BETAINE RECOVERY PROCESS

Abstract: Betaine is recovered from natural sources such as beet molasses, rest molasses and vinasse by diluting the molasses to 25-50% solids, introducing the molasses to the top of a chromatographic column containing a salt of polystyrene sulfonate cation exchange resin crosslinked with from about 2 to about 12 weight percent of divinylbenzene, eluting with water and collecting a fraction of betaine from the downstream side of the resin. When successive feeds with predetermined intervals are made, the feeds may be partly overlapped. The betaine from the preceding feed is then eluted by the dilute molasses from the following feed. The betaine fraction is evaporated under vacuum and the betaine crystallized as anhydrous crystals or as betaine monohydrate.

Description: Betaine Recovery Process Betaine, an important component of beet molasses has the molecular formula of: The compound is amphoteric and shows a neutral reaction in water solution. Betaine is readily soluble in water, and is utilized in animal feeds, including feeds for cattle, pigs and birds. In addition, betaine has pharmaceutical applications. Betaine occurs in roots, grains, and stems of a variety of plants , and the sugar beet has a relatively high content thereof, ranging from 1.0 to 1.5% on a dry solids basis. During processing of the sugar beet to recover sucrose, betaine concentrates in the molasses. Beet molasses normally contains between 3 and 8 percent on a dry solids basis of betaine. Other materials having substantial amounts of betaine include rest molasses from the Steffen process, vinasse, and some run off syrups that are the by-products of sugar refining. From beet molasses, betaine has been recovered by ion exchange, by crystallization as hydrochloride, or by extraction into organic solvents. Several modifications of the ion exchange process have been published; see, for example, U.S. Patent No. 2,586,295, Japanese Patent No. 24904/71, U.S.S.R. Patent No. 445,270, and Schneider F.: Technologie des Zuckers, Verlag Schaper Hannover, 1968, p. 635-636. These prior art methods generally comprise passing molasses through a strong cation exchanger, rinsing the exchanger free from residual solution, and desorbing the betaine by passing a diluted ammonia solution through the resin bed. If beet molasses is subjected to a desugarization process, i.e. the Steffen process, the betaine concentra¬ tes into the rest molasses. A similar raw material for betaine is vinasse, which is residual molasses from a fermentation process. Betaine has been recovered from rest molasses or vinasse by ion exchange, but due to the comparatively high concentration of betaine in these materials, it is also possible to utilize the * low solubility of betaine hydrocloric acid; see British Patent No. 715, 774, U.S. Patent No. 2,519,573, Schneider F.: Technologie des Zuck- ers, Verlag Schaper, Hannover, 1968, p. 1010. From rest molasses, betaine has also been recovered by extraction into organic solvents; see German Patent Appln. No. 2,300,492. Chromatographic methods for the separation of organic compounds are well-known from analytical chemistry. A type of chromatography, the so-called "ion exclusion" chroma ography, has been used for the recovery of sucrose from molasses. A great number of patents and other publi¬ cations on this method can be found in the literature, i.e. D.Gross in CITS 14th Gen. Ass. Brussels 1971, U.S. Patents Nos.2,868,677; 2,937,959; 3,214,293; and 3,884,71 and Canadian Patent No. 754,511. In the ion exclusion pro- cess, molasses is usually separated on a cation exchange resin column in alkali metal form. The sugar fraction is eluted from the column after the nonsugar fraction. It has now been found that betaine can be separate from the sugars and nonsugars of beet molasses by a chrom tographic process. Dilute molasses is supplied to a chrom tographic column. On elution of the dilute molasses from the column with water, there is recovered, as eluate leaving the bottom of the column, a first, nonsugar waste fraction, a second fraction containing a substantial pro- portion of the sugars in the feed, and a third betaine fraction, which is eluted at the tail end after the suσar fraction, and which contains a high proportion of the betaine in the feed, as much as 80% or more on dry sub¬ stance. From the said betaine fraction, betaine.can be recovered by crystallization, or may be recovered as the hydrochloride, if desired. A suitable raw material for betaine production is sugar beet molasses, which normally contains 3-8% of betaine on a dry solids basis. Both rest molasses from a desugarization process and vinasse from a fermentation process are high in betaine and are naturally also very suitable raw materials. Betaine hydrochloride, which is used in pharama- ceutical preparations, for example, can be prepared from the betaine-rich fraction obtained by the process of the present invention ' by a conventional process using an equivalent amount of hydrochloride acid. A flow chart giving a general description of the process of the present invention is shown in Figure 1 of the drawings . Referring to Figure 1 and in accordance with the process of the present invention, molasses con¬ taining betaine is diluted to a solids content of 25-50%, preferably 35-40%, and fed to a large scale chromatograp¬ hic column. The column contains a strong cation exchange resin in alkali metal form; sodium is generally the pre- ferred alkali metal as being more ecnomical. The column of resin is covered with water prior to feeding the di¬ luted molasses thereto. On completion of the molasses feed step, the column is eluted with water at 60-90 C. and the eluate is collected as several fractions . The resin used in the column is preferably an alkali metal salt of sulphonated polystyrene exchange resin crosslinked with from about 2 to about 12 weight percent, and more preferably, from about 3 to about 9 weight percent divinylbenzene (DVB) . The resin is of uniform particle size and has a mean bead diameter pre¬ ferably within the range of about 20 to 400 U.S. mesh, OMPI ^« and most preferably in the approximate range of 0.2-0.5 mm. The height of the resin bed is from about 2.5 to about 10 meters. The feed rate is 0.5-2 cubic meters per hour per square meters of the cross sectional area, of the resin column (m 3/h/m2) . The feed is preferably a betaine-containing beet molasses, a rest molasses, or vinasse, which is diluted with water to contain about 25- 50 weight percent dry substance, preferably about 35-40%. On elution with water, there is recovered from the column as eluate, a first nonsugar waste fraction, a second sugar-containing fraction, and a third fraction consisting principally of betaine. The nonsugar and sugar fractions are subjected to further treatment to recover sugar and rest molasses. These further treatment processe are previously described in the literature and are not part of this invention. Where feed solutions having a realtively low sugar level are used, the second, sugar-containing fraction may not contain commercially significant-quantities of sugar. In that case, the fraction may be used as a cattle food, or a portion or all of it may be returned to the system with the next feed. Further, it has been found that successive feeds of dilute molasses with predetermined feeding intervals, followed by elution with water, may be accomplished. When this is done, it is possible, if desired, to partly overlap the feeds. Thus, the betaine fraction on the column from the preceding feed is eluted using the dilute molasses from the following feed as eluate. In this case, the last fraction of the first feed contains the betaine from the first feed, together with a small portion of the other ingredients of the second feed. An advantage of this procedure is that be¬ cause of the shorter time between eeds, the total pro¬ cessing time for a given quantity of molasses is substan- tially reduced. Betaine is recovered from the fraction consisting principally of betaine termed "Betaine Fraction" in Figur 1, by first evaporating it to from about 77% to about 81% preferably about 80 % dry substance concentration. The solution is then seeded with anhydrous betaine crystals and anhydrous betaine is crystallized by maintaining the temperature at 75-85°C., under a vacuum within the range of about 80-120 millibar during the crystallization. A con¬ ventional vacuum crystallizer, i.e. of the type used in the sugar industry, is suitable for carrying out this step of the process. The water is evaporated, causing the crystals to grow. When crystallization is substantially complete, as represented by Crystallization la in Figure 1, the anhydrous betaine crystals are separated from the mother solution by centrifugation. The run off syrup from the centrifugation is concentrated to 80-90% solids, seed¬ ed with anhydrous betaine crystals, and an additional amount of anhydrous betaine crystals-is recovered by crystallization in a vacuum crystallizer, as shown at Crystallization lb in Figure 1. In the second crystalliza¬ tion, lb, the temperature is maintained at 80-90 C. under a vacuum within the range of about 60-100 millibar. The crystallization time in the first crystalliza¬ tion, la, is 4-10 hours, while in the second, about 6-12 hours are required. The yields are 50-55% of betaine from the first crystallization and 45-50% of betaine from the second. The purity of the crystals is 99% in the first and 98% in the second crystallization. The first and se¬ cond crystallization procedures just described as Crystal¬ lization la and lb provide a product which may be describ¬ ed as a chemically purebetaine product. Pharmaceutical grade betaine monohydrate can be recovered by dissolving in water the crude betaine crys¬ tals obtained in Crystallization la and lb to form a solu¬ tion having about 60% solids, subjecting the thus formed solution to color removal by conventional activated car¬ bon/filtration treatment, and recrystallizing the betaine from water in a vacuum crystallizer at 75-55°C, with a vacuum in the range of about 100-180 millbar. The crystal¬ lization time under these conditions ranges from 2-4 hours, the yield of betaine is 50-55%, based on the total betai¬ ne in the feed, and the purity of the crystals is over 99.3%. This stage of the process is represented in'Figure 1 as Crystallization II. A different route of preparing pure betaine can also be followed. This betaine may be separated from the molasses by- chromatographic separation in two steps: a crude separation in order to collect a betaine-rich frac¬ tion which is then separated a second time to recover a pure betaine solution. A material balance for the two- step separation process is shown in Figure 7. The purity of the betaine solution which is recovered from the se¬ cond separation step is 90%. From this solution betaine is crystallized. The process is described in detail in Examples 7-8. In conducting the betaine recovery process of the present invention, recourse may be had to the use of equipment found in the prior art. The chromatographic column and process described in U.S. Patent No. 3,928,913 as well as the feeding device for the column described in U.S. Patent No. 3,814,253 may be used. Further, auto¬ matic control of the fractionation process based upon measurement of density and optical rotation of sucrose as described in U.S.Patent No. 3,826,905 may be employed. Additional automatic measurements of process variables such as conductivity may be employed and micro-proces¬ sors may be used to advantage in making automatic calcu¬ lations and in carrying out control procedures. Crystal¬ lization of anhydrous betaineadαf betaine monohydrate may be carried out in conventional vacuum crystallizers with forced circulation of the type used in sucrose pro¬ duction. The betaine crystals may be separated from their mother liquor in centrifuges such as the type normally used to separate sucrose crystals from molasses. This invention also relates to the production of betaine from inverted molasses (Hongisto, H. and Heikkila, K.; Desugarisation of cane molasses by the Finnsugar process, Proceedings XVI Congress of International Society of Cane Sugar Technologists, Sao Paulo 1977 Vol. 3 pages 3031-3O98) . In the chromatographic separation of an inverted molasses the betaine is separated from the non-sugars. The invert sugar monosaccharides partly overlap the betaine but a betaine-rich fraction can be obtained. From the betaine-rich fraction the betaine is re¬ covered by conventional ion-exchange treatment (as des¬ cribed on page 2) . A flow chart of betaine recovery from inverted molasses is shown in Figure 10. In Figure 11, the chromatgraphic separation of inverted molasses is shown. In accordance with the process of the present inven¬ tion, beet molasses is inverted by acid or enzymic treat¬ ment according to conventional methods. The inverted mo- lasses is subjected to a chromatographic separation as described above. A betaine-rich fraction, which contains a part of the invert " sugar monosaccharides, is recovered and subjected to ion-exchange treatment according to con¬ ventional methods. The invert sugar fraction from the ion-exchange column is combined with the sugar fraction from the chromatographic separation. The betaine is eluted from the ion-exchange column by diluted ammonia Cor other suitable eluent) . From the neutralized solution betaine is crystallized as anhydrous betaine or as betaine hydro- chloride. The invention will be further described with reference to the following working examples: Example 1 Recovery of betaine from beet molasses Betaine was recovered from beet molasses by- di¬ luting the molasses and pissing it to a chromatographic column, the process and column having the following characteristics: Chromatographic Column Sulphonated polystyrene-divinylbenzene cation exchange re in Na -form. 5.5% DVB. Mean bead diameter 0.45 mm. Bed Height 6.1 m. and bed diameter 2.76 m. The bed was initially totally immersed in water. Flow rate • 5 ζ .8^5 c m ™ 3 -3//hw _(0n.9n7-»7-> m_ 3 3/ ,h,__/m 2 ) Temperature 82°C. Eluent Water Feed 1455 kg dry substance in the form of beet molasses, diluted with water to 39% dry substance. Composition of Solids (% on Dry Substance) Surcrose 62.2 Betaine 6.9 Other Solids 30.9 Seven separate fractions were collected during the large scale chromatographic separation, as shown in Figure 1a of the drawings and Table 1. The composition of the fractions is shown in Table 1 below. Fraction 2 is the waste fraction and is removed from the process for subsequent use as animal food, a fermentation sub¬ strate, or the like. Fraction 5 is the sugar fraction and Fraction 7 the betaine fraction. Fractions 1, 3, 4 and 6 are recycled to the process by combining them with the molasses feed stock for subsequent runs. The recovered betaine fraction contained 72% of the betaine in the feed. The purity of the fraction was 80.6% on dry substance basis. - _ , & TABLE 1 COMPOSITION OF FRACTIONS FROM BEET MOLASSES SEPARATION (Ex1. ) Fraction 1 2 3 4 5 6 7 Minutes 0-17 17-65 ■ 72 -80 -115 -120 -140 Total Solids Concentration g/100 g 3.1 6.6 13.1 15.5 20.0 5.5 4.6 Composition of Solids, Weight % on Dry Substance Sucrose 1.1 20.1 55.0 64.6 92.0 58.3 5.6 Betaine 12.5 0.4 0 0 1.2 37.6 80.6 Other 86.4 79.5 45.0 35.4 6.8 4.1 13.8 Several successive feeds were made with water be¬ ing introduced to the top of the column between each feed as eluent. The resin column was at all times covered with liquid. From each feed, the betaine, which is eluted last as Fraction 7, was recovered just before the non- sugars (other) fraction of the following feed. The time between feeds was 140 minutes. Example 2 Production of anhydrous betaine and betaine monohydrate Anhydrous betaine and betaine monohydrate were recovered, and a material balance for the process is shown in Figure 2. Beet molasses was separated by large scale chromatography as described in Example 1. The be- taine yield in the separation was 75% of the betaine in the feed, and the purity of the solution was 75% on dry substance. Again following the process described in Example 1 , successive feeds of the diluted molasses were made, separations performed, and the betaine fractions obtained thereby from the eluent of each succeeding feed were combined. Water was used as eluent, and 140 minutes elapsed between each feed. The dilute betaine solution thus obtained as the combined betaine fraction contained 4.5% dry substance by weight and was evaporated to 80 weight percent concentration. The concentrated solution thus obtained was seeded with betaine crystals and an¬ hydrous betaine was crystallized, as at la in Figure 2, at 75-85 C. under a vacuum of about 100 millibar. The yield of betaine crystals was 55%. The purity of the crystals was 99%. The crystallization was carried out in a conventional sugar crystallizer with forced circula¬ tion. The crystallization time was 6 hours. The crystals were separated from the mother liquor by centrifugation in a conventional sugar centrifuge. The run off syrup was evaporated, and by crystallization at 80-90°C, lb in Figure 2, and at a vacuum of 60-100 millibar, an additional amount of betaine anhvdride - ^ crystals was recovered. The yield for this crystalliza¬ tions step was 48% and the purity of the crystals 98%. The crystallization time was 8 hours. The run off syrup from the centrifugation of the crystals from this second 5 crystallization, lb, was recycled to the feed solution. In order to produce pharmaceutical grade betaine monohydrate, the anhydrous betaine crystals obtained were dissolved in water to provide a 60% by weight solu¬ tion of solids, and the solution was purified by treat- 10 ment with activated carbon followed by filtration. From * the purified solution, betaine monohydrate was crystalli¬ zed at 80 C. in a sugar crystallizer, at Crystallization II. The yield was 55%, and he purity of the betaine crystals almost 100%. The run off syrup was recycled as 15 feed for crystallization step la. Example 3 Production of crystalline betaine A material balance for the production of crystal- 20 line betaine is shown in Figure 3. Beet molasses was separated by large scale chroma- tography as in Examples 1 and 2. Successive feeds were made and the collected betaine fractions combined. The betaine yield in the fractionation was 80%, and the 25 purity of the betaine solution was also 80% on dry sub¬ stance. The concentration of the betaine solution was 4.0 weight percent. The dilute betaine solution was con¬ centrated by evaporation to ca 80% solids, seeded, and anhydrous betaine was crystallized as in Example 2. The 30 crude anhydrous betaine crystals v.-ere dissolved in water, and the solution subjected to conventional color removal and filtration. From the purified solution, betaine monohydrate was crystallized. The yield was 72 kg betai¬ ne anhydride and 100 kg betaine monohydrate (anhydrous 35 basis) . Example 4 Separation of desugarized rest molasses Betaine was recovered from desugarized rest molas¬ ses by passing it though a chromatographic column having the characteristics and using the operating conditions set forth below: Column : Sulphonated polystyrene-divinylbenzene cation exchange resin in Na -form. Mean bead diameter 0.42 mm. Bed heigth 5.4 m. Bed diameter 0.225 m Flow rate 0.04 m 3 /h (1.007 m 3 /h/m 2 ) Temperature 85°C, Feed Desugarized rest molasses. Dry substance 12 kg as a 40 weight percent solution. Composition of Solids (% on Dry substance) Sucrose 32.4 Betaine 9.1 Other Solids 58.5 Eluent : Water The result of the separation is shown in Figure 4. The Figure shows the situation when successive feeds were made. The nonsugars (other) of the following feed are eluted right after the betaine of the preceding feed. The time between feeds was 145 minutes, and during this time, water was continuously supplied to the top of the column as an eluent and in an amount sufficient to maintain a liquid level above the resin in the column. Table 2 below -shows the composition of the collec¬ ted 4 fractions ' . Fraction -1 is a waste fraction, Fraction 3 is the betaine fraction, and Fractions 2 and 4 are re¬ cycled to the process in order to increase the yield. Because of the relatively low level of sucrose in the feed, no sugar fraction was recovered. TABLE 2 COMPOSITION OF FRACTIONS FROM REST MOLASSES SEPARATION (Ex. 4) Fraction Minutes 10-115 -125 -153 -155 Total Solids Concentra¬ tion g/100 g 14.1 9.0 5.1 3.5 Composition of Solids, Weight % on Dry Substance Sucrose 34.6 33.5 8.8 0 Betaine 1.5 29.7 76.0 60.1 Other 63.9 36.8 15.2 39.9 Example 5 Separation of beet molasses Beet molasses was diluted to 39.6 % dry solids . content and introduced at the top of a chromatographic column of the following characteristics and under the following conditions: Column : Sulphonated polystyrene-divinylbenzene cation exchange resin in Na -form. 6.5% DVB. Mean bead diameter 0.44 mm. Bed height 4.4 m. Bed Diameter 60 cm. Temperature 81.5°C. Flow rate 0.246 m 3 /h (0.870 m 3 /h/m 2 ) Feed Beet molasses, 64 kg dry substance as a 39.6% water solution. Composition of Solids (% on Dry Substance) Sucrose 66.5 Betaine 5.3 Other Solids 28.2 - Eluent : Water The .fractionation is shown in Figure 5. When successive feeds were made, the nonsugars of the follo¬ wing feed were eluted just after the betaine of the pre¬ ceding feed. The time between feeds were 130 minutes. Water was used as eluent between feeds, and the liquid level was maintained at all times above the resin level in the column. Table 3 below shows the distribution of components into the 4 collected fractions. Fraction 1 is the waste or "rest molasses" fraction, Fraction 2 is recycled, Fraction 3 is the sugar fraction, and Fraction 4 the betaine fraction. TABLE 3 COMPOSITION OF FRACTIONS FROM BEET MOLASSES SEPARATION (Ex. 5) Fraction 1 . 2 3 Minutes 5-60 60-80 -105 -135 Total Solids Concentration g/100 g 6.1 18.7 26.1 3.2 Composition of Solids, VJeight % on Dry Substance Sucrose 30.4 67.4 90.9 8.9 Betaine 1.1 0 0 81.3 Other 68.5 32.6 9.1 9.8 Example 6 Vinasse separation Betaine was recovered from vinasse by chromato¬ graphic separation followed by crystallization. Vinasse is a fermentation by-product which contains high amounts of betaine. The separation was carried out on a bench scale solumn. The conditions were: Feed : 0.1 liter diluted vinasse. concentration (c) 30g/100g Flow rate 360 ml/h (0.237 m 3 /h/m 2 ) Resin Zerolit 225, Na-form, 3.5% DVB Column Height 0.83 m Particle Size 0.23 mm Temperature 60°C. Column Diameter 4.4 cm Composition of Feed (% on Dry Substance) Monosaccharides 10.1 Oligosaccharides 4.8 Betaine - 14.0 Others -71.1 The time between two successive feeds was 135 minutes. Water was used as the eluent between feeds. From the eluent, fractions were collected as shown in the following Table 4: TABLE 4 COMPOSITION OF FRACTIONS FROM VINASSE SEPARATION (Ex. 6) Fractions Minutes 0-10.0 10.0-117.5 -120 -135 Total Solids Concentration g/100 g 1.7 4.0 5.5 3.5 Composition of the Fractions % Monosaccharides 8.6 8.9 29.9 15.5 Betaine 42.4 3.9 62.8 75.5 Oligosaccharides and Others 49.0 87.2 7.3 9.0 T8 The feed capacity was 10.4 kg ds/h/m resin. The separation is shown graphically in Figure 6. From the betaine fraction (Fraction 4) , betaine was recovered by crystallization as in Examples 2 and 3. The total yield was increased by recirculations, as in Example 1, to over 80% of the betaine in the feed. Example 7 Betaine production, two separations Betaine was prepared from beet molasses by separa¬ tion in two steps: a crude separation to increase the betaine amount in the solution and a second separation to recover a pure betaine solution. The chromatographic se¬ parations were carried out as in Example 1. The condition in the crude separation, step 1, were as follows: Feed : 2510 1 beet molasses. The concentration of the feed was 39.9 g solids /100 g Flow rate 5.49 m 3 /h (0.918 m 3 /h/m 2 ) Fesin Duolite C 20 Na-form, 6.5% DVB Bed Height 6.1 Particle Size 0.45 mm Bed Diameter 276 cm Time Between Feeds 105 minutes Composition of Feed (% on Dry Substance) Monosaccharides 0.3 Disaccharides 62.4 Betaine 10.6 Others 26.7 Several successive feeds were carried out, with elution with water between feeds. The time between feeds, 105 minutes, was arranged so that the betaine fraction is eluted from the column during the early stages of the next successive feed. Thus, the betaine fraction, normal¬ ly collected as the last fraction, is collected as the first fraction of the next successive series of collected fractions. All feeds were similar and the conditions during successive runs were kept unchanged. The result of the crude separation, Separation 1 of Figure 7, is shown in Figure 8. The eluate was collec¬ ted as six fractions, the composition of which is shown in the following Table 5: TABLE 5 COMPOSITION OF FRACTIONS FROM SEPARATION I, EXAMPLE 7 Fraction 1 2 3 4 5. 6 Minutes 0-25 25-35 -52.5 -74.5 -102.5 -105 Total Solids Concentration g/100 g 7.8 7.8 9.9 15.6 22.2 9.4 Composition of the Fractions % on Dry Substance Monosaccharides 1.9 00 00 00 00 00 Disaccharides 7.3 8.9 37.4 61.5 92.0 70.3 Betaine 59.6 32.6 2.8 00 1.0 17.7 Others 31.2 58.5 59.8 38.5 7.0 12.0 The feed capacity was 21.9 kg ds/h/m . After the several separations were carried out, the betaine-rich fractions (Fraction 1 ) were combined to form the feed solution of the second fractionation, Separation 2 of Figure 7. Fractions 2,4 and 6 were recirculated. The combined solution was evaporated to 39.7% concentration. A concentration range of about 35-40% solids may be used. Fraction 3 was discarded as waste, while Fraction 5 was recovered as the sugar fraction. The conditions in the second fractionation, Sepa¬ ration 2 of Figure 7, were: Feed 3000 1 concentration 39.7 g/100g Flow rate 5.4 m 3 /h (0.903 m 3 /h/m 2 ) Resin Duolite C 20, Na-for , 6.5% DVB Bed Height 6.2 m Particle Size 0.45 mm Bed Diameter 276 cm Time Between Feeds ; 180 minutes The result of * the fractionation is shown in Figure 9. Four fractions were taken as shown in the following Table 6. TABLE 6 COMPOSITION OF FRACTIONS FROM SEPARATION 2, EXAMPLE 7 Fraction 1 2 3 4 Minutes 0-95 95-105 -179 -180 Total Solids Concentration g/100 g 6.1 4.6 11.9 3.9 Composition of the Fractions % on Dry Substance Monosaccharides 1.1 20.6 3.2 00 Disaccharides 32.0 17.1 0.1- 00 Betaine 2.5 57.4 94.9 87.0 Others 64.4 4.9 1.8 13.0 3 The feed capacity was 12.5 kg ds/h/m . The betaine fraction (Fraction 3) contained nearly 95% of ds betaine. Betaine was recovered from the betaine fraction, Fraction 3, by crystallization as described below in Example 8. Fraction 1 was * discarded, and Fractions 2 and 4 were re¬ turned to the system in the next batch. The final run off from the crystallizations was also returned to the feed to the second separation step (Figure 7) . Examp *-le 8 Crystallization of betaine monohydrate Beet molasses was separated by large scale chroma- tography in two steps as described in Example 7. In the tv/o step fractionation process, the betaine yield is 86% and the purity of the betaine solution 90%. The dilute betaine solution was evaporated to 76 weight percent concentration. The concentrated solution was seeded with betaine monohydrate crystals, and betaine monohydrate was crystallized at 80-85°C. under a vacuum of 130-180 millibar. The yield of betaine crystals was 55% (dry basis) and the purity of the crystals was 99.5%. The crystallization time was 4 hours. The crystals were se¬ parated from the mother liquor by centrifugation in a conventional sugar centrifuge. From the run off syrup anhydrous betaine was crystallized as in Example 2. The final run off syrup was recirculated to the separation as shown in the scheme of Figure 7. The total betaine yield was 84.7%. Example 9 Crystallization of anhydrous betaine A betaine solution of 90% purity was prepared as in Example 7. The solution was evaporated to 79% concen¬ tration and seeded with anhydrous betaine crystals. An- hydrous betaine was crystallized at 90-95 C. under a vacuum of 170-200 millbar. The yield was 55% and the purity of the crystals 99 %. The crystallization time was six hours. The run off syrups were treated as in Example Example 10 Chromatographic separation of inverted beet molasses Resin column Sulphonated polystyrene-divinylbenzene * cation exchange resin in Na -form. Mean dead diameter 0.42 mm. Bed height .5.2 m, diameter of column 0.225 . The resin was totally immersed in water. Eluent Water Flow rate 0.880 m 3 /h/m 2 Temperature 78°C Feed solution Enzymically inverted beet molasses. Total amount 13.2 kg dry substance as 35.5, weight % solution Composition: Monosaccharides (invert sugar) 70% on dry substa ce Di- and higher saccharides 3.6 % Betaine 5.7 % Others 20.7 % The chromatgraphic separation was carried out as described previously. From the effluent 5 fractions were collected. The analysis is shown in table 7 and the se¬ paration is presented graphically in Figure 11. Fraction 1 is a waste fraction, fractions 2 and 5 are recycled and fraction 3 and 4 collected as product fractions. The betaine fraction contains 85 % of the betaine present in the feed. (Fraction 4) The betaine fraction is fed to an ion-exchange column, which absorbes the betaine, while the sugars are not absorbed. The eluted sugar solution is combined with the sugar product fraction (Fraction 3) from the chroma¬ tographic separation. The ion-exchanger is then eluted with, diluted ammonia solution to recover the absorbed betaine. From the eluted solution betaine is crystallized as anhydrous betaine as described previously. Table 7 CHROMATGRAPHIC SEPARATION OF INVERTED MOLASSES. COMPOSITION OF FRACTIONS. Fraction 1 2 3 4 5 Time (minutes) 0-65 -75 -105 -145 -155 Total solids kg 2.7 1.0 4.8 4.5 0.1 Concentration g/100 g 7.4 16.2 25.0 18.0 2.3 Composition of fractions in % on dry substance Monosaccharides (invert sugar) 12.1 58.4 92.3 85.0 5.2 Di- and higher saccharides 10.5 8.0 2.5 0.0 0.0 Betaine 0.0 0.0 1.1 14.1 40.4 Others 77.4 33-.6 4.1 • 0.9 54.4 Fraction 4 is the betaine fraction and fraction 3 the invert sugar fraction. The betaine fraction contains 14.1 % betaine and 85 % invert sugar but only traces of other substance. When the betaine-rich fraction is sub- jected to ion-exchange treatment a purified betaine is recovered.

Claims: Claims : 1. A process for recovering betaine from molasses which comprises: (a) diluting the molasses to provide a diluted molasses having a solids content within the approxi¬ mate range of 20-50%, (b) providing a chromatographic column of a salt of a polystyrene sulfonate cation exchange resin cross-coupled with from about 2 to about 12 weight percent of divinylbenzene, the resin being of uni¬ form particle size and having a mean particle size within the range of about 20 to 400 U.S. ' mesh; (c) submerging the column of resin in water, (d) introducing the diluted molasses in uniform supply to the resin surface at the top of the column, (e) eluting the molasses from the column with water to provide an eluate, and (f) recovering from the downstream side of the resin bed a' fraction which consists principally of betaine. 2. The process of Claim 1 wherein the fraction consisting principally of betaine is concentrated by eva¬ poration to a slids content of about 80% by weight, the concentrated solution is seeded with betaine crystals , the solution is subjected to crystallization procedures at 75-95 C. with the application of vacuum, and the an¬ hydrous betaine crystals thus obtained are separated from the solution, leaving a run off syrup. 3. The process of Claim 2 wherein the run off syrup from the crystallization process is recycled to the diluted molasses feed solution. 4. The process of Claim 2 wherein the anhydrous betaine crystals obtained by the crystallization process are dissolved in water to form a solution having about 60% solids, the solution is subjected to a color removal step provided by activated carbon treatment and filtra¬ tion, and the betaine is recrystallized as monohydrate crystals from the solution at 80°C. to recover crystals having a purity of nearly 100% betaine. 5. A process for recovering betaine from molasses which comprises: (a) diluting the molasses to provide a diluted molasses having a solids content within the approxi¬ mate range of 25-50%, (b) providing a column of a salt of a polystyre¬ ne sulfonate cation exchange resin cross-coupled with from about 2 to about 12 weight percent of divinylbenzene, the resin being of uniform particle size and having a mean particle size within the range of about 20 to 400 U.S. mesh, (c) submerging the column of resin in water, (d) introducing the diluted molasses to the column in uniform supply to the resin surface at the top of the column at a flow rate of 0.5 to 2.0 cubic meters per hour per square* meters of the cross-sec¬ tion of the resin column, (e) eluting the molasses from the column with water to provide an eluate, and (f) recovering from the downstream side of the resin bed, (1) a first waste fraction, (2) a second fraction containing a substan¬ tial proportion of the sugars of the feed solu¬ tion, and (3) a third fraction consisting principally of betaine. 6. The process of Claim 5 wherein the third frac¬ tion consisting principally of betaine is concentrated by evaporation to a solids content within the range of about 77 to 81% by weight, the concentrated solution is seeded with betaine crystals, the solution is subjected to crystallization procedures at 75-85 C. with the appli¬ cation of vacuum, and the anhydrous betaine crystals thus obtained are separated from the solution leaving a run off syrup. 7. The process of Claim 6 wherein the run off syrup from the crystallization process is recycled to the diluted molasses feed solution. 8. The process of Claim 6 wherein the anhydrous betaine crystals obtained by the crystallization process are dissolved in water, the solution subjected to a color removal step provided by activated carbon treatment and filtration, and the betaine is recrystallized as mono¬ hydrate crystals from the solution at about 80 C. to recover crystals having a purity of nearly 100% betaine. 9. The process of Claim 1 wherein the fraction which consists principally of betaine is concentrated to about 35-40% solids to form a concentrated crude betaine feed solution, the concentrated feed solution is intro¬ duced in uniform supply to a water-submerged chromato- graphic column as described in Claim 1 , and there is re¬ covered from the downstream side of the column, a waste fraction and a betaine fraction of purity substantially higher than that of the concentrated feed solution. 10. The process of Claim 9 wherein the fractions are seclected to include fractions of lesser purity for recycling. 11. The process of Claim 9 wherein the recovered betaine fraction is concentrated by evaporation to a solids content within the range of about 77 to 81% by weight, the concentrated solution is seeded with betaine crystals, the solution is subjected to crystallization procedures at 85-95°C. with the application of vacuum, and the anhydrous betaine crystals thus obtained are separated from the solution leaving a run off syrup. 2 ? 12. A process for recovering betaine from inverted molasses which comprises: (a) diluting the inverted molasses to provide a diluted solution having a solids content within the approximate range of 20-50%, (b) providing a chromatographic column of a salt of a polystyrene sulfonate cation exchange resin cross- coupled with from about 2 to about 12 weight percent of divinylbenzene, the resin being of uniform particle size within the range of about 20 to 400 U.S. mesh; (c) submerging the column of resin in water, (d) introducing the diluted molasses in uniform supply to the resin surface at the top of the column, (e) eluting the molasses from the column with water to provide an eluate, and (f) recovering from the downstream side of the resin bed a fraction which consists procinpally of betaine. 13. The process of Claim 12 wherein the fraction consisting principally of betaine and containing a part of the invert sugar monosaccharides, is purified and concentrated by ion-exchange treatment, the betaine being eluted from the ion-exchnage column by diluted ammonia and crystallized from the neutralized solution. 14. The process of Claim 13 wherein the invert sugar fraction from the ion-exchange column is combined with the sugar fraction from the chromatographic separa¬ tion. 15. The process of Claim 13 wherein the anhydrous betaine crystals obtained by the crystallization process are dissolved in water to form a solution- having about 60 % solids, the solution is subjected to a color removal step provided by activated carbon treatment and filtra¬ tion, and the betaine is recrystallized as monohydrate crystals from the solution at 80 C. to recover crystals having a purity of nearly 100 % betaine. 16. The process of Claim 15 wherein the run off syrup from the crystalliztion process is recycled to the diluted molasses feed solution.

Inventors: HEIKKILAE H, MELAJA J, MILLNER D, VIRTANEN J
Applicants: SUOMEN SOKERI OY
Application year: 1981
Main classification: C07C101
IPC codes: B01D15, B01J39, C07C227, C07C229, C07D273, C13D3, C13J1