EP0148023A2

EP0148023A2 - Process for the purification of mercury

Info

Publication number: EP0148023A2
Application number: EP84309076A
Authority: EP
Inventors: Giorgio Gavelli; Marino Gramondo; Gianni Donati; Giuseppe Faita; Gian Lorenzo Marziano
Original assignee: Montedipe SpA; Montedison SpA
Current assignee: Montedipe SpA
Priority date: 1983-12-30
Filing date: 1984-12-21
Publication date: 1985-07-10
Also published as: ES539137A0; ES8707568A1; IT8324439A0; DE3477205D1; EP0148023B1; EP0148023A3; IT1170081B

Abstract

@ A process for the purification of mercury from the metal impurities contained therein, wherein the mercury is contacted with an aqueous solution, characterized in that the mercury and the aqueous solution are loaded into reactor (1) in the upper part (2) of which there is present a gas. The mercury and the aqueous solution are circulated by means of a pump (11) installed in an external recirculation circuit (8,9,10), which pump draws the liquid phases from the bottom of the reactor and sends them back into the reactor through a nozzle (3) or a liquid-gas ejector (3,4) arranged in the upper part (2) of the reactor.

As a consequence of the dynamic-flow conditions thus created, the mercury is dispersed in the aqueous phase in the form of minute droplets and is intensely mixed with the aqueous phase, and as a result the impurities pass into the aqueous phase.

Thereby there is achieved an effective removal of the impurities from the mercury.

Description

The present invention relates to a process for the purification of mercury from metal impurities contained therein, and more particularly to the purification of the mercury of electrolytic cells of chlorine-sodium hydroxide and chlorine-potassium hydroxide plants, to the purification of mercury recovered following leaks, and to the purification of mercury of industrial origin.
In chlorine-sodium hydroxide and chlorine-potassium hydroxide plants, one of the main factors that influence the reliability and safety of the mercury amalgam process is the purity of the NaCl or KC1 brine introduced into the cell. Impurities such as iron, calcium and magnesium are normally present in the sodium chloride in quantities varying from 0.01 to 0.3% by weight, while other heavy metals such as chromium, vanadium, molybdenum and magnesium are often present in quantities of the order of 0.01 ppm.
These impurities must be removed from the brine because they tend with time to accumulate in the mercury, where, if they exceed certain threshold concentrations, they catalyze the cathodic development of hydrogen which, mixing with the chlorine developed at the anode, may give rise to explosions.
The impurities present in the mercury also have other adverse effects on the electrolytic process. There may, for instance, form an amalgam foam (called "mercury butter") which disturbs the regular flow of the mercury, as a result of which the cell voltage rises and there may occur short-circuits which will damage the anodes.
Moreover, the wettability between the bottom of the cell and the mercury is reduced, with consequential frequent rupture of the continuity of the amalgam layer, and consequential corrosion of the bottom which has remained uncovered.
The accumulation of impurities in the mercury also causes unbalances in the distribution of the current in the various longitudinal sections as well as cross sections of the cell.
In order to limit the introduction of impurities in the mercury, the brine, before its conveyance to the cells, is subjected to a costly process of chemical and physical purifications.. Since there remain, however, possible accidental pollutions of the brine, the mercury tends nonetheless to grow rich in impurities, as a result of which it is necessary to frequently carry out periodical washings of the cells and purification of the mercury itself, by means of distillation.
It has been suggested to purify the mercury by electrolytic treatment after its dis-amalgamation. To this end the mercury, contacted with an aqueous acid solution, is anodically polarized, whereby the impurities dissolve in the aqueous solution.
This process involves, however, constructional complications, in particular because the mercury which is connected with the negative pole in the electrolysis cell, must be connected to the positive pole in the purification apparatus.
Thus, one aim of the present invention is to provide a simple, cheap and effective process for the purification of mercury from the metal impurities contained in it.
The present invention provides a process for the purification of mercury from metal impurities contained therein, wherein the mercury is contacted with an aqueous solution, characterized in that the mercury and the aqueous solution are fed into a reactor, in the upper part of which a gas is present, and in that the mercury and the aqueous solution are circulated by means of a pump installed in an external recirculation circuit, this pump drawing the liquid phases (mercury and aqueous solution) from the bottom of the reactor and sending them back into the reactor through a nozzle or a liquid-gas ejector arranged in the upper part of the reactor, whereby as a consequence of the dynamic-flow conditions thus created the mercury is dispersed in the form of minute droplets in the aqueous phase, and is intensely mixed with the aqueous phase, as a result of which the impurities pass into the aqueous phase.
The invention will be further described, by way of example only, with reference to the accompanying drawing, which is a schematic view of an apparatus suitable for carrying out the process of the invention.
The drawing shows a reactor 1 which contains in its upper part 2 a gas. Fixed to the upper end of this reactor is arranged a nozzle 3. Furthermore there may be present a converging-diverging tube 4 which is so arranged with respect to the nozzle 3 as to form with this latter a liquid-gas ejector.
The converging-diverging tube 4 is maintained in the reactor 1 in the most suitable position with respect to the nozzle by means of any mechanical device suited for this purpose, for instance by means of fixing spokes fixed to the nozzle itself. The mechanical device is chosen in such a way as not to hinder the passage of the gas from the upper part 2 of the reactor to the inside of the converging-diverging tube 4 itself. The lower part of the tube 4 is immersed in the liquid phases present in the reactor.
Into the upper part 2 of the reactor are fed in the mercury to be purified via a line 5, and the aqueous solution via a line 6. Starting from the bottom 7 of the reactor, there is provided a recirculation line 8-9-10 which leads first to a pump 11 and thereafter to an optional heat exchanger 12 and returns back to the reactor, entering the nozzle 3. From the upper end of the reactor, the gas produced by the purification reaction (hydrogen) flows out through a line 13.
From the part 8 of the recirculation line, between the reactor 1 and the pump 11, there is a branch line 14, in which is installed a valve 15, which allows the discharge of the liquid phases.
The-pump 11 ensures the circulation of the two liquid phases (the mercury and the aqueous solution) in the reactor and in the external recirculation line. The nozzle 3 causes an agitation (or stirring-up) of the liquid phases and the consequential dispersion of the mercury in the aqueous solution, in the form of droplets of small diameter.
If there is present a liquid-gas ejector, such an ejector sucks gas from the top of the reactor, still further increasing in this way the turbulence in the jet and in the reactor, and dispersing gas into the system.
This dispersed gas reduces the coalescence of the mercury particles and provides an extensive exchange surface for the removal of the gas produced by the reaction.
Preferably there is used a liquid-gas ejector, considering the above indicated positive effects that it produces.
The aqueous solution may be either acid, neutral or alkaline. It is preferred to use a mineral acid solution, for example a sulphuric acid solution containing from 0.5% to 10% by weight of H SO . In fact, in the presence of an acid solution, the impurity dissolving reaction proves to be faster. Using an acid solution, the chemical reaction that takes place is, for instance in the case of iron:
There may also be added to the acid solution an oxidizer, for instance H₂O₂ .
The gas present in the reactor may be at atmospheric pressure; however, it may instead be at a reduced pressure: that is, the process may be operated under a vacuum, as a result the only gas present being the gas freed by the reaction (H2 However, it is also possible to work at a pressure higher than atmospheric pressure. The pressure of the gaseous phase is for example from about 10 mmHg to about 5 atmospheres absolute.
When working at atmospheric pressure or above atmospheric pressure, the nature of the gas present in the reactor is not critical; there may be used various types of gases, for example air or nitrogen. The use of air is convenient in as much as it may help to dissolve the impurities because the oxygen contained in the air acts as an oxidiser.
The ratio between the volume of liquid phases sent back into the reactor each hour and the volume of the reactor itself is in general at least 10, more preferably from 50:1 to 150:1. The delivery pressure of the pump is in general at least 0.3 atmospheres, more preferably from 0.7 to 3 atmospheres.
The temperature at which the purification reaction takes place is usually from 20°C to the boiling temperature of the aqueous solution. The purification reaction obviously proceeds faster when the temperature increases, but at high temperatures, in an acid medium, there may arise problems of corrosion of the equipment.
It is useful and convenient to use a pump which will ensure a dispersion of the liquid phases in each other. The mercury droplets tend, in fact, to coalesce in the part 8 of the external recirculation line.
If the pump re-disperses the liquid phases, new mercury droplets form again. The reforming of the mercury droplets accelerates the purification reaction. In fact, if the size (dimensions) of the droplets remains stable in time, there will form concentration gradients and the diffusion of the impurities towards the mercury-water interface will slow down. On the contrary, if the droplets re-coalesce and are formed again with a new surface, the negative effect of the concentration gradients will be appreciably reduced.
Pumps suitable for ensuring an effective dispersion of the liquid phases in each other are for example gear pumps and rotary pumps as well as particular types of centrifugal pumps.
The liquid phases may be discharged through the valve 15 which leads, for instance, to a tank where the purified mercury and the exhausted aqueous solution are separated by decanting.
When purifying the mercury of electrolytic cells, the mercury is subjected to the purifying process after its dis-amalgamation.
In the operation of the cells, the mercury purification system in which the process of the present invention is carried out may be coupled to the conventional purification of the brine, or the latter purification may be dispensed with, as a result of which the only purification carried out is that in accordance with the invention.
It is also possible to carry out a simplified purification of the brine, thus reducing the costs of this operation.
According to one specific embodiment of the process of the invention, the whole flow of mercury which flows out of the dis-amalgamator (disamalgamation apparatus), passes into the purification apparatus shown in the drawing, during all the time of operation of the electrolytic cell or at suitable time intervals. The mercury is separated by decanting from the aqueous phase and then flows back into the cell.
Instead of passing the whole flow of mercury into the purification apparatus, it is possible instead to pass only part of the flow either during the whole time of operation of the cell or at suitable time intervals.
In these two kinds of operation, the purification apparatus is provided with a circulating pump of its own. Thus, the plant will have two pumps, one for the circulation of the mercury in the cell, and one for the purification apparatus. There may instead be used in the plant only one pump which, besides circulating the mercury in the cell, will convey part or the whole of it to the purification apparatus. In this latter case, the mercury will pass only once through the purifying apparatus before being sent back into the cell.
The purification process of the present invention may also be used for purifying the mercury butters gathered during the washing of the cells.
The invention will be further described with reference to the following illustrative Examples

EXAMPLE 1

There was used the apparatus shown in the drawing, equipped with a liquid-gas ejector 3-4, a heat exchanger 12 and a gear pump 11.
The total volume of the reactor and of the recirculation circuit was about 5 litres. The process was conducted discontinuously, at room temperature.
There were introduced into the apparatus 5 litres of a 5% by weight solution of H₂S0₄which was recirculated at a flow-rate of 500 litres/hour. The delivery pressure of the pump equalled 1.1 atmospheres.
Into the reactor were then introduced 500 g of mercury containing 20 ppm of sodium and 15 ppm of iron. After 30 seconds there was drawn a sample of mercury; the content of sodium was found to be less than 1 ppm while that of the iron was less than 3ppm.

EXAMPLE 2

There was used the same apparatus as in example 1 and there were followed the same procedures, except as otherwise specified.
At room temperature, there were treated 500 g of mercury containing 42 ppm of iron with 5 litres of an aqueous solution containing 5% by weight of H₂SO₄ and 0.1% by weight of H₂0₂8 After less than one minute, the content of iron was found to be below 3 ppm.

EXAMPLE 3

There was used the same apparatus as in example 1 and there were followed the same procedures, except as otherwise specified.
500 g of mercury, containing 430 ppm of iron, were treated at 70°C with five litres of an aqueous solution containing 2% by weight of H₂SO₄. After one minute, the content of iron in the mercury had dropped to 10 ppm, and after a further 2 minutes it was found to be below 3 ppm.

EXAMPLES 4-7

There was used the same apparatus as in example 1 and there were followed the same procedures, except as otherwise specified.
The mercury to be treated came from end boxes (examples 4 and 5) and from feed boxes of electrolytic cells of a chlorine-sodium hydroxide plant.
500 g of mercury were treated at room temperature with 3 litres of an aqueous solution containing 2% by weight of H₂SO₄. The initial composition of the mercury and its composition after 5 and 10 minutes of treatment are given in the following table.

Claims

1. A process for the purification of mercury from metal impurities contained therein, wherein the mercury is contacted with an aqueous solution, characterized in that the mercury and the aqueous solution are fed into a reactor (1), in the upper part (2) of which a gas is present, in that the mercury and the aqueous solution are circulated by means of a pump (11) installed in an external recirculation circuit (8,9,10), the said pump drawing the liquid phases from the bottom of the reactor and sending them back into the reactor through a nozzle (3) or a liquid-gas ejector (3.4) arranged in the upper part (2) of the reactor, whereby as a consequence of the dynamic-flow conditions thus created the mercury is dispersed in the aqueous phase in the form of minute droplets and is intensely mixed with the said aqueous phase, as a result of which the impurities pass into the aqueous phase.

2. A process as claimed in claim 1, characterized in that the aqueous solution is a mineral acid solution.

3. A process as claimed in claim 2, characterized in that the mineral acid solution contains an oxidizer.

4. A process as claimed in any of claims 1 to 3, characterized in that the gas present in the reactor is air.

5. A process as claimed in any of claims I to 4, characterized in that the ratio of the volume of the liquid phases sent back into the reactor every hour to the volume of the reactor is at least 10.

6. A process as claimed in any of claims 1 to 5, characterized in that the delivery pressure of the pump (11) is at least 0.3 atmospheres.

7. A process as claimed in any of claims 1 to 6, characterized in that the pump (11) is such as to ensure an effective dispersion of the liquid phases in each other.

8. A process as claimed in any of claims 1 to 7 for the purification of mercury of electrolytic cells of chlorine-sodium hydroxide and chlorine-potassium- hydroxide plants, characterized in that the mercury is subjected to purification after its dis-amalgamation.

9. Mercury purified from its metal impurities according to the process as claimed in any of claims 1 to 8.