Acesulfame potassium composition and its method of manufacture

Abstract

To provide a composition and a method for producing high-purity acesulfame potassium.SOLUTION: A manufacturing method of an acesulfame potassium composition comprises: preparing a crude acesulfame potassium composition comprising acesulfame potassium and acetoacetamide; concentrating the crude acesulfame potassium composition to form an intermediate acesulfame potassium composition comprising water flow, and acesulfame potassium and less than 33 wppm acetoacetamide; and separating the intermediate acesulfame potassium composition to form a purified acesulfame potassium composition comprising acesulfame potassium and less than 33 wppm acetoacetamide. The concentration step is carried out at a temperature below 90°C and the separation step is carried out at a temperature below 35°C.SELECTED DRAWING: None

Description

[Technical field]

[0001]

[0001] This patent application is related to and claims priority to U.S. Provisional Patent Application No. 62 / 397,509, filed Sep. 21, 2016, the disclosure of which is incorporated herein by reference in its entirety.

[0002]

[0002] The present invention relates generally to acesulfame potassium and to a method for producing acesulfame potassium, and more specifically to a method for producing high purity acesulfame potassium. [Background technology]

[0003]

[0003] Acesulfame potassium has a very strong sweet taste and is used as a sweetener in many food-related applications. In a conventional process for producing acesulfame potassium, sulfamic acid is reacted with an amine, e.g., triethylamine, to form an amidosulfamate, such as trialkylammonium amidosulfamate. The amidosulfamate is then reacted with diketene to form an acetoacetamide salt. The acetoacetamide salt can be cyclized, hydrolyzed, and neutralized to form acesulfame potassium. U.S. Patents 5,744,010 and 9,024,016 disclose representative processes for producing acesulfame potassium.

[0004]

[0004] Typically, the acetoacetamide salt intermediate is cyclized to form a cyclic sulfur trioxide adduct by reaction with sulfur trioxide in an inorganic or organic solvent. The solvent typically used in this reaction is an organic solvent such as a halogenated aliphatic hydrocarbon solvent, e.g., dichloromethane. The adduct formed by this reaction is subsequently hydrolyzed and then neutralized with potassium hydroxide to form potassium acesulfame.

[0005]

[0005] Acesulfame potassium products and intermediate compositions produced by conventional processes contain undesirable impurities such as acetoacetamide (and acetoacetamide-N-sulfonic acid). Often limits on the content of various impurities are set by government regulations or customer guidelines. Removal of many of these impurities using standard purification procedures such as evaporation, crystallization, and / or filtration has proven difficult, leading to consumer dissatisfaction and unsatisfactory standards. [Prior art documents] [Patent documents]

[0006] [Patent Document 1] U.S. Patent 5,744,010 [Patent Document 2] U.S. Patent 9,024,016 Summary of the Invention [Problem to be solved by the invention]

[0007] There is a need for improved processes for producing high purity acesulfame potassium compositions which reduce or eliminate the formation of impurities such as acetoacetamide during the synthesis.

[0008]

[0007] All references discussed herein are incorporated herein by reference. [Means for solving the problem]

[0009]

[0008] The present application relates to a purified acesulfame potassium composition. A method for producing a composition comprising the steps of: acesulfame potassium, acetoacetamide, and water; concentrating the crude acesulfame potassium composition to form an intermediate acesulfame potassium composition comprising a water stream, acesulfame potassium, and less than 33 wppm acetoacetamide (and optionally less than 33 wppm acetoacetamide-N-sulfonic acid); and separating the intermediate acesulfame potassium composition to form a purified acesulfame potassium composition comprising acesulfame potassium and less than 33 wppm acetoacetamide. The concentrating step is performed at a temperature below 90°C and the separating step is performed at a temperature of 35°C or less. The weight percent of acetoacetamide in the purified acesulfame potassium composition can be lower than the weight percent of acetoacetamide in the crude acesulfame potassium composition. The intermediate acesulfame potassium composition can contain less than 33 wppm acetoacetamide-N-sulfonic acid. Providing a crude acesulfame composition may include reacting a sulfamic acid with an amine to form an amidosulfamate salt, reacting the amidosulfamate with an acetoacetylating agent to form an acetoacetamide salt, reacting the acetoacetamide salt with a cyclizing agent in a cyclizing agent composition to form a cyclic sulfur trioxide adduct, hydrolyzing the cyclic sulfur trioxide adduct to form an acesulfame-H composition comprising acesulfame-H, and neutralizing the acesulfame-H in the acesulfame-H composition to form a crude acesulfame potassium composition comprising acesulfame potassium and acetoacetamide. The concentrating step may include evaporating the crude acesulfame potassium composition to form a water stream and an intermediate acesulfame potassium composition comprising acesulfame potassium and less than 75% by weight water, and the evaporation residence time may be less than 180 minutes. The separating can include crystallizing the intermediate acesulfame potassium composition to form acesulfame potassium crystals; and filtering the acesulfame potassium crystals to form a purified acesulfame potassium composition.Preferably, concentrating comprises evaporating the crude acesulfame potassium composition to form a water stream and an intermediate acesulfame potassium composition comprising acesulfame potassium and less than 50 wt.% water, and separating comprises crystallizing the intermediate acesulfame potassium composition to form a crystal-containing stream comprising acesulfame potassium crystals; and filtering the crystal-containing stream to form a purified acesulfame potassium composition. The filtration may be performed at a temperature of 35° C. or less, and / or the crystallization may be performed at a temperature of 35° C. or less, and / or may include at least two filtration operations. In some cases, the evaporation may be performed at a temperature below 85° C., the intermediate acesulfame potassium composition may comprise 1 wppb to 33 wppm acetoacetamide (and in some cases less than 33 wppm acetoacetamide-N-sulfonic acid), and the purified acesulfame potassium composition may comprise less than 33 wppm acetoacetamide. In one embodiment, the evaporation can be performed at a temperature below 60° C., the evaporator residence time can be less than 50 minutes, the intermediate acesulfame potassium composition can include 10 wppb to 25 wppm acetoacetamide (and optionally less than 30 wppm acetoacetamide-N-sulfonic acid), and the purified acesulfame potassium composition can include 10 wppb to 15 wppm acetoacetamide. In one embodiment, the evaporation can be performed at a temperature below 46° C., the evaporator residence time can be less than 30 minutes, and the crystallization can be performed at a temperature below 35° C., the intermediate acesulfame potassium composition can include 10 wppb to 12 wppm acetoacetamide (and optionally less than 20 wppm acetoacetamide-N-sulfonic acid), and the purified acesulfame potassium composition can include 10 wppb to 7 wppm acetoacetamide.In some cases, the evaporation is carried out at a temperature ranging from 20° C. to 55° C.; the evaporator residence time is in the range of 1 minute to 300 minutes; the separation is carried out at a temperature ranging from −10° C. to 15° C.; the separation operation residence time is in the range of 1 to 180 minutes; the crude acesulfame potassium composition contains 500 wppm to 2375 wppm acetoacetamide; the intermediate acesulfame potassium composition contains 10 wppb to 20 wppm acetoacetamide, and 10 wppb to 20 wppm acetoacetamide-N-sulfonic acid; and the purified acesulfame potassium composition contains 10 wppb to 10 wppm acetoacetamide, and 1 wppb to 20 wppm acetoacetamide-N-sulfonic acid. The crystallization can be carried out at a pH below 10. The crude acesulfame composition may further comprise a solvent, and the method may further comprise removing the solvent from the crude acesulfame potassium composition prior to evaporating. The method may comprise separating a transition phase comprising at least 2% by weight acetoacetamide from the acesulfame-H composition to form a purified acesulfame-H composition; neutralizing may comprise neutralizing the acesulfame-H in the purified acesulfame-H composition to form a crude acesulfame potassium composition comprising acesulfame potassium and acetoacetamide.In one aspect, the method includes the steps of reacting sulfamic acid with triethylamine to form an amidosulfamate salt; reacting the amidosulfamate salt with diketene to form an acetoacetamide salt; contacting dichloromethane with sulfur trioxide to form a cyclization agent composition; reacting the acetoacetamide salt with sulfur trioxide in the cyclization agent composition to form a cyclic sulfur trioxide adduct; hydrolyzing the cyclic sulfur trioxide adduct to form an acesulfame-H composition; neutralizing the acesulfame-H to form an acesulfame potassium salt. The process includes the steps of forming a crude acesulfame potassium composition comprising acesulfame potassium and less than 10 wppm acetoacetamide; evaporating the crude acesulfame potassium composition to form a water stream and an intermediate acesulfame potassium composition comprising acesulfame potassium and less than 75 wppm water; crystallizing the intermediate acesulfame potassium composition to form acesulfame potassium crystals; and filtering the acesulfame potassium crystals to form a purified acesulfame potassium composition comprising acesulfame potassium and less than 10 wppm acetoacetamide. The evaporation can be performed at a temperature below 50° C., the evaporator residence time can be less than 30 minutes, the filtration can be performed at a temperature below 35° C., and / or the crystallization can be performed at a temperature below 35° C. The present application also describes crude, intermediate, and purified acesulfame potassium compositions produced by the processes described herein. In some cases, the present application describes acesulfame potassium compositions comprising acesulfame potassium and less than 33 wppm, preferably less than 10 wppm, of acetoacetamide, and optionally further comprising less than 33 wppm, preferably less than 10 wppm, of acetoacetamide-N-sulfonic acid. In some cases, the acesulfame potassium compositions further comprise 0.001 wppm to 5 wppm of organic impurities, and / or 0.001 wppm to 5 wppm of at least one heavy metal (e.g., the at least one heavy metal is selected from the group consisting of mercury, lead, and mixtures thereof). In some cases, the acesulfame potassium compositions further comprise mercury present in an amount of 1 wppb to 20 wppm, and / or lead present in an amount of 1 wppb to 25 wppm.

[0010]

[0009] In the following, the present invention will be described in detail with reference to the accompanying drawings. [Brief description of the drawings]

[0011] [Figure 1] FIG. 1 is a process flow sheet of a process for producing acesulfame potassium according to one embodiment of the present invention. [Diagram 2] FIG. 2 is a process flow sheet for a process for producing potassium acesulfame using one embodiment of the processing scheme of the present invention. DETAILED DESCRIPTION OF THE PREFERRED EMBODIMENTS

[0012] Introduction :

[0012] A conventional process for producing acesulfame potassium involves reacting sulfamic acid with an amine in the presence of acetic acid to form an amidosulfamate salt. The amidosulfamate salt is then reacted with an acetoacetylating agent, such as diketene, to form an acetoacetamide salt. The acetoacetamide salt is then reacted with a cyclizing agent, such as sulfur trioxide, to form a cyclic sulfur trioxide adduct. The cyclic sulfur trioxide adduct is then hydrolyzed and neutralized by conventional means to form a crude acesulfame potassium composition comprising acesulfame potassium. The composition is phase separated into an aqueous phase and an organic phase. The majority of the acesulfame potassium separates into the aqueous phase. As used herein, the term "crude acesulfame potassium composition" refers to the initial product of the neutralization reaction (without further purification) or the aqueous phase formed from the phase separation step. The crude acesulfame potassium composition comprises at least 5% by weight acesulfame potassium. Optionally, the crude acesulfame potassium composition may be processed to form an "intermediate acesulfame potassium composition" and / or a "purified acesulfame potassium composition," discussed below.

[0013]

[0013] Conventional acesulfame potassium compositions have been shown to contain several undesirable impurities, among them acetoacetamide and acetoacetamide salts, such as acetoacetamide-N-sulfonate triethylammonium salt. Acetoacetamide-N-sulfonic acid and its salts may also be present. The content limits for these compounds in the purified acesulfame potassium composition are often set by industry purity standards and / or standards established for the particular end product in which acesulfame potassium is used as a sweetener. In some cases, the limits for these impurities are set by government regulations. For most applications, high acesulfame potassium purity levels are preferred. Thus, crude acesulfame potassium compositions are usually treated by various processing operations to reduce the presence of these impurities. A non-limiting list of such processing operations includes evaporation, crystallization, and / or filtration.

[0014]

[0014] Without being bound by theory, it has now been found that these processing operations can cause stresses, such as heat stress, on the acesulfame potassium molecule. This heat stress can also affect acesulfame-H (also known as sweetener acid), which is formed during the hydrolysis step and is a precursor to acesulfame potassium. This stress on acesulfame potassium and possibly acesulfame-H can cause the decomposition of these compounds, resulting in the formation of undesirable impurities. In some circumstances, this stress can cause the decomposition of acesulfame potassium / acesulfame-H to its forming reaction reactants, such as acetoacetamide and / or its salts and / or acetoacetamide-N-sulfonic acid, which can cause the formation of further impurities.

[0015]

[0015] It has also now been discovered that by employing certain process parameters, stress on acesulfame potassium (or acesulfame-H) can be advantageously reduced or eliminated, and / or product decomposition can be advantageously reduced or eliminated, thereby reducing or eliminating the formation of further impurities, ultimately resulting in a high purity final product.

[0016] In particular, it has now been discovered that by conducting the process (or individual process steps) within specific temperature ranges or limits and / or maintaining the process residence time within specific time ranges or limits, the decomposition of acesulfame potassium (or acesulfame-H) and the formation of impurities, including (re)formation of acetoacetamide and its salts, is surprisingly reduced or eliminated. Traditionally, process operations, such as evaporation, have been carried out at higher temperatures to improve process speed and by rapidly removing water. The reduced decomposition of acesulfame potassium and acesulfame-H leads directly to the formation of higher purity crude acesulfame potassium compositions as discussed herein, which simplifies subsequent process operations to form intermediate or purified acesulfame potassium compositions. The process also advantageously results in the formation of intermediate and purified acesulfame potassium compositions having low acetoacetamide-N-sulfamic acid and / or acetoacetamide contents.

[0017]

[0017] We now define further specific terms used in this specification.

[0018] "Acetoacetamide-N-sulfonic acid" as used herein refers to the molecule shown below. In some cases, acetoacetamide-N-sulfonic acid may be a decomposition product of acesulfame potassium or acesulfame-H. As used herein, the term "acetoacetamide-N-sulfonic acid" also includes salts of acetoacetamide-N-sulfamic acid, such as potassium, sodium, and other alkali metal salts.

[0018] [ka]

[0019] As used herein, "acetoacetamide" refers to the following molecule:

[0020] [ka]

[0021] The crude acesulfame composition may be processed to form an intermediate acesulfame potassium composition and a purified acesulfame composition, and the processing steps may include one or more concentration or separation operations.

[0022] "Intermediate acesulfame potassium composition" refers to a composition obtained by concentrating a crude acesulfame potassium composition, e.g., by removing water from the crude acesulfame potassium composition, the intermediate acesulfame potassium composition containing at least 10% by weight acesulfame potassium, based on the total weight of the intermediate acesulfame potassium composition, and having a higher weight percent of acesulfame potassium than that of the crude acesulfame potassium composition.

[0023] "Purified acesulfame potassium composition" refers to a composition obtained by separation, e.g., crystallization and / or filtration (preferably directly), of an intermediate acesulfame potassium composition. The purified acesulfame potassium composition contains at least 15% by weight acesulfame potassium, based on the total weight % of the purified acesulfame potassium composition, and has a higher weight % of acesulfame potassium than that of the intermediate acesulfame potassium composition.

[0024] As used herein, "residence time" refers to the time that a composition (or stream) being treated, e.g., a crude acesulfame potassium composition, is held in a particular processing operation. The residence time begins when the composition being treated is introduced into the processing operation and the residence time continues until the composition is fully dissolved (due to processing). The residence time for a concentration operation, e.g., evaporation, refers to the time from when the crude acesulfame potassium composition is introduced into an evaporator to when the intermediate acesulfame potassium composition is discharged from the evaporator. As another example, the residence time for a separation operation, e.g., crystallization, refers to the time from when the crude acesulfame potassium composition is introduced into a crystallizer to when the intermediate acesulfame potassium composition is discharged from the crystallizer.

[0025]

[0024] The processing of a crude acesulfame potassium composition may involve one or more operations, such as a concentration operation and / or a separation operation. Generally, a concentration operation is not considered a separation operation. In some embodiments, one or more concentration operations and one or more separation operations comprise the overall processing of a crude acesulfame potassium composition, which results in a purified acesulfame potassium composition. In some cases, an overall concentration operation may include multiple individual concentration operations or units, and an overall separation operation may include multiple individual separation operations or units.

[0026] As used herein, "cyclization reaction time" refers to the time from the start of the acetoacetamide salt feed to the end of the acetoacetamide salt feed. In some cases, where indicated, the cyclization reaction time can include additional time after the end of the acetoacetamide salt feed, such as an additional 5 minutes or an additional 1 minute.

[0027] As used herein, "wppm" and "wppb" mean parts per million or parts per billion by weight, respectively, based on the total weight of the respective entire compositions, e.g., the total crude acesulfame potassium composition or the total purified acesulfame potassium composition.

[0028] Formation of Acesulfame Potassium :

[0027] A method for producing a high purity acesulfame potassium composition is described herein. In one aspect, the method includes the steps of providing a crude acesulfame potassium composition comprising acesulfame potassium and acetoacetamide, optionally present in an amount ranging from 1 wppb to 50 wppm; and treating the crude acesulfame potassium composition to form a purified acesulfame potassium composition. The treating can include concentrating the crude acesulfame potassium composition to form a water stream and an intermediate acesulfame potassium composition comprising acesulfame potassium and a minor amount of acetoacetamide; and then separating the intermediate acesulfame potassium composition to form a purified acesulfame potassium composition comprising acesulfame potassium and a minor amount of acetoacetamide. As discussed above, the crude acesulfame potassium composition can be formed by reacting a sulfamic acid with an amine to form an amidosulfamate salt, and then reacting the amidosulfamate salt with an acetoacetylating agent to form an acetoacetamide salt. The acetoacetamide salt can then be cyclized, hydrolyzed, and neutralized (and optionally phase separated), steps which are described in more detail below.

[0029] Importantly, in some embodiments, certain parameters of the concentration and / or separation operations are maintained at particular levels and / or within particular ranges. In some cases, the temperature at which the concentration and / or separation operations are carried out is maintained at a low level. Also, in some embodiments, the residence time (of the crude acesulfame potassium composition in the concentration operation, or of the intermediate acesulfame potassium composition in the separation operation) is maintained at a low level. Without being bound by theory, the result is that less or no additional impurities, such as acetoacetamide, are produced during processing, e.g., during the concentration and / or separation operations, thereby providing a purer purified acesulfame potassium composition. In some cases, the acetoacetamide in the purified acesulfame potassium composition, or in the intermediate acesulfame potassium composition, is reduced. The weight percent acetoacetamide is lower than the weight percent acetoacetamide in the crude acesulfame potassium composition, i.e., the acetoacetamide content is actually reduced during processing.

[0030] In some embodiments, the concentration operation, e.g., one or more of the steps that make up the concentration operation, is carried out at or maintained at a low temperature, e.g., below 90° C., e.g., below 88° C., below 85° C., below 83° C., below 80° C., below 78° C., below 75° C., below 73° C., below 70° C., below 65° C., below 55° C., below 50° C., or below 46° C. In some cases, the temperature of the concentration operation can be maintained above 0° C., e.g., above 10° C., above 15° C., above 20° C., above 22° C., above 25° C., above 35° C., above 40° C., or above 50° C. In terms of ranges, the temperature of the concentration operation may be in the range of 0°C to 90°C, for example, 25°C to 90°C, 55°C to 90°C, 10°C to 88°C, 10°C to 85°C, 75°C to 88°C, 80°C to 88°C, 15°C to 85°C, 75°C to 85°C, 20°C to 83°C, 20°C to 80°C, 22°C to 78°C, 25°C to 75°C, 25°C to 73°C, 15°C to 50°C, 25°C to 65°C, 22°C to 50°C, 20°C to 55°C, 25°C to 70°C, or 30°C to 60°C.

[0031] In some embodiments, the separation operation, e.g., one or more of the steps that make up the separation operation, is carried out at or maintained at a low temperature, e.g., below 35° C., below 30° C., below 25° C., below 20° C., below 15° C., below 10° C., below 8° C., below 6° C., below 5° C., or below 0° C. In some cases, the temperature of the separation operation can be maintained above −25° C., e.g., above −10° C., above 0° C., above 5° C., above 10° C., above 15° C., above 25° C., or above 30° C. In terms of ranges, the temperature of the separation operation may range from −25° C. to 35° C., e.g., −10° C. to 35° C., 0° C. to 35° C., 5° C. to 30° C., −10° C. to 30° C., −10° C. to 25° C., −10° C. to 20° C., −10° C. to 15° C., 0° C. to 25° C., or −10° C. to 30° C. Using the above temperatures in the process advantageously improves the final product purity.

[0032] In some embodiments, the concentration operation, e.g., one or more of the steps that make up the concentration operation, is performed or maintained at a short residence time. In one embodiment, the residence time is less than 180 minutes, e.g., less than 170 minutes, less than 150 minutes, less than 120 minutes, less than 100 minutes, less than 90 minutes, less than 75 minutes, less than 50 minutes, less than 40 minutes, less than 30 minutes, less than 20 minutes, or less than 10 minutes. In terms of the lower limit, the residence time may be at least 1 second, e.g., at least 10 seconds, at least 1 minute, at least 10 minutes, or at least 15 minutes. In terms of ranges, the residence time may range from 1 second to 180 minutes, e.g., 10 seconds to 180 minutes, 1 minute to 180 minutes, 10 minutes to 150 minutes, 1 minute to 50 minutes, 1 minute to 30 minutes, 10 minutes to 100 minutes, 1 minute to 80 minutes, 10 minutes to 80 minutes, 10 minutes to 50 minutes, 15 minutes to 90 minutes, or 15 minutes to 75 minutes. The same residence time limits and ranges can be applied to a separation operation, e.g., one or more of the steps that make up a separation operation. The use of residence times in the concentration operation and / or separation operation advantageously improves final product purity.

[0033] In some embodiments, the concentration operation, e.g., one or more of the steps constituting the concentration operation, is carried out at or maintained at a low pH. In one embodiment, the pH of the separation is maintained below 10.0, e.g., below 9.5, below 9.0, below 8.5, below 8.0, below 7.5, below 7.0, or below 6.5. In terms of ranges, the pH of the concentration operation is preferably maintained between 6.0 and 10.0, e.g., between 6.5 and 9.5, between 7.0 and 9.0, or between 7.5 and 8.5. The same pH limits and ranges can be applied to the separation operation, e.g., one or more of the steps constituting the separation operation. By using low pH levels in the concentration operation or separation operation, the final product purity is advantageously improved.

[0034]

[0033] When evaporation is used in the concentration operation, it can be carried out at the temperature limits and ranges described above. In addition to the benefits of reducing impurities described above, using lower evaporation temperatures significantly limits or eliminates the formation of solids in the evaporator, such as solid acesulfame potassium, which can cause safety issues, such as unnecessary pressure build-up or evaporator explosion.

[0035] The above parameter limits and ranges can be applied to the individual concentration or separation operations that can constitute the entire concentration or separation operation. For example, if the concentration operation can include evaporation, the evaporation can be carried out at a temperature below 90°C, such as below 88°C, below 85°C, below 83°C, below 80°C, below 78°C, below 75°C, below 73°C, below 70°C, below 65°C, below 55°C, below 50°C, or below 46°C. As another example, if the concentration operation can include evaporation, the evaporation can be carried out with a residence time of less than 180 minutes, such as less than 170 minutes, less than 150 minutes, less than 120 minutes, less than 100 minutes, less than 90 minutes, less than 75 minutes, less than 50 minutes, less than 40 minutes, less than 30 minutes, less than 20 minutes, or less than 10 minutes. As another example, if the separation procedure involves crystallization, the crystallization can be carried out at a pH below 10.0, e.g., below 9.5, below 9.0, below 8.5, below 8.0, below 7.5, below 7.0, or below 6.5.

[0036]

[0035] By operating under the temperature, pH, and / or residence time parameters discussed herein, stress on the acesulfame potassium molecule (in the crude acesulfame potassium composition) during the separation operation is advantageously minimized. As a result, less acesulfame potassium decomposes to acetoacetamide during the separation operation. Thus, the intermediate acesulfame potassium composition and the purified acesulfame potassium composition advantageously contain less impurities, such as acetoacetamide (if any), than would normally be formed by decomposition of acesulfame potassium.

[0037]

[0036] The concentrating operation, in some embodiments, includes evaporating the crude acesulfame potassium composition to form a water stream, and an intermediate acesulfame potassium composition comprising acesulfame potassium and less than 75 wt%, e.g., less than 50 wt%, less than 40 wt%, less than 30 wt%, less than 20 wt%, less than 15 wt%, less than 10 wt%, less than 50 wt%, less than 3 wt%, or less than 1 wt% water. The water stream can refer to water that is evaporated from the crude acesulfame potassium composition, e.g., water that is not present in the intermediate acesulfame potassium composition. The evaporation can be carried out at the concentrating operation parameters mentioned herein.

[0038] In some cases, the separation includes a step of crystallizing the intermediate acesulfame potassium composition or a derivative thereof to form a purified acesulfame potassium composition, which may be in the form of acesulfame potassium crystals (or a composition / stream containing acesulfame potassium crystals). The intermediate acesulfame potassium composition may be a stream or composition obtained from concentrating the crude acesulfame potassium composition. The crystallization may be carried out at the separation operating parameters mentioned herein.

[0039] In some embodiments, the separation includes filtering the intermediate acesulfame potassium composition (or a crystal-containing derivative thereof) to form a purified acesulfame potassium composition. The crystal-containing derivative of the intermediate acesulfame potassium composition may be a stream or composition obtained from concentrating a crude acesulfame potassium composition and containing crystals in either dissolved or solid form. Filtration may be performed at the separation operating parameters mentioned herein.

[0040] In a preferred embodiment, the overall process involves evaporating the crude acesulfame potassium composition to produce a water stream, as well as acesulfame potassium and small amounts (see limits / ranges above) of water. forming an intermediate acesulfame potassium composition comprising:

[0041] In one embodiment, the method includes the steps of providing a crude acesulfame potassium composition comprising acesulfame potassium and acetoacetamide and water; and evaporating the crude acesulfame potassium composition to form a water stream, and an intermediate acesulfame potassium composition (disclosed above). In this embodiment, the residence time of the crude acesulfame potassium composition in the evaporator is less than 180 minutes, e.g., less than 170 minutes, less than 150 minutes, less than 120 minutes, less than 100 minutes, less than 90 minutes, less than 75 minutes, less than 50 minutes, less than 40 minutes, less than 30 minutes, less than 20 minutes, or less than 10 minutes. In terms of ranges, residence times may range from 1 second to 180 minutes, for example, 10 seconds to 180 minutes, 1 minute to 180 minutes, 10 minutes to 150 minutes, 10 minutes to 100 minutes, 10 minutes to 80 minutes, 10 minutes to 50 minutes, 15 minutes to 90 minutes, or 15 minutes to 75 minutes.

[0042] In some embodiments, forming the purified acesulfame potassium composition from the intermediate acesulfame potassium composition comprises crystallizing the intermediate acesulfame potassium composition to form acesulfame potassium crystals, and filtering the crystal-containing stream to form the purified acesulfame potassium composition. In a preferred embodiment, a falling film evaporator is used to form the intermediate acesulfame potassium composition.

[0043] The crude acesulfame composition may further comprise a solvent, and in some embodiments, the concentrating operation includes a solvent removal step, e.g., stripping the solvent from the crude acesulfame potassium composition, e.g., prior to concentrating (evaporating). The method may include the steps of providing a crude acesulfame potassium composition; stripping the crude acesulfame potassium composition to form a solvent stream comprising the solvent, and a stripped acesulfame potassium composition comprising less than 50 wt%, e.g., less than 40 wt%, less than 30 wt%, less than 20 wt%, less than 15 wt%, less than 10 wt%, less than 50 wt%, less than 3 wt%, or less than 1 wt% of the solvent, followed by the concentrating and separating operations described above. It has been found that by removing the solvent, e.g., methylene dichloride, the concentration efficiency is surprisingly increased. In addition to the stripping step, the separating operation may further include an evaporation, crystallization, and / or filtration step.

[0044] In some embodiments, the separation operation includes the step of crystallizing the intermediate acesulfame potassium composition to form a crystal-containing stream comprising acesulfame potassium crystals. The crystallization may be carried out at the pH ranges and limits discussed above. The method may further include the step of forming a purified acesulfame potassium composition from the crystal-containing stream. In some embodiments, the forming step includes filtering the crystal-containing stream to form a purified acesulfame potassium composition. This embodiment may also employ a solvent stripping step as described above.

[0045]

[0044] When filtration is used in the separation operation, the filtration is preferably carried out at the temperature limits and ranges of the separation operation discussed herein. When crystallization is used in the separation operation, the crystallization can be carried out at the temperature limits and ranges discussed herein.

[0046] In addition to the temperature limits and ranges, crystallization can be performed at the pH limits and ranges discussed herein. For example, crystallization can be performed at a pH below 10.0, such as below 9.5, below 9.0, below 8.5, below 8.0, below 7.5, below 7.0, or below 6.5. In addition to the benefit of reducing the formation of acetoacetamide, it has also been found that crystallization improves the separation of dimers that may form in side reactions. It is believed that lower pH levels promote the precipitation of the dimer. It has been found that higher pH levels promote the solubility of the dimer. Precipitation advantageously provides for its more efficient separation.

[0047] In addition to the temperature limits and ranges, crystallization can be carried out at the residence time limits and ranges discussed herein. In one embodiment, providing the crude acesulfame potassium composition (which is then concentrated and separated) includes reacting a sulfamic acid with an amine to form an amidosulfamate salt, and reacting the amidosulfamate salt with an acetoacetylating agent to form an acetoacetamide salt. The acetoacetamide salt can then be reacted with a cyclizing agent, optionally in the presence of a solvent, to form a cyclic (sulfur trioxide) adduct composition. In a preferred embodiment, providing the crude acesulfame potassium composition further includes hydrolyzing the cyclic sulfur trioxide adduct to form acesulfame-H, and neutralizing the acesulfame-H to form the crude acesulfame potassium composition. In some embodiments, the neutralizing step includes reacting acesulfame-H (optionally in the acesulfame-H composition) with a neutralizing agent to form the acesulfame potassium composition. This reaction can include reacting acesulfame-H with the neutralizing agent. The acesulfame potassium composition comprises acesulfame potassium and impurities. The formation of a cyclic sulfur trioxide adduct can produce a cyclic sulfur trioxide adduct composition comprising the cyclic sulfur trioxide adduct and further reaction by-products and impurities. Similarly, the formation of acesulfame-H can produce an acesulfame-H composition comprising acesulfame-H and further reaction by-products and impurities.

[0048] The specific methods used to provide the desired temperature and / or residence time characteristics can vary widely. With respect to temperature, heat exchange devices, such as cooling devices, can be used. Temperature maintenance methods are well known in the art.

[0049] With respect to residence times, appropriate valves, gauges, metering devices, and piping may be used to control each of the separate streams to maintain the residence times discussed herein.

[0050] The acesulfame potassium compositions formed by one or more of the processes described herein will be high purity acesulfame potassium compositions, for example, the acesulfame potassium compositions may contain the amounts of acetoacetamide salts discussed above.

[0050] Acesulfame potassium composition :

[0051] The crude acesulfame potassium composition is formed by hydrolyzing a cyclic sulfur trioxide adduct to form an acesulfame-H composition, as discussed herein, and neutralizing the acesulfame-H in the acesulfame-H composition to form a crude acesulfame potassium composition. The product of the neutralization step is phase separated into an aqueous phase and an organic phase. The crude acesulfame potassium composition can be obtained (without further purification) from the aqueous phase. The crude acesulfame potassium composition comprises acesulfame potassium and acetoacetamide, e.g., less than 2800 wppm, e.g., less than 2700 wppm, less than 2600 wppm, less than 2500 wppm, less than 2400 wppm, less than 2000 wppm, less than 1500 wppm, less than 1000 wppm, less than 500 wppm, or less than 100 wppm of acetoacetamide. In some cases, the crude acesulfame potassium composition is substantially free (undetectable) of acetoacetamide, e.g., free of acetoacetamide. In terms of ranges, the crude acesulfame potassium composition can contain from 1 wppm to 2800 wppm, e.g., from 1 wppm to 2700 wppm, from 10 wppm to 2700 wppm, from 20 wppm to 2500 wppm, from 100 wppm to 2500 wppm, from 500 wppm to 2500 wppm, from 1500 to 2400 wppm, from 500 wppm to 2375 wppm, from 600 wppm to 2000 wppm, from 900 to 1900 wppm, from 300 wppm to 1500 wppm, from 400 wppm to 1400 wppm, from 600 wppm to 1200 wppm, or from 700 wppm to 1100 wppm of acetoacetamide.

[0051]

[0052] The crude acesulfame potassium composition may further include acetoacetamide-N-sulfonic acid, which may be present in the amounts discussed above with respect to acetoacetamide.

[0053] A purified acesulfame potassium composition, typically suitable for end-user use, is formed by treating the crude acesulfame potassium composition to remove impurities as discussed herein. The purified acesulfame potassium composition preferably comprises a mixture of acesulfame potassium and less than 33 wppm, e.g., less than 32 wppm, less than 30 wppm, less than 25 wppm, less than 20 wppm, less than 15 wppm, less than 12 wppm, less than 10 wppm, less than 7 wppm, less than 5 wppm, less than 3 wppm, less than 1 wppm, less than 0.8 wppm, less than 0.5 wppm, or less than 0.3 wppm of acetoacetamide. In some cases, the purified acesulfame potassium composition is substantially free of acetoacetamide, e.g., free of acetoacetamide. In terms of ranges, the purified acesulfame potassium composition can contain from 1 wppb to 33 wppm, e.g., from 10 wppb to 32 wppm, from 10 wppb to 25 wppm, from 10 wppb to 15 wppm, from 10 wppb to 12 wppm, from 10 wppb to 10 wppm, from 10 wppb to 7 wppm, from 10 wppb to 5 wppm, from 10 wppb to 3 wppm, from 100 wppb to 15 wppm, from 100 wppb to 10 wppm, or from 100 wppb to 5 wppm of acetoacetamide.

[0052]

[0054] The purified acesulfame potassium composition preferably comprises acesulfame potassium and less than 33 wppm, e.g., less than 32 wppm, less than 30 wppm, less than 25 wppm, less than 20 wppm, less than 15 wppm, less than 12 wppm, less than 10 wppm, less than 7 wppm, less than 5 wppm, less than 3 wppm, less than 1 wppm, less than 0.8 wppm, less than 0.5 wppm, or less than 0.3 wppm of acetoacetamide-N-sulfonic acid. In some cases, the purified acesulfame potassium composition is substantially free of acetoacetamide-N-sulfonic acid, e.g., free of acetoacetamide-N-sulfonic acid. In terms of ranges, the purified acesulfame potassium composition can contain from 1 wppb to 33 wppm, e.g., from 10 wppb to 32 wppm, from 10 wppb to 25 wppm, from 1 wppb to 22 wppm, from 1 wppb to 22 wppm, from 1 wppb to 20 wppm, from 10 wppb to 20 wppm, from 10 wppb to 15 wppm, from 10 wppb to 12 wppm, from 10 wppb to 10 wppm, from 10 wppb to 7 wppm, from 10 wppb to 5 wppm, from 10 wppb to 3 wppm, from 100 wppb to 15 wppm, from 100 wppb to 10 wppm, or from 100 wppb to 5 wppm of acetoacetamido-N-sulfonic acid.

[0053]

[0055] The content of acetoacetamide-N-sulfonic acid and / or acetoacetamide in the crude, intermediate, or purified acesulfame potassium composition can be measured by high performance liquid chromatography (HPLC) analysis according to the European Pharmacopoeia guidelines for thin layer chromatography (2017) (compatible with HPLC). A specific measurement method uses a Shimadzu LC Systems HPLC unit with a CBM-20 Shimadzu controller and equipped with an IonPac NS1 ((5 μm) 150×4 mm) analytical column and an IonPac NG1 guard column (35×4.0 mm). For detection (at wavelengths of 270 nm and 280 nm), a Shimadzu SPD-M20A photodiode array detector can be used. The analysis can be performed at a column temperature of 23° C. As the first eluent, an aqueous mixture of tetrabutylammonium hydrogen sulfate (3.4 g / L), acetonitrile (300 mL / L), and potassium hydroxide (0.89 g / L) can be used; as the second eluent, an aqueous mixture of tetrabutylammonium hydrogen sulfate (3.4 g / L) and potassium hydroxide (0.89 g / L) can be used. Elution can be performed in gradient mode according to the following second eluent flow profile:

[0054] · 0–3 min: constant at 80% (v / v); 3-6 min: Linear decrease to 50% (v / v); · 6–15 min: constant at 50% (v / v); 15-18 minutes: Linear decrease to 0%; 18-22 min: constant at 0%; 22–24 min: linear increase to 80% (v / v); 24~35 min: constant at 80% (v / v). The total flow rate of the eluent may be about 1.2 mL / min. Data collection and calculations may be performed using Shimadzu's LabSolution software.

[0055]

[0056] For example, during a concentration operation, one or more intermediate acesulfame potassium compositions can be formed, for example, by evaporation. The intermediate acesulfame potassium compositions preferably include a mixture of acesulfame potassium and less than 33 wppm, e.g., less than 30 wppm, less than 25 wppm, less than 20 wppm, less than 15 wppm, less than 12 wppm, less than 10 wppm, less than 7 wppm, less than 5 wppm, less than 3 wppm, less than 1 wppm, less than 0.8 wppm, less than 0.5 wppm, or less than 0.3 wppm of acetoacetamide. In some cases, the intermediate acesulfame potassium compositions are free of acetoacetamide, e.g., substantially free of (undetectable) acetoacetamide. In terms of ranges, the intermediate acesulfame potassium composition may comprise from 1 wppb to 33 wppm, e.g., from 10 wppb to 30 wppm, from 10 wppb to 25 wppm, from 10 wppb to 15 wppm, from 10 wppb to 12 wppm, from 10 wppb to 10 wppm, from 10 wppb to 7 wppm, from 10 wppb to 5 wppm, from 10 wppb to 3 wppm, from 100 wppb to 15 wppm, from 100 wppb to 10 wppm, or from 100 wppb to 5 wppm of acetoacetamide. The intermediate acesulfame potassium composition may comprise a mixture of acesulfame potassium and acetoacetamide.

[0056]

[0057] As noted above, a crude acesulfame potassium composition is formed by the reactions, hydrolysis, and neutralization described above. As discussed herein, the crude acesulfame potassium composition is concentrated to form an intermediate acesulfame potassium composition which is then separated to form a purified acesulfame potassium composition. In a preferred embodiment, the temperature at which the concentration operation, e.g., evaporation, is carried out is below 90°C, e.g., below 88°C, below 85°C, below 83°C, below 80°C, below 78°C, below 75°C, below 73°C, below 70°C, below 65°C, below 55°C, below 50°C, or below 46°C (optionally between 0°C and 90°C, e.g., between 25°C and 90°C, between 55°C and 90°C, between 10°C and 8 ... 5°C, 75°C to 88°C, 80°C to 88°C, 15°C to 85°C, 75°C to 85°C, 20°C to 83°C, 20°C to 80°C, 22°C to 78°C, 25°C to 75°C, 25°C to 73°C, 15°C to 50°C, 25°C to 65°C, 22°C to 50°C, 20°C to 55°C, 25°C to 70°C, or 30°C to 60°C); the concentration operation is performed for less than 180 minutes, for example, less than 170 minutes, less than 150 minutes, less than 120 minutes, less than 100 minutes, less than 90 minutes, 70 minutes, or less than 150 minutes. residence times of less than 5 minutes, less than 50 minutes, less than 40 minutes, less than 30 minutes, less than 20 minutes, or less than 10 minutes are used (optionally residence times in the range of 1 second to 180 minutes, e.g., 10 seconds to 180 minutes, 1 minute to 180 minutes, 10 minutes to 150 minutes, 1 minute to 50 minutes, 1 minute to 30 minutes, 10 minutes to 100 minutes, 10 minutes to 80 minutes, 10 minutes to 50 minutes, 15 minutes to 90 minutes, or 15 minutes to 75 minutes are used); °C, for example, below 30°C, below 25°C, below 20°C, below 15°C, below 10°C, below 8°C, below 6°C, below 5°C, or below 0°C (possibly at a temperature in the range of -25°C to 35°C, for example, -10°C to 35°C, 0°C to 35°C, 5°C to 30°C, -10°C to 30°C, -10°C to 25°C, -10°C to 20°C, -10°C to 15°C, 0°C to 25°C, or -10°C to 30°C);The separation procedure uses a residence time of less than 180 minutes, e.g., less than 170 minutes, less than 150 minutes, less than 120 minutes, less than 100 minutes, less than 90 minutes, less than 75 minutes, less than 50 minutes, less than 40 minutes, less than 30 minutes, less than 20 minutes, or less than 10 minutes (in some cases, 1 second to 180 minutes, e.g., 10 seconds to 180 minutes, 1 minute to 180 minutes, 10 minutes to 150 minutes, 10 minutes to 100 minutes, 1 minute to ... a residence time ranging from 10 minutes to 80 minutes, 10 minutes to 50 minutes, 15 minutes to 90 minutes, or 15 minutes to 75 minutes is used); the crude acesulfame potassium composition has less than 2800 wppm, e.g., less than 2700 wppm, less than 2600 wppm, less than 2500 wppm, less than 2400 wppm, less than 2000 wppm, less than 1500 wppm, less than 1000 wppm, less than 500 wppm or less than 100 wppm acetoacetamide (in some cases, 1 wppm to 2800 wppm, e.g., 1 wppm to 2800 wppm, 10 wppm to 2700 wppm, 20 wppm to 2500 wppm, 100 wppm to 2500 wppm, 500 wppm to 2500 wppm, 1500 to 2400 wppm, 500 wppm to 2375 wppm pm, 600 wppm to 2000 wppm, 900 to 1900 wppm, 300 wppm to 1500 wppm, 400 wppm to 1400 wppm, 600 wppm to 1200 wppm, or 700 wppm to 1100 wppm of acetoacetamide) (the crude acesulfame potassium composition may contain the same amount of acetoacetamide-N-sulfonic acid);The intermediate acesulfame potassium composition may contain less than 33 wppm, e.g., less than 32 wppm, less than 30 wppm, less than 25 wppm, less than 20 wppm, less than 15 wppm, less than 12 wppm, less than 10 wppm, less than 7 wppm, less than 5 wppm, less than 3 wppm, less than 1 wppm, less than 0.8 wppm, less than 0.5 wppm, or less than 0.3 wppm acetoacetamide (in some cases, from 1 wppb to 33 wppm, e.g., from 10 wppb to 32 wppb). pm, 10wppb to 25wppm, 10wppb to 15wppm, 10wppb to 12wppm, 10wppb to 10wppm, 10wppb to 7wppm, 10wppb to 5wppm, 10wppb to 3wppm, 100wppb to 15wppm, 100wppb to 10wppm, or 100wppb to 5wppm of acetoacetamide) (the intermediate acesulfame potassium composition may contain the same amount of acetoacetamide-N-sulfonic acid); The purified acesulfame potassium composition may contain less than 33 wppm, e.g., less than 32 wppm, less than 30 wppm, less than 25 wppm, less than 20 wppm, less than 15 wppm, less than 12 wppm, less than 10 wppm, less than 7 wppm, less than 5 wppm, less than 3 wppm, less than 1 wppm, less than 0.8 wppm, less than 0.5 wppm, or less than 0.3 wppm acetoacetamide (in some cases, between 1 wppb and 33 wppm, e.g., between 10 wppb and 32 wppb). pm, 10wppb to 25wppm, 10wppb to 15wppm, 10wppb to 12wppm, 10wppb to 10wppm, 10wppb to 7wppm, 10wppb to 5wppm, 10wppb to 3wppm, 100wppb to 15wppm, 100wppb to 10wppm, 100wppb to 5wppm of acetoacetamide) (the purified acesulfame potassium composition may contain the same amount of acetoacetamide-N-sulfonic acid);

[0057]

[0058] In certain embodiments, the concentration operation, e.g., evaporation, is carried out at a temperature below 85° C., the intermediate acesulfame potassium composition contains from 1 wppb to 33 wppm acetoacetamide (and optionally less than 33 wppm acetoacetamide-N-sulfonic acid) and the purified acesulfame potassium composition contains less than 33 wppm acetoacetamide (and optionally less than 33 wppm acetoacetamide-N-sulfonic acid).

[0058]

[0059] In other particular embodiments, the concentration operation, e.g., evaporation, is conducted at a temperature below 60° C., the evaporator residence time is less than 50 minutes, the intermediate acesulfame potassium composition contains from 10 wppb to 25 wppm acetoacetamide (and optionally less than 30 wppm acetoacetamide-N-sulfonic acid), and the purified acesulfame potassium composition contains from 10 wppb to 15 wppm acetoacetamide (and optionally less than 30 wppm acetoacetamide-N-sulfonic acid).

[0059]

[0060] In other particular embodiments, the concentration operation, e.g., evaporation, is conducted at a temperature below 46° C., the evaporator residence time is less than 30 minutes, and the crystallization is conducted at a temperature below 35° C., the intermediate acesulfame potassium composition contains from 10 wppb to 12 wppm acetoacetamide (and optionally less than 20 wppm acetoacetamide-N-sulfonic acid) and the purified acesulfame potassium composition contains from 10 wppb to 7 wppm acetoacetamide.

[0060]

[0061] In another particular embodiment, the concentration operation, e.g., evaporation, is carried out at a temperature in the range of 25° C. to 90° C., the evaporator residence time is in the range of 10 seconds to 180 minutes, the separation operation, e.g., crystallization and filtration, is carried out at a temperature in the range of −10° C. to 35° C., the separation operation residence time is in the range of 10 seconds to 180 minutes, the crude acesulfame potassium composition comprises 1 wppm to 2800 wppm acetoacetamide and 1 wppm to 2800 wppm acetoacetamide-N-sulfonic acid, the intermediate acesulfame potassium composition comprises 1 wppb to 33 wppm acetoacetamide and 1 wppb to 33 wppm acetoacetamide-N-sulfonic acid, and the purified acesulfame potassium composition comprises 1 wppb to 33 wppm acetoacetamide and 1 wppb to 33 wppm acetoacetamide-N-sulfonic acid.

[0061]

[0062] In another particular embodiment, the concentration operation, e.g., evaporation, is carried out at a temperature in the range of 25° C. to 90° C., the evaporator residence time is in the range of 10 seconds to 180 minutes, the separation operation, e.g., crystallization and filtration, is carried out at a temperature in the range of −10° C. to 35° C., the separation operation residence time is in the range of 10 seconds to 180 minutes, the crude acesulfame potassium composition comprises 1 wppm to 2800 wppm acetoacetamide and 1 wppm to 2800 wppm acetoacetamide-N-sulfonic acid, the intermediate acesulfame potassium composition comprises 1 wppb to 33 wppm acetoacetamide and 1 wppb to 33 wppm acetoacetamide-N-sulfonic acid, and the purified acesulfame potassium composition comprises 1 wppb to 33 wppm acetoacetamide and 1 wppb to 33 wppm acetoacetamide-N-sulfonic acid.

[0062]

[0063] In another particular embodiment, the concentration operation, e.g., evaporation, is carried out at a temperature in the range of 20° C. to 55° C., the evaporator residence time is in the range of 1 minute to 300 minutes, the separation operation, e.g., crystallization and filtration, is carried out at a temperature in the range of −10° C. to 15° C., the separation operation residence time is in the range of 1 minute to 180 minutes, the crude acesulfame potassium composition comprises 500 wppm to 2375 wppm acetoacetamide, the intermediate acesulfame potassium composition comprises 10 wppb to 20 wppm acetoacetamide and 10 wppb to 20 wppm acetoacetamide-N-sulfonic acid, and the purified acesulfame potassium composition comprises 10 wppb to 10 wppm acetoacetamide and 1 wppb to 20 wppm acetoacetamide-N-sulfonic acid.

[0063]

[0064] The acesulfame potassium compositions (crude and / or purified compositions) may in some cases contain organic impurities. The organic impurities may include, among others, haloacesulfame potassium. The acesulfame potassium compositions (crude and / or purified compositions) may also contain heavy metals. The organic impurities and / or heavy metals may be present in an amount ranging from 1 wppb to 25 wppm, e.g., 100 wppb to 20 wppm, 100 wppb to 15 wppm, 500 wppb to 10 wppm, or 1 wppm to 5 wppm, based on the total weight of the respective acesulfame potassium composition (crude or purified composition). Heavy metals tend to be present in relatively high densities, e.g., 3 g / cm. 3 Higher or 7g / cm 3Heavy metals are defined as metals having a higher density than lead. Exemplary heavy metals include lead and mercury. In some cases, the crude or refined acesulfame potassium composition may contain mercury in an amount ranging from 1 wppb to 25 wppm, e.g., 100 wppb to 20 wppm, 100 wppb to 15 wppm, 500 wppb to 10 wppm, or 1 wppm to 5 wppm. In terms of limits, the crude or refined acesulfame potassium composition may contain less than 25 wppm, e.g., less than 20 wppm, less than 15 wppm, less than 10 wppm, or less than 5 wppm of mercury. In some cases, the crude or refined acesulfame potassium composition may contain lead in an amount ranging from 1 wppb to 25 wppm, e.g., 100 wppb to 20 wppm, 100 wppb to 15 wppm, 500 wppb to 10 wppm, or 1 wppm to 5 wppm. In terms of limits, a crude or purified acesulfame potassium composition may contain less than 25 wppm lead, e.g., less than 20 wppm, less than 15 wppm, less than 10 wppm, or less than 5 wppm. In some cases, when potassium hydroxide is formed by a membrane process, the resulting crude or purified acesulfame potassium composition may have very low levels of mercury, if any, e.g., less than 10 wppm, less than 5 wppm, less than 3 wppm, less than 1 wppm, less than 500 wppb, or less than 100 wppb.

[0064] Intermediate reaction parameters :

[0065] The reaction for producing high purity acesulfame potassium is described in more detail below.

[0065] Amidosulfamate formation reaction :

[0066] In the first reaction step, sulfamic acid is reacted with an amine to form a sulfamate. A representative reaction scheme for producing triethylammonium sulfamate using triethylamine as the amine is shown in reaction (1) below.

[0066] [ka]

[0067] Also present in the first reaction mixture is acetic acid, which reacts with an amine, such as triethylamine, to form triethylammonium acetate, as shown in reaction (2) below.

[0068] [ka]

[0069] The amines used in these reactions may vary widely. Preferably, the amine comprises triethylamine. In one embodiment, the amine is selected from the group consisting of trimethylamine, diethylpropylamine, tri-n-propylamine, triisopropylamine, ethyldiisopropylamine, tri-n-butylamine, triisobutylamine, tricyclohexylamine, ethyldicyclohexylamine, N,N-dimethylaniline, N,N-diethylaniline, benzyldimethylamine, pyridine, substituted pyridines such as picoline, lutidine, collidine, or methylethylpyridine, N-methylpiperidine, N-ethylpiperidine, N-methylmorpholine, N,N-dimethylpiperazine, 1,5-diazabicyclo[4.3.0]-non-5-ene, 1,8-diaza The amine may be selected from the group consisting of bicyclo[5.4.0]-undec-7-ene, 1,4-diazabicyclooctane, tetramethylhexamethylenediamine, tetramethylethylenediamine, tetramethylpropylenediamine, tetramethylbutylenediamine, 1,2-dimorpholylethane, pentamethyldiethyltriamine, pentaethyldiethylenetriamine, pentamethyldipropylenetriamine, tetramethyldiaminomethane, tetrapropyldiaminomethane, hexamethyltriethylenetetramine, hexamethyltripropylenetetramine, diisobutylenetriamine, triisopropylenetriamine, and mixtures thereof.

[0070] Acetoacetamide salt formation reaction : Once formed in reaction (1), the sulfamate salt is reacted with an acetoacetylating agent to form an acetoacetamide salt, preferably an acetoacetamide-N-sulfonate triethylammonium salt. Preferably, the acetoacetylating agent comprises diketene, although other acetoacetylating agents can be used with or without diketene.

[0071] In one embodiment, the resulting acetoacetamide salt corresponds to formula (3):

[0072] [ka]

[0073]

[0071] In the formula, M + is a suitable ion. Preferably, M + is an alkali metal ion or N + R 1 R 2 R 3 R 4 R 1 , R 2 , R 3 , and R 4 are each independently an organic group or hydrogen, preferably H, or C 1 ~C 8 Alkyl, C 6 ~C 10 It may be cycloalkyl, aryl, and / or aralkyl. In a preferred embodiment, R 1 is hydrogen, and R 2 , R 3 , and R 4 is alkyl, for example ethyl.

[0074] A representative reaction scheme for forming an acetoacetamide salt uses trialkylammonium amidosulfamate and diketene as reactants to produce the acetoacetamide triethylammonium salt as shown in reaction (4) below.

[0075] [ka]

[0076] In one embodiment, the reaction is carried out in the presence of a catalyst, which may vary widely. In some embodiments, the catalyst comprises one or more amines and / or phosphines. Preferably, the catalyst comprises triethylamine. In some cases, trimethylamine serves as both the catalyst and the reactant.

[0077] In one embodiment in which the amidosulfamate-forming reaction and the acetoacetamide salt-forming reaction are carried out in separate reactors, the second reaction mixture includes amidosulfamate, diketene, and a catalyst, such as triethylamine. Preferably, the catalyst is carried over from the first reaction to the reaction mixture of the second reaction. The second reaction mixture is then subjected to conditions effective to form the acetoacetamide salt.

[0078] In one embodiment, the composition of the second reaction mixture may be similar to the composition of the first reaction mixture. In a preferred embodiment, the reaction product of the amidosulfamate-forming reaction provides the amidosulfamate component of the second reaction mixture. In addition to the above-mentioned components, the second reaction mixture may further include reaction by-products from the first reaction, or unreacted starting materials.

[0079] In one embodiment, the amount of acetoacetylating agent, e.g., diketene, should be at least equimolar to the reactant amidosulfamate provided. In one embodiment, the process can use an excess of diketene, but the excess is preferably less than 30 mole percent, e.g., less than 10 mole percent. Larger excesses are also contemplated.

[0080] The amidosulfamate-forming reaction and / or the acetoacetamide salt-forming reaction can use an organic solvent. Suitable inert organic solvents include any organic solvent that does not react in an undesirable manner with the starting materials, cyclization agent, final product, and / or catalyst in the reaction. The solvent preferably has the ability to at least partially dissolve the amidosulfamate. Representative organic solvents include halogenated aliphatic hydrocarbons, preferably having 4 or fewer carbon atoms, such as methylene chloride, chloroform, 1,2-dichloroethane, trichloroethylene, tetrachloroethylene, trichlorofluoroethylene; aliphatic ketones, preferably having 3 to 6 carbon atoms, such as acetone, methyl ethyl ketone; aliphatic ethers, preferably cyclic aliphatic ethers having 4 or 5 carbon atoms, such as tetrahydrofuran, dioxane; lower aliphatic carboxylic acids, preferably having 2 to 6 carbon atoms, such as acetic acid, propionic acid; aliphatic nitriles, preferably acetonitrile; N-alkyl substituted amides of carbonic acid and lower aliphatic carboxylic acids, preferably having 5 or fewer carbon atoms, such as tetramethylurea, dimethylformamide, dimethylacetamide, N-methylpyrrolidone; aliphatic sulfoxides, preferably dimethylsulfoxide, and aliphatic sulfones, preferably sulfolane.

[0081] Particularly preferred solvents include dichloromethane (methylene chloride), 1,2-dichloroethane, acetone, glacial acetic acid, and dimethylformamide, with dichloromethane (methylene chloride) being particularly preferred. The solvents may be used either alone or in mixtures. In one embodiment, the solvent is a halogenated aliphatic hydrocarbon solvent, preferably the solvent is dichloromethane. Chloroform and tetrachloromethane are also representative solvents.

[0082] In one embodiment, the acetoacetamide salt forming reaction is carried out at a temperature ranging from -30°C to 50°C, for example, from 0°C to 25°C. The reaction pressure can vary widely. In a preferred embodiment, the reaction is carried out at atmospheric pressure, although other pressures are contemplated. The reaction time can vary widely, preferably from 0.5 hours to 12 hours, for example, from 1 hour to 10 hours. In one embodiment, the reaction is carried out by introducing the amidosulfamate and metering in the diketene. In another embodiment, the reaction is carried out by introducing the diketene and metering in the amidosulfamate. The reaction can be carried out by introducing the diketene and amidosulfamic acid and metering in the catalyst.

[0083] Once formed, each reaction product is optionally subjected to one or more purification steps. For example, the solvent can be separated from the reaction product, for example by distillation, and the residue (mainly acetoacetamide-N-sulfonate) can be recrystallized from a suitable solvent, such as, for example, acetone, methyl acetate, or ethanol.

[0084] Cyclization and Hydrolysis : The acetoacetamide salt is reacted with a cyclizing agent, such as a cyclizing agent in a cyclizing agent composition, in the presence of a solvent to form a cyclic sulfur trioxide adduct, and in some cases a cyclic (sulfur trioxide) adduct composition containing impurities. In some cases, a cooling step is performed prior to the cyclic sulfur trioxide adduct forming reaction. In one embodiment, the cyclization is performed by using at least an equimolar amount of the cyclizing agent. The cyclizing agent can be dissolved in an inert inorganic or organic solvent. The cyclizing agent is generally used in molar excess, such as up to a 20-fold excess, or up to a 10-fold excess based on the total moles of the acetoacetamide salt. A representative cyclization reaction using sulfur trioxide as the cyclizing agent is shown below in reaction (5).

[0085] [ka]

[0086] In one embodiment, the weight ratio of solvent to cyclizing agent in the cyclizing agent composition is at least 1:1, such as at least 2:1, or at least 5:1. In one embodiment, the weight ratio of solvent to cyclizing agent in the cyclizing agent composition is in the range of 1:1 to 25:1, such as 1:1 to 10:1, 2:1 to 10:1, or 5:1 to 10:1.

[0087] The cyclizing agent may be any compound that will initiate ring closure of the acetoacetamide salt. Sulfur trioxide is the preferred cyclizing agent, although other cyclizing agents are contemplated. The cyclization agent can be added to the reaction mixture either in solid or liquid form, or by condensation in the vapor. Suitable inert inorganic or organic solvents are those liquids which do not react in an undesirable manner with sulfur trioxide or with the starting materials or end products of the reaction. Preferred organic solvents include, but are not limited to, halogenated aliphatic hydrocarbons, preferably having 4 or fewer carbon atoms, such as methylene chloride (dichloromethane), chloroform, 1,2-dichloroethane, trichloroethylene, tetrachloroethylene, trichlorofluoroethylene; esters of carbonic acid with lower aliphatic alcohols, preferably methanol or ethanol; nitroalkanes, preferably having 4 or fewer carbon atoms, especially nitromethane; alkyl-substituted pyridines, preferably collidine; and aliphatic sulfones, preferably sulfolane. Particularly preferred solvents for the cyclization reaction include dichloromethane (methylene chloride), 1,2-dichloroethane, acetone, glacial acetic acid, and dimethylformamide, with dichloromethane (methylene dichloride) being particularly preferred. Other solvents, such as those mentioned herein, may also be suitable as solvents. The solvents can be used either alone or in mixtures. In one embodiment, the solvent is a halogenated aliphatic hydrocarbon solvent, preferably the solvent is dichloromethane. The process can use these solvents alone or in mixtures thereof.

[0088] In some cases, the solvent in the cyclizing agent composition can be selected from (1) concentrated sulfuric acid, (2) liquid sulfur dioxide, or (3) an inert organic solvent. In a preferred embodiment, the same solvent is used in both the acetoacetamide salt-forming reaction and the cyclization reaction. One advantage is that the solution obtained in the acetoacetamide salt-forming reaction can be used immediately in the cyclization without isolating the acetoacetamide salt-forming reaction product.

[0089] In one embodiment, the reaction temperature for the cyclization reaction is in the range of −70° C. to 175° C., for example, −40° C. to 60° C. The pressure at which the reaction is carried out can vary widely. In one embodiment, the reaction is carried out at a pressure in the range of 0.01 MPa to 10 MPa, for example, 0.1 MPa to 5 MPa. Preferably, the reaction is carried out at atmospheric pressure.

[0090] The acetoacetamide salt can be introduced into the cyclization reactor, and a cooled cyclization agent composition, for example a solution of the cyclization agent, optionally in a solvent, can be metered into the reactor. In a preferred embodiment, both reactants (acetoacetamide salt and cyclization agent) are fed simultaneously into the reactor. In one embodiment, the cooled cyclization agent composition is first introduced into the reactor and the acetoacetamide salt is added. Preferably, at least a portion of the cyclization agent composition is introduced into the reactor, and then the acetoacetamide salt and (further) cyclization agent are metered in, either continuously or in portions, preferably while maintaining the temperature as described above.

[0091] The acetoacetamide salt can be introduced into the reactor and the cyclizing agent composition can be metered into the reactor. In a preferred embodiment, both reactants are fed into the reactor simultaneously. In one embodiment, the cyclizing agent composition is first introduced into the reactor and the acetoacetamide salt is added. Preferably, at least a portion of the cyclizing agent composition is introduced into the reactor and then the acetoacetamide salt and (further) cyclizing agent are metered in, either continuously or in portions, preferably while maintaining the temperature as described above.

[0092]

[0090] Forming the crude acesulfame potassium composition from the cyclic sulfur trioxide adduct composition, in some embodiments, includes the steps of hydrolyzing the cyclic sulfur trioxide adduct to form an acesulfame-H composition; neutralizing the acesulfame-H in the acesulfame-H composition to form a crude acesulfame potassium composition; and forming the acesulfame potassium composition from the crude acesulfame potassium composition.

[0093] The cyclic sulfur trioxide adduct can be hydrolyzed by conventional means, for example with water, and the forming process can include the step of hydrolyzing the cyclic sulfur trioxide adduct to form the acesulfame-H composition. Acesulfame-H is referred to as a sweetening acid.

[0094] A representative hydrolysis reaction scheme is shown in reaction (6) below.

[0095] [ka]

[0096]

[0093] Addition of water induces phase separation. The majority of the sweetener acid acesulfame-H (6-methyl-3,4-dihydro-1,2,3-oxathiazin-4-one 2,2-dioxide) formed by hydrolysis, e.g. at least 60% by weight, at least 70%, at least 80%, or at least 90%, is present in the organic phase. The remainder of the sweetener acid is present in the aqueous phase, which can be extracted and optionally added to the sweetener acid in the organic phase. When dichloromethane is used as the reaction medium, e.g. a molar excess of water or ice based on sulfur trioxide can be added to the cyclic sulfur trioxide adduct / sulfur trioxide solution.

[0097] In some cases, the hydrolysis step includes adding water to the cyclic sulfur trioxide adduct. In preferred embodiments, the weight ratio of water to acetoacetamide salt is greater than 1.3:1, e.g., greater than 1.5:1, greater than 1.7:1, greater than 2:1, or greater than 2.2:1. Use of these ratios can result in reduced formation of acetoacetamide-N-sulfonic acid and / or acetoacetamide in the neutralized crude acesulfame potassium composition, e.g., the crude acesulfame potassium composition can include the amounts of acetoacetamide-N-sulfonic acid discussed herein.

[0098] Surprisingly, the temperature at which water is initially fed to the hydrolysis reaction, as well as reaction parameters such as temperature, do not significantly affect the formation of impurities, such as the formation of organics, or the formation of 5-chloro-acesulfur. It has been found that at lower temperatures, such as temperatures below about -35°C or below -22°C, ice tends to accumulate in the reaction mixture. As the ice melts, further reaction is triggered to begin and the temperature rises rapidly. This increase in temperature surprisingly resulted in a product with much higher levels of impurities. In some cases, the hydrolysis includes adding hydrolysis water to the cyclic sulfur trioxide adduct to form a hydrolysis reaction mixture and reacting the mixture to form the acesulfame-H composition. In some embodiments, the temperature of the hydrolysis reaction mixture, or the temperature at which the hydrolysis water is fed to the reactor, is maintained at greater than -35°C, e.g., greater than -30°C, greater than -25°C, greater than -24°C, greater than -23°C, greater than -22°C, greater than -21.5°C, greater than -21°C, or greater than -20°C. In terms of ranges, the temperature of the hydrolysis reaction mixture, or the temperature at which the hydrolysis water is fed to the reactor, is optionally maintained at a temperature in the range of −35° C. to 0° C., e.g., −30° C. to −5° C., −20° C. to −5° C., −30° C. to −20° C., −25° C. to −21° C., or −25° C. to −21.5° C.

[0099] After the addition of water, the reaction solvent, e.g. dichloromethane, can be removed by distillation or the acesulfame-H remaining in the organic phase can be extracted with a more suitable solvent. Suitable solvents are those which are sufficiently stable to sulfuric acid and have a satisfactory dissolving capacity. Other suitable solvents are esters of carbonic acid, e.g. dimethyl carbonate, diethyl carbonate, and ethylene carbonate, or esters of organic monocarboxylic acids, e.g. isopropyl formate and isobutyl formate, ethyl acetate, isopropyl acetate, butyl acetate, isobutyl acetate, and neopentyl acetate, or esters of dicarboxylic acids or amides which are not miscible with water, e.g. tetrabutylurea. Isopropyl acetate and isobutyl acetate are particularly preferred.

[0100]

[0097] It has now been found that in addition to the organic sweetener acid-dichloromethane phase and the aqueous phase, a transition phase can be formed. The transition phase can contain a large amount of impurities, such as acetoacetamide. The transition phase can contain a greater amount of such impurities than the organic phase. Advantageously, the transition phase can be removed from the organic sweetener acid-dichloromethane phase, thereby greatly reducing its impurity content. The process can employ a step of phase separating the acesulfame-H composition. The phase separation can form a sweetener acid-dichloromethane phase, an aqueous phase, and the transition phase described above, which contains at least 2% by weight, such as at least 5% by weight, at least 10% by weight, at least 20% by weight, at least 30% by weight, or at least 50% by weight of impurities. The process can include separating the transition phase from the acesulfame-H composition to form a purified acesulfame-H composition. The purified acesulfame-H composition can then be used to form a purified acesulfame potassium composition, for example, by neutralization and processing.

[0101] The organic phases are combined and then diluted with, for example, Na 2 SO 4The mixture is dried at 400° C. and evaporated. The sulfuric acid carried over in the extraction can be removed by appropriately adding an aqueous alkali solution to the organic phase. For this purpose, dilute aqueous alkali can be added to the organic phase until the pH reached in the aqueous phase corresponds to that of the pure 6-methyl-3,4-dihydro-1,2,3-oxathiazin-4-one 2,2-dioxide at the same concentration in the same two-phase system of extractant and water.

[0102] Neutralization : Neutralization of acesulfame-H produces a non-toxic salt of acesulfame-H, such as potassium acesulfame. In one embodiment, neutralization is carried out by reacting acesulfame-H with a suitable base, such as potassium hydroxide, particularly potassium hydroxide produced by the membrane process. Other suitable bases include, for example, KOH, KHCO 3 , K 2 CO 3 , and potassium alcoholate. Representative examples of neutralizing agents using potassium hydroxide include The reaction scheme is shown in reaction (7) below.

[0103] [ka]

[0104] In some cases, the neutralization is carried out or maintained at a low pH level, which may advantageously further result in the reduction or elimination of the formation of impurities, such as acetoacetamide salts. In this context, "carrying out" means starting the neutralization step at a low pH level, and "maintaining" means carrying out the step to ensure that the pH is maintained within the low pH range throughout the neutralization step. In one embodiment, the neutralization step is carried out or maintained at a pH below 10.0, such as below 9.5, below 9.0, below 8.5, below 8.0, below 7.5, below 7.0, or below 6.5. In terms of ranges, the neutralization step is preferably carried out or maintained at a pH between 6.0 and 10.0, such as between 6.5 and 9.5, between 7.0 and 9.0, or between 7.5 and 8.5.

[0105]

[0101] In some cases, the pH during the neutralization step can be maintained within a desired range by manipulating the components of the neutralization reaction mixture, including acesulfame-H and the neutralizing agent (and even the solvent). For example, the composition of the neutralization reaction mixture can include 1% to 95% by weight, e.g., 10% to 85% by weight, or 25% to 75% by weight, of the neutralizing agent; and 1% to 95% by weight, e.g., 10% to 85% by weight, or 25% to 75% by weight, of the acesulfame-H. These concentration ranges are based on the mixture of the neutralizing agent and acesulfame-H (without the solvent).

[0106] In one embodiment, acesulfame-H can be neutralized and extracted directly from the purified organic extract phase using an aqueous potassium base solution. Acesulfame potassium is then precipitated in crystalline form, if appropriate after evaporation of the solution, which can also be recrystallized for purification.

[0107] In one embodiment, the process is not a small batch process or a laboratory scale process. For example, the method of the present invention for producing a purified acesulfame potassium composition can produce at least 50 grams per batch, e.g., at least 100 grams per batch, at least 500 grams per batch, at least 1 kilogram per batch, or at least 10 kilograms per batch of purified acesulfame potassium composition. In terms of rate, the method of the present invention can produce at least 50 grams per hour, e.g., at least 100 grams per hour, at least 500 grams per hour, at least 1 kilogram per hour, or at least 10 kilograms per hour of purified acesulfame potassium composition.

[0108] FIG. 1 shows a representative acesulfame potassium process according to the methods described herein. FIG. 1 shows process 100. Process 100 includes an amidosulfamate-forming reactor 102, and an acetoacetamide salt-forming reactor 104. Although FIG. 1 shows separate reactors for the two intermediate-forming reactions, other configurations, such as a one-reactor process, are within the contemplation of the present method. Sulfamic acid is fed to amidosulfamate-forming reactor 102 through sulfamic acid feed line 106. One or more amines, preferably triethylamine, are fed to amidosulfamate-forming reactor 102 through amine feed line 108. In addition to sulfamic acid and one or more amines, acetic acid is also fed (through feed line 110) to amidosulfamate-forming reactor 102. The resulting reaction mixture in amidosulfamate-forming reactor 102 is as discussed above. In amidosulfamate-forming reactor 102, sulfamic acid and an amine are reacted (in the presence of acetic acid) to produce a crude amidosulfamate composition that exits reactor 102 via line 112. Although not shown, a reaction solvent, such as dichloromethane, may also be present in amidosulfamate-forming reactor 102.

[0109] The crude amidosulfamate composition in line 112 is sent to the acetoacetamide salt-forming reactor 104. Diketene is fed to the acetoacetamide salt-forming reactor 104 through feed line 114. In the acetoacetamide salt-forming reactor 104, the amidosulfamate and diketene react to produce a crude acetoacetamide salt composition which exits the reactor 104 through line 118. Although not shown, dichloromethane can also be present in the acetoacetamide salt-forming reactor 104.

[0110]

[0106] Through supply lines 121 and 123, a cyclizing agent (sulfur dioxide) and a solvent (dichloromethane) are fed to vessel 119. Vessel 119 is preferably the vessel in which a cyclizing agent composition comprising these two components is formed. Through line 125, the cyclizing agent composition comprising both the cyclizing agent and the solvent is discharged from vessel 119.

[0111]

[0107] The crude acetoacetamide salt composition is fed via line 118 to cyclization reactor 120. A cyclization agent composition is also fed (via line 125) to cyclization reactor 120. Line 125 is preferably formed of materials and sized and shaped to facilitate the residence times discussed herein. Within cyclization reactor 120, the acetoacetamide salts in the crude acetoacetamide salt composition in line 118 are cyclized to discharge a cyclic sulfur trioxide adduct stream via line 124.

[0112]

[0108] The cyclic sulfur trioxide adduct in line 124 is fed to hydrolysis reactor 126. Water is fed to hydrolysis reactor 126 through water feed line 128. In hydrolysis reactor 126, the cyclic sulfur trioxide adduct is hydrolyzed to produce a crude acesulfame-H composition which is discharged from hydrolysis reactor 126 through line 130 and fed to phase separation unit 132. Phase separation unit 132 separates the contents of line 130 into an organic phase 134 and an aqueous phase 136. Organic phase 134 contains a major amount of the acesulfame-H in line 130 and a solvent, such as methylene chloride. Aqueous phase 136 is discharged through line 137 and contains triethylammonium sulfate, and optionally sulfuric acid and small amounts of acesulfame-H. The aqueous phase can be further purified to separate and / or recover acesulfame-H and / or triethylammonium sulfate. The recovered acesulfame-H can be combined with the acesulfame from the organic phase (not shown).

[0113]

[0109] The organic phase 134 is discharged from the phase separation unit 132 and sent (through line 140) to an extraction column 138. Water is supplied to the extraction column 138 through a water supply line 142. The water extracts residual sulfate from the contents of line 140 and a purified acesulfame-H composition is discharged from the extraction column 138 through line 144. The extracted The sulfate leaves extraction column 138 via line 145.

[0114]

[0110] The purified acesulfame-H composition in line 144 is sent to neutralization unit 146, which is also provided with potassium hydroxide (through line 148). The addition of potassium hydroxide to neutralization unit 146 (through line 148) can be adjusted to achieve and / or maintain a desired pH level during the neutralization discussed herein. The potassium hydroxide neutralizes the acesulfame-H in the purified acesulfame-H composition to produce a product comprising acesulfame potassium, dichloromethane, water, potassium hydroxide, and impurities such as acetoacetamide, which is discharged from neutralization unit 146 through line 150. This product can be considered a crude acesulfame potassium composition.

[0115]

[0111] The crude acesulfame potassium product stream in line 150 may be sent to a processing section 156 to recover purified acesulfame potassium (shown exiting stream 152). In addition to the purified acesulfame potassium, dichloromethane and potassium hydroxide may be separated from the crude acesulfame potassium product stream, as shown by stream 154. The contents of stream 154 may be recovered and / or recycled to the process. Processing section 156 may include one or more of the processing steps described herein, such as stripping, evaporation, crystallization, and filtration.

[0116]

[0112] The product in line 150 is sent to a phase separation unit 160. Phase separation unit 160 separates the product in line 150 into an organic phase 162 and an aqueous phase 164. The aqueous phase 164 contains the majority of the acesulfame potassium in line 150 and some impurities. The organic phase 162 contains potassium hydroxide, dichloromethane, and water, and can be further processed to recover these components. The aqueous phase 164 (without further processing) can be considered a crude acesulfame potassium composition. The aqueous phase 164 can optionally be processed to form a purified acesulfame potassium composition.

[0117]

[0113] Aqueous phase 164 is sent via line 166 to processing unit 156. Within processing unit 156, aqueous phase 164 is processed to obtain a purified acesulfame potassium composition (a product that can be sold), shown as being discharged via stream 152. In addition to the purified acesulfame potassium composition, dichloromethane and potassium hydroxide can be separated. These components exit processing unit 156 via line 154. The contents of stream 154 can be recovered and / or recycled to the process.

[0118]

[0114] Figure 2 shows a representative processing section. Crude acesulfame potassium product stream 250 is fed to processing section 256. In particular, crude acesulfame potassium product stream 250 is fed to stripper 252 for stripping the solvent therefrom. The solvent in stream 254 is discharged from stripper 252 and sent for further processing, such as reuse or recycle. Stripped acesulfame potassium stream 257, containing a small amount of solvent, is discharged from stripper 252 and sent to evaporator 258. It has been discovered that removing the solvent prior to evaporation unexpectedly provides the benefits of improved evaporation operation.

[0119]

[0115] Water is removed from the stripped acesulfame potassium stream in line 257 by evaporator 258 to form a water stream 260 and an intermediate acesulfame potassium composition stream 262. Evaporator 258 is preferably a falling film evaporator. Intermediate acesulfame potassium composition stream 262 is sent to crystallizer 264 to produce crystal-containing stream 266 and recycle stream 268. Crystal-containing stream 266 is then sent to filtration unit 270 to filter impurities to produce purified acesulfame potassium composition stream 272 and impurities stream 274. The processing units may be beneficially operated with the separation parameters discussed herein.

[0120]

[0116] The present invention also relates to the following aspects. Form 1: A method for producing a purified acesulfame potassium composition, comprising the steps of: (a) providing a crude acesulfame potassium composition comprising acesulfame potassium, acetoacetamide, and water; (b) concentrating the crude acesulfame potassium composition to form a water stream and an intermediate acesulfame potassium composition comprising acesulfame potassium and less than 33 wppm acetoacetamide; (c) separating the intermediate acesulfame potassium composition to form a purified acesulfame potassium composition comprising acesulfame potassium and less than 33 wppm acetoacetamide; Includes; The above process, wherein said concentrating step (b) is carried out at a temperature below 90°C and said separating step (c) is carried out at a temperature below 35°C.

[0121]

[0118] Mode 2: The preparing step (a) reacting a sulfamic acid with an amine to form an amidosulfamate; reacting said amidosulfamate salt with an acetoacetylating agent to form an acetoacetamide salt; reacting the acetoacetamide salt with a cyclizing agent in a cyclizing agent composition to form a cyclic sulfur trioxide adduct; hydrolyzing the cyclic sulfur trioxide adduct to form an acesulfame-H composition comprising acesulfame-H; and neutralizing the acesulfame-H in the acesulfame-H composition to form a crude acesulfame potassium composition; 2. The method of claim 1, comprising:

[0122]

[0119] Form 3: The method of any of the previous forms, wherein said intermediate acesulfame potassium composition comprises less than 33 wppm acetoacetamido-N-sulfonic acid.

[0120] Form 4: The method of any of the preceding forms, wherein concentrating comprises evaporating the crude acesulfame potassium composition to form a water stream and an intermediate acesulfame potassium composition comprising acesulfame potassium and less than 75% by weight water.

[0123]

[0121] Form 5: The process of any of the preceding forms, wherein the evaporation residence time is less than 180 minutes.

[0122] Form 6: The method of any of the preceding forms, wherein said intermediate acesulfame potassium composition comprises less than 33 wppm acetoacetamido-N-sulfonic acid.

[0124]

[0123] Form 7: The separation is crystallizing the intermediate acesulfame potassium composition to form acesulfame potassium crystals; and filtering the acesulfame potassium crystals to form a purified acesulfame potassium composition; The method of any of the preceding aspects, comprising:

[0125]

[0124] Form 8: The method of any of the preceding forms, wherein the filtration is carried out at a temperature of 35°C or less.

[0125] Form 9: The process of any of the preceding forms, wherein said crystallization is carried out at a temperature of 35°C or less.

[0126] Form 10: The process of any of the previous forms, wherein said crystallization is performed at a pH below 10.

[0126]

[0127] Form 11: The evaporation is carried out at a temperature lower than 85° C., and the intermediate acesulfame potassium The method of any of the preceding forms, wherein the purified acesulfame potassium composition contains between 1 wppb and 33 wppm acetoacetamide and the purified acesulfame potassium composition contains less than 33 wppm acetoacetamide.

[0127]

[0128] Form 12: The method of any of the previous forms, wherein said intermediate acesulfame potassium composition further comprises less than 33 wppm of acetoacetamido-N-sulfonic acid.

[0129] Form 13: The process of any of the preceding forms, wherein said evaporating is conducted at a temperature below 60° C., said evaporator residence time is less than 50 minutes, said intermediate acesulfame potassium composition comprises from 10 wppb to 25 wppm acetoacetamide, and said purified acesulfame potassium composition comprises from 10 wppb to 15 wppm acetoacetamide.

[0128]

[0130] Form 14: The method of any of the previous forms, wherein said intermediate acesulfame potassium composition comprises less than 30 wppm of acetoacetamido-N-sulfonic acid.

[0131] Form 15: The process of any of the preceding forms, wherein said evaporation is conducted at a temperature in the range of 20° C. to 55° C.; said evaporator residence time is in the range of 1 minute to 300 minutes; said separation is conducted at a temperature in the range of −10° C. to 15° C.; said separation operation residence time is in the range of 1 minute to 180 minutes; said crude acesulfame potassium composition comprises 500 wppm to 2375 wppm acetoacetamide; said intermediate acesulfame potassium composition comprises 10 wppb to 20 wppm acetoacetamide and 10 wppb to 20 wppm acetoacetamide-N-sulfonic acid, and said purified acesulfame potassium composition comprises 10 wppb to 10 wppm acetoacetamide and 1 wppb to 20 wppm acetoacetamide-N-sulfonic acid.

[0129]

[0132] Form 16: (i) the evaporation is performed at a temperature below 46°C; (ii) the evaporator residence time is less than 30 minutes; (iii) the crystallization is carried out at a temperature below 35° C.; (iv) the intermediate acesulfame potassium composition comprises 10 wppb to 12 wppm of acetoacetamide; and (v) The method of any of the preceding forms, wherein the purified acesulfame potassium composition comprises from 10 wppb to 7 wppm of acetoacetamide.

[0130]

[0133] Form 17: The method of any of the previous forms, wherein said intermediate acesulfame potassium composition comprises less than 20 wppm of acetoacetamido-N-sulfonic acid.

[0134] Form 18: The process of any of the preceding forms, wherein said crude acesulfame potassium composition further comprises a solvent, and said process further comprises removing the solvent from said crude acesulfame potassium composition prior to said evaporating.

[0131]

[0135] Form 19: The process of any of the preceding forms, wherein the weight percent of acetoacetamide in said purified acesulfame potassium composition is lower than the weight percent of acetoacetamide in said crude acesulfame potassium composition.

[0132]

[0136] Form 20: Separating a transition phase comprising at least 2% by weight of acetoacetamide from said acesulfame-H composition to form a purified acesulfame-H composition; The method of any of the preceding aspects, further comprising:

[0133]

[0137] Form 21: The process of any of the preceding forms, wherein said neutralizing comprises neutralizing acesulfame-H in said purified acesulfame-H composition to form a crude acesulfame potassium composition comprising acesulfame potassium and acetoacetamide.

[0134]

[0138] Form 22. The concentrating step comprises evaporating the crude acesulfame potassium composition to obtain a water solution. and forming an intermediate acesulfame potassium composition comprising acesulfame potassium crystals, and a stream comprising acesulfame potassium and less than 50% by weight water, said separating comprising: crystallizing said intermediate acesulfame potassium composition to form a crystal-containing stream comprising acesulfame potassium crystals, and filtering said crystal-containing stream to form said purified acesulfame potassium composition.

[0135]

[0139] Form 23: The method of any of the preceding forms, wherein said filtering comprises at least two filtering operations.

[0140] Form 24: A purified acesulfame potassium composition produced or capable of being produced or obtainable or obtainable by the process of any of Forms 1-22.

[0136]

[0141] Form 25. A method of producing a purified acesulfame potassium composition comprising the steps of: (a) reacting sulfamic acid with triethylamine to form an amidosulfamate salt; (b) reacting the amidosulfamate with diketene to form an acetoacetamide salt; (c) contacting dichloromethane with sulfur trioxide to form a cyclization agent composition; (d) reacting the acetoacetamide salt with sulfur trioxide in the cyclizing agent composition to form a cyclic sulfur trioxide adduct; (e) hydrolyzing the cyclic sulfur trioxide adduct to form an acesulfame-H composition; (f) neutralizing the acesulfame-H to form a crude acesulfame potassium composition comprising acesulfame potassium and acetoacetamide; (g) evaporating the crude acesulfame potassium composition to form a water stream and an intermediate acesulfame potassium composition comprising acesulfame potassium and less than 75% by weight water; (h) crystallizing the intermediate acesulfame potassium composition to form acesulfame potassium crystals; and (i) filtering the acesulfame potassium crystals to form a purified acesulfame potassium composition comprising acesulfame potassium and less than 10 wppm acetoacetamide; Includes; The process above, wherein the evaporation is carried out at a temperature below 50° C. and the evaporator residence time is less than 30 minutes.

[0137]

[0142] Form 26: The process of Form 24, wherein said filtering is performed at a temperature below 35° C. and said crystallizing is performed at a temperature below 35° C.

[0143] Form 27: A purified acesulfame potassium composition produced or produceable or obtainable or obtainable by the process of Forms 24 or 25.

[0138]

[0144] Form 28: An acesulfame potassium composition comprising acesulfame potassium and less than 33 wppm, preferably less than 10 wppm acetoacetamide.

[0145] Form 29: The acesulfame potassium composition of Form 27 or 28, further comprising less than 33 wppm, preferably less than 10 wppm, of acetoacetamide-N-sulfonic acid.

[0139]

[0146] Form 30: The acesulfame potassium composition of any of Forms 27 to 29, further comprising from 0.001 wppm to 5 wppm of organic impurities, and / or from 0.001 wppm to 5 wppm of at least one heavy metal.

[0140]

[0147] Form 31: The acesulfame potassium composition of Forms 27-30, wherein said at least one heavy metal is selected from the group consisting of mercury, lead, and mixtures thereof.

[0148] Form 31: The acesulfame potassium composition of any one of Forms 27 to 31, wherein said mercury is present in an amount from 1 wppb to 20 wppm.

[0141]

[0149] Form 31: The acesulfame potassium composition of Forms 27-32, wherein said lead is present in an amount from 1 wppb to 25 wppm. EXAMPLES

[0142]

[0150] The following examples are included to illustrate the processes and compositions and are not intended to limit the scope of the application. Formation of Crude Acesulfame Potassium Composition :

[0151] 100 mmol of sulfamic acid, 99.5% pure, was suspended in 50 mL of dichloromethane in a flask under reflux. Under continuous stirring, 105 mmol of trimethylamine was added within about 3 minutes. During this time, the temperature rose to about 42° C. (the boiling point of dichloromethane) due to an exothermic acid / base reaction. The first reaction mixture was stirred for about 15 more minutes until no solid precipitate was observed in the flask. Next, 10 mmol of acetic acid was added to the first reaction mixture and stirred for about 15 more minutes. At this point, 110 mmol of diketene was added dropwise within 7 minutes of the acetic acid addition to form a second reaction mixture. All of the diketene was added to the second reaction mixture and after about 15 minutes of reaction time, the second reaction mixture was cooled. The resulting cooled second reaction mixture contained about 30% acetoacetamide-N-sulfonate triethylammonium salt. If necessary, additional batches of the cooled second reaction mixture were prepared.

[0143]

[0152] A sulfur trioxide / dichloromethane composition containing about 15% by weight sulfur trioxide and about 85% by weight dichloromethane was prepared by contacting the two components with each other in a separate container.

[0144]

[0153] A second flask (a 4-neck round bottom flask fitted with a mechanical stirrer, a thermometer, and a feed vessel) was placed in a cooling bath containing a mixture of isopropanol and dry ice. Approximately 200 g of the acetoacetamide-N-sulfonate triethylammonium salt solution and approximately 577 g of the sulfur trioxide / dichloromethane composition were weighed out. Approximately 15% by weight (approximately 87 g) of the total sulfur trioxide / dichloromethane composition was first fed into the reaction flask under continuous stirring by the mechanical stirrer. When the temperature of the flask contents reached −35° C. (via the cooling bath), the remainder of the sulfur trioxide / dichloromethane composition and all of the acetoacetamide-N-sulfonate triethylammonium salt solution were fed into the second flask. The solvent was in contact with the cyclization agent for less than one hour prior to the formation of the cyclic sulfur trioxide adduct, e.g., before the acetoacetamide-N-sulfonate triethylammonium salt solution was fed to the second flask. The feed rate was controlled such that the temperature of the contents of the second flask was maintained between −25° C. and −35° C. during the feed / cyclization reaction. After the reactants were fed, the reaction was allowed to proceed for approximately an additional minute. The cooling bath was then removed.

[0145]

[0154] After about 1 minute, the temperature of the flask contents reached about -22°C. At this point, the hydrolysis was initiated by feeding deionized water to the flask. The water was fed over a period of 10 minutes. The hydrolysis reaction was exothermic. The water was added slowly such that the temperature was maintained between -20°C and -5°C. After the water was added, the reaction mixture was allowed to reach room temperature.

[0146]

[0155] The hydrolysis products were phase separated using a separatory funnel: the heavier organic sweetener acid-dichloromethane phase (acesulfame-H composition) was separated off and the remaining aqueous phase was discarded.

[0147]

[0156] The acesulfame-H in the acesulfame-H composition was neutralized with 10% potassium hydroxide solution. Neutralization was performed at 25° C.±1° C. The addition of potassium hydroxide was completed within 20 minutes. After the neutralization process was completed, further phase separation was performed using a separatory funnel to obtain an aqueous phase containing acesulfame potassium (and some impurities), and an organic phase. The aqueous phase was considered the crude acesulfame potassium composition. This crude acesulfame potassium composition was divided into two portions and treated as discussed below. The remaining dichloromethane in the organic phase was discarded.

[0148] Example 1: Evaporation / Crystallization :

[0157] A first portion of the crude acesulfame potassium composition was evaporated under reduced pressure in a rotary evaporator at 45° C. for about 20 minutes. As a result, about 50% of the water evaporated from the crude acesulfame potassium composition. After the water was removed, an intermediate acesulfame potassium composition remained. The intermediate acesulfame potassium composition was then isolated and cooled, for example to 5° C. in a refrigerator.

[0149]

[0158] Cooling resulted in the precipitation of crude crystals containing mostly acesulfame potassium. These crude crystals were considered as the purified acesulfame potassium composition. The crude crystals were separated from the liquid and analyzed for yield and impurities, e.g., acetoacetamide. Tests for acetoacetamide (AAA) content were performed using the HPLC equipment and techniques discussed herein. In particular, HPLC analysis was performed using a Shimadzu LC Systems HPLC unit equipped with a CBM-20 Shimadzu controller and an IonPac NS1 ((5 μm) 150×4 mm) analytical column and an IonPac NG1 guard column (35×4.0 mm). For detection (at wavelengths of 270 nm and 280 nm), a Shimadzu SPD-M20A photodiode array detector was used. The analysis was performed at a column temperature of 23° C. As the first eluent, an aqueous mixture of tetrabutylammonium hydrogen sulfate (3.4 g / L), acetonitrile (300 mL / L), and potassium hydroxide (0.89 g / L) was used; as the second eluent, an aqueous mixture of tetrabutylammonium hydrogen sulfate (3.4 g / L) and potassium hydroxide (0.89 g / L) was used. Elution was performed in gradient mode according to the following second eluent flow profile:

[0150] · 0–3 min: constant at 80% (v / v); 3-6 min: Linear decrease to 50% (v / v); · 6–15 min: constant at 50% (v / v); 15-18 minutes: Linear decrease to 0%; 18-22 min: constant at 0%; 22–24 min: linear increase to 80% (v / v); 24~35 min: constant at 80% (v / v). The total eluent flow rate was approximately 1.2 mL / L. Data collection and calculations were performed using Shimadzu LabSolution software.

[0151] Comparative Example A: Evaporation / Crystallization :

[0159] The second portion of the crude acesulfame potassium composition was evaporated in a rotary evaporator at 90° C. under reduced pressure for about 180 minutes. As a result, about 50% of the water was evaporated from the crude acesulfame potassium composition. After the water was removed, an intermediate acesulfame potassium composition remained. The intermediate acesulfame potassium composition was then separated and cooled, for example to 5° C. in a refrigerator.

[0152]

[0160] Upon cooling, crude crystals precipitated containing mostly acesulfame potassium. These crude crystals were considered to be the purified acesulfame potassium composition. The crude crystals were separated from the liquid and analyzed for yield and impurities, e.g., acetoacetamide. The tests were carried out using the HPLC equipment and techniques discussed above. The results for Example 1 and Comparative Example A are shown in Table 1.

[0153] [Table 1]

[0154]

[0161] The temperature of the concentration of the crude acesulfame potassium composition and the separation operation of the intermediate acesulfame potassium composition have an effect on acetoacetamide formation. Without being bound by theory, it is believed that the acetoacetamide impurity forms as a result of thermal stress during the high temperature concentration of the crude acesulfame potassium composition, e.g., during the initial evaporation step. As shown, if the temperature of the concentration operation is kept below 90°C, no further post-crystallization separation is required to maintain the acetoacetamide content below a preferred level, e.g., below 10 wppm.

[0155] Example 2 and Comparative Examples B to D :

[0162] The decomposition effects of temperature and pH on the acesulfame potassium composition during processing were also studied. Acesulfame potassium was diluted in enough water to form a 16% aqueous solution. This aqueous solution was divided into multiple portions (Example 2 and Comparative Examples B-D). These portions of the aqueous solution (except for Example 2) were heated under reflux condensation to simulate a concentration operation. In Comparative Example D, a small amount of 10% potassium hydroxide was added to each portion of the aqueous solution prior to heating to bring the pH of the resulting solution to about 9.8. For each portion, the crystals (intermediate acesulfame potassium composition) were removed from the remaining liquid (after heating) and analyzed for impurities formed by decomposition, such as acetoacetamide-N-sulfonic acid (AAA-NSH). Tests for acetoacetamide-N-sulfonic acid content were performed using the HPLC equipment and techniques discussed above. The processing conditions and resulting impurity contents are shown in Table 2.

[0156] [Table 2]

[0157]

[0163] As shown in Table 2, during conventional concentration operating conditions, the use of high temperatures, long heating times (simulating residence times), and high pH can cause decomposition of acesulfame potassium (or acesulfame-H), which leads to the formation of additional impurities, such as acetoacetamide-N-sulfonic acid. By using the concentration operating parameters discussed herein, the impurities formed during decomposition are reduced or eliminated, thereby resulting in a purified acesulfame potassium composition of higher purity, i.e., a purified acesulfame potassium composition having a low acetoacetamide-N-sulfonic acid content.

[0158]

[0164] Although the present invention has been described in detail, modifications within the spirit and scope of the invention will be readily apparent to those skilled in the art. In view of the above discussion, the relevant knowledge in the art, and the references discussed above in connection with the background and detailed description (all of which are incorporated herein by reference). Furthermore, it should be understood that the various aspects of the invention and the various aspects and various parts of the various features set forth above and / or in the appended claims can be combined or exchanged in whole or in part. As will be appreciated by those skilled in the art, in the above description of the various aspects, other aspects are shown and these aspects can be appropriately combined with other aspects. Furthermore, those skilled in the art will recognize that the above description is for illustrative purposes only and is not intended to limit the present invention. The claims as of the filing of this application are reproduced below. [1] A method for producing a purified acesulfame potassium composition, comprising the steps of: (a) providing a crude acesulfame potassium composition comprising acesulfame potassium, acetoacetamide, and water; (b) concentrating the crude acesulfame potassium composition to form a water stream and an intermediate acesulfame potassium composition comprising acesulfame potassium and less than 33 wppm acetoacetamide; (c) separating the intermediate acesulfame potassium composition to form a purified acesulfame potassium composition comprising acesulfame potassium and less than 33 wppm acetoacetamide; Includes; The above process, wherein said concentrating step (b) is carried out at a temperature below 90°C and said separating step (c) is carried out at a temperature below 35°C. [2] The preparing step (a) reacting a sulfamic acid with an amine to form an amidosulfamate; reacting said amidosulfamate salt with an acetoacetylating agent to form an acetoacetamide salt; reacting the acetoacetamide salt with a cyclizing agent in a cyclizing agent composition to form a cyclic sulfur trioxide adduct; hydrolyzing the cyclic sulfur trioxide adduct to form an acesulfame-H composition comprising acesulfame-H; and neutralizing the acesulfame-H in the acesulfame-H composition to form the crude acesulfame potassium composition; The method according to claim 1, comprising: [3] The method of [1], wherein the intermediate acesulfame potassium composition contains less than 33 wppm acetoacetamido-N-sulfonic acid. [4] The concentration, evaporating said crude acesulfame potassium composition to form a water stream and said intermediate acesulfame potassium composition comprising acesulfame potassium and less than 75% by weight water; The method according to claim 1, comprising: [5] The method according to [4], wherein the evaporation residence time is less than 180 minutes. [6] The method of [5], wherein the intermediate acesulfame potassium composition contains less than 33 wppm acetoacetamido-N-sulfonic acid. [7] The separation is: crystallizing the intermediate acesulfame potassium composition to form acesulfame potassium crystals; and filtering said acesulfame potassium crystals to form said purified acesulfame potassium composition; The method according to claim 4, comprising: [8] The method according to [7], wherein the filtration is carried out at a temperature of 35°C or less. [9] The method according to [7], wherein the crystallization is carried out at a temperature of 35°C or lower.

[10] The method according to [7], wherein the crystallization is carried out at a pH lower than 10.

[11] The method of [4], wherein the evaporation is performed at a temperature below 85°C, and the intermediate acesulfame potassium composition contains from 1 wppb to 33 wppm acetoacetamide, and the purified acesulfame potassium composition contains less than 33 wppm acetoacetamide.

[12] The method of

[11] , wherein the intermediate acesulfame potassium composition further comprises less than 33 wppm of acetoacetamido-N-sulfonic acid.

[13] The method of [4], wherein the evaporation is conducted at a temperature below 60°C, the evaporator residence time is less than 50 minutes, the intermediate acesulfame potassium composition contains from 10 wppb to 25 wppm acetoacetamide, and the purified acesulfame potassium composition contains from 10 wppb to 15 wppm acetoacetamide.

[14] The method of

[13] , wherein the intermediate acesulfame potassium composition contains less than 30 wppm acetoacetamido-N-sulfonic acid.

[15] The method of [4], wherein the evaporation is carried out at a temperature in the range of 20°C to 55°C, the evaporator residence time is in the range of 1 minute to 300 minutes, the separation is carried out at a temperature in the range of -10°C to 15°C, the separation operation residence time is in the range of 1 minute to 180 minutes, the crude acesulfame potassium composition contains 500 wppm to 2375 wppm acetoacetamide, the intermediate acesulfame potassium composition contains 10 wppb to 20 wppm acetoacetamide and 10 wppb to 20 wppm acetoacetamide-N-sulfonic acid, and the purified acesulfame potassium composition contains 10 wppb to 10 wppm acetoacetamide and 1 wppb to 20 wppm acetoacetamide-N-sulfonic acid.

[16] (i) the evaporation is performed at a temperature of less than 46°C; (ii) the evaporator residence time is less than 30 minutes; (iii) the crystallization is carried out at a temperature below 35° C.; (iv) the intermediate acesulfame potassium composition comprises 10 wppb to 12 wppm of acetoacetamide; and (v) The method according to [4], wherein the purified acesulfame potassium composition contains 10 wppb to 7 wppm of acetoacetamide.

[17] The method of

[16] , wherein the intermediate acesulfame potassium composition contains less than 20 wppm acetoacetamido-N-sulfonic acid.

[18] The method of [4], wherein the crude acesulfame potassium composition further comprises a solvent, and the method further comprises removing the solvent from the crude acesulfame potassium composition prior to the evaporation.

[19] The method of [1], wherein the weight percent of acetoacetamide in the purified acesulfame potassium composition is lower than the weight percent of acetoacetamide in the crude acesulfame potassium composition.

[20] separating a transition phase comprising at least 2% by weight of acetoacetamide from the acesulfame-H composition to form a purified acesulfame-H composition; The method according to [2], further comprising:

[21] The method of

[20] , wherein the neutralizing comprises neutralizing the acesulfame-H in the purified acesulfame-H composition to form the crude acesulfame potassium composition comprising acesulfame potassium and acetoacetamide.

[22] The method of [1], wherein said concentrating comprises evaporating the crude acesulfame potassium composition to form a water stream and an intermediate acesulfame potassium composition comprising acesulfame potassium and less than 50% by weight water, and said separating comprises crystallizing the intermediate acesulfame potassium composition to form a crystal-containing stream comprising acesulfame potassium crystals, and filtering the crystal-containing stream to form the purified acesulfame potassium composition.

[23] The method according to

[22] , wherein the filtration comprises at least two filtration operations.

[24] A purified acesulfame potassium composition produced by the method described in [1].

[25] A method for producing a purified acesulfame potassium composition, comprising the steps of: (a) reacting sulfamic acid with triethylamine to form an amidosulfamate salt; (b) reacting the amidosulfamate with diketene to form an acetoacetamide salt; (c) contacting dichloromethane with sulfur trioxide to form a cyclization agent composition; (d) reacting the acetoacetamide salt with sulfur trioxide in the cyclizing agent composition to form a cyclic sulfur trioxide adduct; (e) hydrolyzing the cyclic sulfur trioxide adduct to form an acesulfame-H composition; (f) neutralizing the acesulfame-H to form a crude acesulfame potassium composition comprising acesulfame potassium and acetoacetamide; (g) evaporating the crude acesulfame potassium composition to form a water stream and an intermediate acesulfame potassium composition comprising acesulfame potassium and less than 75% by weight water; (h) crystallizing the intermediate acesulfame potassium composition to form acesulfame potassium crystals; and (i) filtering the acesulfame potassium crystals to form a purified acesulfame potassium composition comprising acesulfame potassium and less than 10 wppm acetoacetamide; Includes; The process above, wherein the evaporation is carried out at a temperature below 50° C. and the evaporator residence time is less than 30 minutes.

[26] The method according to

[25] , wherein the filtration is carried out at a temperature below 35°C and the crystallization is carried out at a temperature below 35°C.

[27] A purified acesulfame potassium composition produced by the method described in

[25] .

[28] An acesulfame potassium composition comprising acesulfame potassium and less than 33 wppm, preferably less than 10 wppm, of acetoacetamide.

[29] The acesulfame potassium composition of

[28] , further comprising less than 33 wppm, preferably less than 10 wppm, of acetoacetamide-N-sulfonic acid.

[30] The acesulfame potassium composition according to

[28] , further comprising 0.001 wppm to 5 wppm of organic impurities and / or 0.001 wppm to 5 wppm of at least one heavy metal.

[31] The acesulfame potassium composition according to

[30] , wherein the at least one heavy metal is selected from the group consisting of mercury, lead, and mixtures thereof.

[32] The acesulfame potassium composition according to

[31] , wherein the mercury is present in an amount of 1 wppb to 20 wppm.

[33] The acesulfame potassium composition according to

[31] , wherein the lead is present in an amount of 1 wppb to 25 wppm.

Claims

1. 1. A method for producing a purified acesulfame potassium composition, comprising: (a) providing a crude acesulfame potassium composition comprising acesulfame potassium, acetoacetamide, and water, reacting a sulfamic acid with an amine to form an amidosulfamate; reacting said amidosulfamate salt with an acetoacetylating agent to form an acetoacetamide salt; reacting the acetoacetamide salt with a cyclizing agent in a cyclizing agent composition to form a cyclic sulfur trioxide adduct; hydrolyzing the cyclic sulfur trioxide adduct to form an acesulfame-H composition comprising acesulfame-H; and neutralizing the acesulfame-H in the acesulfame-H composition to form the crude acesulfame potassium composition. a process comprising: (b) evaporating the crude acesulfame potassium composition to form an intermediate acesulfame potassium composition comprising acesulfame potassium, less than 75 wt. % water, and less than 33 wppm acetoacetamide, and a water stream; (c) separating the intermediate acesulfame potassium composition to form the purified acesulfame potassium composition comprising acesulfame potassium, less than 33 wppm acetoacetamide, and less than 33 wppm acetoacetamide-N-sulfonic acid; Including; The process of claim 1, wherein said evaporation step (b) is carried out at a temperature below 85° C. and said separation step (c) is carried out at a temperature of 35° C. or less, and further wherein the evaporation residence time is less than 180 minutes.

2. The separation comprises: crystallizing the intermediate acesulfame potassium composition to form acesulfame potassium crystals; and filtering said acesulfame potassium crystals to form said purified acesulfame potassium composition; The method of claim 1 , comprising:

3. 3. The method of claim 2, wherein the filtration is carried out at a temperature of 35° C. or less.

4. 3. The method of claim 2, wherein the crystallization is carried out at a temperature of 35° C. or less.

5. 3. The method of claim 2, wherein the crystallization is carried out at a pH below 10.

6. 2. The method of claim 1, wherein the evaporation is conducted at a temperature below 60° C., the evaporation residence time is less than 50 minutes, the intermediate acesulfame potassium composition comprises from 10 wppb to 25 wppm acetoacetamide, and the purified acesulfame potassium composition comprises from 10 wppb to 15 wppm acetoacetamide.

7. 7. The method of claim 6, wherein the intermediate acesulfame potassium composition contains less than 30 wppm acetoacetamide-N-sulfonic acid.

8. 2. The method of claim 1, wherein the evaporation is conducted at a temperature in the range of 20° C. to 55° C., the evaporation residence time is in the range of from 1 minute to less than 180 minutes, the separation is conducted at a temperature in the range of −10° C. to 15° C., the separation operation residence time is in the range of 1 to 180 minutes, the crude acesulfame potassium composition comprises 500 wppm to 2375 wppm acetoacetamide, the intermediate acesulfame potassium composition comprises 10 wppb to 20 wppm acetoacetamide and 10 wppb to 20 wppm acetoacetamide-N-sulfonic acid, and the purified acesulfame potassium composition comprises 10 wppb to 10 wppm acetoacetamide and 1 wppb to 20 wppm acetoacetamide-N-sulfonic acid.

9. (i) the evaporation is carried out at a temperature below 46°C; (ii) the evaporation residence time is less than 30 minutes; (iii) the crystallization is carried out at a temperature below 35° C.; (iv) the intermediate acesulfame potassium composition comprises 10 wppb to 12 wppm acetoacetamide; and (v) The method of claim 1, wherein the purified acesulfame potassium composition comprises from 10 wppb to 7 wppm acetoacetamide.

10. 10. The method of claim 9, wherein the intermediate acesulfame potassium composition contains less than 20 wppm acetoacetamide-N-sulfonic acid.

11. 2. The method of claim 1, wherein the crude acesulfame potassium composition further comprises a solvent, and the method further comprises removing the solvent from the crude acesulfame potassium composition prior to the evaporation.

12. 2. The method of claim 1, wherein the weight percent of acetoacetamide in the purified acesulfame potassium composition is lower than the weight percent of acetoacetamide in the crude acesulfame potassium composition.

13. separating a transition phase comprising at least 2% by weight of acetoacetamide from said acesulfame-H composition to form a purified acesulfame-H composition; The method of claim 1 further comprising:

14. 14. The method of claim 13, wherein said neutralizing comprises neutralizing the acesulfame-H in the purified acesulfame-H composition to form said crude acesulfame potassium composition comprising acesulfame potassium and acetoacetamide.

15. 2. The method of claim 1, wherein said evaporating comprises evaporating said crude acesulfame potassium composition to form a water stream and an intermediate acesulfame potassium composition comprising acesulfame potassium and less than 50% by weight water, and said separating comprises crystallizing said intermediate acesulfame potassium composition to form a crystal-containing stream comprising acesulfame potassium crystals, and filtering said crystal-containing stream to form said purified acesulfame potassium composition.

16. The method of claim 15, wherein the filtering comprises at least two filtering operations.

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