Process for the Fabrication of Sodium Bicarbonate and Boric Acid From Borosodium Ores

The present invention is directed to a process for producing sodium bicarbonate and boric acid by carboammoniac attack of borosodium ores, or minerals, such as tincal, or borax.

In the processes for treatment of borate minerals, borocalcium minerals, for example colemanite (2CaO.3B.sub.2 O.sub.3.5H.sub.2 O), are generally transformed into boric acid while the borosodium minerals such as tincal (borax) (Na.sub.2 O.2B.sub.2 O.sub.3.10H.sub.2 O) and the borocalcosodium minerals such as boronatrocalcite (ulexite) (Na.sub.2 O.2CaO.5B.sub.2 O.sub.3.16H.sub.2 O) are most often converted into borax or sodium borate in order to valorize their Na.sub.2 O content (Brauer u. d' Ans - Fortschritte in der anorganischen Chemie - 1877-1917 -- (1922) -- Vol. I -- Part 2, page 2596).

Thus, in French Patent No. 1,256,827 of May 11th, 1960, filed by S.p.A. Larderello, there is described a process for producing boric acid by carboammoniac attack of colemanite or other borocalcium minerals. According to this patent, one begins, for example, with colemanite, which is ground, possibly calcined, then treated with a solution of ammonium bicarbonate and ammonia or carbonic anhydride and ammonia, while being agitated, for several hours, at a temperature between ambient temperature and 90.degree. C. to produce the reaction:

the resulting suspension being filtered in order to separate the calcium carbonate, and the remaining solution of ammonium borates being brought to the boiling point in order to concentrate it and to eliminate the ammonia which is recycled:

After a substantial concentration of the solution, it is cooled in order to crystallize the boric acid; the crystals are separated, washed and dried while the mother liquors return to the concentration circuit.

The borosodium minerals such as tincal (borax) and kernite (Na.sub.2 O.2B.sub.2 O.sub.3.4H.sub.2 O) are normally treated by simple recrystallization to produce pure borax. If it is desired to finally obtain boric acid, the mineral or the pure borax is treated with an acid, for example sulphuric acid (Ullmann's Encyklopaedie der technischen Chemie -- 3rd edition -- 1953 -- Vol. 4 -- pages 587 and 591-593).

Applicant has discovered that it is worthwhile to apply to borosodium minerals not containing calcium, particularly to tincal, the carboammoniac attack proposed by Larderello S.p.A. for borocalcium minerals. Instead of precipitating calcium carbonate, one obtains sodium bicarbonate which can be separated and converted into sodium carbonate by calcination, while yielding at the same time a rich carbonic anhydride usable for the carboammoniac attack.

Thus, the present invention relates to a process for fabricating boric acid by carboammoniac attack of a borate mineral, the process according to the invention involving treating a finely ground borosodium mineral in an aqueous medium with carbonic anhydride and ammonia in a manner to precipitate sodium bicarbonate which is separated, the remaining mother liquor being cooled in order to obtain crystals of an ammonium borate which are separated, redissolved and the obtained solution decomposed by thermal means in order to form ammonia which is recycled to the mineral treatment and a boric acid solution, with the acid being separated by crystallization. The mother liquor of the crystallization of the ammonium borate can be recycled for the dissolution of the mineral. The mother liquor of the crystallization of the boric acid can be used for redissolving the crystals of ammonium borate.

According to a preferred embodiment of the invention, the carboammoniac attack is not effectuated on a solution of raw borosodium mineral, but rather on pure hydrated sodium biborate, for example Na.sub.2 O.2B.sub.2 O.sub.3.5H.sub.2 O, obtained by recrystallization from a mineral solution.

FIGS. 1-3 are schematic diagrams of various embodiments of installations which can be used for the practice of the present invention.

The process according to the present invention essentially involves a fabrication technique which approaches that employed to produce sodium carbonate from sodium chloride in and ammonia-soda plant, but in which the sodium chloride is replaced by borosodium mineral or sodium borate. Thus, in the case of the use of tincal as the starting material, roughly the following reactions will occur:

with respect to the classic soda-works, this process presents the advantage of avoiding the formation of residual calcium products and, moreover, reduces pollution, while yielding boric acid which constitutes a product of considerable commercial value.

This process is also of value with respect to that described in French Patent No. 1,256,827 of Larderello, because it produces sodium carbonate instead of calcium carbonate.

For practical embodiments of the invention, several examples of which will be given below, one can utilize apparatus of the same type as those utilized in standard soda-works, in particular absorbers for the formation of carboammoniac solutions using recovered ammonia and carbonic anhydride, and a carbonation column refrigerated at its lower part for precipitating the sodium bicarbonate.

The portion of the installation employed for recovering the ammonia and forming the boric acid will be more simple, since in the present procedure it is not necessary to utilize lime due to the fact that the ammonium borates are of much greater thermal instability than ammonium chloride and it is sufficient to heat them, for example by means of a vapor applied by indirect contact or direct contact, in order to decompose them into boric acid, water and ammonia.

In the classic ammonia-soda plant, the solubility of sodium chloride is very high and almost independent of temperature. The dissolution of the sodium chloride can be effectuated at cold temperatures, before and possibly after the crystallization of the sodium bicarbonate.

The borosodium minerals such as tincal, on the other hand, are very insoluble at cold temperatures, above all when in the presence of ammonium borate.

In order to crystallize ammonium borate, it is necessary to effectuate the operations in the following order:

addition of borosodium mineral

crystallization of sodium bicarbonate

crystallization of ammonium borate.

In order for the efficiency of the cycle to be high, it is necessary that a substantial amount of borosodium mineral be added, but its dissolution may possibly be incomplete before the introduction of the solution to the bicarbonation column. In effect, during the crystallization of sodium bicarbonate, the weight ratio Na.sub.2 O/B.sub.2 O.sub.3 in solution decreases, the solution becomes impoverished in Na.sub.2 O and the solubility of the borosodium mineral increases; this latter then dissolves completely.

In addition to a high B.sub.2 O.sub.3 content, the mother liquors of crystallization of the sodium bicarbonate should contain a maximum of ammonia in order to reduce the partial pressure of carbonic anhydride.

The sodium bicarbonate crystallization conditions conforming to these requirements have been determined.

At fixed temperature, the mother liquors of sodium bicarbonate crystallization can be saturated in 4 solid phases: NaHCO.sub.3, NH.sub.4 HCO.sub.3, (NH.sub.4).sub.2 O.2B.sub.2 O.sub.3.4H.sub.2 O and (NH.sub.4).sub.2 O.4B.sub.2 O.sub.3.6H.sub.2 O. In effect, in the system Na.sub.2 O -- (NH.sub.4).sub.2 O -- -- B.sub.2 O.sub.3 -- CO.sub.2 -- H.sub.2 O there are 5 independent components. In the presence of 4 solid phases, 1 liquid phase and 1 vapor phase, the variance of the system is: V= 5-6+ 2= 1.

It thus results that if the temperature is fixed, the pressure as well as the compositions of the liquid and gaseous phases are determined. It therefore remains to select a temperature at which the solubilities will be sufficiently high without the pressure exceeding 1 to 2 kg/cm.sup.2, which values are achieved in standard soda-plants.

Solubility tests performed in selecting a temperature of 30.degree. C. have shown that at this temperature the content of B.sub.2 O.sub.3 in the saturated solution in the 4 above-cited solid phases is low (126 g/kg) and the Na.sub.2 O content is high (29 g/kg). The yield of a cycle based on the crystallization of NaHCO.sub.3 at 30.degree. C. is mediocre, but the effective pressure is only 0.3 kg/cm.sup.2.

The yield is improved by effecting the crystallization at 50.degree. C.; in the presence of the same solid phases, the effective pressure rises to 1.2 kg/cm.sup.2 but the results are more advantageous:

content of B.sub.2 O.sub.3 : 167 g/kg

content of Na.sub.2 O: 27 g/kg

Table 1 below provides the complete results for these two tests:

From the mother liquors of the crystallization of sodium bicarbonate, one can crystallize different ammonium borates:

(NH.sub.4).sub.2 O.5B.sub.2 O.sub.3.8H.sub.2 O : ammonium pentaborate

(NH.sub.4).sub.2 O.2B.sub.2 O.sub.3.4H.sub.2 O : ammonium biborate

(NH.sub.4).sub.2 O.4B.sub.2 O.sub.3.6H.sub.2 O : ammonium tetraborate.

The precipitation of ammonium pentaborate implies modifying the composition of the NaHCO.sub.3 mother liquors by a partial stripping of ammonia. It has been observed that the presence of CO.sub.2 in the form of NaHCO.sub.3 is favorable. By cooling to 15.degree. C. a solution containing

Na.sub.2 O , g/kg : 27

(NH.sub.4).sub.2 O , g/kg : 26

B.sub.2 o.sub.3 , g/kg : 170

while injecting CO.sub.2, it results that ammonium pentaborate is crystallized and the mother liquors have the following composition:

Na.sub.2 O , g/kg : 31

(NH.sub.4).sub.2 O , g/kg : 16

B.sub.2 o.sub.3 , g/kg : 110

The precipitation of the ammonium biborate occurs more favorably. The mother liquors of crystallization of sodium bicarbonate are found in the domain of crystallization of ammonium biborate. By subjecting these mother liquors to a simple pressure reduction followed by a cooling to 26.degree. C., it is possible to crystallize ammonium biborate under particularly advantageous conditions since the mother liquors contain:

Na.sub.2 O , g/kg : 49

(NH.sub.4).sub.2 O , g/kg : 95

B.sub.2 o.sub.3, g/kg : 58.

The crystals recovered have a composition close to the theoretical composition of ammonium biborate. Moreover, it has been noted that the addition of NH.sub.4 OH to the mother liquors of crystallization of sodium bicarbonate permits a substantial increase in the quantity of ammonium biborate crystallized; the results of tests appear in Table 2 below:

In order to practice the process on an industrial scale, several variations can be imagined. There will be given below examples concerning the use of tincal in the framework of:

(1) the crystallization of NaHCO.sub.3 and of ammonium pentaborate at 30.degree. C.

(2) the crystallization of NaHCO.sub.3 and of ammonium pentaborate at 50.degree. C.

(3) the crystallization of NaHCO.sub.3 and of ammonium biborate at 50.degree. C. with elimination of the impurities of the tincal in the cycle

(4) the crystallization of NaHCO.sub.3 and of ammonium biborate at 50.degree. C. utilizing purified tincal.

Examples 3 and 4 represent preferred embodiments of the invention.

According to example 3, finely ground tincal is introduced into an aqueous medium, the mixture passing into a washer-decanter than into an absorber where it comes into contact with ammonia and carbonic anhydride recovered from a subsequent stage, the carboammoniacal solution of tincal thus obtained being introduced into a carbonation column where it is subjected to the action of a gas rich in carbonic anhydride in a manner to precipitate sodium bicarbonate. The sodium bicarbonate is separated, the remaining mother liquor being cooled in order to crystallize ammonium biborate. The ammonium biborate is separated, redissolved and the obtained solution decomposed by thermal action in order to form ammonia which is recycled to the absorber and a solution of boric acid from which the acid is separated by crystallization. The mother liquor of the separation of the acid is recycled in order to redissolve the crystals of ammonium biborate and the mother liquor of the separation of the ammonium biborate is evaporated in order to recover ammonia and carbonic anhydride. The latter are delivered to the absorber while the remaining solution is utilized for dissolving the mineral. The lower part of the carbonization column is maintained at about 50.degree. C.

According to example 4, use is not made of tincal in its naturally occurring state, but rather pure hydrated sodium borate crystals obtained by recrystallization from a tincal solution, the mother liquor of this crystallization being reused for the dissolution of the mineral. The crystals of hydrated sodium borate thus obtained are introduced into a carbonation column which also receives a carboammoniacal solution recovered in a subsequent stage and a gas rich in carbonic anhydride in a manner to precipitate sodium bicarbonate, the mother liquor remaining after the separation of the sodium bicarbonate is enriched with recovered ammonia and is then cooled in order to crystallize ammonium biborate which is separated, redissolved and the obtained solution decomposed by thermal means in order to form a solution of boric acid, from which the acid is separated by crystallization, and of ammonia. One part of the latter is recycled in order to enrich, with respect to ammonia, the mother liquor from the separation of sodium bicarbonate and the other part is delivered to an absorber which also receives the mother liquor from the crystallization of the ammonium biborate, the carboammoniacal solution thus formed in this absorber being delivered to the carbonation column. The lower part of the carbonation column is maintained at about 50.degree. C.

If the preliminary refinement of the tincal is carried out in a manner to crystallize the pentahydrated sodium biborate, there is no water which would have to be evaporated during the cycle.

One starts with finely ground tincal (Na.sub.2 O.2B.sub.2 O.sub.3.10H.sub.2 O), which is not purified, or refined, and this material is treated in an installation having the form illustrated schematically in FIG. 1. The finely ground tincal is introduced into a reservoir 1 where it is mixed with mother liquor coming from a centrifuge 8 in which ammonium pentaborate is separated. The mixture passes from reservoir 1 to a decanter-washer 2 into which is introduced washing water and from which the slurry or sediment is withdrawn. The supernatent mineral suspension then passes into a chiller-absorber 3 where it comes into contact with a mixture of carbonic anhydride and ammonia derived from stripping installations 6 and 10 provided for this purpose. The ammoniacal liquor formed in unit 3 passes into carbonation column 4 which is also supplied with the rich carbonic anhydride and which is cooled in its lower portion in order to bring the temperature thereat to 30.degree. C. The pressure established is effectively 2.9 kg/cm.sup.2. The aqueous suspension of sodium bicarbonate is filtered in a filter 5, the NaHCO.sub.3 being able to, as in a standard soda-works, be converted into sodium carbonate, which yields CO.sub.2 that can be utilized in bicarbonation column 4. The filtrate, which consists of an aqueous solution containing sodium bicarbonate, sodium borate, ammonium bicarbonate and above all ammonium borate, is subjected to a vapor stripping action by indirect contact in stripper 6 from which there is collected a mixture of ammonia and carbonic anhydride which is delivered to the absorber 3. The remaining solution is cooled to 15.degree. C. in a cooler 7 into which carbonic anhydride is injected, in order to provoke a crystallization of ammonium pentaborate whose crystals are separated from the mother liquor in the centrifuge 8, the remaining mother liquor being conveyed to the reservoir 1 in which the tincal being introduced is dissolved, while the crystals are redissolved in a dissolver 9 by means of water and mother liquor coming from the boric acid centrifuge 12. The ammonium pentaborate solution formed in dissolver 9 is subjected to a direct contact vapor stripping in stripper 10 in order to decompose it into ammonia and a boric acid solution, the ammonia being conveyed to the absorber 3. The boric acid solution is crystallized in a crystallizer 11, the crystals are separated from the mother liquor in the centrifuge 12 and then more thoroughly dried in a dryer 13 while the mother liquor coming from centrifuge 12 is redelivered to dissolver 9.

Table 3 below sets forth the flow rates of the various components and the compositions of the products at the various locations in the processing system, the flow rates being those which correspond to one ton of solution at the outlet of filter 5. The location numerals appearing in the column headings designate locations bearing the same reference numerals in FIG. 1. (FIG. 1) Ammonium penta- Reservoir Absorber Carbonation Stripper Crystal- borate decompo- Location 1 3 Column 4 6 lizer 7 sition in 9-13 Mother Liquor Input of Re- Carbo- Tincal Recycled from Tincal Solu- cycled NH.sub.3 ammoniacal NaHCO.sub.3 CO.sub.2 NH.sub.3 and CO.sub.2 Vapor CO.sub.2 NH.sub.3 Heating Boric Ingredient Input Centrifuge 8 tion Input and CO.sub.2 Solution Input Output Input Input Output Output Input Injection Input Recovery Vapor Acid Flow rates, kg/t column solution output Na.sub.2 O 12 25 37 -- 37 12 -- 25 -- -- 25 -- -- -- -- -- (NH.sub.4).sub. 2 O -- 13 13 65 78 -- --78 61 -- 17 -- 4 4 -- -- B.sub.2 O.sub.3 26 89 115 -- 115 -- -- 115 -- -- 115 -- 26 -- -- 26 CO.sub.2 -- 10 10 105 115 17 7 105 105 -- -- 10 -- -- -- -- H.sub.2 O 33 648 681 -- 681 4 -- 677-- 18 659 -- 11 -- 9 20 Total 71 785 856 170 1026 33 7 1000 166 18 816 1041 4 9 46 Compositions, g/kg Na.sub.2 O 162 32 43 -- 36 369 -- 25 -- -- 31 -- -- -- -- -- (NH.sub.4).sub.2 O -- 17 15 382 76 -- -- 78 367 -- 21 -- 96 1000 -- -- B.sub.2 O.sub.3 365 113 134 -- 112 -- -- 115 -- -- 141 -- 639 -- -- 563 CO.sub.2 -- 13 12 618 112 524 1000 105 633 -- -- 1000 -- -- -- -- H.sub.2 O 473 825 796 -- 664 107 -- 677 -- 1000 807 -- 265 -- 1000 437

It is noted that the efficiency of the cycle is mediocre and that it is necessary to desorb and then reabsorb large quantities of ammonia.

In order to increase the yield of the cycle, the same process is carried out but in adjusting the temperature at the bottom of the carbonation column 4 of FIG. 1 to 50.degree. C. The necessary effective pressure is 1.0 kg/cm.sup.2. The installation utilized is identical to that of Example 1 and is thus also shown in FIG. 1.

Table 4 below sets forth the flow rates of the various components and the compositions of the products at the various locations in the installation, the flow rates being with respect to one ton of solution at the outlet of filter 5. The location numerals appearing in the Table correspond to the reference numerals appearing in FIG. 1. (FIG. 1) Ammonium penta- Reservoir Absorber Carbonation Stripper Crystal- borate decompo- Location 1 3 Column 4 6 lizer 7 sition in 9-13 Mother Liquor Input of Re- Carbo- Tincal Recycled from Tincal Solu- cycled NH.sub.3 ammoniacal NaHCO.sub. 3 CO.sub.2 NH.sub.3 and CO.sub.2 Vapor CO.sub.2 NH.sub.3 Heating Boric Ingredient Input Centrifuge 8 tion Input and CO.sub.2 Solution Input Output Input Input Output Output Input Injection Input Recovery Vapor Acid Flow rates, kg/t column solution output Na.sub.2 O 33 27 60 -- 60 33 -- 27 -- -- 27-- -- ---- -- (NH.sub.4).sub. 2 O -- 14 14 121 135 -- -- 135 110 -- 25 -- 11 11 -- -- B.sub.2 O.sub.3 74 96 170 -- 170 -- --170 -- -- 170 -- 74 -- -- 74 CO.sub.2 -- 38 38 150 188 47 9 150 150 -- -- 38 -- -- -- -- H.sub.2 O 96 431 527 -- 527 9 -- 518 -- 56 462 -- 31 -- 26 57 Total 203 606 809 271 1080 89 9 1000 260 56 684 38 116 11 26 131 Compositions, g/kg Na.sub.2 O 162 45 7 -- 56 369 -- 27 -- -- 39 -- -- -- -- -- (NH.sub.4).sub.2 O -- 23 17 446 125 -- -- 135 423 -- 37 -- 96 1000 -- -- B.sub.2 O.sub.3 365 158 210 -- 157 -- -- 170 -- -- 249 -- 639 -- -- 563 CO.sub.2 -- 63 47 534 174 524 1000 150 577 -- -- 1000 -- -- -- -- H.sub.2 O 473 711 652 -- 488 107 -- 518 -- 1000 675 -- 265 -- 1000 437

The results of Example 2 are more favorable than those of Example 1. The yields of the cycle increase, but it remains necessary to desorb and then reabsorb large quantities of ammonia.

Instead of crystallizing ammonium pentaborate, it is possible to crystallize ammonium biborate. It has been seen that the treatment conditions are then more favorable because the mother liquors of the crystallization of sodium bicarbonate are within the domain of crystallization of ammonium biborate. This example has been carried out by adjusting the temperature at the bottom of the carbonation column to 50.degree. C.; the necessary effective pressure is 1 kg/cm.sup.2.

The entirety of the apparatus utilized is shown in FIG. 2 where the individual units are given the same reference numerals as in FIG. 1 if they are also present in the apparatus of FIG. 1.

The soda part remains practically unchanged. The ground tincal is introduced into the reservoir 1 where it is mixed with mother liquor coming from an evaporator 14. The mixture passes to the decanter-washer 2 then to the absorber 3 where it comes in contact with ammonia and carbonic anhydride coming from the tube-type evaporator 14 and the stripping unit 10. The ammoniacal liquor formed passes to the carbonation column 4 supplied with rich carbonic anhydride and cooled in its lower portion to bring the temperature thereat to 50.degree. C., the effective pressure being approximately equal to 1 kg/cm.sup.2. The sodium bicarbonate suspension is filtered in filter 5, NaHCO.sub.3 being separated and the mother liquor delivered, no longer to a stripping zone, but directly to the cooler or crystallizer 7 operating at 26.degree. C., where the carbonic anhydride is liberated while forming crystals of ammonium biborate which are separated in centrifuge 8. The treatment of the crystals is performed, as in Example 1, in dissolver 9, stripping unit 10, boric acid crystallizer 11, centrifuge 12 and dryer 13. On the other hand, the mother liquors of the crystallization of ammonium biborate pass into the evaporator 14 from which there is recovered NH.sub.3 and CO.sub.2 which are delivered into the absorber 3, the mother liquors going into the reservoir 1 where further quantities of tincal are dissolved.

Table 5 below gives the flow rates of the various components and the compositions of the products at various stages of the fabrication process, the flow rates being with respect to one ton of solution at the outlet of filter 5. The numerals represent locations and correspond to the reference numerals appearing in FIG. 2. (FIG. 2) Ammonium biborate Evaporator Reservoir Absorber Carbonation Crystal- decomposition Location 14 1 3 Column 4 lizer 7 in 9-13 Carbo- Mother Input of Input of ammoniated liquor Tincal gas from gas from Tincal Liquor Vapor Gas Tincal from evapo- solution evaporator stripper Solution CO.sub.2 NaHCO.sub.3 Heating Boric Ingredient Input Output Output Input rator 14 input 14 10 Input Input Output Input Input vapor acid Flow rates, kg/t column solution output Na.sub.2 O 27 -- -- 27 56 83 -- -- 83 -- 56 27 -- -- (NH.sub.4).sub.2 O 88 -- 88 -- -- -- 88 47 135 -- -- 135 47 -- -- B.sub.2 O.sub.3 44 -- -- 44 126 170 -- -- 170 -- -- 170 126 -- 126 CO.sub.2 150 -- 150 -- -- -- 150 -- 150 80 80 150 -- -- -- H.sub.2 O 453 82 -- 371 163 534 -- -- 534 -- 16 518 65 33 98 Total 762 82 238 442 345 787 238 47 1072 80 152 1000 238 33 224 Compositions, g/kg Na.sub.2 O 35 -- -- 61 162 105 -- -- 77 -- 369 27 -- -- -- (NH.sub.4).sub.2 O 115 -- 370 -- -- -- 370 1000 126 -- -- 135 198 -- -- B.sub.2 O.sub.3 58 -- -- 100 365 216 -- -- 159 -- -- 170 528 -- 563 CO.sub.2 197 -- 630 -- -- -- 630 -- 140 1000 524 150 -- -- -- H.sub.2 O 595 1000 -- 839 473 679 -- -- 498 -- 107 518 274 1000 437

In this example, the yield of the cycle is increased. The complete dissolution of the tincal before start of crystallization of sodium bicarbonate is only necessary if the mineral is impure. The dissolving of the tincal requires a temperature close to 100.degree. C. and the totality of the ammonia will be desorbed. In order to reabsorb the ammonia, it is necessary to cool the solution and this leads to the crystallization of Na.sub.2 B.sub.4 O.sub.7.10H.sub.2 O and of Na.sub.2 B.sub.4 O.sub.7.5H.sub.2 O. These crystals only disappear in proportion with the appearance of sodium bicarbonate.

One can avoid the desorption of ammonia by utilizing purified tincal as the starting material. The present example gives the results obtained in a process providing for the preliminary purification of the tincal by crystallization of hydrated sodium borate. If the purification of the tincal is carried out in a manner to crystallize the pentahydrated sodium borate, there is no water to evaporate in the cycle since the total reaction is then:

it is not necessary to assure the complete dissolution of the pure borax, because a dissolution will be produced in proportion with the appearance of crystals of sodium bicarbonate in the carbonation column.

One installation suitable for carrying out such a process constituting an embodiment of the invention is shown in FIG. 3 where the units represented in FIGS. 1 and 2 are given the same reference numerals.

The finely ground raw tincal passes to the dissolver 1, to the decanter-washer 2, then into a crystallizer 15 and into a centrifuge 16, after which it is introduced into the carbonation column 4 together with rich CO.sub.2 and the ammonia recovered in the absorber 3 from the mother liquor coming from the centrifuge 8 for the ammonium biborate crystals and from the stripping of the solution of crystals of (NH.sub.4).sub.2 O.2B.sub.2 O.sub.3.4H.sub.2 O in stripping unit 10. The temperature of crystallization of the sodium bicarbonate is 50.degree. C. The sodium bicarbonate filter 5 separates the solid NaHCO.sub.3 and leaves a mother liquor which passes to an absorber 17 where it receives part of the ammonia recovered in stripping unit 10. This mother liquor, thus enriched in ammonia, passes to the crystallizer 7 operating at 26.degree. C. and to the centrifuge 8 where crystals of ammonium biborate are separated, the mother liquor being conveyed to the absorber 3 as indicated above.

These crystals are redissolved in dissolver 9 in the mother liquor from the boric acid centrifuge 12, then the solution passes to the stripping unit 10 which liberates the ammonia supplied to the absorber 3 and a boric acid solution, the latter finally being subjected to crystallization in crystallizer 11 and a centrifuging in centrifuge 12. The centrifuged crystals are further dried as in the previous examples.

Table 6 below gives the flow rates of the various components and the compositions of the products at the various stages of the fabrication process, the flow rates being with respect to one ton of solution at the outlet of filter 5. The numerals appearing in the table correspond to the reference numerals in FIG. 3. (FIG. 3) Centri- Decomposition of Absorber Carbonation Filter Absorber Crystal- fuge the NH.sub.4 biborate Location 3 Column 4 5 17 lizer 7 8 9 to 12 Mother Solution Sodium Liquid Liquid Liquid Crystals liquor Input borate Input Input Input from NH.sub.3 from from centri- from Ab- 5H.sub.2 O CO.sub.2 from NaHCO.sub.3 from NH.sub.3 from from Liquid centri- Vapor NH.sub.3 from Boric Ingredient Stripper 10 fuge 8 sorber 3 Input Input column 4 Output filter 5 Stripper 10 Absorber 17 Output fuge 8 Input Stripper 10 Acid Flow rates, kg/t column solution output Na.sub.2 O -- 35 35 50 -- 85 50 35 -- 35 35 -- -- -- -- (NH.sub.4).sub.2 O 22 101 123 -- -- 123 -- 123 20 143 101 42 -- 42 -- B.sub.2 O.sub.3 -- 46 46 113 -- 159 -- 159 -- 159 46 113 -- -- 113 CO.sub.2 -- 140 140 -- 71 211 71 140 -- 140 140 -- -- -- -- H.sub.2 O -- 484 484 73 -- 557 14 543 -- 543 484 59 36 -- 88 Total 22 806 828 236 71 1135 135 1000 20 1020 806 214 36 42 201 Compositions, g/kg Na.sub.2 O -- 43 42 213 -- 75 369 35 -- 34 43 -- -- -- -- (NH.sub.4).sub.2 O 1000 125 149 -- -- 108 -- 123 1000 140 125 198 -- 1000 -- B.sub.2 O.sub.3 -- 57 56 478 -- 140 -- 159 -- 156 57 528 -- -- 563 CO.sub.2 -- 174 169 -- 1000 186 524 140 -- 137 174 -- -- -- -- H.sub.2 O -- 601 584 309 -- 491 107 543 -- 533 601 274 1000 -- 437

Of the four cycles described above, the fourth is of greatest interest. It permits achieving a good yield, or efficiency, while avoiding the description of the ammonia and the necessity of reabsorbing it. This preferred cycle implies a preliminary purification of the tincal by crystallization and the crystallization of the sodium bicarbonate in the presence of solid tincal.

The present invention is not limited to the specific examples given herein by way of illustration. It can in particular be adapted to the treatment of borosodium minerals other than tincal, for example kernite. Moreover, it encompasses the modifications directly suggested to one skilled in the art and the use of techniques known as being equivalent to those specified herein.