Patent Publication Number: US-4220627-A

Title: Process for the treatment of raw materials containing arsenic and metal

Description:
BACKGROUND OF THE INVENTION 
     The present invention relates to the treatment of raw materials which contain arsenic and metal, in order to produce a metal-free arsenic product and an arsenic-free metal sulfate, by leaching the raw material with an aqueous solution of sulfuric acid and by crystallizing the metals in the form of sulfates from the separated aqueous solution, which is then separated from the metal sulfate crystals. 
     The process according to the invention can be used for the treatment of any arsenic- and metal-bearing raw materials the metals of which dissolve in a sulfuric acid solution in the form of sulfates and the arsenic of which can be recovered as a metal-free arsenic product, such as a solution of H 3  AsO 4  or NaAsO 2 , or solid As 2  O 3 . Suitable raw materials include metal arsenides and arsenates, such as the arsenides or thioarsenides of cobalt and nickel, and arsenic matte. A raw material especially suitable for treatment by the process according to the invention it the arsenic-bearing precipitate produced in the electrolytic zinc process; it is obtained by cementation by means of zinc powder and by the addition of some arsenic compound in order to cement the cobalt and nickel out from the zinc sulfate solution. As a result of this purification process a cementate is obtained in which the cobalt and nickel are in the form of arsenides (MeAs) and which also contains a small guantity of copper arsenides and metallic copper. This purification process is described in U.S. Pat. No. 3,979,266. 
     Cementates of the above type, produced by solution purification, used to have a high copper content and were therefore regarded as raw materials for copper production. Owing to their high arsenic content these raw materials were not, however, very desirable raw materials for smelting plants. There was another disadvantage in that the arsenic was wasted, at least as regards the zinc plants. U.S. Pat. No. 3,979,266 discloses a process by which it is possible to lower considerably the copper concentration in the arsenide cementate, and consequently the cementate can be used as raw material in the production of cobalt and nickel. However, in principle this cementate causes the same problem as above. The arsenic content in the cementate substantially lowers the selling value of the cementate, while the arsenic present in the cementate is wasted as regards a zinc plant. Various processes have been introduced for the treatment of these cementates. U.S. Pat. No. 3,979,266 discloses a process of leaching the arsenic in sodium hydroxide and returning it as As 2  O 3  to the solution purification, while the metals are recovered in the form of a hydroxide precipitate. The precipitate has, however, proved to be difficult to filter and wash. Finnish Lay-Open Print 770646 describes another process, in which the zinc, copper, and cobalt are first leached in acid and then a cobalt-rich precipitate is precipitated from this solution. The residue is then leached by means of alkali lye to remove the arsenic. The residue is a suitable raw material for the production of copper, and the arsenic is precipitated from the solution as copper arsenate, which is returned to solution purification. 
     There is also a prior known method for the treatment of arsenides, whereby arsenides are extracted by means of a sulfuric acid solution and the solution is thereafter evaporated so as to precipitate the metal sulfates and to recover the arsenic as a sulfuric acid-bearing H 3  AsO 4  solution (Journal of the South African Institute of Mining and Metallurgy, July 1969, p. 654). It is, however, difficult to separate arsenic and metal sulfates effectively from each other by this process, since a very strong solution of sulfuric acid and arsenic acid must be used for a complete precipitation of the metal sulfates. This results in a very viscous solution, which complicates the separation and the washing of the crystal mass. 
     The object of the present invention is therefore to provide a process for the treatment of arsenic- and metal-bearing raw materials to produce a metal-free arsenic product and an arsenic-free metal sulfate, whereby the disadvantages involved in the previously known processes mentioned above are eliminated. 
     SUMMARY OF THE INVENTION 
     According to the invention, raw materials which contain arsenic and metal are leached at an elevated temperature and eventually under oxidizing conditions to convert the arsenic to a 5-valent form, whereafter the metal sulfates are crystallized out by cooling from a selectively separated arsenate-bearing aqueous solution, and arsenic is removed at least from a secondary flow of the aqueous solution before the aqueous flow is returned to the leaching operation. 
     DESCRIPTION OF THE PREFERRED EMBODIMENTS 
     In the process according to the invention it is not necessary to crystallize the metal sulfates completely out from the separated arsenate-bearing aqueous solution, firstly since a closed solution cycle is used, and secondly, since arsenic can be separated very selectively from the mother liquor after the crystallization. The removal of arsenic from this mother liquor need not be complete, either, since after the removal of arsenic the solution is returned to the leaching of raw material. Thus the present invention comprises the leaching of arsenic- and metal-bearing raw materials by means of an aqueous solution in a closed solution cycle which includes, in addition to the leach, two selective removal stages, one for metal sulfates and the other for arsenic. 
    
    
     The invention is described below in more detail with reference to the accompanying drawing, which depicts a flow diagram of the process according to the invention. 
    
    
     Arsenide precipitate is fed to the leaching stage, at which a suitable sulfuric acid concentration is maintained and oxygen is dispersed in the form of either gaseous oxygen or air into the aqueous solution. The sulfuric acid concentration is not critical for the success of the process, for it affects only the reaction velocity, but since a high sulfuric acid concentration enhances both the reaction velocity and the performance of both of the following removal stages, the sulfuric acid concentration is maintained at a rather high level, and approx. 100 g H 2  SO 4  /l has experimentally been found suitable. The leaching temperature is selected as one at which the solubility of the metal sulfates is maximal. Temperatures in the range of about 50°-100° C. are generally employed. In leaching a raw material in which the metals are copper and nickel, the temperature is preferably 90°-100° C., while the highest solubility of cobalt sulfate is at approx. 65°-70° C. When treating an arsenide precipitate from a zinc process, the precipitate containing all the three metals, the temperature is a compromise between the above-mentioned temperatures, depending on the predominant metal. 
     At the end of the leach the solution is cooled or the solution is allowed to cool as much as is practical. It can be cooled to approx. 30° C., for example, which is fully possible by means of generally available cooling water. Thereby the metal sulfates crystallize. Fresh sulfuric acid is added preferably to this stage of the solution cycle, since a high sulfuric acid concentration curbs the coprecipitation of arsenic with the sulfates, while more sulfates can be precipitated as their solubility lowers with increasing acid concentration. The sulfate crystals are removed by filtering, and then washed. 
     The next stage is arsenic removal, which can be performed by different methods. Two methods are described below, and the selection between them depends on the local conditions. It has been shown that H 3  AsO 4  can very selectively be extracted by means of tributyl phosphate or dibutylbutyl phosphate from the solution obtained from the crystallization. The extraction is performed without adding any neutralizing agents or foreign chemicals. A high sulfuric acid concentration in the solution promotes, however, the extraction, and therefore the addition of fresh sulfuric acid to the crystallization stage is advantageous even at this stage. The extraction is performed using tributyl phosphate or dibutylbutyl phosphate dissolved in some suitable hydrocarbon to which some higher alcohol may have been added to enhance the separation of the phases. The stripping is performed with water. The extraction is easy to perform so that the output H 3  AsO 4  solution contains at minimum 100 g As/l, and thereafter this solution can be returned to solution purification. Thus the arsenic can be kept in the aqueous solution throughout the process, which is highly hygienic. 
     In another method for the removal of arsenic, arsenate is reduced to arsenite, whereby the As 2  O 3  precipitates. The reduction can be performed using, for example, sulfur dioxide. Thereafter the As 2  O 3  can be returned to the solution purification, either as such or as an environmentally less hazardous NaAsO 2  solution, which is obtained by dissolving the precipitated As 2  O 3  in sodium hydroxide after the mother liquor from the As 2  O 3  precipitation has been removed by decanting. 
     Above, the process according to the invention has been described as applied to the treatment of arsenide cementate obtained from zinc plants. It is, however, evident, that even other raw materials can be treated by it. The main thing is that arsenic can be dissolved in a 5-valent form (=as arsenate) to make possible the selective crystallization of sulfates. If the arsenic is in a 3-valent form, the As 2  O 3  coprecipitates with the crystals. Naturally, the raw material need not be arsenide, which is leachable under oxidizing conditions, but it can just as well as arsenate, which is extractable with sulfuric acid solution alone, without oxidation. 
     The metal sulfates obtained can be used as raw materials for the production of pure metals or pure metal salts. The arsenic obtained is also a valuable commodity, and especially if the arsenic has been removed by extraction, the H 3  AsO 4  solution obtained after the evaporation of the solution is an excellent initial material for the production of saturation agents and pesticides. 
     The invention is described below in more detail with the aid of an example. 
     EXAMPLE 
     Precipitate obtained from the solution purification of the zinc process was leached as follows: 
     
         ______________________________________                                    
Solid content     =           200 g/l                                     
Temperature       =           95° C.                               
Initial H.sub.2 SO.sub.4 concentration                                    
                  =           300 g/l                                     
Final H.sub.2 SO.sub.4 concentration                                      
                  =           120 g/l                                     
______________________________________                                    
 
    
     Air was injected into the solution and dispersed well. 
     After six hours the color of the leach residue had turned white and the leach was discontinued. The results obtained: 
     
         __________________________________________________________________________
        Cu   Co   Ni   Zn   Cd   As   Pb   H.sub.2 O.sub.4                
__________________________________________________________________________
Precipitate                                                               
before leach                                                              
        45.2 3.6  4.2  6.0  0.28 16.5 5.3  %                              
Precipitate                                                               
after leach                                                               
        0.14 &lt;0.025                                                       
                  &lt;0.025                                                  
                       0.13      0.2  30   &#34;                              
Leaching                                                                  
yield   99.9 &gt;99.9                                                        
                  &gt;99.9                                                   
                       99.6      99.7 --   &#34;                              
Solution                                                                  
before leach                                                              
        28   17   27   36   2    120       300 g/l                        
Solution                                                                  
after leach                                                               
        118  24   35   48   2.6  153       120 g/l                        
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     The solution fed into the leach had been obtained by running it a few times through the process according to the flow diagram shown in the figure, and thus the example illustrates the results obtained in a continuous-working process. Sulfuric acid was added to the solution at 200 g H 2  SO 4  /l, the solution was then cooled to 30° C. and maintained at this temperature for 6 hours. The crystals produced were removed by filtering and then washed with a small quantity of water (0.2 ml H 2  O/l g of precipitate). The following results were obtained: 
     
         ______________________________________                                    
         Cu   Co     Ni     Zn  Cd  As   Pb  H.sub.2 O.sub.4              
______________________________________                                    
Solution before                                                           
crystallization                                                           
           118    24     35   48  2.6 153  --  120 g/l                    
Solution after                                                            
crystallization                                                           
           26     17     26   37  2.1 152  --  320 g/l                    
Precipitation Me                                                          
           102    100    113  92  83           %                          
Leached Me                                                                
Analysis of                                                               
crystals   18     1.4    1.7  2.4 0.1 0.1  2   %                          
Coprecipitation                                                           
of arsenic                            1.5                                 
(calculated on the basis of arsenic content)                              
in the arsenide precipitate)                                              
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     Half of the solution was extracted using tributyl phosphate. 
     In order to extract arsenic from the solution obtained from the crystallization of metal sulfates, an extraction agent was prepared which contained tributyl phosphate 85% by vol. and Shellsol K (an aliphatic hydrocarbon with a distillation range of 194°-251° C. and a specific weight of 0.79 g/cm 3 ) 15% by vol. 
     One part (by vol.) of the solution obtained from the crystallization and 1.4 parts (by vol.) of the tributyl phosphate solution used previously for the arsenic extraction in question and then regenerated with water were stirred for 5 minutes at 30° C. The separated organic phase obtained was stirred for an equal length of time at the same temperature with one tenth of its volume of water, whereafter the again separated organic phase was mixed in the same manner with half of its volume of water. 
     The analysis values of the aqueous solutions have been compiled in the table below. 
     
         __________________________________________________________________________
          Cu  Co  Ni  Zn  Cd  As  Pb                                      
                                    H.sub.2 SO.sub.4                      
__________________________________________________________________________
Solution after        g/l                                                 
crystallization                                                           
          26  17  26  37  2.1 152 --                                      
                                    320                                   
Solution after                                                            
extraction                                                                
          27  17  25  38  2.1 76  --                                      
                                    228                                   
Solution obtained                                                         
by a phase volume                                                         
ratio of 10                                                               
          0.20                                                            
              0.30                                                        
                  0.25                                                    
                      0.15                                                
                          0.01                                            
                              128 --                                      
                                    292                                   
Solution obtained                                                         
by a phase volume                                                         
ratio of 2                                                                
          0.014                                                           
              0.013                                                       
                  0.011                                                   
                      0.010                                               
                          0.001                                           
                              86  --                                      
                                    66                                    
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     It can be seen from the table above that arsenic can be extracted highly selectively. The trace amounts of coextracted metals can be removed simply by washing the extraction agent with a small quantity of water. 
     On the other hand, considerable quantities of arsenic were coextracted. Calculations show that the separation factor 
     
         S.sub.As,H.sbsb.2.sub.SO.sbsb.4 =C.sub.As /C.sub.As /C.sub.H.sbsb.2.sub.SO.sbsb.4 /C.sub.H.sbsb.2 SO.sbsb.4 
    
     where C As  and C H .sbsb.2 SO .sbsb.4 are the concentrations of arsenic and sulfuric acid in the organic phase, C As  and C H .sbsb.2 SO .sbsb.4 the concentrations of arsenic and sulfuric acid in the aqueous phase, is in the order of 2.5 for both the extraction and the water wash. For an expert it is thus evident that the extraction can be performed in such a manner that a nearly sulfate-free arsenic acid product is obtained. By a countercurrent extraction of the above sulfate solution in, for example, two extraction stages, and by a countercurrent wash in four washing stages, and by the combining of the obtained wash solution with the sulfate solution fed into the countercurrent extraction, an arsenic acid product is recovered which has a sulfate content of less than 10% of the arsenic content of the product. The extraction and wash experiment was repeated by the process described above, the only difference being that iron had been added to the sulfate solution in the form of ferric sulfate. The analysis showed that after the addition of iron the sulfate solution contained iron 25 g/l. Within the limits of the precision of the analysis, the extraction and wash results were the same as above. As regards iron, the results were: 
     
         ______________________________________                                    
Solution after extraction                                                 
                       24 g/l Fe                                          
Wash solution obtained with                                               
a phase volume ratio of 10                                                
                       2.2 g/l Fe                                         
Wash solution obtained with                                               
a phase volume ratio of 2                                                 
                       0.16 g/l Fe                                        
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     The results show that in spite of the fact that iron dissolves at a somewhat higher rate than other metals experimented with, iron can also be removed effectively from the extraction agent by means of a small quantity of water. The possibility of obtaining an iron-free H 3  AsO 4  product is significant in, for example, the production of arsenic-bearing saturation products and pesticides. 
     One half of the solution was fed into a reactor, where sulfur dioxide was injected through the solution, the temperature being maintained at 60° C. 
     After ten hours the As 5+  concentration had dropped to 26 g/l, and an As 2  O 3  precipitate had been produced. The solution was cooled to 30° C. and the solution was removed by decanting. The solution, which contained NaOH 60 g/l, was fed into the reactor and stirred until the precipitate had dissolved completely. Before the leaching a sample was taken of As 2  O 3 , and this sample was washed with a small quantity of water. 
     Results: 
     
         __________________________________________________________________________
        Cu  Co Ni Zn Cd  As.sup.5+                                        
                             As.sup.3+                                    
                                 H.sub.2 SO.sub.4                         
__________________________________________________________________________
Solution before                                                           
reduction                                                                 
        28  17 27 36 2   220 3   300 g/l                                  
Solution after                                                            
reduction                                                                 
        28  17 27 36 2   26  7   405 g/l                                  
As.sub.2 O.sub.3 yield   88      5   %                                    
As.sub.2 O.sub.3 analysis                                                 
        0.006                                                             
            0.01                                                          
               0.02                                                       
                  0.02                                                    
                     0.001   75.5                                         
                                 0.03                                     
Coprecipitation                                                           
of metal as                                                               
a percentage of                                                           
the quantity                                                              
entering the                                                              
process 0.01                                                              
            0.3                                                           
               0.5                                                        
                  0.3                                                     
                     0.3     588                                          
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     The solution was returned to the leach of raw material. 
     As can be seen from the above, more arsenic was obtained from the solution as As 2  O 3  then entered the leach. This means that only part of the solution needs to be fed through arsenic removal. Thus a high arsenic concentration can be stored in the solution by circulating it between the leach and the crystallization. This is advantageous for the next arsenic removal and in any case it is possible to obtain an arsenic-free metal sulfate.