PROCESS FOR SEPARATING MALTOSE FROM MIXTURES OF MALTOSE WITH GLUCOSE OR OTHER SACCHARIDES

Abstract: Maltose is selectively separated from mixtures of maltose with glucose or DP3 or DP4+ polysaccharides by contacting the mixture with an adsorbent comprising a low aluminium Y-type zeolite having up to 15 atoms of aluminium per unit cell, under maltose adsorption conditions, and thereafter contacting the maltose-containing adsorbent with a desorbent comprising water under desorbent conditions selected to recover high purity maltose.

Description: Maltose (malt sugar) is a reducing sugar widely used as a nutrient or sweetener in the food industry. It is also used as a culture medium and stabilizer for polysulphides. It is primarily obtained by the enzymatic action of diastase or beta-amylase on starch. Starch hydrolysate may contain approximately 72% of maltose, 1% of glucose and 27% of higher polysaccharides. At the present time, there are no known methods for commercially extracting the maltose present in starch hydrolysate from polysaccharides having a degree of polymerization (DP) greater than glucose. GB-A-1585369 discloses a process for separating a monosaccharide, such as fructose or glucose, from an oligosaccharide, such as maltose, using X zeolites exchanged with Ba or K cations, or Y zeolites exchanged with Ba, Sr, Ca, Cs, Na or NH₄. This process, however, is not capable of separating maltose from glucose and a polysaccharide. This invention relates to a process for separating maltose from a sugar source containing a mixture of maltose and at least one other sugar. Specifically, the invention is concerned with a process for separating the recovering high purity maltose from a sugar source which contains glucose and/or polysaccharides having a DP of 3, 4 and higher, including starch or other high DP polysaccharides. More specifically, the invention concerns the use of a faujasite adsorbent having a very low aluminium content and particularly, up to 15 atoms of aluminium per unit cell. The faujasites are useful because they have a pore size large enough to admit the sugar molecules being adsorbed. Silicalite and ZSM-5, on the other hand, have pore sizes too small to admit the saccharide molecules and, hence, are not effective for this separation. The preferred faujasite adsorbents contain up to 9 aluminium atoms per unit cell and more preferably, from 5 to 9 aluminium atoms per unit cell. As hereinbefore set forth, the present invention is concerned with a process for separating maltose from an aqueous mixture containing maltose and at least one other saccharide. The process is effected by passing a feed mixture containing one or more components over an adsorbent of the type hereinafter described in greater detail. The passage of the feed stream over the adsorbent will result in the adsorption of maltose, while permitting the other components of the feed stream to pass through the treatment zone in an unchanged condition. Thereafter, the maltose will be desorbed from the adsorbent by treating the adsorbent with a desorbent material, preferably water. Preferred adsorption and desorption conditions include a temperature of from 20 to 200°C and a pressure of from atmospheric to 500 psig (100 to 3550 kPa), more preferably atmospheric to 250 psig (100 to 1825 kPa) to ensure a liquid phase. The most particularly preferred conditions are 65°C and about 50 psig (445 kPa). In the accompanying Drawings Figure 1 is a chromatographic trace showing separation of maltose from glucose and higher oligosaccharides, i.e., having a degree of polymerization of 3, 4 and more by an adsorbent comprising dealuminated Y faujasite. Figure 2 is a chromatographic trace showing separation of maltose from glucose and oligosaccharides. Figure 3 is a chromatographic trace showing separation of maltose from oligosaccharides DP3 and DP4+. For purposes of this invention, the various terms which are hereinafter used may be defined in the following manner. A "feed mixture" is a mixture containing one or more extract components and one or more raffinate components to be separated by the process. The term "feed stream" indicates a stream of a feed mixture which passes to the adsorbent used in the process. An "extract component" is a compound or type of compound that is more selectively adsorbed, while a "raffinate component" is a compound or type of compound that is less selectively adsorbed. The term "desorbent material" means generally a material capable of desorbing an extract component. The term "desorbent stream" or "desorbent input stream" means a stream in which desorbent material passes to the adsorbent. The term "raffinate stream" or "raffinate output stream" means a stream in which a raffinate component is removed from the adsorbent. The composition of the raffinate stream can vary from essentially 100% desorbent material to essentially 100% raffinate components. The term "extract stream" or "extract output stream" means a stream in which an extract material which has been desorbed by a desorbent material is removed from the adsorbent. The composition of the extract stream, likewise, can vary from essentially 100% desorbent material to essentially 100% extract components. At least a portion of the extract stream and preferably, at least a portion of the raffinate stream from the adsorption -desorption process, are passed to separation means, typically fractionators, where at least a portion of desorbent material is separated to produce an extract product and a raffinate product. The terms "extract product" and "raffinate product" mean products produced by the process containing, respectively, an extract component and a raffinate component in higher concentrations than those found in the extract stream and the raffinate stream. The feed mixtures which are separated by the process of the present invention are mixtures containing maltose; a specfic mixture, which is preferably treated according to the present invention, comprising starch hydrolysate. As hereinbefore discussed, starch hydrolysate will contain about 72% of maltose, as well as other sugars and polysaccharides such as glucose, maltotriose (DP3), DP4 and higher (hereinafter DP4+) and starch, said other sugars and polysaccharides being present in varying amounts. The adsorbents used according to the present invention have been found to adsorb maltose selectively, while allowing the other components in the mixture to pass unchanged through the system. It has also been found that the initial capability of the adsorbent selectively to adsorb maltose is maintained during the actual use in the separation process over an economically desirable life. In addition, as previously set forth, the adsorbent possesses the ability to separate components of the feed, that is, the adsorbent possesses adsorptive selectivity for one component over other components. The adsorbents used in the separation process of this invention are the so-called dealuminated Y-type zeolites e.g. those obtained from Toyo Soda Manufacturing Co., Ltd., of Shinnanyo, Japan, having respectively 15, 9 and 5 aluminium atoms per unit cell. It has been determined that zeolites of this type which are not dealuminated, and have 38 aluminium atoms per unit cell, will not effect the desired separation between maltose and either glucose or polysaccharides, which appears to indicate an upper limit to the amount of aluminium in the zeolitic structure. Furthermore, it appears that the lower the aluminium content, the greater the separation between maltose and glucose. The zeolites may be made by one or more of the processes described by Julius Scherzer, Catalytic Materials, Amer. Chem. Soc ., 1984, pp. 157-200, but preferably by the thermal dealumination process described on pages 158-161 involving the hydrothermal treatment of NH₄ Y zeolite, or described in US-A-3293192, to form the class of dealuminated Y zeolites referred to as "ultrastable". The number of aluminium atoms per unit cell of each sample used was determined by x-ray diffractometry measurement of the cell dimension, and comparing the dimension with previously recorded cell dimensions correlated with aluminium content. Relative selectivity can be expressed not only for one feed compound over another, but can also be expressed between any feed mixture component and the desorbent material. The selectivity, (B), is defined as the ratio of the two components of the adsorbed phase divided by the ratio of the same two components in the unadsorbed phase at equilibrium conditions, as shown in Equation 1, below: where C and D are two components of the feed represented in weight percent, and the subscripts A and U represent the adsorbed and unadsorbed phases respectively. The equilibrium conditions are determined when the feed passing over a bed of adsorbent does not change composition after contacting the bed of adsorbent. In other words, there is no net transfer of material between the unadsorbed and adsorbed phases. Where selectivity of the adsorbent for two components approaches 1.0, there is no preferential adsorption by the adsorbent of one component over the other; they are both adsorbed (or non-adsorbed) to about the same degree. As the value of (B) becomes less than or greater than 1.0, there is a preferential adsorption by the adsorbent of one component over the other. When comparing the selectivity by the adsorbent of one component C over component D, a (B) value larger than 1.0 indicates preferential adsorption of component C within the adsorbent. A (B)value less than 1.0 would indicate that component D is preferentially adsorbed, leaving an unadsorbed phase richer in component C and an adsorbed phase richer in component D. Ideally, desorbent materials should have a selectivity of 1 or slightly less than 1 with respect to all extract components, so that all of the extract components can be desorbed as a class with reasonable flow rates of desorbent material and so that extract components can displace desorbent material in a subsequent adsorption step. While separation of an extract component from a raffinate component is theoretically possible when the selectivity of the adsorbent for the extract component with respect to the raffinate component is just slightly greater than 1.0, it is preferred that such selectivity should approach a value of 2.0. Like relative volatility, the higher the selectivity, the easier the separation is to perform. Higher selectivities permit a smaller amount of adsorbent to be used. The third important characteristic is the rate of exchange of the extract component of the feed mixture material, or, in other words, the relative rate of desorption of the extract component. This characteristic relates directly to the amount of desorbent material that must be employed to recover the extract component from the adsorbent; faster rates of exchange reduce the amount of desorbent material needed to remove the extract component and therefore permit a reduction in operating costs. With faster rates of exchange, less desorbent material has to be pumped through the process, and separated from the extract stream for reuse in the process. Desorbent materials used in various prior art adsorptive separation processes vary depending upon such factors as the type of operation employed. In the swing-bed system, in which the selectively adsorbed feed component is removed from the adsorbent by a purge stream, desorbent selection is not as critical, and desorbent material comprising gaseous hydrocarbons such as methane, ethane, etc., or other types of gases, such as nitrogen or hydrogen, may be used at elevated temperatures or reduced pressures, or both, to purge effectively the adsorbed feed component from the adsorbent. However, in adsorptive separation processes which are generally operated continuously at substantially constant pressures and temperatures to ensure liquid phase, the desorbent material must be judiciously selected to satisfy many criteria. Firstly, the desorbent material should displace an extract component from the adsorbent with reasonable mass flow rates without itself being so strongly adsorbed as unduly to prevent an extract component from displacing the desorbent material in a subsequent adsorption cycle. Expressed in terms of the selectivity (hereinbefore discussed in more detail), it is preferred that the adsorbent be more selective for all of the extract components over a raffinate component, than it is for the desorbent material over a raffinate component. Secondly, desorbent materials must be compatible with the particular adsorbent and the particular feed mixture. More specifically, they must not reduce or destroy the critical selectivity of the adsorbent for an extract component over a raffinate component. Additionally, desorbent materials should not chemically react with, or cause a chemical reaction of, either an extract component or a raffinate component. Both the extract stream and the raffinate stream are typically removed from the adsorbent in admixture with desorbent material, and any chemical reaction involving a desorbent material and an extract component, or a raffinate component, or both, would complicate or prevent product recovery. Since both the raffinate stream and the extract stream typically contain desorbent materials, such desorbent materials should additionally be substances which are easily separable from the feed mixture that is passed into the process. Without a method of separating at least a portion of the desorbed material present in the extract stream and the raffinate stream, the concentration of an extract component in the extract product, and the concentration of a raffinate component in the raffinate product, would not be very high, nor would the desorbent material be available for further use in the process. It is contemplated that at least a portion of the desorbent material will be separated from the extract and the raffinate streams by distillation or evaporation, but other separation methods, such as reverse osmosis, may also be employed, alone or in combination with distillation or evaporation. Since the raffinate and extract products of the present invention are foodstuffs intended for human consumption, desorbent materials should also be non-toxic. Finally, desorbent materials should also be materials which are readily available and, therefore, reasonable in cost. A dynamic testing apparatus is employed to test various adsorbents with a particular feed mixture and desorbent material, to measure the adsorbent characteristics of adsorptive capacity, selectivity and exchange rate. The apparatus comprises an adsorbent chamber of approximately 70 ml volume, having inlet and outlet portions at opposite ends of the chamber. The chamber is contained within a temperature control means and, in addition, pressure control equipment is used to operate the chamber at a constant predetermined pressure. Quantitative and qualitative analytical equipment, such as refractometers, polarimeters and chromatographs, can be attached to the outlet line of the chamber, and used to detect quantitatively or determine qualitatively, one or more components in the effluent stream leaving the adsorbent chamber. A pulse test, performed using this apparatus and the following general procedure, is used to determine selectivities and other data for various adsorbent systems. The adsorbent is filled to equilibrium with a particular desorbent material by passing the desorbent material through the adsorbent chamber. At a convenient time, a pulse of feed containing known concentrations of maltose, glucose and other oligosaccharides, all diluted in desorbent, is injected for a duration of several minutes. Desorbent flow is resumed, and the maltose, glucose and other oligosaccharides are eluted as in a liquid-solid chromatographic operation. The effluent can be analyzed on-stream or, alternatively, effluent samples can be collected periodically and later analyzed separately by analytical equipment and traces of the envelopes of corresponding component peaks developed. From information derived from the test, adsorbent performance can be rated in terms of void volume, retention volume for an extract or a raffinate component, selectivity for one component over the other, and the rate of desorption of an extract component by the desorbent. The retention volume of an extract or a raffinate component may be characterized by the distance between the centre of the peak envelope of an extract or a raffinate component and the peak envelope of the tracer component, or some other known reference point. It is expressed in terms of the volume in cubic centimeters of desorbent pumped during this time interval, represented by the distance between the peak envelopes. Selectivity, (B), for an extract component over a raffinate component, may be characterized by the ratio of the distance between the centre of the extract component peak envelope and the tracer peak envelope (or other reference point) to the corresponding distance between the centre of the raffinate component peak envelope and the tracer peak envelope. The rate of exchange of an extract component with the desorbent can generally be characterized by the width of the peak envelopes at half intensity. The narrower the peak width, the faster the desorption rate. The desorption rate can also be characterized by the distance between the centre of the tracer peak envelope and the disappearance of an extract component which has just been desorbed. This distance is again the volume of desorbent pumped during this time interval. The adsorbent may be employed in the form of a dense compact fixed bed, which is alternately contacted with the feed mixture and desorbent materials. In the simplest embodiment of the invention, the adsorbent is employed in the form of a single static bed, in which case the process is only semi-continuous. In another embodiment, a set of two or more static beds may be employed in fixed-bed contact with appropriate valving, so that the feed mixture is passed through one or more adsorbent beds while the desorbent materials can be passed through one or more of the other beds in the set. The flow of feed mixture and desorbent materials may be either upwards or downwards through the desorbent. Any conventional apparatus employed in static bed fluid-solid contacting may be used. Countercurrent moving bed or simulated moving bed countercurrent flow systems, however, have a much greater separation efficiency than fixed adsorbent bed systems and are, therefore, preferred. In the moving bed or simulated moving bed process, the adsorption and desorption operations are continuously taking place, which allows both continuous production of an extract and a raffinate stream and the continual use of feed and desorbent streams. One preferred embodiment of this process utilizes what is known in the art as the simulated moving bed countercurrent flow system. The operating principles and sequence of such a flow system are described in US-A-2985589. In such a system, it is the progressive movement of multiple liquid access points down an adsorbent chamber that simulates the upward movement of adsorbent contained in the chamber. Only four of the access lines are active at any one time: those for the feed input stream, desorbent inlet stream, raffinate outlet stream, and extract outlet stream. Coincident with this simulated upward movement of the solid adsorbent, is the movement of the liquid occupying the void volume of the packed bed of adsorbent. So that countercurrent contact is maintained, a liquid flow down the adsorbent chamber may be provided by a pump. As an active liquid access point moves through a cycle, that is, from the top of the chamber to the bottom, the chamber circulation is pumped through different zones which require different flow rates. A programmed flow controller may be provided to set and regulate these flow rates. The active liquid access points effectively divide the adsorbent chamber into separate zones, each of which has a different function. In this embodiment of the present process, it is generally necessary that three separate operational zones are present in order for the process to take place, although, in some instances, and optional fourth zone may be used. The adsorption zone, zone 1, is defined as that portion of the adsorbent located between the feed inlet stream and the raffinate outlet stream. In this zone, the feedstock contacts the adsorbent, an extract component is adsorbed, and a raffinate stream is withdrawn. Since the general flow through zone 1 is from the feed stream which passes out of the zone, the flow in this zone is considered to be in a downstream direction when proceeding from the feed inlet to the raffinate outlet streams. Immediately upstream with respect to fluid flow in zone 1 is the purification zone, zone 2. The purification zone is defined as that portion of the adsorbent between the extract outlet stream and the feed inlet stream. The basic operations taking place in zone 2 are the displacement, from the non-selective void volume of the adsorbent, of any raffinate material carried into zone 2 by the shifting of adsorbent into this zone, and the desorption of any raffinate material adsorbent within the selective pore volume of the adsorbent or adsorbed on the surfaces of the adsorbent particles. Purification is achieved by passing a portion of extract stream material leaving zone 3 into zone 2 at the upstream boundary of zone 2 (the extract outlet stream), to effect the displacement of raffinate material. The flow of material in zone 2 is in a downstream direction from the extract outlet stream to the feed inlet stream. Immediately upstream of zone 2 with respect to the fluid flowing in zone 2, is the desorption zone, or zone 3. The desorption zone is defined as that portion of the adsorbent between the desorbent inlet and the extract outlet streams. The function of the desorption zone is to allow a desorbent material which passes into this zone to displace the adsorbed material produced by contact with feed in zone 1 in a previous cycle of operation. The flow of fluid in zone 3 is essentially in the same direction as that of zones 1 and 2. In some instances, an optional buffer zone, zone 4, may be utilized. This zone, defined as that portion of the adsorbent between the raffinate outlet stream and the desorbent inlet stream, if used, is located immediately upstream with respect to the fluid flow to zone 3. Zone 4 would be utilized to conserve the amount of desorbent utilized in the desorption step, since a portion of the raffinate stream which is removed from zone 1 can be passed into zone 4 to displace desorbent material from that zone into the desorption zone. Zone 4 will contain enough adsorbent so that raffinate material present in the raffinate stream passing out of zone 1 and into zone 4 can be prevented from passing into zone 3, thereby contaminating the extract stream removed from zone 3. When the fourth operational zone is not utilized, the raffinate stream passing from zone 1 to zone 3 must be carefully monitored in order that the flow directly from zone 1 to zone 3 can be stopped when there is an appreciable quantity of raffinate material present in the raffinate stream passing from zone 1 into zone 3 so that the extract outlet stream is not contaminated. A cyclic advancement of the input and output streams through the fixed bed of adsorbent can be accomplished by utilizing a manifold system, in which the valves in the manifold are operated in a sequential manner to effect the shifting of the input and output streams, thereby allowing a flow of fluid with respect to solid adsorbent in a countercurrent manner. Another mode of operation which can effect the countercurrent flow of solid adsorbent with respect to fluid involves the use of a rotating disc valve in which the input and output streams are connected to the valve and the lines, through which pass the feed input, extract output, desorbent input and raffinate output streams, are advanced in the same direction through the adsorbent bed. Both the manifold arrangement and disc valve are known in the art. Specifically, rotary disc valves which can be utilized in this operation are described in US-A-3040777 and 3422848. In many instances, one operational zone will contain a much larger quantity of adsorbent than some other operational zone. For instance, on some operations the buffer zone can contain a minor amount of adsorbent as compared to the adsorbent required for the adsorption and purification zones. It can also be seen that when a desorbent is used which can easily desorb extract material from the adsorbent, a relatively small amount of adsorbent will be needed in a desorption zone as compared to the amount needed in the buffer zone or adsorption zone or purification zone or all of them. Since it is not required that the adsorbent be located in a single column, the use of multiple chambers or a series of columns is within the scope of the invention. It is not necessary that all of the input or output streams be simultaneously used, and in fact, in many instances, some of the streams can be shut off while others effect an input or output of material. The apparatus which can be utilized to effect the process of this invention, can also contain a series of individual beds connected by connecting conduits upon which are placed input or output taps to which the various input or output stream can be attached and alternatively and periodically shifted to effect continuous operation. In some instances, the connecting conduits can be connected to transfer taps which, during normal operation, do not function as a conduit through which material passes into or outof the process. It is contemplated that at least a portion of the extract output stream will pass into a separation means wherein at least a portion of the desorbent material can be separated to produce an extract product containing a reduced concentration of desorbent material. Preferably, but not necessary to the operation of the process, at least a portion of the raffinate output stream will also be passed to a separation means wherein at least a portion of the desorbent material can be separated to produce a desorbent stream which can be reused in the process and a raffinate product containing a reduced concentration of desorbent material. Separation will typically be by crystallization. The design and operation of crystallization apparatus is well known in the separation art. Although both liquid and vapour phase operations can be used in many adsorptive separation processes, liquid-phase operation is preferred for this process because of the lower temperature requirements and because of the higher yields of extract product that can be obtained with liquid-phase operation compared with those obtained with vapour-phase operation. Adsorption conditions will include a temperature from 20 to 200°C, with 20 to 100°C being more preferred, and a pressure from atmospheric (100 kPa) to 500 psig (3550 kPa), with from atmospheric (100 kPa) to 250 psig (1825 kPa) being more preferred to ensure maintenance of liquid phase. Desorption conditions will include the same range of temperatures and pressures as used for adsorption conditions. The size of the units which can utilize the process of this invention can vary anywhere from those of pilot plant scale (see for example US-A-3706812) to those of commercial scale, and can range in flow rates from as little as a few ml's an hour up to many thousands of litres per hour. Another embodiment of a simulated moving bed flow system suitable for use in the process of the present invention is the cocurrent high efficiency simulated moving bed process disclosed in US-A-4402832 and 4478721. This process may be preferred, because of its energy efficiency and lower capital intensity, when products of slightly lower purity are acceptable. The Examples below present test results for various adsorbent and desorbent materials when using the previously described dynamic testing apparatus. EXAMPLE 1 In this Example, a test was run using a dealuminated Y-type zeolite having 9 aluminium atoms per unit cell, to determine the separation of maltose from a mixture representative of that expected from an enzymatic degradation of starch by beta-amylase or diastase. The dealuminated Y-type zeolite of this example was bound in Bentolite clay and had an average bulk density of 0.536 g/ml. The adsorbent was packed in an 8.4 mm diameter column having a total volume of 70 ml. The feed mixture consisted of 10 g of the carbohydrate mixture given in Table 1 diluted with 10 g of distilled water, resulting in a solution containing 50% of solids. Maltrin 150 is a commercially available mixture containing 88% of saccharides having a degree of polymerization of 4 or more (DP4+), 8.1% of maltotriose, having a DP of 3, about 3% of maltose and less than 2% of glucose. The experiment began by passing a water desorbent through the column at a flow rate of 1.4 ml/min. and a temperature of 65°C. At a convenient time, 2 ml of feed was injected into the column after which flow of desorbent was immediately resumed. Figure 1 provides a graphical representation of the retention by the adsorbent of the various sugars in the feed. A consideration of the centre of the peak envelope for each concentration curve reveals separation of maltose from the other feed mixture sugars. While a substantial portion of the maltose curve does lie within the glucose curve, there is adequate maltose/glucose selectivity, as seen by the differences in retention volume (Δ R.V.) shown in Table 2; B (selectivity) maltose/glucose is 1.18, calculated in the manner discussed heretofore. Excellent selectivity of the adsorbent for maltose compared to the DP3 and DP4+ component was found shown by the large Δ R.V. in Table 2. EXAMPLE 2 To show the separation of maltose by an adsorbent with a different amount of aluminium in the crystalline structure, another test was run in the same testing apparatus using a Y-type zeolite having 5 aluminium atoms per unit cell. The zeolite was bound with silica, which had no effect on the separation. The feed mixture consisted of the following: The pulse test was conducted in the same manner was Example 1. Figure 2 shows graphically the relative retention of the sugars by the adsorbent. By considering the locations of the centres of the peak envelopes for each component, it is apparent that a good separation of maltose from glucose and from DP3 and DP4 was obtained. The difference between the retention volumes peaks of maltose and glucose is 3.5 ml and between maltose and DP3 + DP4+ is 12.0 ml. B maltose/glucose = 1.3; B maltose/maltotriose = 1.95. In a computer simulation of a separation based on the above data and Figure 2, the material balance in Table 4 was obtained using a feed having the following composition (all on a dry solids basis). Maltose 72.0% Glucose 1.0 DP3 13.0 DP4+ 14.0 Others 0.0 The adsorbent was the same faujasite used in the first part of this Example having 5 aluminium atoms per unit cell. The total volume of adsorbent used was 2553.1 cu. ft. (72.3 m³) weight 127,654 lbs. (57.955 tonnes). The simulation was based on a countercurrent simulated moving bed system described hereinabove and in US-A-2985589, with 24 beds, each 7.4 ft. (2.26 m) in diameter and 2.5 ft. (0.76 m) high. The selectivity of maltose/glucose was 1.36. The selectivity of maltose/DP3 is 1.95. The selectivity of maltose/DP4+ is very high, since the DP4+ component is adsorbed in minute quantities only. EXAMPLE 3 Another pulse test was conducted with the same feed mixture, using a dealuminated Y faujasite zeolite having 15 aluminium atoms per unit cell. Figure 3 shows the separation of maltose from DP3 and DP4+, but glucose is eluted at the same time as the maltose with no separation. The difference between the retention volume peaks of maltose and DP3 and DP4+ is 8.5, and good separation can be achieved thereby. No separation is achieved between maltose and glucose (R.V. = 0 and B maltose/glucose = 0.85). EXAMPLE 4 Example 2 was repeated, except that the faujasite had 38 aluminium atoms per unit cell. As in Example 3, the glucose is eluted with the maltose. Maltotriose has less than 1 ml difference in retention volume, indicating that no separation of maltose from either glucose or DP3 saccharides is practically realized.

Claims: A process for separating maltose from a mixture of maltose with glucose and/or a polysaccharide characterized by contacting said mixture at adsorption conditions with an adsorbent comprising a dealuminated Y-type zeolite, thereby selectively adsorbing said maltose, removing the nonadsorbed portion of said mixture from contact with said adsorbent and thereafter recovering high purity maltose by contacting the resulting maltose-containing adsorbent with a desorbent comprising water at desorption conditions. A process according to Claim 1 characterized in that said dealuminated Y-type zeolite has up to 15 aluminium atoms per unit cell. A process according to Claim 1 or 2 wherein characterized in that said dealuminated Y-type zeolite has 5 to 9 aluminium atoms per unit cell. A process according to any one of Claims 1 to 3 characterized in that said adsorption and desorption conditions include a temperature range from 20 to 100°C and a pressure from atmospheric to 250 psig (100 to 1825 kPa). A process according to any one of Claims 1 to 4 characterized in that said mixture comprises maltose, glucose and at least one polysaccharide. A process according to any one of Claims 1 to 5 characterized in that said polysaccharide has a degree of polymerization of 3 or greater. A proces according to any one of Claims 1 to 5 characterized in that said polysaccharide is maltotriose. A process according to any one of Claims 1 to 7 characterized in that the mixture is produced by the enzymatic action of diastase or beta-amylase on starch.

Inventors: GOODMAN, WALTER HUGH
Applicants: UOP (A NEW YORK GENERAL PARTNERSHIP)
Application year: 1987
Main classification: C13K7
IPC codes: C07H1, C13K7, C07H3