METHOD FOR PRODUCING POTASSIUM SULFATE FROM POTASSIUM CHLORIDE AND SULFURIC ACID

Abstract

A process is provided for producing potassium sulfate from potassium chloride and sulfuric acid. The process entails mixing potassium chloride with the water to form a potassium chloride slurry which is mixed with recycled sulfuric acid to form a K.sup., Ct, SO.sub.4.sup.2 acid mixture. This mixture is subjected to a crystallization process that produces potassium sulfate crystals and a hydrochloric acid-water vapor. The hydrochloric acid is separated from the hydrochloric acid-water vapor to form a hydrochloric acid solution.

Claims

1-29. (canceled)

30. A method for producing potassium sulfate and hydrochloric acid comprising: mixing water with potassium chloride to form a potassium chloride slurry or solution; mixing the potassium chloride slurry or solution with recycled sulfuric acid to form a K.sup.+, Cl.sup., SO.sub.4.sup.2 acid mixture; subjecting the K.sup.+, Cl.sup., SO.sub.4.sup.2 acid mixture to an evaporative crystallization process and producing a concentrate containing potassium sulfate crystals and a hydrochloric acid-water vapor; directing the concentrate containing the potassium sulfate crystals to a solids-liquid separator and separating the potassium sulfate crystals from the concentrate and yielding a filtrate; washing the potassium sulfate crystals with water; and wherein after separating the potassium sulfate crystals from the concentrate, mixing the filtrate with a source of sulfuric acid to produce a hydrochloric acid-rich vapors and a stream of sulfuric acid that forms at least a part of the recycled sulfuric acid mixed with the potassium chloride slurry or solution; and mixing the hydrochloric acid-rich vapors with the hydrochloric acid-water vapor produced by the crystallization process and wherein the hydrochloric acid-rich vapors and the hydrochloric acid-water vapor are directed to an adsorption unit which produces a hydrochloric acid solution having a concentration of 20-35% hydrochloric acid by wt.

31. The method of claim 30 wherein the filtrate includes dissolved salts and after mixing the sulfuric acid with the filtrate, precipitating the dissolved salts from the filtrate-sulfuric acid mixture.

32. The method of claim 30 including concentrating the hydrochloric acid/water vapor produced by the crystallization process to form a vapor stream having a higher hydrochloric acid concentration than the hydrochloric acid/water vapor produced by the crystallization process.

33. The method of claim 30 further including: mixing sulfuric acid with the filtrate to form a sulfuric acid-rich stream; wherein washing the potassium sulfate crystals with water produces a waste stream; and mixing the waste stream with the sulfuric acid-rich stream and recycling the resulting mixture to the crystallization process.

34. The method of claim 30 wherein the evaporative crystallization process is carried out in a crystallizer unit and the method includes directing the filtrate to a dechlorination unit and mixing sulfuric acid with the filtrate to produce a sulfuric acid-rich stream and recycling the sulfuric acid-rich stream to the crystallizer unit.

35. The method of claim 30 including directing the hydrochloric acid-water vapor through an absorption unit and producing a hydrochloric acid solution.

36. The method of claim 30 including directing the hydrochloric acid-water vapor to hydrochloric acid scrubber or condenser unit which produces water vapor and a hydrochloride acid solution and thereafter subjecting the hydrochloride acid solution to treatment in an absorption unit to concentrate the hydrochloric acid solution.

37. The method of claim 36 wherein before subjecting the hydrochloric acid to treatment in the absorption unit, treating the hydrochloric acid solution in an extractive distillation or dual pressure unit.

38. The method of claim 30 including directing the hydrochloric acid-water vapor to an extractive distillation-HCl vapor dehydration unit into which a feed of H.sub.2SO.sub.4 is provided which in turn produces a concentrated HCl/H.sub.2O vapor and a diluted H.sub.2SO.sub.4 solution which is recycled to the crystallization process.

39. The method of claim 38 wherein the concentrated HCl/H.sub.2O vapor is directed to an absorption unit which produces an HCl solution.

40. The method of claim 30 wherein the crystallized potassium sulfate is directed to a wash leg and contacted with a countercurrent flow of a potassium sulfate solution.

41. The method of claim 30 further including separating the hydrochloric acid from the hydrochloric acid/water vapor to form a hydrochloric acid solution.

42. The method of claim 30 including spraying a KOH solution onto the potassium sulfate crystals to neutralize residual acid on the crystals or mother liquor moisture on the crystals.

43. A method for producing potassium sulfate and hydrochloric acid comprising: mixing water with potassium chloride to form a potassium chloride slurry or solution; mixing the potassium chloride slurry or solution with recycled sulfuric acid to form a K.sup.+, Cl.sup., SO.sub.4.sup.2 acid mixture; subjecting the K.sup.+, Cl.sup., SO.sub.4.sup.2 acid mixture to an evaporative crystallization process and producing a concentrate containing crystals comprising potassium and sulfate in the form of K.sub.2SO.sub.4, KHSO.sub.4, or a mixture of both; directing the concentrate containing said crystals of potassium and sulfate to a solids-liquid separator and separating said crystals comprising potassium and sulfate from the concentrate and yielding a filtrate; and washing the crystals comprising potassium and sulfate with water.

44. The method of claim 43 wherein after separating said crystals comprising potassium and sulfate from the concentrate, mixing the filtrate with a source of sulfuric acid to produce a hydrochloric acid vapor and a stream of sulfuric acid that forms at least a part of the recycled sulfuric acid mixed with the potassium chloride slurry or solution; and mixing the hydrochloric acid vapor with the hydrochloric acid/vapor produced by the crystallizer unit.

45. The method of claim 44 wherein the filtrate includes dissolved salts and after mixing the sulfuric acid with the filtrate, precipitating the dissolved salts from the filtrate-sulfuric acid mixture.

46. The method of claim 43 including concentrating the hydrochloric acid/water vapor produced by the crystallization process to form a vapor stream having a higher hydrochloric acid concentration than the hydrochloric acid/water vapor produced by the crystallization process.

47. The method of claim 43 further including: mixing sulfuric acid with the filtrate to form a sulfuric acid-rich stream; wherein washing the crystals comprising potassium and sulfate with water produces a waste stream; and mixing the waste stream with the sulfuric acid-rich stream and recycling the resulting mixture to the crystallization process.

48. The method of claim 43 wherein the evaporative crystallization process is carried out in a crystallizer unit and the method includes directing the filtrate to a dechlorination unit and mixing sulfuric acid with the filtrate to produce a sulfuric acid-rich stream and recycling the sulfuric acid-rich stream to the crystallizer unit.

49. The method of claim 43 including directing the hydrochloric acid-water vapor through an absorption unit and producing a hydrochloric acid solution.

50. The method of claim 43 including directing the hydrochloric acid-water vapor to hydrochloric acid scrubber or condenser unit which produces water vapor and a hydrochloride acid solution and thereafter subjecting the hydrochloride acid solution to treatment in an absorption unit to concentrate the hydrochloric acid solution.

51. The method of claim 50 wherein before subjecting the hydrochloric acid to treatment in the absorption unit, treating the hydrochloric acid solution in an extractive distillation or dual pressure unit.

52. The method of claim 43 including directing the hydrochloric acid-water vapor to an extractive distillation-HCl vapor dehydration unit into which a feed of H.sub.2SO.sub.4 is provided which in turn produces a concentrated HCl/H.sub.2O vapor and a diluted H.sub.2SO.sub.4 solution which is recycled to the crystallization process.

53. The method of claim 52 wherein the concentrated HCl/H.sub.2O vapor is directed to an absorption unit which produces an HCl solution.

54. The method of claim 43 wherein the crystals comprising potassium and sulfate is directed to a wash system and contacted with a countercurrent flow of a potassium sulfate solution.

55. The method of claim 43 further including separating the hydrochloric acid from the hydrochloric acid/water vapor to form a hydrochloric acid solution.

56. The method of claim 43 further including spraying a KOH solution on the crystals comprising potassium and sulfate to neutralize residual acid or mother liquor moisture on the crystals.

Description

DESCRIPTION OF THE DRAWINGS

[0012] FIG. 1 is a schematic illustration of a basic process for producing potassium sulfate and hydrochloric acid.

[0013] FIG. 2 is a schematic illustration of a potassium sulfate production process similar in many respects to that shown in FIG. 1 but including additional processes for treating the HCl/H.sub.2O vapors produced by the crystallizer to produce a more concentrated HCl solution.

[0014] FIG. 3 is a schematic illustration of a potassium sulfate production process similar to FIG. 2 but includes another alternative process for treating the HCl/H.sub.2O vapors produced by the crystallizer to produce a more concentrated HCl solution.

[0015] FIG. 4 is yet another alternative design for a potassium sulfate production process where the crystallized potassium sulfate is subjected to additional washings to increase the quality of potassium sulfate produced.

[0016] FIG. 5 is a schematic illustration of a process for producing potassium sulfate and hydrochloric acid but including an option for precipitating magnesium and calcium salts which may be added to the potassium sulfate or to a waste stream.

[0017] FIG. 6 comprises solubility diagrams for K.sub.2SO.sub.4, H.sub.2SO.sub.4 and H.sub.2O.

DESCRIPTION OF EXEMPLARY EMBODIMENTS

[0018] The present invention may be applied in a number of exemplary embodiments. At a basic level, the present invention follows a method in which a potassium chloride (KCl) slurry or solution is contacted with a recycled H.sub.2SO.sub.4 rich stream in an evaporative crystallizer. The crystallization process produces the desired product, crystallized K.sub.2SO.sub.4, and a vapor mixture of HCl and H.sub.2O. Each of these products may then undergo further treatment; for example, the HCl/H.sub.2O vapor may be processed to produce a concentrated HCl solution, while the crystallized K.sub.2SO.sub.4 may undergo cleaning processes.

[0019] FIG. 1 shows an exemplary embodiment. Water and potassium chloride are first introduced in a dissolution unit 10, producing the KCl slurry or solution which is directed to a crystallizer unit 12. A recycled H.sub.2SO.sub.4 rich stream is also directed to the crystallizer unit 12, and reacts with the KCl slurry to produce K.sub.2SO.sub.4 and HCl, and H.sub.2O. Alternatively, the recycled H.sub.2SO.sub.4 rich stream is mixed with the KCl slurry upstream of the crystallizer unit 12. Crystallizer unit 12 should be set and controlled such that very little to no chloride salt will crystallize with the K.sub.2SO.sub.4. After evaporative crystallization occurs, the crystallizer unit 12 produces a concentrate containing crystallized K.sub.2SO.sub.4 and an HCl/H.sub.2O vapor. In some cases and as an option, the concentrate produced by the crystallizer unit 12 includes crystals comprising potassium sulfate or potassium bisulfate or mixtures of both. The concentrate containing the crystallized K.sub.2SO.sub.4 is sent to a separation and dewatering unit 14, whereupon the solid salt crystals are separated from the concentrate to yield a filtrate. The solids, including K.sub.2SO.sub.4 crystals are then directed to a washing unit 16 to ensure that no entrained liquor, which might affect the salt quality after drying, remains. After washing, the final desired K.sub.2SO.sub.4 product is collected.

[0020] The filtrate produced by the solids-liquid separation or dewatering unit 14 is directed to a dechlorination unit 20. This unit removes almost all Chloride from the filtrate to produce HCl rich vapors, which are then combined with the HCl/H.sub.2O vapor produced by the crystallizer unit 12. H.sub.2SO.sub.4 is added to the remaining filtrate in the dechlorination unit 20, producing an H.sub.2SO.sub.4 rich solution. This further has the effect of increasing the acidity of the H.sub.2SO.sub.4 rich solution high enough such that the residual chloride in the filtrate forms concentrated HCl, while the potassium bisulfate remains soluble. At this stage, impurities from the raw KCl, such as magnesium and calcium, may be removed as precipitated sulfate solids to improve the quality of the final potassium and sulfate crystals. The liquid solution produced by mixing the filtrate from the separation/dewatering unit 14 with H.sub.2SO.sub.4 is combined with the waste stream produced from the washing unit 16 to produce a recycled H.sub.2SO.sub.4 rich stream, which is directed back to the crystallizer unit 12 for reaction. The HCl rich vapors from the dechlorination unit 20 and the HCl/H.sub.2O vapor from crystallizer unit 12 are directed to an absorption unit 18, producing a high concentration HCl solution. This high concentration HCl solution in one embodiment is about 20-35% HCl by weight.

[0021] Because the exact composition of the HCl/H.sub.2O vapor from crystallizer unit 12 and thus the final concentration of the HCl solution is governed by the acidity level in the liquor in the crystallizer unit 12 and the residual potassium content after crystallization, instances may occur in which the final HCl solution does not meet a desired or threshold concentration. Therefore, in cases where the concentration of HCl in the vapor produced by the crystallizer unit 12 is relatively low, it may be desirable to provide a concentration process that increases the HCl concentration.

[0022] FIG. 2 illustrates an alternate process similar to that of FIG. 1, but including an HCl scrubber or condenser unit 24. The HCl/H.sub.2O vapor from crystallizer unit 12 is directed to the scrubber or condenser unit 24, which produces H.sub.2O vapor and a concentrated HCl solution (for example in the range of 16-20% by weight). This concentrated solution is then directed to an optional extractive distillation or dual pressure unit 26, generating highly concentrated HCl vapors which can be directed to the absorption unit 18 to produce an HCl solution having a purity of approximately 20-35 wt. %.

[0023] In the case that the HCl solution has a lower concentration than desired but is close to the required concentration for reuse, FIG. 3 describes an alternative method to FIG. 2. The method described is similar to that in FIG. 2, but replaces the HCl scrubber or condenser unit 24 with an extractive distillation-HCl vapors dehydration unit 28, into which a feed of H.sub.2SO.sub.4 is provided. With an input stream of low concentration HCl/H.sub.2O vapor, the unit 28 produces a concentrated HCl/H.sub.2O vapor and a diluted H.sub.2SO.sub.4 solution, which may be recycled to the crystallizer unit 12.

[0024] Finally, depending on other constituents such as chloride and potassium bisulfate content in the crystallized K.sub.2SO.sub.4, the produced K.sub.2SO.sub.4 salt may require additional cleaning to improve quality. FIG. 4 describes an exemplary embodiment of the present invention in which, after undergoing the process steps described in FIG. 1, the crystallized K.sub.2SO.sub.4 is directed to a wash leg 30 and contacted with a counter-current flow of a potassium sulfate solution. This wash leg aims to increase the quality of the K.sub.2SO.sub.4 and may be paired with a dosage of a neutralizing base, such as KOH, in a second washing and dewatering unit 32 to further reduce the chloride and salt acidity. This further has the effect of converting possible residual potassium bisulfate into potassium sulfate. The KOH may be sprayed as a solution onto the crystals and/or in the K.sub.2SO.sub.4 dissolution tank 34.

[0025] FIG. 5 shows another embodiment of the process of the present invention. It is similar in many respects to the process shown in FIG. 1 and described above. However, as an option, the H.sub.2SO.sub.4-rich solution produced by the dechlorination unit 20 is directed to a separation/dewatering unit 36. Calcium and magnesium salts are precipitated and filtered and may be either added to the K.sub.2SO.sub.4 final product or to a waste stream in cases where a high K.sub.2SO.sub.4 purity is required.

[0026] The drawings show the production of K.sub.2SO.sub.4. It is appreciated by those skilled in the art that the process may also produce KCl and KHSO.sub.4. Indeed, in some instances the quantity of KCl and/or KHSO.sub.4 may actually exceed the quantity of K.sub.2SO.sub.4 produced. Therefore, the mixing of the potassium chloride slurry or solution with sulfuric acid will form a K.sup.+, Cl.sup., SO.sup.2 acid mixture and once subjected to a crystallization process produces a concentrate containing sulfate and potassium salts.

[0027] There are numerous advantages to the process described above. The present invention provides a process that rearranges the reactant flows into a one-stage crystallization process that enhances hydrochloric acid recovery in optimum conditions while allowing crystallization of potassium sulfate at medium acidity levels. In particular, the potassium chloride and sulfuric acid reactants are not injected at the same process step in order to shift the acidity profile compared to some conventional processes. The hydrochloric acid/water evaporation and K.sub.2SO.sub.4crystallization are potentially performed in the same process unit. The reactants and products are expected to have a better and at least the same quality as conventional potassium sulfate production processes while resulting in significantly lower investment costs, as well as lower operation and maintenance costs. Also, the operating temperature is kept high enough to limit any potassium chloride co-precipitation with the potassium sulfate crystals. The process also provides a first washing and dewatering step for the potassium sulfate crystals which allows for displacing the solution acidity to a specific dechlorination step. The process also describes an optional second washing/dewatering step that allows for adjusting the potassium sulfate crystal properties to meet highest quality requirements.

[0028] The present invention may, of course, be carried out in other specific ways than those herein set forth without departing from the scope and the essential characteristics of the invention. The present embodiments are therefore to be construed in all aspects as illustrative and not restrictive and all changes coming within the meaning and equivalency range of the appended claims are intended to be embraced therein.