ELECTROCHEMICAL CELL AND PROCESS

Abstract: An electrochemical cell comprises a housing (1, 2) divided by a perforated generally horizontal plate (3) into an upper chamber (4) and a lower chamber (5). Bipolar electrodes (19, 21) are disposed in the upper chamber (4) above perforations (23) in the plate (3), between electrolyte inlet and outlet weirs (11, 13) for flowing electrolyte over the plate (3). The lower chamber (5) is a gas-supply chamber for passing a gas, e.g. propylene, up through the perforations (23), so as to bubble the gas through electrolyte (e.g. NaBr solutions) on the plate (3) and into the upper gas-collection chamber (4). A reactor may be formed by stacking several cells with their electrolyte flows in cascade. The cell is particularly suitable for electro-organic syntheses involving a gaseous reactant.

Description: ELECTROCHEMICAL CELL AND PROCESS Technical Field The invention relates to electrochemical cells r particularly for carrying out electrochemical reactions involving a gaseous reactant or in which gas is supplied for another purpose such as purging or sweeping away a product of reaction, or as a buffering agent or to inhibit unwanted reactions. The invention is more specifically, but not exclusively, concerned with an electrochemical cell for electro-organic synthesis, for example the electro¬ chemical oxidation of unsaturated and poly- nsaturated hydrocarbons, The electrochemical production of propylene oxide is particularly interesting, and will be discussed in greater detail by way of example. Background Art In the electrochemical production of propy¬ lene oxide, propylene is converted to propylene halohydrin by reaction with, halogen generated ±n situ by the anodic oxidation of _.he halide salt of an alkali metal in aqueous solution. The propylene halohydrin is converted to propylene oxide by reaction with the hydroxyl group at the cathode from which hydrogen is -liberated. The general'scheme of reaction when sodium bromide is used as the electrolyte is: Anode 2 Br " . 3r, + 2 e C 3_.H,6_ + Br2. + H2_0 + HBr Cathode 2 H-0 f- H- + 2 OH- - 2e , C 3 H 6 BrOH + OH *- C 3 K_0 + H„0 + Br Overall C3-H6- + H20 —^ C3-H6.O + H2 In principle, only water, propylene and electrical energy are consumed in the formation of propylene oxide and hydrogen. The halide electrolyte, sodium bromide, is continuously oxidized and re¬ generated within the cell for further use, although losses of bromine may be caused by the formation of hypobromite and bromine gas. - The advantages of this electrochemical route, which obviates the production of waste calcium chloride encountered in the conventional chemical process, have long been recognized but attempts to implement it have not proved to be very effective. French Patent Specification No. 1,375,973 and ~ i. German Auslegeschrift No. 1,258,856 proposed the use of diaphragm cells in which propylene halohydrin is . generated at a porous anode and passes through the diaphragm into an alkaline catholyte in a porous cathode where it is saponified to propylene oxide. However, these cells are complex and the efficiency low. U.S. Patent Specification No. 3,394,059 proposed carrying out the halohydrin process in a non- divided cell, preferably a flowing mercury cathode cell, in which propylene was simply bubbled into the electro- lyte. Again, the performance was poor and F. Beck (IUPAC XXIVth International Congress, Hamburg, 1973, Vol.5, "Applied Electrochemistry", pages 111-136) has claimed an improved performance using a capillary gap cell. In this, propylene dispersed in a dilute NaBr electrolyte is supplied through a central hole 5 in a pile of electrode discs and flows radially out¬ wards between the discs. The gap between the elec¬ trode discs was made small CO•2 to 0.5 mm), to enable * low bromide concentrations to be handled with low ohmic losses. A current efficiency of 70% or just Q above and an energy consumption of Q.23 - 0.30 kwh/ gmol propylene oxide are reported for a small capillary gap cell, but scaling up this cell for- industrial production would involve difficulties. Fleischmann et al, (.Symposium on Electro- 5 chemical Engineering _I, Newcastle 1971, Editor J.D. Thornton) have studied the synthesis of propylene oxide using a bipolar packed bed cell. The cell consisted of a packed bed made up of a mixture of conducting and non-conducting particles. The Q conducting particles become bipolar by using dilute electrolyte in the cell and applying sufficient voltage gradient between the contact electrodes so as to over¬ come the resistance drop in the electrolyte. Using glass coated with graphite as the conducting particles 5 and glass beads as the non-conducting particles, all particles having a diameter of about.0.05 cm, the energy consumption o .such a cell was found to be high, in the range of 2.5 - 3 kwh/gmol propylene oxide. A bipolar rod flow cell was used by King et al, 0 CTrans. Inst. Chem. Eng. , 53, 1975) for the production of propylene oxide. The cell consisted of vertical rows of electrically—conductive rods, separated from one another by a small gap. The electrolyte was fed to the top rods, flowed downvmrds over the vertical 5 rows and was collected from the bottom rods for re- "gUR£_ £^ circulation. The gaseous reactant, propylene, was passed up the space between the vertical rows, in continuous contact with the electrolyte film. The current efficiency of this cell was of the order of 70% and the energy consumption is estimated in the range 0.35 - 0.4 kwh/gmol propylene oxide. R.E. . Jansson et al. have developed a bipolar electrochemical pump cell for which an energy yield below 0.2 kwh/gmol of propylene oxide is claimed (Journal of App. Electrochemistry, 7, (1977) , 437-443) for trial experiments on a laboratory scale using a cathode rotating at 3000 rpm with an electrode gap of 0.25 mm. However, the structure is not easily scaled-up for industrial production. Various other cell structures designed to provide a gas supply to the electrolyte are also known. For example, in the electrowinning of metals such as copper, it is well known to supply a gas through bubble tubes situated below the electrodes in order to agitate the electrolyte (e.g. see U.S. Patent Specification No. 3,875,041 and the earlier patents referred to therein). Another suggestion made in U.S. Patent Specification No. 3,259,049 was to provide electrolyte agitation in an electroplating tank using a hollow, flat manifold which is placed in the electrolyte, under the electrodes, and has a perforated upper surface for bubbling gas up into the electrolyte, the gas being supplied to the manifold via a gas flow tube. In contrast to the fixed bubble- tube arrangements, the entire manifold structure was made removable to facilitate periodic cleaning to remove fragments which may block the perforations in the manifold. Disclosure of Invention An object of the invention is to provide an B 0 i\ " AΓ > ORIGINAL electrochemical cell specifically (but not exclusively) for the production of propylene oxide and which can be designed to meet up. to the following requirements better than the previously proposed cells: 1) Simplicity of the mechanical construction; 2) Good heat and mass transfer characteristics; 3) Simplicity of operation and continuous operation; 4) ' Good gas-liquid contact; and 5) Good mixing of anolyte and catholyte products. 0 According to the invention, in its simplest form, an electrochemical cell comprises electrodes disposed over a perforated generally horizontal plate, an electrolyte inlet and an electrolyte outlet spaced apart on opposite sides of the electrodes across the 5 perforated plate, and a cell housing which is divided by the perforated plate into an upper chamber and a lower chamber. The lower chamber is a gas supply chamber from which, in use, gas passes up through perforations in the plate and bubbles through electro- Q lyte on the plate to collect in the upper chamber. The electrolyte inlet and electrolyte outlet of the cell are each advantageously formed by a weir. The top of the inlet weir is higher than the top of the outlet weir which in turn is higher than the top of the 5 electrodes. Hence, by controlling the supply of fresh electrolyte to the inlet weir, the electrolyte is made to flow over the inlet weir and between the electrodes as it passes across the perforated plate, while spent or reacted electrolyte flows out over the outlet weir at a 0 chosen rate.' These weirs may be formed by upstanding plates integral with or fixed on the perforated plate. The electrodes, advantageously a bipolar array of vertical plate-like electrodes 'disposed in spaced parallel relationship to provide channels between the ^-^ -^ y- electrolyte inlet and outlet,, may rest on the perforated plate which.,, in this instance, will be made of electric¬ ally insulating material. The perforations in the plate can be arranged in rows each spaced about mid-way between 5 adjacent electrodes. Perforations in the form of gen¬ erally circular bores having a diameter of about 1 mm hav been found satisfactory, but- perforations of other form and size can be used. The bottom of the lower chamber of the cell Q housing can serve as a receptacle for a pool of spent or reacted electrolyte which flows via a downcomer tube leading from the aforementioned outlet weir into the * pool from which electrolyte is removed via an outlet and may be recycled. Fresh electrolyte can be supplied to 5 the aforementioned inlet weir via an incomer tube which extends down through the upper chamber of the cell housi into the electrolyte retained by the inlet weir. The upper and lower chambers may be formed by upper and lower sections of a box-like cell housing, the 0 sections being separated by .the aforesaid plate which is perforated only in the region under the electrodes. A • rectangular enclosure for the electrodes may thus be formed by the side walls of the upper housing section fitting against upstanding plates forming the inlet and 5 outlet weirs. These side walls can carry inset termina electrodes of the electrode array. The invention also concerns an electrochemical reactor formed by stacking several cells according to th invention in a column whereby the gas-collection chamber Q of each cell (except the top one) forms the gas-supply chamber for the cell above. In other words, the per¬ forated plate of each cell (except the lowest one) forms the top of the gas-collection chamber of the cell below. With this arrangement, in operation, gas passes up 5 througb. the cells from the bottom of the column to the top, bubbling through the electrolyte in each cell. Preferably, the electrolyte outlets and inlets of the successive cells are connected in cascade so that the electrolyte ' flows down the column from one cell to the 5 next, the electrolyte flowing across the perforated plate of each cell from the inlet to the outlet and then down to the inlet of the cell below. Each cell of such a reactor can have the aforementioned preferred features of a single cell unit, such as the electrolyte Q inlets and outlets being formed By weirs. Another aspect of the invention is a method of carrying out an electrochemical process or reaction using a cell according to the invention, this method comprising passing gas up through the perforations in 5 the plate s o that it bubbles into the electrolyte on the plate. Depending on the reaction, the method may be operated continuously, i.e. continuously, supplying gas, electrolyte and electric current, or discontinuously, i.e. with an intermittent supply of gas, electrolyte and/ 0 or current. Yet another aspect of the invention is a method of carrying out an electrochemical process or reaction using a reactor formed by a column of cells according to the invention, this method comprising flowing 5 electrolyte down the column from. one cell to the next and across -the perforated plate of each cell, and passing gas up through the perforations in the successive plates so that the gas bubbles through the electrolyte on each plate. This method may also be operated continuously Q or discontinuously. The gas may be a reactant or a mixture of reac.ants, or may serve another purpose, for instance an inert purge gas such as nitrogen may be used to sweep away a product of reaction, or a buffering agent such as 5 CO- or .NH_ may be used to control the pH of the electro- -Bϋkt^ OΛ1PI lyte, for example to inhibit unwanted reactions. In addition to the preparation of propylene oxide, the cell according to the invention could be used in the electro-synthesis of other products such as the formation of butylene oxide from butene. Another important application is the electro¬ chemical treatment of some effluent gases. Generally speaking, many applications concern the situation where one or more of the reactants is a gas and where mixing of anolyte and catholyte is advantageous or inconsequen¬ tial. Brief Description of Drawings Embodiments of the invention are shown, by way of example, in the accompanying drawings, in which: Fig. 1 is a cross-section of a cell along the line I-I of Fig. 2; Fig. 2 is a cross-section along the line II-II of Fig. 1; Fig, 3 is a sectional view of the cell of Figs. 1 and 2 along the line III-III of Fig. 1; Fig. 4 is a cut-away view similar to Fig. 1, of part of a column formed of several cells connected in cascade. Best modes for carrying out the Invention The cell of Figs. 1 to 3 comprises a generally rectangular box-like housing composed of an upper section 1 and a lower section 2. A plate 3, fixed between flanges 34 of the upper and lower sections 1,2 divides the housing into an upper chamber 4 and a lower chamber 5. The joints between the flanges 34 and the plate 3 are sealed by gaskets 6. The upper chamber 4 has an electrolyte inlet section 7, an electrode section 8 and an electrolyte outlet section 9. • The inlet section 7 comprises an incomer tube 10 which passes through the top 35 of the 5 upper section 1 and extends down to near the plate 3, between an upstanding plate 11 and three side walls 36 -of the section 1. The plate 11, which is integral with the plate 3, extends across the width of the chamber 4 and forms an inlet weir which, in use, holds a pool of 10 electrolyte at a level 12, this electrolyte being del¬ ivered via the incomer tube 10. The electrolyte outlet section 9 comprises an outlet weir plate 13 which also extends across the width of the chamber 4, but is formed by one wall of an 15 enlarged square end 14 of a downcomer tube 15 which passes through a hole 16 in the plate 3. The square end 14 is fitted in a corresponding square recess defined by the side walls 36 of the upper section 1 and an upstanding plate 17 integral with the plate 3. The 20. top of the outlet, weir plate 13, is lower than the top of the inlet weir plate 11 and, in use, it maintains electrolyte in the electrode section 8 at a level 18. In the electrode section 8 are disposed seven electrodes 19 in .the form of plates held in spaced 25 parallel relationship in vertical grooves 20 in the plates 11 and 17. The electrodes 19 are disposed between two terminal electrodes 21 which are inset in the side walls 36 through which pass current leads 22. The plate 11 at one end of the spaced electrodes, and 30 the plates 17 and 13 at the other end define, with the side walls 36 of the section 1, an electrolyte receptacle whose' bottom is formed by a perforated central part of the plate 3. The perforations in the plate 3, indicated at 23, are in the form of circular holes or bores having 35 a diameter of about 1mm, arranged in eight rows each of -10- seven equally-spaced holes disposed mid-way between the adjacent electrodes 19 or 19 and 21. The upper, housing section 1 also comprises, in its top 35, a gas outlet pipe 24 for the removal of 5 gas from the upper chamber 4. In the lower chamber 5, the downcomer tube 15 extends near to the bottom, below the level of an upstanding wall 30 which forms a trap or weir holding a pool of outgoing electrolyte at a level 31. In the 0 bottom of the lower section 2 is an outlet pipe 32 for removing the electrolyte which has flowed over the weir wall 3Q. The lower housing section 2 also has a gas inlet pipe 33 for delivering gas into the lower chamber 5. Electrolyte in the bottom of the chamber 5 prevents this 15 gas from escaping via the outlet pipe 32 or the down¬ comer tube 15, so that the gas passes up through the perforations 23 in the plate 3 and bubbles into the electrolyte between the electrodes 19, and 19 and 21 in the electrode section 8. 20. To operate the cell, the electrolyte outlet pipe 32 is connected to the incomer tube 10 by an electrolyte circulating system, and the gas outlet pipe 24 is connected to the inlet pipe 33 by a gas circula¬ ting system. The electrolyte is circulated at a chosen 25 rate so that fresh electrolyte from the incomer tube 10 flows over the inlet weir, namely the plate 11, across the electrode section _, i.e. through the parallel channe defined between the electrodes 19, and 19 and 21, and out over the outlet weir plate 13. The gas is also cir- 30 culated at a chosen rate, which can be adjusted independently of the electrolyte flow rate. It passes from -the lower chamber 5 up through the perforations 23 and bubbles through the electrolyte between the electrodes 19, and 19 and 21 into the upper or gas-collection chambe 35 4. When all of the flows have been set up, current is supplied to the electrodes 13 and 21. In some instances, i.e. when the gas is a reactant, current is supplied to the electrodes as the gas is supplied, and the operation -is advantageously continuous, i.e. with constant electrolyte and gas flowrates. In other instances, however, it may be advantageous to operate discontinuously, i.e. with an intermittent flow of electrolyte or .gas or both, with- current supply during the appropriate phase.- The product of the electro- chemical reaction may be taken off as a gas and removed from the gas stream before recirculating, or may be : taken off dissolved in the electrolyte, in which case it is removed from the electrolyte before recycling. For the production of propylene oxide, the product will partition itself between the electrolyte and the gas phase and may therefore advantageously be removed through- -the σas outlet pipe 24 and separated by conden¬ sation . Industrial applicability A cell as shown in Figs. 1 to 3 was used for the production of propylene oxide. The electrodes were plates of graphite each 6.3 cm high, 8.3 __. long and 0.3 cm thick ' and spaced apart by ' a distance cf about 4 ___. The electrolyte, 5 litres of 0.2M or 0.2K aBr solution, was flowed at a constant rate, in the range from about 20 3 to 45 cm /sec. Propylene gas was also circulated, using a supply of fresh propylene at. a constant rate in the 3 range from about 5 to 40 cm /sec. Before supplying a constant current (.at from 1 to 2A and a constant voltage from 25 to 4QV) , the propylene was circulated for several minutes, to remove air from the cell housing and to saturate the electrolyte solution. Operation was carried out at ambient temperature and atmospheric , . pressure and the pH of the electrolyte was maintained between about 11. and 12 by ^_V ^ adding HBr solution. Gas and liquid samples were checked at 1/2 hourly intervals. In some instances, a foaming agent ( . "Decon", Trademark) was added with a view to promoting rapid mass transport of the reactants to the electrodes, and to increase the solubility of propylene. The results showed a high current efficien about 80.%, and a low energy consumption, 0.2 to 0.3 " kwh/gmol of propylene . oxide when operating at low temperature, low current and low gas flowrate using dilute NaBr. For the epoxidation of 1-butεne using th same cell, an energy consumption of 0.26 kwh/gmol of butylene oxide was achieved at a current efficiency approaching that obtained with propylene oxide. These performances may be improved by optimizing the cell dimensions and process conditions and, possibly, by operating at elevated pressures. As shown in Fig. 4, several cells similar to that of Figs. 1 to 3 can be stacked in a column with the electrolyte flow system connected in cascade. In Fig. 4, the same parts are designated by the same references as before, some parts of the intermediate cells -being designated by double references. The upper section 1 of the housing of the top cell and the lower section 2 of the housing of the bottom cell are exactly the same as the upper and lower sections 1 and 2 of Figs. 1 and 2. However, in the reactor column, the perforated plate 3 forming the bottom of one cell also forms the top of the gas collection chamber 4 of the cell below and its perforations 23 act as the gas outlet for that chamber; the downcomer tube 15 for the discharge of electrolyte from one cell forms the incomer tube 10 of the cell below; the gas collection chamber 4 of eac cell (except the top one), forms the gas supply chamber 5 for the cell above; and so- forth. In operation of this reactor column, gas is supplied at the bottom of the column, via the inlet pipe 33, passes up through the successive cells, bubbling up through the electrolyte in each electrode section 8, and is removed from the top of the column via the outlet pipe 24. Electrolyte is supplied at the top 35 of the column via the top incomer tube 10 and, as indicated by the arrow, cascades down from one cell to the next, flowing across the electrode section 8 of each cell, and is removed from the bottom of the column via the outlet pipe 32. As before, current is supplied to the electrodes of each cell and the operation may be continuous or discontinuous. Many variations may be made to the described embodiments. Various electrode materials can be used, depending on the reaction: ..in particular, dimen- sionally-stable metal electrodes will be preferred for some reactions. Also, the electrodes need not be bipolar. In some instances, spaced parallel electrodes can be disposed transverse to the general direction of flow of electrolyte across the perforated plate. Various shapes and sizes of perforations can be provided in this plate and, instead of being disposed between the adjacent electrodes, for certain reactions these per¬ forations could lead into porous or foraminous electrodes disposed on the perforated plate. Instead of the preferred electrolyte inlet and outlet weirs, other means could be provided to enable a flow of the electrolyte generally across the perforated.plate, while maintaining a given electrolyte level. OΛ.PI

Claims: CLAIMS 1. An electrochemical cell, comprising electrodes disposed over a perforated generally hori¬ zontal plate, an electrolyte inlet and an electrolyte outlet spaced apart on opposite sides of the electrodes across the perforated plate, and a cell housing which is divided by the perforated plate into an upper chamber and a lower chamber, wherein the lower chamber is a gas supply chamber for passing gas via the perforations in the perforated plate through the electrolyte located above the plate in the upper chamber. 2. The electrochemical cell of Claim 1, wherein the electrolyte inlet and the electrolyte outlet are each- formed by a weir, 3. The electrochemical cell of Claim 2, wherein the top of the electrolyte inlet weir is higher than the top of the electrolyte outlet weir which is higher than the top of the electrodes. 4. The electrochemical cell of Claim 2 or 3, wherein the weirs are formed by plates upstanding from the perforated plate. 5. The electrochemical cell of claim 1, comprising a bipolar array of vertical plate-like electrodes disposed in spaced parallel relationship to define channels between the electrolyte inlet and the electrolyte outlet. 6. The electrochemical cell of claim 5, wherein the bipolar electrodes rest on the perforated plate, which is made of electrically-insulating material, and wherein the perforations in the plate are arranged in rows spaced about mid-way between adjacent electrodes. 7. The electrochemical cell of claim 2, wherein a bottom part of the lower chamber forms a receptacle for a pool of reacted electrolyte, and a downcomer tube leads from the electrolyte outlet weir -~_ _} R E O to the bottom part of the lower chamber, for the delivery of reacted electrolyte to the pool. 8. The electrochemical cell of claim 7, comprising an incomer tube extending down through the upper chamber, for the delivery of fresh electrolyte to the electrolyte inlet weir. 9. The electrochemical cell of claim 1, wherein the upper and lower chambers are formed by respective separate upper and lower sections of a box-like cell housing, the housing sections are separated by and secured to the periphery of the plate and the per¬ forations are disposed in the plate only in the region under the electrodes. 10. The electrochemical cell of claim 9, wherein the.upper housing section has facing side walls which fit against upstanding plates forming electrolyte inlet and outlet weirs to define a rectangular enclosure for the electrodes. 11. The electrochemical cell of claim 10, comprising a bipolar array of vertical plate-like electrodes disposed in spaced parallel relationship to define channels between the electrolyte inlet and electrolyte outlet weirs, said electrode array including terminal electrodes inset in said facing side walls of the upper housing section. 12. An electrochemical cell, comprising: a cell housing; a perforated generally horizontal plate dividing the cell housing into an upper chamber and a lower chamber; electrodes disposed in the upper chamber ~ over perforations in the perforated plate; and means defining an electrolyte inlet and an electrolyte outlet spaced apart on opposite sides of the electrodes across '_ _T EA7 the perforated plate to maintain electrolyte on the perforated plate at an intermediate level of the upper chamber so as at least partially to immerse the electrodes and define a gas-collection space in the upper chamber above the electrolyte; the lower housing chamber constituting a gas supply chamber for passing gas up through perforations in the plate so as to bubble the gas through the electrolyte on the plate and into the gas-collection space 13. An electrochemical reactor comprising (I) a plurality of cells, each cell comprising (i) electrodes disposed over a perforated generally horizontal plate and (ii) an electrolyte inlet and (iii) an electrolyte outlet spaced apart on opposite sides of the electrodes across t perforated plate, and (.II) a reactor housing in which the cells are stacked in a columnar arrangement, the perfora- ted plates of the cells dividing the reactor housing into superimposed chambers, each perforated plate being dis¬ posed over a gas-supply chamber for passing gas up throug perforations in the plate to bubble through electrolyte on the plate and collect in the chamber thereabove and which (.except for that of the top cell) forms the gas- supply chamber for the cell above. 14. The electrochemical reactor of claim 13, wherein the electrolyte inlet and the electrolyte outlet of each cell are formed by weirs. 15. The electrochemical reactor of claim 14, wherein the top of the electrolyte inlet weir of each cell -is higher than the top of the electrolyte outlet weir which is higher than the top of the electrodes. 26, The electrochemical reactor of claim 14 or 15, wherein the weirs are formed by plates upstanding from the perforated plates, 17. The electrochemical reactor of claim 13, wherein each cell comprises a bipolar array of vertical plate-like electrodes disposed in spaced parallel relationship to define channels between the electrolyte inlet and the electrolyte outlet of the cell. 18. The electrochemical reactor of claim 17, wherein the electrodes rest on the perforated plate of the associated cell, each plate is made of electrically- insulating material and the perforations in each plate are arranged in rows spaced about mid-way between the respective adjacent electrodes. 19. The electrochemical reactor of claim 14, comprising downcomer tubes for delivering electrolyte from the electrolyte outlet weir of each cell (.except the lowest one) to the electrolyte inlet weir of the cell below. 20. The electrochemical reactor of claim 19, wherein a bottom part of the lowest chamber forms a receptacle for a pool of reacted electrolyte and a further downcomer tube leads from the electrolyte outlet of the lowest cell to the bottom part of the lowest chamber, for the delivery of reacted electrolyte to the pool. 21. The electrochemical reactor of claim 2Q, comprising an incomer tube extending down through the top chamber, for the delivery of fresh electrolyte to the electrolyte inlet weir of the top cell. 22. The electrochemical reactor of claim 13, wherein the respective sections of the reactor housing are separated by and secured to the periphery of the respective horizontal plates, which are perforated only in the regions under the electrodes of the respective cells of the reactor. 23. The electrochemical reactor of claim 22, wherein each housing section Cexcept the lowest one) has facing side walls which fit against upstanding plate forming electrolyte inlet and outlet weirs to define a rectangular enclosure for the electrodes of the respecti cell. 24. The electrochemical reactor of claim 23, - wherein each cell comprises a bipolar array of vertical plate-like electrodes disposed in spaced parallel rela¬ tionship to define channels between the electrolyte inle and outlet weirs of the cell, each electrode array including terminal electrodes inset in the facing side walls of the respective housing section. 25. An electrochemical reactor comprising: . a reactor housing; a plurality of mutually-spaced perforated generally horizontal plates disposed in superimposed relationship to divide the reactor housing into superimposed chambers; electrodes disposed in each chamber (.except the lowest one) over perforations in the respective plate; means defining an electrolyte inlet and an electrolyte outlet spaced apart on opposite sides of the electrodes across each perforated plate to maintain elec¬ trolyte on the perforated plate at an intermediate level of the respective chamb so as at least partially to immerse the respective electrodes and define a gas- ' collection space in the chamber above the electrolyte; each chamber (except the top one) con¬ stituting a gas-supply chamber for passing ga up through perforations in perforated plat at the top of the chamber to bubble the ga through the electrolyte on the plate and into the gas-collection space in the chamber thereabove and which (except for that of the top cell) forms the gas- supply chamber for the cell above; - and means connecting the electrolyte outlets and inlets of successive cells in cascade to flow electrolyte down the reactor from the electrolyte outlet of one cell to the electrolyte inlet of the cell below. 26. A method of carrying out an electrochemical process or reaction in an electrochemical cell comprising electrodes disposed over a perforated generally hori- zontal plate, an electrolyte inlet and an electrolyte outlet spaced apart on opposite sides of the electrodes across the perforated plate, and a cell housing which is divided by the perforated plate into an upper chamber and a lower gas-supply chamber, the method comprising passing gas from the gas-supply chamber up through per¬ forations in the plate to bubble through electrolyte on the plate and collect in the upper chamber. 27. A method of carrying out an electro¬ chemical process or reaction in an electrochemical reac- tor comprising (I) a plurality of cells, each cell comprising (_i) electrodes disposed over a perforated generally horizontal plate and (.ϋ) an electrolyte inlet and (iii) an electrolyte outlet spaced apart on opposite sides of the electrodes across the perforated plate, and (II) a reactor housing in which the cells are stacked in a columnar arrangement, the perforated plates dividing the reactor-housing into superimposed chambers, each perforated plate being disposed over a gas-supply chamber for passing gas up through perforations in the plate to bubble through electrolyte on -the plate and collect in the chamber thereabove and which (except for that of the top cell) forms the gas-supply chamber for the cell above, the method comprising flowing electrolyte down the columnar reactor from one cell to the next and across the perforated plate of each cell, and passing gas up through the perforations in the successive plates so that the gas bubbles through the electrolyte on each plate. 28. The method of claim 26 or 27, wherein the gas is a reactant in the electrochemical reaction. 29. The method of claim 26 or 27, wherein the gas is propylene and the electrolyte is a halide salt of an alkali metal in aqueous solution.

Inventors: GOODRIDGE F, PLIMLEY R
Applicants: GOODRIDGE F, PLIMLEY R
Application year: 1978
Main classification: C25B9
IPC codes: C07D303, C25B3, C25B9