US3759804A - Electrochemical oxidation of thallium derivatives - Google Patents

Electrochemical oxidation of thallium derivatives Download PDF

Info

Publication number
US3759804A
US3759804A US00115477A US3759804DA US3759804A US 3759804 A US3759804 A US 3759804A US 00115477 A US00115477 A US 00115477A US 3759804D A US3759804D A US 3759804DA US 3759804 A US3759804 A US 3759804A
Authority
US
United States
Prior art keywords
ions
anolyte
thallous
compartment
catholyte
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Expired - Lifetime
Application number
US00115477A
Other languages
English (en)
Inventor
Bris L Le
D Michelet
M Rakoutz
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Rhone Poulenc SA
Original Assignee
Rhone Poulenc SA
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Rhone Poulenc SA filed Critical Rhone Poulenc SA
Application granted granted Critical
Publication of US3759804A publication Critical patent/US3759804A/en
Anticipated expiration legal-status Critical
Expired - Lifetime legal-status Critical Current

Links

Images

Classifications

    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01G—COMPOUNDS CONTAINING METALS NOT COVERED BY SUBCLASSES C01D OR C01F
    • C01G15/00—Compounds of gallium, indium or thallium
    • C01G15/003—Preparation involving a liquid-liquid extraction, an adsorption or an ion-exchange
    • C—CHEMISTRY; METALLURGY
    • C25—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES; APPARATUS THEREFOR
    • C25B—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES FOR THE PRODUCTION OF COMPOUNDS OR NON-METALS; APPARATUS THEREFOR
    • C25B1/00—Electrolytic production of inorganic compounds or non-metals

Definitions

  • the present invention relates to an electrochemical process for oxidising thallous ions to thallic ions.
  • metal ions reducible to metals are thallous and/or thallic ions, scarcely anything other than platinised platinum or platinised titanium is suitable for the cathode.
  • platinised platinum or platinised titanium is suitable for the cathode.
  • the more common and generally less expensive metals such as stainless steel or copper cannot be used in this process.
  • the main subject of the present invention is to provide an electrochemical process for oxidising thallous ions which does not have the aforementioned disadvantage and which allows cathodes based on common metals to be employed.
  • the present invention provides a process for the electrochemical oxidation of thallous ions to thalic ions which comprises passing a direct electric current between an anode and a cathode of an electrolysis cell divided into at least two compartments by at least one membrane having anion exchange properties, the anolyte comprising thallous and thallic ions and the catholyte comprising an alkali metal hydroxide, an ammonium hydroxide, an alkali metal salt of a volatile weak acid or an ammonium salt of a volatile weak acid.
  • catholyte denotes the solution in the cathode compartment and the term anolyte denotes the solution in the anode compartment.
  • a cell having two compartments separated by a single anion exchange membrane is used.
  • This first way will be denoted, in the text that follows, by (M and the two compartments will be denoted by (A) for the anode compartment, and (Ct) for the cathode compartment.
  • the nature of the solvent or solvents contained in the catholyte and the anolyte is not critical, it is usually preferred to use water.
  • the amount of thallous and thallic ions present in the anolyte is preferably such that the number of gram atoms of thallium per litre of solution is: between 0.01 and 0.8, particularly between 0.1 to 0.5.
  • an acid for example perchloric acid, sulphuric acid, nitric acid, fiuoroboric acid, alkylsulphuric acids, or saturated aliphatic acids which are soluble in water, such as acetic acid. It is usually preferred, and especially in a sulphuric acid medium, to operate at a pH below 2; with an aliphatic acid it is preferred to operate at a pH less than 5.
  • the catholyte containing an alkali metal or ammonium hydroxide or salt of a volatile weak acid the alkali metal may be lithium, sodium, potassium, rubidium or caesium and the ammonium compound may be quaternary or otherwise.
  • Ammonium derivatives which can be used are compounds comprising the grouping of formula:
  • R represents an organic radical, particularly alkyl, the group (I) preferably containing not more than 16 carbon atoms and preferably being in the form of a salt of a volatile weak acid.
  • Carbonates and bicarbonates are conveniently used as salts of a volatile weak acid.
  • the concentration of alkali metal or ammonium compound in the catholyte is generally between 0.1 and 5 mols/litre and preferably between 0.5 and 2 mols/litre.
  • the anion exchange membranes separating the various compartments can be homogeneous membranes or heterogeneous membranes; the exchange groups can, in particular, be ammonium, phosphonium or sulphonium groups, as well as amine groups when the catholyte contains a salt of a volatile Weak acid.
  • Ion exchange membranes of which the permeation selectivity (measured according to the technique described in French patent specification No. 1,584,187) is greater than 40%, preferably greater than are preferably used.
  • the electric current densities in the process according to the invention are generally between 0.5 and a./ dmfi, preferably between 5 and 25 a./dm.
  • An electrically conducting material which is insoluble in the anolyte under the operating conditions is used as used as the material constituting the anode.
  • Suitable materials include graphite, platinum, lead dioxide, as well as lead and its alloys, particularly with silver, antimony and tin.
  • the cathode may be of steel, particularly stainless steel, iron, copper, chromium, nickel, graphite, mercury or lead or its alloys, particularly with silver, antimony and tin.
  • a simple electrolysis cell or an assembly of cells joined together for example by the filterpress system can be used.
  • the oxidation according to the invention can be carried out continuously or discontinuously.
  • the electrolyser is fed with a solution of TH and simultaneously electrolysed solution is withdrawn.
  • the process of the invention can also be combined in one and the same system with an oxidation process for organic compounds using Tl the thallous-thallic solution continuously circulating alternately, first in the electrolysis cell, and then in the oxidisor for the organic compound.
  • the operating conditions are generally controlled so as to maintain an electrolyte temperature which is neither below C. nor above 60 C.
  • the oxidation is preferably carried out at a temperature in the range 1535 C.
  • the liquid (also called electrolyte) used in the compartment of type (B should have the same characteristics as those defined previously for the catholyte; it is preferred in practice that the composition of the electrolyte (B be the same as that of the catholyte, except for the fact that the latter does not contain any thallous ions at all; the concentration of the alkali metal or ammonium derivative in the electrolyte (B can however be different to that of the catholyte.
  • the electrolyte (B is preferably subjected to a separate electrolysis in an auxiliary electrolyser, which allows any traces of thallium which may be present to be deposited in metal form;
  • this auxiliary electrolyser which is of small dimensions in practice, is advantageous provided with an anion exchange membrane separating the catholyte and the anolyte, and the catholyte consists of liquid which comes from (B and the anolyte has a composition similar to that of the catholyte except as regards thallium, which is absent in the anolyte of this auxiliary electrolyser.
  • the liquid (or electrolyte) present in the compartment of type (B is an aqueous solution containing thallous ions, thallic ions being absent or almost absent (preferably less than 0.1% by weight, calculated as T1 metal).
  • This solution can also contain an acid; the proportion of thallous ions and the nature and proportion of acid in this solution are selected in accordance with the same criteria as for the anolyte.
  • the compartments (B are fed with the thallous solution coming from a reactor using thallic ions, and then the thallous solution leaving (B is transferred to the anode compartment (A), where it is subjected to anodic oxidation.
  • the compartments of type (A) and (B are simultaneously fed with a thallous solution such as that coming from a reactor for the oxidation of olefines by thallic ions, the solution present in the compartment (B is withdrawn at a rate sufficient to maintain the proportion of thallic ions Within the limit indicated above, and the said solution which has been withdrawn from the compartment (B is transferred directly to the reactor for utilising the thallic ions; anolyte is withdrawn simultaneously to transfer it also to the reactor for utilising the thallic ions.
  • a thallous solution such as that coming from a reactor for the oxidation of olefines by thallic ions
  • the oxidation process according to the invention allows good electrical yields to be obtained. It also prevents any progressive concentration of non-thallous or non-thallic salts or ions in the anolyte.
  • the (M and (M methods of carrying out the process according to the invention moreover allow the deposit of thallium on the cathode to be removed, this deposit having a tendency to be formed during operations of a very long duration when the permeation selectivity of the membranes is not close to 100%.
  • the (M method allows the life of the membranes to be increased.
  • Thallic ions are useful as catalysts in the oxidation of organic compounds e.g. olefines, as described in US. patent specification No. 3,048,636 and in such processes are reduced to thallous ions.
  • the process of the present invention is useful in converting such thallous ions back to thallic ions.
  • Tl+ is oxidised to Tl+++ in an electrolysis cell having the following characteristics:
  • Catholyte 100 cm. of aqueous 2.5 N sodium hydroxide solution.
  • Anolyte 500 cm. of aqueous solution initially containing one mol/litre of sulphuric acid and 99 millimols/litre of thallous sulphate. Stirring is performed by means of a magnetic stirrer.
  • Anion exchange memberane homogeneous memberane containing quaternary ammonium groups and based on a divinylbenzene-styrene copolymer (exchange capacity: 0.55 milliequivalent/g.; permeation selectivity: 90%).
  • the cathode-membrane distance is 5 mm.
  • the anode-membrane distance is 10 mm.
  • the electric current passed is 5 a.
  • the voltage is 8 v.
  • the temperature is 27 C.
  • the useful surfaces of the anode and cathode are equal to 2 dm.
  • the cathode is of stainless steel.
  • the nature The expansion vessel is fed at a rate of about 25 cmfi/ minute.
  • the membrane has a permeation selectivity of 72%.
  • the anolyte initially contains 0.4 gram ions/litre of thalof the anode is indicated in the table
  • EXAMPLE 9 A circulation of electrolyte is established in each of the I compartments of the electrodialyser; the rate of movel 1S OXIdIScd to Ti in an electroly l Cell having ment over the electrodes is 30 cm./seconds; the electhree compartments, the p ing OH it OIIS being as trolyte circuits pass through a cooler, which allows the 15 follows:
  • the letter M indicates a concentration The i f of lead. contamzmg 10% of antlmony; its of 1 mol/litre; in the case where this letter is preceded usg u sur ace ⁇ area is 1 by a number this latter indicates the concentration ex-
  • the Cathode havmg the same surface area 15 of Stamless pressed in mols/litre.
  • the degree of convarsion is the fraction (percentage The two membranes separating the three compartments in numbers f ions) f converted into 13+ in the are heterogeneous membranes containing quaternary course f the experiment ammonium groups; the matrix and the ion exchange
  • the electric current yield is the percentage of coulom-bs T6510 f in P P Q y Weight, of 32/63; the which have served to oxidise 11+ to 13+ matrix 1s a vinyl chloride/butyl maleate copolymer TABLE I Catholyte Anolyte Concentration Degree Electric Current of con cuirent Nature of the Concen- Volume, Volume, $12 894. passed Voltage Number of version, yield, Ex. anode Nature tration cm.
  • cm. B04112 initial in a. 1n v. coulombs percent percent 1 750 000 1 0.165 20 4. 30,000 71.5 01.5 2 iiEiL'IIIIIIIIIII $285 750 600 0.5 0.171 20 4.2 31,825 78 96.5 as 1 3- 193 a a s 0 N OH ii i880 600 1 0.165 10 as 30,700 67.5 84.5
  • EXAMPLE 7 and 5 lead back from the expansion vessels 12 and 13 to the anode and cathode compartments.
  • Expansion vessel 12 has inlet and outlet ports 10 and 11 for anolyte.
  • the initial concentration of thallous ions is 0.298 gram ions/litre.
  • the total volume of anolyte in circulation is 600 cmfi.
  • the total volume of catholyte in circulation is 1000 cm
  • the ion exchange membrane which contains quaternary ammonium groups, has a permeation selectivity of 89%
  • a solution containing 0.298 gram ions/litre of Tl+ (in the form of sulphate) and 1 mol/ litre of H 80 is introduced via port 10, at the rate of approximately 26.1 cmfi/minute, to the anolyte; simultaneously the same quantity of electrolysed solution is withdrawn from the anolyte via port 11.
  • thallic ions are obtained with a degree of conversion of 68% and with an electric current yield of 84.5%.
  • the current passed is 27 a.
  • the voltage is 5.1 v.
  • the ion exchange resin is a resin containing quaternary ammonium groups and is based on a styrene-divinylbenzene copolymer.
  • the permeation selectivity of the membrane is 78%, and its substitution resistance is 15 ohms cmF.
  • each compartment is 1 mm., and an interposed polypropylene grill allows the membranes to be kept in place and the outflow of the liquids to be suitably distributed.
  • the electrolytes which pass through the three compartments circulate in co-current, the pressure at the inlet being 2.3 bars absolute and at the outlet being 1.1 bars.
  • the liquid passing through the central compartment and the catholyte are initially an aqueous normal solution of sodium hydroxide.
  • a closed circuit circulation is established in the anolyte and in the catholyte.
  • the anolyte consists initially of an aqueous solution containing 100 g./l. of thallous sulphate and 20% by weight of H 50 it is fed at the: rate of 0.5 litre/hour by a solution having the same composition; the amount of anolyte is kept constant by a feed at a corresponding rate of flow.
  • the current passed is 10 a.
  • the temperature is 30 C.
  • the voltage is 6 v.
  • Electrolysis is carried out for 5 3 hours.
  • the anode is of lead and has a useful surface area of 1
  • the cathode is of stainless steel and has the same surface area.
  • the three membranes are identical to those of Example 9.
  • the thickness of the compartments is 1 mm., these compartments being provided with spacers as in Example 9.
  • the electrolytes passing through the four compartments circulate in co-current, the pressure at the inlet being 2.2 bars absolute, and at the outlet being 1 bar absolute.
  • the catholyte and electrolyte contained in the compartment next to the cathode compartment consist initially of an aqueous normal solution of sodium hydroxide.
  • the catholyte circulates in a closed circuit.
  • the electrolyte contained in compartment (B next to the cathode compartment circulates and is subjected to an auxiliary electrolysis in the same way as the electrolyte of the central compartment (B of Example 9,
  • the anolyte consists initially of an aqueous solution containing 8.7% by weight of sulphuric acid and 7.02% by weight of TH (taken as Tl metal) in the form of Tl SO
  • the electrolyte contained in the compartment (B next to the anode compartment has initially the same composition as the anolyte.
  • a closed circuit circulation is established in the anolyte
  • the compartment (B next to the anode compartment is ,fed continuously at the rate of 0.456 l./hur with a thallous solution having the same composition as that given for the anolyte at the start of the electrolysis; withdrawal of liquid from the same compartment allows the amount of liquid circulating therein to be kept constant, and serves to feed the anolyte.
  • a fraction of the anolyte is withdrawn so as to keep its volume constant.
  • the current passed is a.
  • the temperature is about 27 C.
  • the voltage is 6.4 v.
  • a process for the electrochemical oxidation of thallic ions which comprises passing a direct electric current between an anode and a cathode of an electrolysis cell divided into at least two compartments by at least one membrane having anion exchange properties, the anolyte comprising thallous and thallic ions and the catholyte comprising a compound M+A- where M+ represents an alkali metal or ammonium ion and A- represents a hydroxide, carbonate or hydrogen carbonate ion.
  • liquid contained in the compartment next to the anode compartment is an aqueous solution containing thallous ions.
  • a process according to claim 1 wherein the electrolyte temperature is 0 C. to 60 C.
  • alkali metal is lithium, sodium, potassium, rubidium or caesium and the ammonium ion is of formula NH R where x and y are independently 0 or a positive integer, the sum x+y being equal to 4, and R represents an alkyl radical the group R containing up to 16 carbon atoms.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Inorganic Chemistry (AREA)
  • Engineering & Computer Science (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Electrochemistry (AREA)
  • Materials Engineering (AREA)
  • Metallurgy (AREA)
  • Electrolytic Production Of Non-Metals, Compounds, Apparatuses Therefor (AREA)
US00115477A 1970-02-17 1971-02-16 Electrochemical oxidation of thallium derivatives Expired - Lifetime US3759804A (en)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
FR7005623A FR2077830A1 (enExample) 1970-02-17 1970-02-17
FR7047548A FR2119888B2 (enExample) 1970-02-17 1970-12-31

Publications (1)

Publication Number Publication Date
US3759804A true US3759804A (en) 1973-09-18

Family

ID=26215559

Family Applications (1)

Application Number Title Priority Date Filing Date
US00115477A Expired - Lifetime US3759804A (en) 1970-02-17 1971-02-16 Electrochemical oxidation of thallium derivatives

Country Status (10)

Country Link
US (1) US3759804A (enExample)
JP (1) JPS515634B1 (enExample)
BE (1) BE763036A (enExample)
CA (1) CA933485A (enExample)
CH (1) CH517665A (enExample)
DE (1) DE2107619A1 (enExample)
FR (2) FR2077830A1 (enExample)
GB (1) GB1303589A (enExample)
NL (1) NL7101701A (enExample)
SE (1) SE373392B (enExample)

Families Citing this family (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN114314809A (zh) * 2021-12-16 2022-04-12 中国科学院生态环境研究中心 一种分散型污水处理装置与方法

Family Cites Families (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
NL214802A (enExample) * 1956-02-22
US3486992A (en) * 1967-02-15 1969-12-30 Cincinnati Milling Machine Co Process for electrolytic oxidation of thallium or cerium salts

Also Published As

Publication number Publication date
CH517665A (fr) 1972-01-15
GB1303589A (enExample) 1973-01-17
CA933485A (en) 1973-09-11
NL7101701A (enExample) 1971-08-19
FR2119888A2 (enExample) 1972-08-11
JPS515634B1 (enExample) 1976-02-21
SE373392B (sv) 1975-02-03
DE2107619A1 (de) 1971-09-02
FR2077830A1 (enExample) 1971-11-05
FR2119888B2 (enExample) 1973-11-23
BE763036A (fr) 1971-08-16

Similar Documents

Publication Publication Date Title
US4849073A (en) Direct electrochemical reduction of nitric acid to hydroxylamine nitrate
EP0532188A2 (en) Electrochemical process
JPH04500097A (ja) 水酸化第四アンモニウムの製造の改良方法
RU2153538C2 (ru) Способ получения гидроксидов и/или гидроксооксидов металлов путем диафрагменного анализа
JPH02197590A (ja) レドックス反応方法及びそのための電解槽
US4968394A (en) Method of reducing excess nitric acid in aqueous hydroxylamine nitrate solutions
US2739934A (en) Electrolytic purification of uranium
US3779876A (en) Process for the preparation of glyoxylic acid
ES349961A1 (es) Un procedimiento para la oxidacion electrolitica de una so-lucion de una sal de un ion metalico polivalente.
EP0043854B1 (en) Aqueous electrowinning of metals
US3775272A (en) Mercury diaphragm chlor-alkali cell and process for decomposing alkali metal halides
US3413203A (en) Electrolytic oxidation of cerium
JPH05238736A (ja) クロモ硫酸の電気化学的再生法
US3450609A (en) Electrolytic process for preparing hydrogen fluoride
US2832728A (en) Electrolytic precipitation of uranium values from carbonate leach liquors
US3645864A (en) Process for the preparation of a p-amino phenol by the electrolytic reduction of nitrobenzene
Bramer et al. Electrolytic Regeneration of Spent Pickling Solutions
SU310538A1 (enExample)
US3616323A (en) Electrochemical conversion of phenol to hydroquinone
ES306422A1 (es) Procedimiento de refinado electrolitico de una aleaciën de niquel
US4402805A (en) Electrochemical process to prepare p-hydroxymethylbenzoic acid with a low level of 4-CBA
US2485258A (en) Electrodepositing lead on copper from a nitrate bath
Sharma Electro chemistry
US4381229A (en) Process for electrochemical reduction of terephthalic acid
EP0170632A2 (en) Process for the cathodic electrowinning of metals, with the corresponding acid generation, from their salt solutions