considered is as follows:
oxalic acid employed -- 3,423 g
oxalic acid consumed -- 2,220 g
glyoxylic acid produced -- 1,674 g
current yield -- 86.6%
yield of glyoxylic acid relative to the oxalic acid consumed --
91.7%
EXAMPLE 2
In this experiment, an apparatus similar to that described in
Example 1 is used, but the usable surface area of the electrode is
0.8 dm.sup.2.
Electrolysis is carried out under the following conditions:
current density -- 25 A/dm.sup.2
temperature -- 23.degree.C
electrolysis voltage -- 5.3 V
speed of flow of the electrolytes over the electrodes -- 1
m/second
the catholyte is degassed with a stream of nitrogen of -- 100
l/hr.
Catholyte introduced initially: 1.630 l of a 5.8% aqueous solution
of oxalic acid (commercial oxalic acid, recrystallised once from
water). This solution is electrolysed for 1 hour and recrystallised
oxalic acid containing 17.2 g of pure oxalic acid is then
introduced again into the catholyte. This addition is repeated
every 30 minutes during the first 9 hours of electrolysis. The
volume of catholyte is kept constant at 1.600 l. After a total
electrolysis time of 9 hours, the hydrogen, which is liberated from
the catholyte, represents an instantaneous current yield of 10.7
percent.
The catholyte is found to contain 8.5 percent glyoxylic acid and
4.35 percent oxalic acid.
3 cm.sup.3 of a 40 percent (weight/weight) solution of
tetra-(n-butyl)-ammonium hydroxide, (i.e. to provide a
concentration of 2.9 .times. 10.sup.-.sup.3 mol/l) are then added
to the catholyte. From this time onwards, 0.220 l/hour of a 17.2
percent aqueous solution of oxalic acid, to which
tetra(n-butyl)-ammonium hydroxide has been added so that the
concentration of tetra-butyl-ammonium ions is 2.9 .times.
10.sup..sup.-3 mol/l, is run in. Electrolysis is carried out under
these conditions for 14 hours. The evolution of hydrogen remains
constant during this entire period and represents an instantaneous
current yield of 3.5 percent.
The yield of glyoxylic acid during the last 14 hours of the
experiment was evaluated. In order to make this evaluation, the
catholyte, which was removed, and the contents remaining in the
cell are combined, giving 4.930 l.
This solution was found to contain 435 g glyoxylic acid and 207 g.
oxalic acid.
Electric current yield -- 77.5 percent
Yield of glyoxylic acid relative to the oxalic acid used up: 92.5
percent.
EXAMPLE 3
The apparatus described in Example 2 is used and electrolysis is
carried out under the following conditions:
current density -- 25 A/dm.sup.2
voltage -- 5.55 V
temperature -- 10.degree.-12.degree.C
speed of flow of the electrolytes over the electrodes -- 1
m/second
degassing of the catholyte with a stream of nitrogen of about 150
l/hour.
Catholyte introduced initially: 1 litre of a 3.57 percent aqueous
solution of oxalic acid (commercial acid recrystallised once from
water).
Electrolysis is carried out for 1 hour 45 minutes, supplying the
catholyte with 0.110 l/hour of a 35.7 percent hot (80.degree.C)
solution of oxalic acid and removal as in previous Examples to keep
the volume constant. The hyrodgen produced at this instant
represents an instantaneous electrical yield of 3.9 percent.
Five g of a 40 percent by weight aqueous solution of
tetra-(n-butyl)-ammonium hydroxide are then added. Electrolysis is
continued for 4 hours 15 minutes with the same rate of feed
catholyte as above; 2 g of the tetra-butyl-ammonium hydroxide
solution mentioned above are then added. Electrolysis is continued
under the same conditions for 1 hour 30 minutes. The volume of the
catholyte is brought to 1.600 l and electrolysis is continued for 6
hours, keeping the volume of the catholyte at 1.6 l by suitable
removal.
From this time onwards and until the end of the experiment, the
catholyte is supplied with a 19.1 percent aqueous solution of
oxalic acid, at the rate of 0.230 l/hour. The evolution of hydrogen
represents an electrical yield which is constant and substantially
equal to 1 percent.
At the end of the experiment, the apparatus is emptied and the
liquid obtained is combined with the liquid removed.
Glyoxylic acid was obtained with an average current yield of 91%
and a yield of 93.2 percent relative to the oxalic acid used
up.
EXAMPLE 4
The apparatus described in Example 2 is used.
The electrolysis conditions are as follows:
current density -- 25 A/dm.sup.2
voltage -- 5.3 V
temperature -- 23.degree.C
speed of flow of the electrolytes over the electrodes -- 1
m/second
The catholyte is degassed with a stream of nitrogen of 100 l/hour
and the hydrogen formed is measured in the gas which comes off.
Catholyte introduced initially: 2 l of a 5.85 percent aqueous
solution of oxalic acid (commercial acid which has not been
recrystallised. This solution is electrolysed for 1 hour 15 minutes
and 17.9 g of oxalic acid are then added to the catholyte every 30
minutes until the end of the experiment. After a total electrolysis
time of 4 hours, the hydrogen produced represents a current yield
of 10.5 percent. 4 cm.sup.3 of an aqueous solution containing 0.5
mol of tributyl-lauryl-ammonium hydroxide/litre are then added.
Electrolysis is continued for 2 hours and the hydrogen evolved,
which then represents a current yield of 0.1 percent, is
measured.
EXAMPLE 5
The reduction of commercial oxalic acid is carried out in a cell
similar to that of Example 1.
The electrolysis conditions are as follows:
current density -- 25 A/dm.sup.2
voltage -- 6.3 V
temperature -- 20.degree.C
speed of flow of the electrolytes over the electrodes -- 1
m/second
The catholyte is degassed with a stream of nitrogen of 300
l/hour.
Catholyte introduced initially: 10 l of a 5 percent aqueous
solution of oxalic acid (commercial acid recrystallised once from
water).
This solution is electrolysed for 29 hours, adding 114 g of oxalic
acid to the catholyte every hour. After operating for 18 hours,
0.500 l of water is added every hour at the same time as the oxalic
acid, and the volume of the catholyte is kept at 10 l.
At the 29th hour, the catholyte contains 9.55 percent glyoxylic
acid and 4.55 percent oxalic acid.
At this instant, the hydrogen produced represents an instantaneous
current yield of 9.55 percent.
1 cm.sup.3 of a solution containing 0.36 mol of
triethyl-(n-stearyl)-ammonium hydroxide/litre is then added to the
catholyte. During the 13 hours of electrolysis which follow, the
hydrogen evolved approximately represents a current yield of about
1.7 percent (constant instantaneous yield). Since the additive is
gradually removed by the withdrawal, the hydrogen evolved then
increases and represents 6.7 percent of the current yield 2 hours
later.
0.2 cm.sup.3 of the solution containing 0.36 mol of
triethyl-(n-stearyl)-ammonium hydroxide/litre is then added to the
catholyte. During the 14 hours which follow, the hydrogen evolved
represents an instantaneous current yield which remains at about
1.2 percent.
EXAMPLE 6
The procedure of Example 4 is followed, using, as the quaternary
ammonium derivative, 5 cm.sup.3 of a solution containing 1 mol of
triethyl-(n-hexyl)-ammonium bicarbonate/litre.
After 6 hours 40 minutes of electrolysis without an adjuvant, the
hydrogen produced represents a current yield of 3.7 percent. The
solution of triethyl-(n-hexyl)-ammonium bicarbonate is added to the
catholyte, the volume of which is 2 l. After the addition, the
current yield corresponding to the hydrogen produced becomes 0.9
percent.
EXAMPLE 7
The procedure of Example 4 is followed, using pyridine as the
adjuvant.
After 10 hours 15 minutes of electrolysis without an adjuvant, the
hydrogen produced represents a current yield of 9.6 percent.
One g of pyridine is then added to the catholyte; at the end of 15
minutes the current yield for the hydrogen is no more than 4.6
percent; 1 cm.sup.3 of pyridine is again added to the catholyte and
electrolysis is continued for a further 3 hours 30 minutes under
the same conditions. During all this time, the instantaneous
current yield corresponding to the hydrogen produced remains
constant and equal to 4 percent.
EXAMPLE 8
The procedure of Example 4 is followed, using quinoline as the
adjuvant. After 5 hours of electrolysis without an adjuvant, the
hydrogen produced represents a current yield of 6.5 percent. 0.25
cm.sup.3 of quinoline is added to the catholyte, the volume of
which is 2 l. The current yield corresponding to the hydrogen
produced after the addition of the adjuvant is no more than 4.1
percent.
EXAMPLE 9
The procedure of Example 4 is followed, using 2,2'-dipyridyl as the
adjuvant.
After 1 hour of electrolysis without an adjuvant, the hydrogen
produced represents a current yield of 21 percent. 0.25 g of
2,2'-dipyridyl is then added to the catholyte, the volume of which
is 2 l. The current yield corresponding to the hydrogen produced
after the addition of the adjuvant is no more than 2.2 percent.
EXAMPLE 10
Electrolysis is carried out in an apparatus similar to that of
Example 1, under the following conditions.
Anolyte: 10 percent by weight aqueous solution of sulphuric
acid.
Catholyte: during the first 10 hours, the apparatus is supplied at
the rate of 0.27 l/hour with an aqueous solution, at 80.degree.C,
containing 57.2 percent by weight of oxalic acid and 0.007 g/l of
trimethyl-stearyl-ammonium chloride.
After the 10th hour and up to the 105th hour, the apparatus is
supplied at the rate of 0.68 l/hour with a solution, at
60.degree.C, containing 25.3 percent by weight of oxalic acid and
0.014 g/l of trimethyl-stearyl-ammonium chloride.
The catholyte is removed at the rate of 0.74 1/hour.
Current density 24 A/dm.sup.2
Electrolysis temperature : about 11.degree.C (maintained by
cooling)
Electrolysis voltage 5.9 V
The anolyte and the catholyte are degassed with a stream of
nitrogen (100 l/hour)
Speed of flow of the electrolytes : l m/second.
Starting from the tenth hour, the various parameters defining the
electrolysis conditions remained practically constant.
The material balance of the operation is as follows:
oxalic acid (dihydrate) employed -- 18.025 kg
oxalic acid (dihydrate) recovered -- 3.855 kg
glyoxylic acid produced -- 7.747 kg ##SPC5##
current yield for the production of glyoxylic
acid 89.2%
current yield for the production of hydrogen: 2 percent
* * * * *