CA1279174C - Manufacture of arsenic acid - Google Patents

Abstract

ABSTRACT

Manufacture of Arsenic Acid Manufacture of arsenic acid by oxidation of arsenic trioxide with hydrogen peroxide is potentially hazardous, especially when making concentrated solutions of arsenic acid as sought by the users. The process also can suffer from substantial wasteful decomposition of hydrogen peroxide. The problems arise from or are exacerbated by the nature of the reactants, the exothermic character of the principal and decomposition reactions and the formation of localised hot spots.
The problems can be ameliorated by introducing the reagents with agitation into a body of reaction product and maintaining the reaction mixture at a temperature of not more than 70°C and preferably 45 to 55°C. By carrying out the process in such a manner, it can accomodate even low grade arsenic trioxide as reagent.

Description

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Manufacture of Arsenic Acid The present invention relates to a process for the manufacture of arsenic acid and in particular the manufacture of an aqueous solution thereof.
In aqueous solution, arsenic acid has the formula H3As04. It is crystallised as a hydrate and can be progressively dehydrated by the stepwise removal of water molecules to form respectively the meta and pyro arsenic acids. Arsenic acid as such, or in dehydrated form has long been used as a biocide and as a component of a class of timber preservative products.
Hitherto, methods and proposed methods for the industrial production of arsenic acid have in many instances included the oxidation of arsenious oxide which has the formula As203 and which is known also by a variety of other names such as white arsenic, crude arsenic, arsenous oxide or, confusingly, simply as "arsenic". Although a range of oxidising agents has been proposed, manufacturing activity has centred upon the use of nitric acid as oxidant, together with some appropriately selected catalyst. Such a process has continued to find favour despite the known disadvantage that the reaction produces substantial volumes of gaseous nitrogen oxides, leading to foaming and boil over problems and which need a large plant to scrub them from the effluent and be oxidised to reform nitric acid. Also the process suffers from the problem of temperature control, and that such problems are exacerbated by the enforced move towards the use of lower grade arsenic trioxide starting material.

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Although other methods have been proposed, these too - suffer from disadvantages. Thus, for example, in GB-A-2113194, the nitric acid method is modified by uqing oxygen as the oxidant and nitric acid as a catalyst only in conjunction with iodide, in a pressurised reactor, but it would appear from the text that the amount of nitric acid present is critical, in that if too small an amount is present, the reaction stops prematurely whereas if excess is present the continued regeneration of iodide is suppressed, which would therefore prevent the reaction cycle to proceed in the desired manner. In view of the fact also that nitric acid can be consumed by impurities in the starting material, it will be recognised that operation of the process can readily be disrupted.
One further oxidising agent that has been proposed is hydrogen peroxide, in SU-A-510430. In this specification, the Russian Patentees describe two methods of operation using hydrogen peroxide. In the first method, 30-35%
hydrogen peroxide is added dropwise or in a fine stream at 60-70C into a slurry of arsenic trioxide and water which has been heated to boiling point by the bubbling through of live steam. Subsequently, cold water is added to the reaction vessel and the mixture is then slowly heated up to boiling point which is maintained for a subsequent 2-3 hours. The Russian Patentees confirmed that such a process was complex and took a long time, and suffered from the disadvantage that the hydrogen peroxide must be introduced slowly during which period strict temperature control was necessary, since disturbance of the temperature conditions could lead to an explosion. In view of the disadvantages in that process, the Russian Patentees employed, instead, hydrogen peroxide diluted to a concentration of 10-20%
concentration and they alleged that this could be employed at between 110-150% of the stoichiometric amount to oxidise the arsenic trioxide. However, even when they used pharmaceutical grade reagents, i.e. reagents free from substantial amount of impurities that would catalytically ~2~L7~
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decompose hydrogen peroxide, Example 2 needed 170% of the stoichiometric amount of hydrogen peroxide and even so produced a final solution concentration of only about 30%
arsenic acid. Such a product is rejected by the use industry which demands arsenic acid concentrations in the region of at lèast 65% and preferably 75-85% w/w ~or which the use of a more concentrated hydrogen peroxide reagent rather than a diluted reagent would be required. In other words, in order to satisfy the requirements of the industry, in terms of ~inal arsenic acid concentration, any proposed hydrogen peroxide process must simultaneously avoid the dilution ~aught by the Russian Patentees and also ameliorate their decomposition problems whilst overcoming the control problems inherent in using concentrated hydrogen peroxide which the Patentees identify in their summary of the prior art.
In the course of investigating the reaction between arsenic trioxide and hydrogen peroxide, the inventor of the present invention carried out a series of trials.
Theoretical calculations showed that a concentrated arsenic acid product demanded the use of concentrated hydrogen peroxide as reagent, especially if a significant proportion would be lost by decomposition. He determined that addition of commercially available arsenic trioxide to a body of a concentrated hydrogen peroxide would represent a hazardous process especially on a full size manufacturing scale since the presence from the start of the entire amount of concentrated hydrogen peroxide would not only maximise the loss due to decomposition of the hydrogen peroxide induced by impurities from the arsenic trioxide introduced, but also would thus maximise the risk of foaming, ejection of product from the reaction vessel or at worst promote an explosion.
On the other hand, when concentrated hydrogen peroxide is added to the arsenic trioxide, there are once again significant sa~ety problems, in that, at least initially, the mixture forms an extremely dense slurry that is very hard to mix, with the result that the exothermic nature o~

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the oxidation reaction coupled with very poor heat transfer on a manufacturing scale promotes the formation of localised hot spots in which rapid decomposition of hydrogen peroxide is observable together with steam evolution and the inherent dangers associated with such peroxidic decomposition. On a manufacturing scale, the problems are exceedingly dif~icult to control, other than by very slow addition of the reagent.
Such findings thus confirm the analysis of the prior art made by the Russian Patentees.
Accordingly, it is an object of the present invention to provide a process which is capable of making ooncentrated arsenic acid solution by oxidation of arsenic trioxide with hydrogen peroxide, but avoiding or ameliorating the aforementioned manufacturing difficulties.
According to the present invention there is provided a process for the manufacture of arsenic acid by reaction between arsenic trioxide and hydrogen peroxide in which the reagents are introduced with agitation into a body of fluid comprising an aqueous solution of arsenic acid, and maintaining the temperature of the reaction mixture at a temperature below 70C. By introducing the reagent in such a manner, it is possible to ameliorate or overcome the disadvantages inherent in the prior art methods of using hydrogen peroxide and especially the disadvantages and danger that may occur when one reagent is brought directly into contact with the other reagent.
It is convenient to consider the present invention in the context of batch reactions, one especially convenient method comprising a cycle in which one batch-worth of both reagents is introduced progressively into the body o~
arsenic acid and permitted to react for at lea~t a minimum reaction period and then the corresponding volume of product is withdrawn from the augmented body of aqueous arsenic acid solution. It is preferable for the body to comprise at least one batch-worth of reagents and in practice, on a manufacturing scale conveniently comprises at least 5 and often from 10-15 batches-worth of product. Conveniently 12~
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this can be expres~ed in terms of the moles of arsenic present in the body of arsenic acid solution and moles introduced per batch of arsenic trioxide. By carrying out the process in this way, it was found that the reaction exotherm could be readily controlled, and losses of reagent by decomposition kept down to acceptable levels, even with impure arsenic trioxide starting material.
Advantageously, the process of the present invention can accommodate the use of concentrated hydrogen peroxide, that is to say at least 35% w/w H202, preferably at least 45% w/w H22 and normally up to 75% w/w H202. Even allowing for some loss of hydrogen peroxide due to impurity-induced decomposition, it is therefore possible to produce, directly and in relative safety, an arsenic acid solution having a concentration of at least 65% and preferably in the region of 75-85% by the selection of appropriately concentrated hydrogen peroxide. In other words, the process is readily capable of producing a product having a concentration desired by the use industry. It is especially suitable to employ from 50% w/w H22 to 70% w/w H22 in that such solutions are commercially available and readily transportable, as well as producing a high concentration product.
The hydrogen peroxide solution can contain one or more stabilisers that are effective in an acidic medium, such as pyrophosphates, and/or orthophosphates, and/or organic phosphonates including hydroxy alkyl diphosphonates and amino methylene phosphonates and/or wholly organic stabilisers such as dipicolinic acid and hydroxyquinolines and phenols, optionally substituted around the aromatic nucleus by non-interfering substituents. It will be recognised that the value of including such stabilisers increases as the purity of the arsenic trioxide starting material diminishes and its particle size increases.
It i3 desirable to add at least a stoichiometric amount of hydrogen peroxide, based on the arsenic trioxide, ramely at least 2 ~oles per mole of arsenic trioxide of formula ..

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As203. In practice, a minor proportion of the hydrogen peroxide is often consumed by side reactions or decompo~ition and accordingly it is preferable to employ a suitable excess amount of hydrogen peroxide in each batch.
Purity is one of the factors influencing the selection of the amount o~ hydrogen peroxide, and a second factor is the particle size of the arsenic trioxide. It is normal for the amount o~ hydrogen peroxide to be selected in the range of 105% of the stoichiometric amount to 200%, in the context of an As203 purity ranging from above 99% down to 92%. By way of example if the starting material is rather coarse then, for high purity As203 starting material, it is advisable to employ from 105% to 115% of the stoichiometric amount; for the intermediate purity material around 98% purity, it i~
convenient often to use from ~15-130% of the stoichiometric amount of hydrogen peroxide; for low grade starting material of e.g. 96-97% purity it is usually desirable to select in the range of 120-150% of the stoichiometric amount, and for really low grade material, such as below 95% purity, it is usual to employ at least 125%, and typically up to 175%.
However, when more finely ground starting material is used, less hydrogen peroxide is wasted in side reactions or decomposition with a result that nearly all the arsenic present can be oxidised into solution using no more than 125~ of the stoichiometric amount for any material having a - purity of 90~ arsenic or over, in practice often from 105 to 125%. Under-addition of hydrogen peroxide can result in particulate arsenious oxide remaining in suspension at the end of the reaction, and to avoid build-up of solids the 3o residual amount should be filtered off or alternatively be taken into account in calculating the amount of hydrogen peroxide to add in the subsequent batch.
It will further be recognised that use of an increasing excess amount of hydrogen peroxide introduced at a given concentration translates to a dilution of the resultant arsenic acid product. Such dilution can be offset, if desired, by employing a correspondingly higher concentration 27917~

of hydrogen peroxide.
It i~ most convenient for the arsenic trioxide to be introduced in powder form. To at least some extent there is a correlation between the efficiency of use of hydrogen peroxide for oxidising the arsenic trioxide and the particle size of the latter, smaller particles being more favoured.
This can manifest itself as an overall reduced hydrogen peroxide requirement or in improved separation of arsenic from the impurities in the starting material. It is desirable for the average particle size to be below 500 micrometres, and in many instances will be at least 40 micrometres. The starting materials in many instances have such low particle sizes but if not they can be achieved by conventional grinding equipment. It will be recognised that very small particles of e.g. below 50 micrometers can form agglomerates e.g. up to 200 micrometers in size. Such agglomerates can also be used very readily in the instant process.
One important feature of the presen~ invention is the temperature which is maintained in the reaction vessel during the introduction of the reagents and the subsequent reaction. The reaction itself is exothermic and thus it has been found in practice that a temperature of above ambient can be maintained throughout the reaction period without introduction of external heat, and indeed the mixture is typically subjected to external cooling throughout the reaction period. The rate of the reaction, is however, somewhat sensitive to temperature, and it is preferable therefore to maintain a temperature of at least 35C in order to maintain an acceptable rate of reaction and in many embodiments, the temperature is controlled to at least 40C.
It wîll be recognised that the provision of the arsenic acid body of fluid assists in the maintenance of a controlled reaction temperature in that it provides a larger volume for the dispersal of the heat of reaction, thereby, at the same time, diluting any inherent temperature rise and presenting an augmented volume for external cooling means as well as .279~
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providing a more fluid medium and thus reducing heat transfer problems. By so doing, it is able to obviate or at least ameliorate problems of localised temperature build-up to above the SADT t~elf accelerating decomposition temperature). In practice, the reaction mixture temperature is maintained at up to 60C, and especially at around 45 to 55~, in order to balance the twin and opposed criteria of increasing reaction rate versus reduced safety margin. Hence increased potential throughput is balanced against an increased likelihood of the reaction passing out of control when a higher design temperature of the reaction is permitted. In practice, it will be recognised that the temperature is often controlled by balancing the cooling with the rate of introduction of, in particular, the aqueous hydrogen peroxide solution.
It is a further advantageous feature of the process described herein that even though the reaction mixture is preferably maintained at a temperature of at least 35C, it is normally possible to commence the reaction at markedly lower temperatures, without the provision of external heat.
Thus, for example, even where the body of arsenic acid solution initially has a temperature of 0C, introduction of the reagents can be made and within a single batch, the reaction temperature can normally restore itself to the preferred temperature conditions.
In practice, the reaction is conducted by introducing the reagents simultaneously or alternatively, or aliquots of the solid reagent and continuous addition of the aqueous hydrogen peroxide into the body of arsenic acid solution 3o until the desired amount of each has been introduced. It convenient for the reagents to be introduced over a period of from 1 to 5 hours and the overall reaction period to be selected within the range of from 2 to 10 hour~, including the period during which the reactants are introduced. It will be recognised that, to at least a certain extent, the reaction period is interlinked with the reaction temperature and that should the reaction be conducted at a temperature .
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from ambient to 35C, proportionately longer periodq o~
introduction and reaction time should be employed.
Alternatively or by way of supplement, a sample of the reaction mixture can be analysed at intervals for residual hydrogen peroxide concentration and the product withdrawn when substantially no hydrogen peroxide remains.
In some valued embodiments, especially when all or most of the particles of the arsenic trioxide starting material are below 500 micrometers, the prooess is operated according to the following combination of process conditions. A batch of particulate arsenic trioxide containing at least 92~ by weight As203 and from 105 to 125% of the stoichiometric amount of hydrogen peroxide as an aqueous solution containing 45 to 75% w/w H202 are introduced gradually into a body of aqueous arsenic acid containing from 5 to 15 moles As per mo~e As in said batch, thereby f'orming a reaction ~ix~ure, the rea~tion mixture is agitated and maintained at a te~p~rature in t~e range o~ ~D to 600C ~or a perlod o~ a~
least Z hours after introduction o~ the reagents commen~e~, 20 and thereafter a frao~ion oP the mlxtur~ ls withdrawn as product. Within that ~mbination o~ Qondltlons, the earlier identi~ied narrower pre~erred ranges ~or any or all o~ those conditions Qan naturally be uqed.
In order to assist the reaction, and particularly in 25 conjun~tion with the processing oP lower grade starting material, it can be advantageous to introduce a cataly~ic amount o~ an iodide, particularly potassium iodide into the reaction mixture, typically in an amount o~ up to 0.2% w~w and especially in an amount Prom 0.01 to 0.10% w/w. In addition, it is desirable to promote wetting of the arsenic trioxide on introduction into the reaction mixture, by including, for example, a small amount of a wetting agent, typically bentonite in a total amount of up to 0.1% w/w and often from 0.01 to 0.03% w/w on the mixture. By promoting the wetting of the arsenic trioxide~ the period is reduced during which it floats upon the surface of the reaction mixture where it can form localised spot~ ~rom which heat --` 12~91~

dissipation is slow.
One aspect of the invention of practical importance when the reaction iq carried out on a large scale is the thorough mixing of the reagents with the body of arsenic acid into which are introduced. It will be recognised that concentrated arsenic acid solutions, for example those containing over 70% w/w arsenic acid are dense, viscous fluids. Thus, there is a tendency especially for the arsenic trioxide starting material to float, at least initially, because conventionally it is in the form of a powder. When it floats it remains as a crust of small particles on the surface of the body of the reaction mixture. It is recognised that the benefit of the instant invention could be dissipated if the reagents were permitted to come into contact primarily as surface films or if hydrogen peroxide, for example, is introduced onto a surface comprising principally a crust of unreacted arsenic trioxide starting material. In consequence, it is highly advantageous for the introduction of the two starting materials to be separated, either by location or sequential addition, in both instances the body of arsenic acid product and reactant being mixed to such an extent that when it comes into contact with the second starting material, no such localised concentration of the first starting material have been permitted to remain. One particularly convenient method for effecting such a separation comprises the introduction of the two reactants into separated zones of the body of fluid, such as into separate vessels with the body of reaction mixture circulating between the two of them. In practice, such a circulating reactor system normally requires fluid to be pumped from one vessel to the other from which it is permitted to flow under gravity such as over a weir back to the first vessel and the pumping itself can provide sufficient agitation in respect of the vessel into which the aqueous hydrogen peroxide is added.
In the other reaction vessel, it is preferable to incorporate a mechanical agitator that is of sufficient 127~

power and is adapted to blend the surface layer of ~olid particles within the main body of the ~luid in that vessel.
The fluid product typically contains a residual amount of solids, part of which represent unreacted arsenic trioxide and part impurities. It is most convenient for such solids to be filtered off. Although all the body of arsenic acid could be filtered after the production of each batch, it is generally preferable to filter merely the amount of product withdrawn. It has been observed that the - 10 small amount of solid separated at this stage tends to include rather large particles compared with the average particle size of the starting material. Analysis of the solids has shown that they tend to have a lower arsenic content than that of the starting material, indicating that preferential dissolution of the arsenic has occured.
Advantageously, such preferential dissolution seems, on present indications, to be noticeable with the relatively impure starting materials i.e. those in which the potential problem of impurities is greatest. In view of the foregoing, it can be advantageous not to recycle the separated solids, although where the impurity content of the product would still fall within customer-tolerated limits solids recycling can result in some further recovery of arsenic.
It is preferable for the reaction vessel to be operated at slightly sub-ambient pressure with vented gases being passed through a scrubbing system designed to remove all arsenic oxide particies and arsenic acid solution entrained in the gases. Since the primary oxidant hydrogen peroxide in the present invention is introduced in liquid form rather than as oxygen gas and does not generate substantial gaseous reaction products like nitrogen oxides, the scrubbing system need only be small scale in compounds ~ith plants of comparable manufacturing capacity employing respectively air or nitric acid as oxidant.
Having described the invention in general terms~
specific embodiments will now be described more ~uliy by way 2 ~ fl of example only. Attention is drawn to the poisonous nature of both arsenic trioxide and arsenic acid to humans and the need therefore for appropriate safety precautions to be adopted in order to avoid contact with them.
Ex~les 1-7 Each of Examples 1-7 was carried out in a jacketted 60 litre stainless steel vessel fitted with an agitator and temperature probe and having an offtake for product at its base. The vessel was cooled by passing mains supply water through the jacket.
In each Example, 15 litr-es of an aqueous arsenic acid solution having a concentration of approximately 75 to 80% w/w arsenic acid was introduced into the reaction vessel, ~orming the body of product into which the reactants would subsequently be introduced. In ~xample 1 the body comprised laboratory grade arsenic acid and in the subsequent Examples product from earlier Examples was used instead.
Initially the body of arsenic acid had a temperature of about 16C, namely ambient temperature. Arsenic trioxide (15kg) and a supra-stoichiometric amount of hydrogen peroxide (50~ w/w, commercially available from Interox Chemicals Limited) indicated in the following Table 1 were then each introduced into the reaction vessel over a period of 3 hours, the arsenic trioxide being introduced in 30 equal aliquots and the hyrogen peroxide in a continuous stream. Bentonite (3g, 0.02% of the total arsenic trioxide) ~as introduced into the reactor together with the first aliquot of arsenic trioxide.

3 During the course of introduction of approximately the first 10% of the reactants, the reaction vessel was agitated, but cooling water was not being circulated through the reactor jacket. During that period the temperature o~
the reactior mixture rose from ambient temperature to about 40C. During the remainder of the reaction period, the cooling water was circulated at such a rate that the temperature in the vessel was maintained at 40C +/ 3C.

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The reaction was allowed to continue at 40C ~or a ~urther hour after all the reagents had been introduced and then the reactor contents were discharged and the total re~idual solids content of the batch determined. From this determination, the extent to which the arsenic had been converted to arsenic acid was determined and, expressed as a percentage in the following Table under the term "reaction efficiency". Naturally, allowance was made ~or any other solids present such as the added bentonite and any solids introduced with the original body of arsenic acid solution.
In a modification of Example 1 in Examples 3 to 7 inclusive a catalyst, potassium iodide (50g, 0.1% w/w of the arsenic trioxide) was introduced together with the first aliquot o~ arsenic trioxide. In a ~urther modification in Example 7 only, the reaction temperature was permitted to rise to 50C whereupon it was subsequently con~rolled to within +/- 3C by adjustment in the rate o~ flow o~ cooling water.
Periodically, samples of the liquor in the reaction vessel were taken and analysed for residual peroxide content. The reaction conditions and results are summarised in Table 1 below.
Table 1 Example As203 H22 Product Analysis Reaction No. ~urity addition Total H3As04 e~iciency % % solids % w/w %
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1 99.9 110 3.7 78.5 99.3 2 99.9 110 4.8 81.0 99.1 3 94.9 150 1.0 74.8 99.8 4 94.9 120 5.3 76.6 99.0 94.9 135 4.6 75.1 99.1 6 99.1 120 6.8 80.0 98.7 7 99.1 120 2.6 84.0 99.
From Table 1 above, it will be seen that using the method o~ the instant invention, it was possible to readily obtain an arsenic acid concentration of around 75% or higher even from starting material as impure as below 95% arsenic trioxide. Thus, it will be observed that with all grades, a reaction efficiency of over 99% was attainable and from a consideration of the total solids content it can also be seen that not all of the impurities went into solution. ~y a comparison of Examples 1 and 2 with subsequent Examples 3 to 5 and 6~7, it will be recognised that there is a broad correlation between purity of the arsenic trioxide starting material and the amount of hydrogen peroxide required for virtually complete oxidation. By comparison, it will be recalled that Example 2 of SU-A-510430 with pharmaceutical grade As203 needed 175% of the stoichiometric amount of hydrogen peroxide and even then could produce a concentration of only 29~. It will also be observed by comparison between Examples 6 and 7 that increasing the reaction temperature from 40 to 50 enhanced both the reaction efficiency and reduced the total solids content in the product liquor.
By way of comparison, further experiments were conducted into the reaction between hydrogen peroxide and arsenic trioxide in which the reactants were brought directly into contact with each other, and not indirectly through separate introduction into a body of the reaction product. These further experiments were conducted using an intermediate grade of arsenic trioxide containing 97.2% w/w .4s203. In view of the increased hazard when employing such a technique, they were carried out on a smaller scale, as follows. A predetermined amount of hydrogen peroxide, 150%
of the stoichiometric amount and at 35% w/w solution, was introduced into a round bottom flask equipped with a stirrer and then over a period of 3 hours 50 gms of arsenic trioxide was introduced slowly together with 0.01 g bentonite. The temperature was maintained at 40C. After all the arsenic trioxide had been introduced, the reactants were allowed to react for a further 1 hour at the reaction temperature. The product was analysed as in the Examples. At the end of the reaction it was found that only ~6.5% oxidation to arsenic 1279~

acid had occurred, with a peroxide residual equivalent to 3%
of the stoichiometric amount. The reactantq were modified by also adding potassium iodide as catalyst. In the presence of 0.1% w/w and 0. 5% w/w potassium iodide, the extent of oxidation was increased to respectively 97.8% and 96.9% with peroxide residuals of 3% of the stoichiometric amount and 0.3% of the stoichiometric amount. Increasing the reaction temperature to 50C also produced a 96.9%
oxidation but with no residual peroxide. It is readily apparent that this technique was substantially more wasteful in terms of peroxide decomposition than the technique according to the present invention.
Examples 8_to 13 Each of these small scale Examples was carried out 15 using a very low grade arsenic trioxide starting material containing 70.15% arsenic, calculated as the metal, equivalent to 92.6% as As203, (50g) and 50% w/w aqueous hydrogen peroxide at 150% or 175% of the stoichiometric amount. In Examples 8 and 9, the arsenic trioxide had been previously ground to a particle size of below 710 micrometres and in Examples 10 to 13 to below 425 micrometres.
In each of these Examples a body of arsenic acid solution (~2.7% w~w, 105g) was introduced into a glass 25 vessel equipped with a stirrer and a baffle, separating the point of introduction of the two reagents subsequently.
During the next three hours, arsenic trioxide was introduced with stirring at approximately evenly spaced intervals in aliquots of about 0. 5g, and the hydrogen peroxide was pumped in a constant rate. Additionally, 0.1% w/w KI and 0.02~ w/w bentonite was introduced with the first aliquot of arsenic trioxide. The temperature of the reaction mixture was held at 50C during the introduction but during the subsequent period of an hour cooling to around 40C was observed. The 35 product was then filtered, the solid residue analysed and the % of arsenic that had been oxidised was calculated.
The results are summarised in Table 2, the arsenic 12~7917~1 content in the residue being calculated as As203 and the impurity content being the balance and thus including any undissolved K and bentonite.
Table 2 5Example H2o2 Solid Residue % of No.Addition Total Arsenic Impurity arsenic % weight Content Content oxidised g g g 8 175 6.6 3.4 3.2 92.9 9 150 5.9 3.4 2.5 92.9 175 4.4 1 7 2.7 96.4 11 150 4.0 1.2 2.8 97.4 12 125 3.4 0.8 2.6 97.7 13 110 3.8 0.9 2.9 97.6 From Table 2, it can be seen clearly that the solid residue contains a much higher proportion o~ the impurities than did the starting material indicating preferential solubilisation of the arsenic. Secondly, it will be noted that the smaller particle size of Examples 10 to 13 led to improved arsenic oxidation whilst leaving a similar amount of impurities as solid residue.

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Claims (15)

1. In a process for the manufacture of arsenic acid by reaction between arsenic trioxide and aqueous hydrogen peroxide the improvement comprising introducing arsenic trioxide having a purity of at least 90% w/w and an aqueous solution containing 35% to 75% w/w hydrogen peroxide with agitation into a body of fluid comprising an aqueous solution of arsenic acid, said body comprising at least half the volume of mixture after all the reagents have been introduced, maintaining the temperature of the reaction mixture at a temperature below 70°C, during reaction between arsenic trioxide and hydrogen peroxide, and subsequently withdrawing a fraction of the resultant mixture as aqueous arsenic acid product and retaining the remainder of the mixture as the body of fluid for introduction of further arsenic trioxide and hydrogen peroxide.

2. A process according to claim 1 in which the reaction mixture is controlled to a temperature of 35° to 60°C.

3. A process according to claim 2 in which the reaction mixture is controlled to a temperature of 45°C to 55°C

4. A process according to claim 1 in which the amount of hydrogen peroxide introduced is selected within the range of 105 to 200% of the stoichiometric amount.

5. A process according to claim 4 in which the amount of hydrogen peroxide introduced is selected inversely to the purity of the arsenic trioxide.

6. A process according to claim 1 in which the reaction period lasts 2 to 10 hours after introduction of the reagents commences.

7. A process according to claim 1 comprising gradually introducing a batch of particulate arsenic trioxide containing at least 92% by weight As2O3 and from 105 to 125% of the stoichiometric amount of hydrogen peroxide as an aqueous solution containing 45 to 75% w/w H2O2 into a body of fluid comprising aqueous arsenic acid containing from 5 to 15 moles As per mole As in said batch, thereby forming a reaction mixture, agitating the reaction mixture, maintaining the reaction mixture at a temperature in the range of 40 to 60°C for a period of at least 2 hours after introduction of the reagents commences, and thereafter withdrawing a fraction of the mixture as product.

8. A process according to claim 7 in which the two reagents are introduced simultaneously into two zones of the body of fluid which are then brought into contact.

9. A process according to claim 8 in which the body of fluid is recycled between the zones.

10. A process according to claim 1 employing up to 0.5% w/w based on the arsenic trioxide starting material of an oxidation catalyst.

11. A process according to claim 1 in which up to 0.5% w/w based on the arsenic trioxide starting material of wetting agent is introduced therewith.

12. A process according to claim 10 wherein said catalyst comprises potassium iodide.

13. A process according to claim 11 wherein said wetting agent comprises bentonite.

14. A process according to claim 1 wherein said arsenic acid is present in said body of fluid in an amount of at leat 65% by weight and in which said arsenic acid is present in said aqueous product solution in an amount of at least 65% by weight.

15. A process according to claim 7 wherein said arsenic acid is present in said body of fluid in an amount of at least 65% by weight and in which arsenic acid is present in the withdrawn product fraction in amount of at least 65% by weight.