CA1215361A - Process for producing a high-purity maltose - Google Patents
Process for producing a high-purity maltoseInfo
- Publication number
- CA1215361A CA1215361A CA000408629A CA408629A CA1215361A CA 1215361 A CA1215361 A CA 1215361A CA 000408629 A CA000408629 A CA 000408629A CA 408629 A CA408629 A CA 408629A CA 1215361 A CA1215361 A CA 1215361A
- Authority
- CA
- Canada
- Prior art keywords
- maltose
- fraction
- column
- glucose
- exchange resin
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
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Classifications
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07H—SUGARS; DERIVATIVES THEREOF; NUCLEOSIDES; NUCLEOTIDES; NUCLEIC ACIDS
- C07H3/00—Compounds containing only hydrogen atoms and saccharide radicals having only carbon, hydrogen, and oxygen atoms
- C07H3/04—Disaccharides
-
- C—CHEMISTRY; METALLURGY
- C13—SUGAR INDUSTRY
- C13K—SACCHARIDES OBTAINED FROM NATURAL SOURCES OR BY HYDROLYSIS OF NATURALLY OCCURRING DISACCHARIDES, OLIGOSACCHARIDES OR POLYSACCHARIDES
- C13K7/00—Maltose
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- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Life Sciences & Earth Sciences (AREA)
- Biochemistry (AREA)
- Health & Medical Sciences (AREA)
- Engineering & Computer Science (AREA)
- Biotechnology (AREA)
- General Health & Medical Sciences (AREA)
- Genetics & Genomics (AREA)
- Molecular Biology (AREA)
- Saccharide Compounds (AREA)
- Preparation Of Compounds By Using Micro-Organisms (AREA)
Abstract
PROCESS FOR PRODUCING A HIGH-PURITY MALTOSE
Abstract of the Disclosure An invention providing a process for producing a high purity maltose is disclosed.
More precisely, the invention relates to a process for producing a high-purity maltose, comprising applying a material starch sugar solution with a maltose content of at least 70 %
to a column packed with a strongly-acidic cation exchange resin of alkali metal- or alkaline earth metal-form; fractionating by charging thereto water the solution into HIGH-DEXTRIN FRACTION, HIGH-DEXTRIN-MALTOSE FRACTION, HIGH-MALTOSE FRACTION, HIGH-MALTOSE-GLUCOSE FRACTION, and HIGH-GLUCOSE FRACTION, in the givn order; and recovering the HIGH-MALTOSE FRACTION.
In comparison with any conventional processes for pro-ducing a high-purity maltose with the use of ion exchange resin, the practise of the invention does constantly provide a fraction with a maltose content of 93 % or higher, and enable industrial-scale production of a high-purity maltose much easier at lower-cost.
Abstract of the Disclosure An invention providing a process for producing a high purity maltose is disclosed.
More precisely, the invention relates to a process for producing a high-purity maltose, comprising applying a material starch sugar solution with a maltose content of at least 70 %
to a column packed with a strongly-acidic cation exchange resin of alkali metal- or alkaline earth metal-form; fractionating by charging thereto water the solution into HIGH-DEXTRIN FRACTION, HIGH-DEXTRIN-MALTOSE FRACTION, HIGH-MALTOSE FRACTION, HIGH-MALTOSE-GLUCOSE FRACTION, and HIGH-GLUCOSE FRACTION, in the givn order; and recovering the HIGH-MALTOSE FRACTION.
In comparison with any conventional processes for pro-ducing a high-purity maltose with the use of ion exchange resin, the practise of the invention does constantly provide a fraction with a maltose content of 93 % or higher, and enable industrial-scale production of a high-purity maltose much easier at lower-cost.
Description
1;~1536~
Detailed Description of the Invention The present invention relates to a process fo~ producing a high-purity maltose.
Recently, various advantages of maltose in food products and pharmaceuticals have been established one after another, thus its uses have expanded rapidly in their productions. The expanded uses have inevitably led to increasing demands for a high-purity maltose.
Conventionally, maltose have been available as a saccha-rified starch product with a maltose content of about 40 - 50 w/w % on dry solid basis (all percentages as used in the SPECIFICATION mean "weight percentages on dry solid basis"
unless specified otherwise) which is obtainable by subjecting a liquefied starch solution to the action of malt enzyme.
Recent advances in starch saccharification technique enable a relatively easier production of a saccharified starch product with a maltose content of 50 % or higher by combination of, for example, ~-amylase with starch debranching enzyme.
The above described starch saccharification technique, however, from ecomonical and technical standpoints, render the direct production of a high-purity maltose with a maltose content of 90 % or higher much difficult.
Some attempts to obtain a high-purity maltose are dis-closed in recent patent applications which comprise applying a ~:lS;361 starch sugar solution containing maltose to a column of anion exchange resin: For example, Japan Patent Publication No.
46,290/77 discloses an attempt for producing a high-purity maltose, comprising preparing a starch sugar solution sub-stantially consisting of dextrin and about 65 % maltose, and applying the solution to an anion exchange resin of OH-form to adsorb the maltose constituent and also to remove the dextrin constituent. Since, however, in a process according to the attempt the maltose constituent is adsorbed on the anion exchange resin of OH-form, the solution should be applied to the resin at the possible lowest temperature, preferably, below 20C, to prevent the isomerization of the maltose constituent:
thus, the increase in viscosity and microbial contamination as well as low purification capability are unavoidable, and render its industrial-scale practise very difficult. Further, Japan Patent Publication No.20,579/79 discloses an attempt for producing a high-purity maltose which comprises applying a starch sugar solution, containing glucose and maltose, to a column, packed with an anion exchange resin of S032 - or SO3H -form, to fractionate the solution into the glucose- and maltose-constituents. The attempt is, however, inadequate as a process for industrial-scale production of a high-purity maltose because the bonding of S032 - or SO3H -group is labile.
The present inventors have investigated processes for a high-purity maltose using a strongly-acidic cation exchange resin, more par~icularly, of alkali metal- or alkaline earth metal-~orm, instead of anion exchange resin which has the above described disadvantages.
The efforts resulted in the finding that a high-purity maltose is easily obtainable by applying a material starch sugar solution with a maltose content of at least 70 % to a column packed with a strongly-acidic cation exchange resin of alkali metal- or alkaline earth metal-form; fractionating by charging thereto water the solution into HIHG-DEXTRIN FRACTION, HIGH-DEXTRIN-MALTOSE FRACTION, HIGH-MALTOSE FRACTION, HIGH-MALTOSE~GLUCOSE FRACTION, and HIGH-GLUCOSE FRACTION (the terms "HIGH-A FRACTION" and "HIGH-A-B FRACTION" as used in the SPECIFICATION shall mean the eluted fractions containing A, or A and B as predominant constituent(s) respectively), in the given order; and recovering the HIGH-MALTOSE FRACTION.
Also, the efforts resulted in the additional finding that the objective high-purity maltose is constantly obtainable in higher concentration and at higher recovery yield by employing a method where the material starch sugar solution is applied to the column together with the previously obtained HIGH-DEXTRIN--MALTOSE- and/or HIGH-MALTOSE GLUCOSE-FRACTIONs, and wherein the resul~ant HIGH-DEXTRIN MALTOSE- and/or HIGH-MALTOSE-GLUCOSE-FRACTIONs are applied to the column together with a fresh material starch sugar solution in the next fractionation step.
The above described findings led to the present invention.
S3~
In one aspect the invention p~ovides a proc~ss for the separation of maltose from a feed solution by the utilization of an ion exc~larlge resin, comprising: (a) providing a feed solution containing at least 7~ maltose based on the weight or the dry solid, the remainder con-sisting essentially of glucose and dextr-ns; (b) sequen-tially aamitting predetermined volumes o~ the feed solution and water to a column of a strongly acidic cation exchange resin having sulphonyl groups of an alkali metal or alkaline earth metal f~rm; (c) sequentially separating the effluents from the column into the following fractions:
a first fraction rich in dextrins, a second fraction rich in dextrins, but highly contaminated with maltose, a third fraction o` substantially pure maltose, a fourth fraction rich in maltose, but highly contamina-ted wi-th glucose, and a fifth ,~raction rich in glucose; (d) recovering the third fraction of substantially pure maltose;
(e) sequentially adrnitting into the column: the second fraction obtained in the step (c), a feed solution having a maltose content of at least 70~ based on the weight of dry solid, and the rem~inder consisting essentially of glucose and dextrin, t:~e fourth fraction obtained in the step (c), and water; and (f) repeating steps (c), (d) and (e) in a cyclic manner.
~ a -mab/v~
.~.~
i,.~ ' ~lS3~
The material starch sugar solution usable in the invention may be one of those substantially-ketose-free mixture solution of aldoses derived from starch, which gives a ~IIGH-MALTOSE
FRACTION with a maltose content of 90 %, preferably, 93 Z or higher, in a high recovery yield when subjected to the ~rac-tionation according to the invention: For example, the ma-terial starch sugar solution may be a saccharified starch solution whcih is obtainable by subjecting st~rch to the actions of starch-degrading enzymes, e.g., a- and ~-amylases, and starch-debranching enzyme, or may be an aqueous solution of a commercially-available starch sugar product, but ~heir maltose content should be at least 70 %.
The strongly-acidic cation exchange resin of alkali metal-or alkaline earth metal-form usable in the invention may be one or more members of stylene-divinylbenzene copolymer resins, for example, bearing sulphonyl groups of alkali metal- or alkaline earth metal-form, such as Na+, K+, Ca2+, or Mg2t: Commercially-available resins are, for example, Dowex 50WX2 , Dowex 50WX4 , and Dowex 501~X8 , products of Dow C~emical Company, Midland, Michigan, U.S.A., Amberlite CG-120 , a product of Rohm ~ Haas Company, Philadelphia, Pennsylvania, U.S.A., XT-1022E ~ a product of Tokyo Chemical Industries, Kita-ku, Tokyo, Japan, and Diaion* SK lB , Diaion* SK 102 , and Diaion*
SK 104 , products of Mitsubishi Chemical Industries Limited, Tokyo, Japan. All of these resins have excellent fractionating capability to obtain the HIGH-MA~TOSE FRACTION, and are highly *~ ~e mark ~l~1536~
heat- and abrasion-resistant, thus they are advantageously feasible for producing a high-purity maltose on an industrial-scale.
In the process according to the invention, the resin with a nominal particle size of about 0.01 - 0.5 mm is packed in one or more columns. The bed depth preferred in the invention is generally 7 m or longer. If two or more columns are used, they are cascaded to give a total bed depth of 7 m or longer.
As to the column usable in the invention, any column can be used regardless of its material, size, and shape so far as the objectives of the invention can be attained therewith:
Column may be, for example, of glass, plastic or stainless steel; and its shape is, for example, in cylindrical or square pillar form, but should be devised to give the possible effec-tive laminar flow when the material starch sugar solution is applied to the column packed with the resin.
The following descriptions concretely explain the detailed method to practise the present invention.
After packing a strongly-acidic cation exchange resin of alkali metal- or alkaline earth metal-form, in an aqueous suspension, in one or more columns to give a total bed depth of 7 m or longer, while keeping the temperature in the column(s) at 45 - 85C, the column(s) is applied with the material starch sugar solution, concentration of about 10 - 70 w/w %, in an amount of about 1 - 60 v~v % against the bed volume, and then charged upwards or downwards with water at a flow rate of 1~5361 about SV 0.1 - 2.0 to effect fractionation of the material starch sugar solution into HIGH-DEXTRIN FRACTION, HIGH-DEXTRIN--MALTOSE FRACTION, HIGH-MALTOSE FRACTION, HIGH-MALTOSE-GLUCOSE
FRACTION, and HIGH-GLUCOSE FRACTION, in the given order, followed by the harvest of the HIGH-MALTOSE FRACTION.
Although the eluted fractions are generally collected in about 1 - 20 v/v % against the bed volume, they may be dis-tributed automatically into the FRACTIONs.
When the material starch sugar solution is applied to the column prior to, after, or together with the application of the previously obtained HIGH-DEXTRIN-MALTOSE- and/or HIGH-MALTOSE--GLUCOSE-FRACTIONs, the amount of water required for substantial fractionation of the starch sugar solution can be extremely reduced, and the maltose constituent in the solution can be recovered in higher purity, higher concentration, and higher recovery yield: Preferably, the previously obtained HIGH-DEXTRIN-MALTOSE FRACTION, the material starch sugar solution, and the previously obtained HIGH-MALTOSE-GLUCOSE FRACTION may be applied successively to the column in the given order.
Although the HIGH-MALTOSE FRACTION thus obtained can be used intact, it may be, if necessary, treated further as follows: The FRACTION may be subjected to conventional purifi-cation steps, e.g., filtration, decolourization and/or deioni-zation. Then, the purified product is, for example, concen-trated to obtain a syrup, or crystallized to obtain a mascuit which may be spray-dried into crystalline powder, or separated ~iS361 into mother liquor and maltose crystals of much higher purity.
The high-purity maltose thus obtained is favourably usable in various uses, e.g., for production of food products or pharmaceuticals.
The following EXPERIMENTs explain the present invention in more detail.
EXPERIMENT
.
Material s~arch sugar solution The material starch sugar solutions, used in this LXPE~I-MENT, were prepared with commercially-available starch sugar products as listed in TABLE I, products of Hayashib~ra Company, Limited, Okayama, Japan, by dissolving or diluting them in water to give respective concentrations of 45 w/w %.
Dowex*50WX4 (Na ) , a commercially-available strongly-acidic cation exchange resin of alkali metal-form, a product of Dow Chemimcal Company, Midland, Michigan, U.S.A., in an aqueous suspension, was packed in a jacketted stainless steeL column, inside diameter, 5.4 cm, to give a bed depth of 10 m.
While keeping the temperature in the column at 75C ? each material starch sugar solution, listed in TABLE I, was appl;ed to the column in an amount of 5 vtv % against the bed volume, and fractionated by charging thereto 75C hot water at a flow rate of SV 0.4, followed by the harvest of the HIGH-MALTOSE
FRACTION with a maltose content of 93 Z or higher. The results are given in TABLE II.
The experimental results, as shown in TABLE II, confirm that when the maltose content in the material starch sugar solution is 70 ~ or higher, a HIGH-MALTOSE FRACTION with a maltose content of 93 % or higher is easily obtainable in an *trade m~r]c 3~
_xtremely higher recovery yield, i.e., 80 % or higher, against the maltose constituen-t in the material starch sugar solution.
TABLE
Sugar composition ~%) A B C D
Maltrup 7.1 48.0 44.9 Malstar 3.2 66.0 30.8 HM-75 1.0 76.8 22.2 Sunmalt 4.3 85.0 10.7 _ Maltose H 0.6 91.5 7.9 _ Note: A is the material starch sugar solution ~trade ~ark~;
B, glucose; C, maltose; and D, maltotriose and higher oligosacc~arides.
TABLE II
-Maltrup 48.0 132.2 44.2 control Malstar 66.0 231.7 56.3 control _ HM-75 76.8 403.6 84.3 present invention I _ Sunmalt 85.0 ~83.8 91.3 present invention Maltose H 91.5 548.8 96.2 present invention . _ Note: A is the material starch sugar solution ttrade mark); B , maltose content in the material starch sugar solution (~); C, maltose yield in the HIGH-~LTOSE FRACTION (g); D, maLtose yield against the maltose constituent in the material starch sugar solution ~%); and E, remarks.
1:~153~i~
EXPERIME~T 2 -Bed depth Similarly as in EXPFRIMENT 1, the strongly-acidic cation exchange resin of alkali metal-from was packed in one or two columns to give respective total bed depths in the range of 1 -20 m as in TABLE III.
While keeping the temperature in the columns of different bed tepth~ at 75C, 45 w/w Z ~queou~ ~olution aliquots of "~unmalt", a comme~ically-~ail~ble ~rch sugar powder with a msltose content of 85.0 %, RegistQred Trade Mark o Hayashib~ra Company, Limited, Okayama, Japan, were applied to the-columns in an amount of 5 v/v % against the bed volume, and then fractionated by charging thereto 75C hot water at a flow rate of SV 0.4, followed by the harvest of the HIGH-MALTOSE FRACTION
with a maltose content of 93 % or hlgher. The results are given in TABLE III.
The exper$mental resultR, as shown in TA8LE III, conf$rm that when the bed depth is 7 m or longer, a HIGH-MALTOSE
FRACTION with a maltose content of 93 % or higher is easily obtainable in an extremely higher recovery yield, i.e., 80 % or higher, against the maltose constituent in the material starch sugar solution.
1S36;~
TABLE III
A I B C D E
_ 1 1 114.5 30.1 56.9 3 1 343.5 102.1 64.2 _ 1 572.5 192,9 72.8 ~ , _ . ~ , , _ _ 7 1 801,5 324.9 87.6 _ __ _ . 10 - 1 1145.0 483.8 91.3 _ _ 1 1715,5 739.3 93.0 .. _ .
Detailed Description of the Invention The present invention relates to a process fo~ producing a high-purity maltose.
Recently, various advantages of maltose in food products and pharmaceuticals have been established one after another, thus its uses have expanded rapidly in their productions. The expanded uses have inevitably led to increasing demands for a high-purity maltose.
Conventionally, maltose have been available as a saccha-rified starch product with a maltose content of about 40 - 50 w/w % on dry solid basis (all percentages as used in the SPECIFICATION mean "weight percentages on dry solid basis"
unless specified otherwise) which is obtainable by subjecting a liquefied starch solution to the action of malt enzyme.
Recent advances in starch saccharification technique enable a relatively easier production of a saccharified starch product with a maltose content of 50 % or higher by combination of, for example, ~-amylase with starch debranching enzyme.
The above described starch saccharification technique, however, from ecomonical and technical standpoints, render the direct production of a high-purity maltose with a maltose content of 90 % or higher much difficult.
Some attempts to obtain a high-purity maltose are dis-closed in recent patent applications which comprise applying a ~:lS;361 starch sugar solution containing maltose to a column of anion exchange resin: For example, Japan Patent Publication No.
46,290/77 discloses an attempt for producing a high-purity maltose, comprising preparing a starch sugar solution sub-stantially consisting of dextrin and about 65 % maltose, and applying the solution to an anion exchange resin of OH-form to adsorb the maltose constituent and also to remove the dextrin constituent. Since, however, in a process according to the attempt the maltose constituent is adsorbed on the anion exchange resin of OH-form, the solution should be applied to the resin at the possible lowest temperature, preferably, below 20C, to prevent the isomerization of the maltose constituent:
thus, the increase in viscosity and microbial contamination as well as low purification capability are unavoidable, and render its industrial-scale practise very difficult. Further, Japan Patent Publication No.20,579/79 discloses an attempt for producing a high-purity maltose which comprises applying a starch sugar solution, containing glucose and maltose, to a column, packed with an anion exchange resin of S032 - or SO3H -form, to fractionate the solution into the glucose- and maltose-constituents. The attempt is, however, inadequate as a process for industrial-scale production of a high-purity maltose because the bonding of S032 - or SO3H -group is labile.
The present inventors have investigated processes for a high-purity maltose using a strongly-acidic cation exchange resin, more par~icularly, of alkali metal- or alkaline earth metal-~orm, instead of anion exchange resin which has the above described disadvantages.
The efforts resulted in the finding that a high-purity maltose is easily obtainable by applying a material starch sugar solution with a maltose content of at least 70 % to a column packed with a strongly-acidic cation exchange resin of alkali metal- or alkaline earth metal-form; fractionating by charging thereto water the solution into HIHG-DEXTRIN FRACTION, HIGH-DEXTRIN-MALTOSE FRACTION, HIGH-MALTOSE FRACTION, HIGH-MALTOSE~GLUCOSE FRACTION, and HIGH-GLUCOSE FRACTION (the terms "HIGH-A FRACTION" and "HIGH-A-B FRACTION" as used in the SPECIFICATION shall mean the eluted fractions containing A, or A and B as predominant constituent(s) respectively), in the given order; and recovering the HIGH-MALTOSE FRACTION.
Also, the efforts resulted in the additional finding that the objective high-purity maltose is constantly obtainable in higher concentration and at higher recovery yield by employing a method where the material starch sugar solution is applied to the column together with the previously obtained HIGH-DEXTRIN--MALTOSE- and/or HIGH-MALTOSE GLUCOSE-FRACTIONs, and wherein the resul~ant HIGH-DEXTRIN MALTOSE- and/or HIGH-MALTOSE-GLUCOSE-FRACTIONs are applied to the column together with a fresh material starch sugar solution in the next fractionation step.
The above described findings led to the present invention.
S3~
In one aspect the invention p~ovides a proc~ss for the separation of maltose from a feed solution by the utilization of an ion exc~larlge resin, comprising: (a) providing a feed solution containing at least 7~ maltose based on the weight or the dry solid, the remainder con-sisting essentially of glucose and dextr-ns; (b) sequen-tially aamitting predetermined volumes o~ the feed solution and water to a column of a strongly acidic cation exchange resin having sulphonyl groups of an alkali metal or alkaline earth metal f~rm; (c) sequentially separating the effluents from the column into the following fractions:
a first fraction rich in dextrins, a second fraction rich in dextrins, but highly contaminated with maltose, a third fraction o` substantially pure maltose, a fourth fraction rich in maltose, but highly contamina-ted wi-th glucose, and a fifth ,~raction rich in glucose; (d) recovering the third fraction of substantially pure maltose;
(e) sequentially adrnitting into the column: the second fraction obtained in the step (c), a feed solution having a maltose content of at least 70~ based on the weight of dry solid, and the rem~inder consisting essentially of glucose and dextrin, t:~e fourth fraction obtained in the step (c), and water; and (f) repeating steps (c), (d) and (e) in a cyclic manner.
~ a -mab/v~
.~.~
i,.~ ' ~lS3~
The material starch sugar solution usable in the invention may be one of those substantially-ketose-free mixture solution of aldoses derived from starch, which gives a ~IIGH-MALTOSE
FRACTION with a maltose content of 90 %, preferably, 93 Z or higher, in a high recovery yield when subjected to the ~rac-tionation according to the invention: For example, the ma-terial starch sugar solution may be a saccharified starch solution whcih is obtainable by subjecting st~rch to the actions of starch-degrading enzymes, e.g., a- and ~-amylases, and starch-debranching enzyme, or may be an aqueous solution of a commercially-available starch sugar product, but ~heir maltose content should be at least 70 %.
The strongly-acidic cation exchange resin of alkali metal-or alkaline earth metal-form usable in the invention may be one or more members of stylene-divinylbenzene copolymer resins, for example, bearing sulphonyl groups of alkali metal- or alkaline earth metal-form, such as Na+, K+, Ca2+, or Mg2t: Commercially-available resins are, for example, Dowex 50WX2 , Dowex 50WX4 , and Dowex 501~X8 , products of Dow C~emical Company, Midland, Michigan, U.S.A., Amberlite CG-120 , a product of Rohm ~ Haas Company, Philadelphia, Pennsylvania, U.S.A., XT-1022E ~ a product of Tokyo Chemical Industries, Kita-ku, Tokyo, Japan, and Diaion* SK lB , Diaion* SK 102 , and Diaion*
SK 104 , products of Mitsubishi Chemical Industries Limited, Tokyo, Japan. All of these resins have excellent fractionating capability to obtain the HIGH-MA~TOSE FRACTION, and are highly *~ ~e mark ~l~1536~
heat- and abrasion-resistant, thus they are advantageously feasible for producing a high-purity maltose on an industrial-scale.
In the process according to the invention, the resin with a nominal particle size of about 0.01 - 0.5 mm is packed in one or more columns. The bed depth preferred in the invention is generally 7 m or longer. If two or more columns are used, they are cascaded to give a total bed depth of 7 m or longer.
As to the column usable in the invention, any column can be used regardless of its material, size, and shape so far as the objectives of the invention can be attained therewith:
Column may be, for example, of glass, plastic or stainless steel; and its shape is, for example, in cylindrical or square pillar form, but should be devised to give the possible effec-tive laminar flow when the material starch sugar solution is applied to the column packed with the resin.
The following descriptions concretely explain the detailed method to practise the present invention.
After packing a strongly-acidic cation exchange resin of alkali metal- or alkaline earth metal-form, in an aqueous suspension, in one or more columns to give a total bed depth of 7 m or longer, while keeping the temperature in the column(s) at 45 - 85C, the column(s) is applied with the material starch sugar solution, concentration of about 10 - 70 w/w %, in an amount of about 1 - 60 v~v % against the bed volume, and then charged upwards or downwards with water at a flow rate of 1~5361 about SV 0.1 - 2.0 to effect fractionation of the material starch sugar solution into HIGH-DEXTRIN FRACTION, HIGH-DEXTRIN--MALTOSE FRACTION, HIGH-MALTOSE FRACTION, HIGH-MALTOSE-GLUCOSE
FRACTION, and HIGH-GLUCOSE FRACTION, in the given order, followed by the harvest of the HIGH-MALTOSE FRACTION.
Although the eluted fractions are generally collected in about 1 - 20 v/v % against the bed volume, they may be dis-tributed automatically into the FRACTIONs.
When the material starch sugar solution is applied to the column prior to, after, or together with the application of the previously obtained HIGH-DEXTRIN-MALTOSE- and/or HIGH-MALTOSE--GLUCOSE-FRACTIONs, the amount of water required for substantial fractionation of the starch sugar solution can be extremely reduced, and the maltose constituent in the solution can be recovered in higher purity, higher concentration, and higher recovery yield: Preferably, the previously obtained HIGH-DEXTRIN-MALTOSE FRACTION, the material starch sugar solution, and the previously obtained HIGH-MALTOSE-GLUCOSE FRACTION may be applied successively to the column in the given order.
Although the HIGH-MALTOSE FRACTION thus obtained can be used intact, it may be, if necessary, treated further as follows: The FRACTION may be subjected to conventional purifi-cation steps, e.g., filtration, decolourization and/or deioni-zation. Then, the purified product is, for example, concen-trated to obtain a syrup, or crystallized to obtain a mascuit which may be spray-dried into crystalline powder, or separated ~iS361 into mother liquor and maltose crystals of much higher purity.
The high-purity maltose thus obtained is favourably usable in various uses, e.g., for production of food products or pharmaceuticals.
The following EXPERIMENTs explain the present invention in more detail.
EXPERIMENT
.
Material s~arch sugar solution The material starch sugar solutions, used in this LXPE~I-MENT, were prepared with commercially-available starch sugar products as listed in TABLE I, products of Hayashib~ra Company, Limited, Okayama, Japan, by dissolving or diluting them in water to give respective concentrations of 45 w/w %.
Dowex*50WX4 (Na ) , a commercially-available strongly-acidic cation exchange resin of alkali metal-form, a product of Dow Chemimcal Company, Midland, Michigan, U.S.A., in an aqueous suspension, was packed in a jacketted stainless steeL column, inside diameter, 5.4 cm, to give a bed depth of 10 m.
While keeping the temperature in the column at 75C ? each material starch sugar solution, listed in TABLE I, was appl;ed to the column in an amount of 5 vtv % against the bed volume, and fractionated by charging thereto 75C hot water at a flow rate of SV 0.4, followed by the harvest of the HIGH-MALTOSE
FRACTION with a maltose content of 93 Z or higher. The results are given in TABLE II.
The experimental results, as shown in TABLE II, confirm that when the maltose content in the material starch sugar solution is 70 ~ or higher, a HIGH-MALTOSE FRACTION with a maltose content of 93 % or higher is easily obtainable in an *trade m~r]c 3~
_xtremely higher recovery yield, i.e., 80 % or higher, against the maltose constituen-t in the material starch sugar solution.
TABLE
Sugar composition ~%) A B C D
Maltrup 7.1 48.0 44.9 Malstar 3.2 66.0 30.8 HM-75 1.0 76.8 22.2 Sunmalt 4.3 85.0 10.7 _ Maltose H 0.6 91.5 7.9 _ Note: A is the material starch sugar solution ~trade ~ark~;
B, glucose; C, maltose; and D, maltotriose and higher oligosacc~arides.
TABLE II
-Maltrup 48.0 132.2 44.2 control Malstar 66.0 231.7 56.3 control _ HM-75 76.8 403.6 84.3 present invention I _ Sunmalt 85.0 ~83.8 91.3 present invention Maltose H 91.5 548.8 96.2 present invention . _ Note: A is the material starch sugar solution ttrade mark); B , maltose content in the material starch sugar solution (~); C, maltose yield in the HIGH-~LTOSE FRACTION (g); D, maLtose yield against the maltose constituent in the material starch sugar solution ~%); and E, remarks.
1:~153~i~
EXPERIME~T 2 -Bed depth Similarly as in EXPFRIMENT 1, the strongly-acidic cation exchange resin of alkali metal-from was packed in one or two columns to give respective total bed depths in the range of 1 -20 m as in TABLE III.
While keeping the temperature in the columns of different bed tepth~ at 75C, 45 w/w Z ~queou~ ~olution aliquots of "~unmalt", a comme~ically-~ail~ble ~rch sugar powder with a msltose content of 85.0 %, RegistQred Trade Mark o Hayashib~ra Company, Limited, Okayama, Japan, were applied to the-columns in an amount of 5 v/v % against the bed volume, and then fractionated by charging thereto 75C hot water at a flow rate of SV 0.4, followed by the harvest of the HIGH-MALTOSE FRACTION
with a maltose content of 93 % or hlgher. The results are given in TABLE III.
The exper$mental resultR, as shown in TA8LE III, conf$rm that when the bed depth is 7 m or longer, a HIGH-MALTOSE
FRACTION with a maltose content of 93 % or higher is easily obtainable in an extremely higher recovery yield, i.e., 80 % or higher, against the maltose constituent in the material starch sugar solution.
1S36;~
TABLE III
A I B C D E
_ 1 1 114.5 30.1 56.9 3 1 343.5 102.1 64.2 _ 1 572.5 192,9 72.8 ~ , _ . ~ , , _ _ 7 1 801,5 324.9 87.6 _ __ _ . 10 - 1 1145.0 483.8 91.3 _ _ 1 1715,5 739.3 93.0 .. _ .
2* 2290.0 994.1 93.8 Note~ A is total bed tepth (m)~ B, number of columns; C, amount of the material starch sugar solution applied ~ml)~ D, maltose yield in the HIGH-MALTOSE FRACTION
(g); E, maltose yield against the mal~ose constituent in the material starch sugar solution (%); and *) means two columns were cascaded.
~ZlS36P
Fractionation temperature After packing, similarly as in EXPERIMENT 1, the strongiy-acidic cation exchange resin of alkali metal-form in columns to give respective bed depths of 10 m, material starch sugar solution aliquots, prepared similarly as in EXPERIMENT 2, were applied thereto, and fractionated similarly as in the same EXPERIMENT, except that the col~mns were kept at different temperatures in the range of 35 - 95C during the fraction-ation, followed by the har~e~t of the HIGH-MALTOSE FRAC~ION
with a maltose co~tent of 93 % or higher. The results are ~iven in TAB~E IV.
The experimental results, as shown in TABLE IV, confirm that when the column i~ kept at a temperature in the range of 45 - 85C, a HIBH-MALTOS~ FRACTION with a malto~e content of 93 % o~ higher i8 eAsily obtainable in an extremely higher recovery yield, i.e., 80 % or higher, against the maltose constituent in the material starch sugar solution with less fear of causing browning reaction.
TAsLE IV
-_ B C = E
374.7 70.7 0.023 easy ~30.2 81.2 0.059 easy , _ 471.1 88.9 0.105 easy _ .
~76.9 90.0 0.150 easy _ , _ _ 483.8 91.3 0.176 easy , _ 485.9 91.7 0.205 easy _ 472.2 89.1 0.496 difficult Note2 A i~ the fractionation temperature (C)~ B, total yield o su~ar constituent~ with a maltose content of 93 % or higfier ~g~; C, maltosc yield agalnst the maltose constituent in the material ~tarch sugar solution (%)~ D, colourization degree, obtained by mea~uring the absorbance of the HIGH-MALTOSE FRACTION
in 10 cm cell (A, - A72n ), and reducing t~e obtained value i~8 ~at i~ ~Onw/w % solution; and E, decolourization using 0.1 % activated carbon against sugar constituents.
~ 3~ ~
Several embodiments o~ the invention are disclosed hereinafter.
::` EXAMPLE
A material starch sugar solution was prepared by diiuting HM-75 , trade mark of a commercially available starch sugar syrup with a malto6e contant of 76.~ %, a product of Hayashl-bara Company, Limited, Okayama, Japan, in water to give a concen.tration of 45 w/w %.
XT-1022E (Na~) , a commercially-available strongly-acidic cation exchange resin of alkali metal-form, a product of Tokyo ~hemical Industries, Kita-ku, Tokyo, Japan. in an aqueous su6pension, wa~ pac~ed in four jackette~ stainless steel ~olumns, in3ide di~meter, 5.4 cm, to give respective bed ~epths o 5 m, and the column~ were cascaded to g~ve a total bed depth of 20 m.
While keeping the temperature in the columns at 55C, the material starch sugar solution was applied thereto in an amount 5 v/v % against the bed volume, and then fractionated by charging thereto 55C hot water at a flow rate of SV 0.13, followed by the harvest of the HIGH-MALTOSE FRACTIO~ with a *trade mark maltose content of 93 % or higher.
The FRACTION contained 808.2 g maltose, and the recovery yield was extremely high, i.e., 84.3 %, against the maltose constituent in the material starch sugar solution.
A material starch sugar solution was prepared by dis-solving "Sunmalt", a commercially-available starch sugar powder with a maltose content of 85.0 %, Registered Trade Mark of Hayashibara Company, Limited, Okayama, Japan, in water to give a concentration of 60 w/w %, The resin, used in EXAMPLE 1, was converted into K+-form in usuaL way, and packed in a ~acketted stainless steel column, inside diameter, 2.2 cm, to give a bed depth of 10 m.
While keeping the temperature in the column at 60C, the material starch sugar solution was applied thereto in an amount of 3 v/v % against the bed volume, and then ~ractionated by charging thereto 60C hot water at a flow rate of SV 0.2, followed by the harvest of the HIGH-MALTOSE FRACTION with a maltose content of 93 % or higher.
The FRACTION contained 65.7 g maltose, and the recovery yield was extremely high, i.e., 88.3 %, against the maltose constituent in the material starch sugar solution.
53~;1 A material starch sugar solution was prepared by dis-solving "Sunmalt", a commercially-available starch sugar powder with a maltose content of 85.0 %, Registered Trade Mark of Hayashibara Company, Limited, Okayama, Japan, in water to give a concentration of 45 w/w %.
Dowex* 50WX4 (Mg2~) , a commercially-available strongly-acidic cation exchange resin of alkaline earth metal-form, a product of Dow Ghemical Company, Midland, Michigan, U.S.A,, in an aqueous suspension, was packed in fresh columns of the same materlal and dimensions as uEed in EXAMPJ.E 1 to give a total bed depth of 15 m.
While keeping the temperature in the columns at 75C, the material starch sugar solution was applied thereto in an amount o~ 6,6 v/v % against the bed volume, and then fractionated by charg~ng thereto 75C hot water at a flow rate of SV 0.13, followed by the harvest of the HIGH-MALTOSE FRACTION with a maltose content of 93 % or higher.
The FRACTION contained 913.7 g maltose, and the recovery yield was extremely high, i.e., 87.1 %, against the maltose constituent in the material starch sugar solution.
*trade mark ~1S3~
In this EXAMPLE, a dual-stage fractionation was carried out .
The first fractionation was carried out as follows:
Similarly as in EXAMPLE 1, a material starch sugar solution was applied to a column, and fractionated except that the material starch sugar solution was applied to the column in an amount of 20 v/v % against the bed volume. The elution pattern is given in Figure, where Fractions A through E show HIGH-DEXTRIN
FRACTION, HIGH-DEXTRIN-MALTOSE FRACTION, HIGH-MALTOSE FRACTION, HIGH-MALTOSE-GLUCOSE FRACTION, and HIGH-GLUCOSE FRACTION
respectively, and where the elution is effected in the given order. Fraction C, the HIGH-MALTOSE FRACTION, wa3 harvested, and Fractions A and E were removed from the fractionation system.
The additional fractionation was carrled out as follows:
The column was appl~ed succees~vely w~th Fraction B, the material starch sugar solution in an amount of about lO v/v %
against the bed volume, and Fraction D, in the given order, then charged with 75C hot water similarly as in EXAMPLE 3 to effect fractionation, followed by the harvest of the HIGH-MALTOSE FRACTIONs with a maltose content of 94 %. The addi-tional fractionation was repeated up to 30 batches in total, and the averaged results per batch were calculated: On an average, one HIGH-MALTOSE FRACTION contained 1483 g maltose, ~2~i36~
and the recovery yield was extremely high, i.e , 93.3 ~, against the maltose constituent in the materiaL starch sugar solution.
A material starch sugar solution was p~epared by dis-solving Maltose H , trade mark of a commercially-available starch sugar powder with a maltose content of 91.5 ~, a product of Hayashibara Company, Limited, Okayama, Japan, in water to give a concentration of 45 w/w %.
Amberlitc CG-120 (Ca2~) , a commerclally-available strongly-acidic cation exchange resin of alkatine earth metal-from, a product of Rohm & Haas Company, Philadelphia, Pennsyl-vania, U.S.A., was packed in fresh colu~.ns of the same material and dimensions as used in EXAMPLE 1 to give a totaL bed depth of 10 ~.
Also, in this EXAMPLE, a dual-stage fractionation was carried out. The irst fractionation w~s carried out as follows: While keeping the temperature in the columns at 80C, the material starch sugar solution was ~pplied thereto in an amount of 20 vlv % against the bed volume, and then fraction-ated by charging thereto 80~ hot water at a flow rate of SV
O.6 to obtain a similar elution pattern as in EXAMPLE 4.
*-trade mark .
536~
Similarly as in E~AMPLE 4, Fraction C, the HIGH-MALTOSE
FRACTION, was harvested, and Fractions A and E were removed from the fractionation system.
The additional fractionation was carried out as follows:
The column was applied successively with Fraction B, the material starch sugar solution in an amount of 10 v/v % against the bed volume, and Fraction D, in the given order, and then charged with 80C hot water at a flow rate of SV 0.6 to eff~ct fractionation, followed by the harvest of the resultant HIGH-MALTOSE FRACTIONs with a maltose content of 96 % or higher.
The additional fractionation was repeated up to 100 batches ln total, and the averaged results per batch were calculated: On `an average, one HIGH-MALTOSE FRACTION contained 1084 g maltose, and the recovery yield was extremely high, i.e., 95 %, against the maltose constituent in the material starch sugar solution.
Brief Explanation of Figure ~ Figure shows the elution pattern of the material starch sugar ~olution upon the fractionation, where Fractions A
through E show the HIGH-DEXTRIN FRACTION, HIGH-DEXTRIN-MALTOSE
FRACTION, HIGH-MALTOSE FRACTION, HIGH-MALTOSE-GLUCOSE FRACTION, and HIGH-GLUCOSE FRACTION respectively.
(g); E, maltose yield against the mal~ose constituent in the material starch sugar solution (%); and *) means two columns were cascaded.
~ZlS36P
Fractionation temperature After packing, similarly as in EXPERIMENT 1, the strongiy-acidic cation exchange resin of alkali metal-form in columns to give respective bed depths of 10 m, material starch sugar solution aliquots, prepared similarly as in EXPERIMENT 2, were applied thereto, and fractionated similarly as in the same EXPERIMENT, except that the col~mns were kept at different temperatures in the range of 35 - 95C during the fraction-ation, followed by the har~e~t of the HIGH-MALTOSE FRAC~ION
with a maltose co~tent of 93 % or higher. The results are ~iven in TAB~E IV.
The experimental results, as shown in TABLE IV, confirm that when the column i~ kept at a temperature in the range of 45 - 85C, a HIBH-MALTOS~ FRACTION with a malto~e content of 93 % o~ higher i8 eAsily obtainable in an extremely higher recovery yield, i.e., 80 % or higher, against the maltose constituent in the material starch sugar solution with less fear of causing browning reaction.
TAsLE IV
-_ B C = E
374.7 70.7 0.023 easy ~30.2 81.2 0.059 easy , _ 471.1 88.9 0.105 easy _ .
~76.9 90.0 0.150 easy _ , _ _ 483.8 91.3 0.176 easy , _ 485.9 91.7 0.205 easy _ 472.2 89.1 0.496 difficult Note2 A i~ the fractionation temperature (C)~ B, total yield o su~ar constituent~ with a maltose content of 93 % or higfier ~g~; C, maltosc yield agalnst the maltose constituent in the material ~tarch sugar solution (%)~ D, colourization degree, obtained by mea~uring the absorbance of the HIGH-MALTOSE FRACTION
in 10 cm cell (A, - A72n ), and reducing t~e obtained value i~8 ~at i~ ~Onw/w % solution; and E, decolourization using 0.1 % activated carbon against sugar constituents.
~ 3~ ~
Several embodiments o~ the invention are disclosed hereinafter.
::` EXAMPLE
A material starch sugar solution was prepared by diiuting HM-75 , trade mark of a commercially available starch sugar syrup with a malto6e contant of 76.~ %, a product of Hayashl-bara Company, Limited, Okayama, Japan, in water to give a concen.tration of 45 w/w %.
XT-1022E (Na~) , a commercially-available strongly-acidic cation exchange resin of alkali metal-form, a product of Tokyo ~hemical Industries, Kita-ku, Tokyo, Japan. in an aqueous su6pension, wa~ pac~ed in four jackette~ stainless steel ~olumns, in3ide di~meter, 5.4 cm, to give respective bed ~epths o 5 m, and the column~ were cascaded to g~ve a total bed depth of 20 m.
While keeping the temperature in the columns at 55C, the material starch sugar solution was applied thereto in an amount 5 v/v % against the bed volume, and then fractionated by charging thereto 55C hot water at a flow rate of SV 0.13, followed by the harvest of the HIGH-MALTOSE FRACTIO~ with a *trade mark maltose content of 93 % or higher.
The FRACTION contained 808.2 g maltose, and the recovery yield was extremely high, i.e., 84.3 %, against the maltose constituent in the material starch sugar solution.
A material starch sugar solution was prepared by dis-solving "Sunmalt", a commercially-available starch sugar powder with a maltose content of 85.0 %, Registered Trade Mark of Hayashibara Company, Limited, Okayama, Japan, in water to give a concentration of 60 w/w %, The resin, used in EXAMPLE 1, was converted into K+-form in usuaL way, and packed in a ~acketted stainless steel column, inside diameter, 2.2 cm, to give a bed depth of 10 m.
While keeping the temperature in the column at 60C, the material starch sugar solution was applied thereto in an amount of 3 v/v % against the bed volume, and then ~ractionated by charging thereto 60C hot water at a flow rate of SV 0.2, followed by the harvest of the HIGH-MALTOSE FRACTION with a maltose content of 93 % or higher.
The FRACTION contained 65.7 g maltose, and the recovery yield was extremely high, i.e., 88.3 %, against the maltose constituent in the material starch sugar solution.
53~;1 A material starch sugar solution was prepared by dis-solving "Sunmalt", a commercially-available starch sugar powder with a maltose content of 85.0 %, Registered Trade Mark of Hayashibara Company, Limited, Okayama, Japan, in water to give a concentration of 45 w/w %.
Dowex* 50WX4 (Mg2~) , a commercially-available strongly-acidic cation exchange resin of alkaline earth metal-form, a product of Dow Ghemical Company, Midland, Michigan, U.S.A,, in an aqueous suspension, was packed in fresh columns of the same materlal and dimensions as uEed in EXAMPJ.E 1 to give a total bed depth of 15 m.
While keeping the temperature in the columns at 75C, the material starch sugar solution was applied thereto in an amount o~ 6,6 v/v % against the bed volume, and then fractionated by charg~ng thereto 75C hot water at a flow rate of SV 0.13, followed by the harvest of the HIGH-MALTOSE FRACTION with a maltose content of 93 % or higher.
The FRACTION contained 913.7 g maltose, and the recovery yield was extremely high, i.e., 87.1 %, against the maltose constituent in the material starch sugar solution.
*trade mark ~1S3~
In this EXAMPLE, a dual-stage fractionation was carried out .
The first fractionation was carried out as follows:
Similarly as in EXAMPLE 1, a material starch sugar solution was applied to a column, and fractionated except that the material starch sugar solution was applied to the column in an amount of 20 v/v % against the bed volume. The elution pattern is given in Figure, where Fractions A through E show HIGH-DEXTRIN
FRACTION, HIGH-DEXTRIN-MALTOSE FRACTION, HIGH-MALTOSE FRACTION, HIGH-MALTOSE-GLUCOSE FRACTION, and HIGH-GLUCOSE FRACTION
respectively, and where the elution is effected in the given order. Fraction C, the HIGH-MALTOSE FRACTION, wa3 harvested, and Fractions A and E were removed from the fractionation system.
The additional fractionation was carrled out as follows:
The column was appl~ed succees~vely w~th Fraction B, the material starch sugar solution in an amount of about lO v/v %
against the bed volume, and Fraction D, in the given order, then charged with 75C hot water similarly as in EXAMPLE 3 to effect fractionation, followed by the harvest of the HIGH-MALTOSE FRACTIONs with a maltose content of 94 %. The addi-tional fractionation was repeated up to 30 batches in total, and the averaged results per batch were calculated: On an average, one HIGH-MALTOSE FRACTION contained 1483 g maltose, ~2~i36~
and the recovery yield was extremely high, i.e , 93.3 ~, against the maltose constituent in the materiaL starch sugar solution.
A material starch sugar solution was p~epared by dis-solving Maltose H , trade mark of a commercially-available starch sugar powder with a maltose content of 91.5 ~, a product of Hayashibara Company, Limited, Okayama, Japan, in water to give a concentration of 45 w/w %.
Amberlitc CG-120 (Ca2~) , a commerclally-available strongly-acidic cation exchange resin of alkatine earth metal-from, a product of Rohm & Haas Company, Philadelphia, Pennsyl-vania, U.S.A., was packed in fresh colu~.ns of the same material and dimensions as used in EXAMPLE 1 to give a totaL bed depth of 10 ~.
Also, in this EXAMPLE, a dual-stage fractionation was carried out. The irst fractionation w~s carried out as follows: While keeping the temperature in the columns at 80C, the material starch sugar solution was ~pplied thereto in an amount of 20 vlv % against the bed volume, and then fraction-ated by charging thereto 80~ hot water at a flow rate of SV
O.6 to obtain a similar elution pattern as in EXAMPLE 4.
*-trade mark .
536~
Similarly as in E~AMPLE 4, Fraction C, the HIGH-MALTOSE
FRACTION, was harvested, and Fractions A and E were removed from the fractionation system.
The additional fractionation was carried out as follows:
The column was applied successively with Fraction B, the material starch sugar solution in an amount of 10 v/v % against the bed volume, and Fraction D, in the given order, and then charged with 80C hot water at a flow rate of SV 0.6 to eff~ct fractionation, followed by the harvest of the resultant HIGH-MALTOSE FRACTIONs with a maltose content of 96 % or higher.
The additional fractionation was repeated up to 100 batches ln total, and the averaged results per batch were calculated: On `an average, one HIGH-MALTOSE FRACTION contained 1084 g maltose, and the recovery yield was extremely high, i.e., 95 %, against the maltose constituent in the material starch sugar solution.
Brief Explanation of Figure ~ Figure shows the elution pattern of the material starch sugar ~olution upon the fractionation, where Fractions A
through E show the HIGH-DEXTRIN FRACTION, HIGH-DEXTRIN-MALTOSE
FRACTION, HIGH-MALTOSE FRACTION, HIGH-MALTOSE-GLUCOSE FRACTION, and HIGH-GLUCOSE FRACTION respectively.
Claims (8)
PROPERTY OR PRIVILEGE IS CLAIMED ARE DEFINED AS FOLLOWS:
1. A process for the separation of maltose from a feed solution by the utilization of an ion exchange resin, comprising:
(a) providing a feed solution containing at least 70% maltose based on the weight of the dry solid, the remainder consisting essentially of glucose and dextrins;
(b) sequentially admitting predetermined volumes of the feed solution and water to a column of a strongly acidic cation exchange resin having sulphonyl groups of an alkali metal or alkaline earth metal form;
(c) sequentially separating the effluents from the column into the following fractions:
a first fraction rich in dextrins, a second fraction rich in dextrins, but highly contaminated with maltose, a third fraction of substantially pure maltose, a fourth fraction rich in maltose, but highly contaminated with glucose, and a fifth fraction rich in glucose;
(d) recovering the third fraction of substantially pure maltose;
(e) sequentially admitting into the column:
the second fraction obtained in the step (c), a feed solution having a maltose content of at least 70% based on the weight of dry solid, and the remainder consisting essentially of glucose and dextrin, the fourth fraction obtained in the step (c) and water; and (f) repeating steps (c), (d) and (e) in a cyclic manner.
(a) providing a feed solution containing at least 70% maltose based on the weight of the dry solid, the remainder consisting essentially of glucose and dextrins;
(b) sequentially admitting predetermined volumes of the feed solution and water to a column of a strongly acidic cation exchange resin having sulphonyl groups of an alkali metal or alkaline earth metal form;
(c) sequentially separating the effluents from the column into the following fractions:
a first fraction rich in dextrins, a second fraction rich in dextrins, but highly contaminated with maltose, a third fraction of substantially pure maltose, a fourth fraction rich in maltose, but highly contaminated with glucose, and a fifth fraction rich in glucose;
(d) recovering the third fraction of substantially pure maltose;
(e) sequentially admitting into the column:
the second fraction obtained in the step (c), a feed solution having a maltose content of at least 70% based on the weight of dry solid, and the remainder consisting essentially of glucose and dextrin, the fourth fraction obtained in the step (c) and water; and (f) repeating steps (c), (d) and (e) in a cyclic manner.
2. A process in accordance with claim 1, wherein the maltose content in the third fraction is 93% or higher, based on the weight of the dry solid.
3. A process in accordance with claim 1, where-in the bed depth of the column is at least 7 m.
4. A process in accordance with claim 1, where-in the temperature of the column of the resin is kept at 45-85°C.
5. A process in accordance with claim 1, wherein the cation exchange resin is in the form of Na+, K+, Ca2+, or Mg2+.
6. A process in accordance with claim 1, wherein the concentration of the dry solid solute in the feed solution is in the range of 10-70 w/w%.
7. A process in accordance with claim 1, wherein the water is admitted to the column at a flow rate of SV 0.1-2Ø
8. In the process for producing a high-purity maltose which comprises applying an aqueous solution con-taining maltose to a column packed with an ion exchange resin, and fractionating the solution into the maltose- and other sugar constituents, the improvement wherein a material starch sugar with a maltose content of at least 70% is applied to a column packed with a strongly-acidic cation exchange resin of alkali metal- or alkaline earth metal-form, and fractionated by charging thereto water into HIGH-DEXTRIN FRACTION, HIGH-DEXTRIN-MALTOSE FRACTION, HIGH-MALTOSE FRACTION, HIGH-MALTOSE GLUCOSE FRACTION, and HIGH-GLUCOSE FRACTION, in the given order, followed by the harvest of the HIGH-MALTOSE FRACTION.
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP121725/1981 | 1981-08-03 | ||
| JP56121725A JPS5823799A (en) | 1981-08-03 | 1981-08-03 | Production of high purity maltose |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CA1215361A true CA1215361A (en) | 1986-12-16 |
Family
ID=14818330
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CA000408629A Expired CA1215361A (en) | 1981-08-03 | 1982-08-03 | Process for producing a high-purity maltose |
Country Status (6)
| Country | Link |
|---|---|
| US (1) | USRE33047E (en) |
| JP (1) | JPS5823799A (en) |
| CA (1) | CA1215361A (en) |
| DE (1) | DE3228838A1 (en) |
| FR (1) | FR2510581B1 (en) |
| GB (1) | GB2106912B (en) |
Families Citing this family (59)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS6067000A (en) * | 1983-09-19 | 1985-04-17 | 三菱化学株式会社 | Maltose separating method |
| JPH0631285B2 (en) * | 1984-02-09 | 1994-04-27 | 株式会社林原生物化学研究所 | Method for producing high-purity oligoglucosylfructoside |
| JPS61205494A (en) * | 1985-03-11 | 1986-09-11 | Sanmatsu Kogyo Kk | Production of branched dextrin and straight-chain oligosaccharide |
| JPH0693840B2 (en) * | 1985-10-04 | 1994-11-24 | 昭和産業株式会社 | Sugar liquid purification method |
| JPH0198601A (en) * | 1987-10-13 | 1989-04-17 | Gunei Kagaku Kogyo Kk | Preparation of high-purity isomalto-oligosaccharide |
| JP2838798B2 (en) * | 1988-02-04 | 1998-12-16 | 株式会社林原生物化学研究所 | Polypeptide having isoamylase activity and its use |
| US5272136A (en) * | 1991-10-12 | 1993-12-21 | Kabushiki Kaisha Hayashibara Seibutsu Kagaku Kenkyujo | 5-0-α-D-Glucopyranosyl-L-ascorbic acid, and its preparation and uses |
| JP3072535B2 (en) * | 1991-10-21 | 2000-07-31 | 株式会社林原生物化学研究所 | 5-O-α-D-glucopyranosyl-L-ascorbic acid, its production method and use |
| JP3134235B2 (en) * | 1991-10-23 | 2001-02-13 | 株式会社林原生物化学研究所 | Method for producing 2-O-α-D-glucopyranosyl-L-ascorbic acid high content |
| JP3172925B2 (en) * | 1992-02-25 | 2001-06-04 | 株式会社林原生物化学研究所 | Method for producing neotrehalose and its use |
| DE69332781T2 (en) * | 1992-12-28 | 2004-02-12 | Kabushiki Kaisha Hayashibara Seibutsu Kagaku Kenkyujo | Purification of trehalose |
| US5677442A (en) * | 1992-12-28 | 1997-10-14 | Kabushiki Kaisha Hayashibara Seibutsu Kagaku Kenkyujo | Method of crystallizing trehalose without using organic solvent |
| JPH0770165A (en) * | 1993-06-28 | 1995-03-14 | Hayashibara Biochem Lab Inc | Nonreducing oligosaccharide, its production and use thereof |
| JP3633648B2 (en) * | 1993-07-20 | 2005-03-30 | 株式会社林原生物化学研究所 | Maltose / trehalose converting enzyme, its production method and use |
| JP3605129B2 (en) * | 1993-12-15 | 2004-12-22 | 株式会社林原生物化学研究所 | Non-reducing oligosaccharide having neotrehalose structure, method for producing the same and use thereof |
| DE69510116T2 (en) * | 1994-02-23 | 1999-11-18 | Kabushiki Kaisha Hayashibara Seibutsu Kagaku Kenkyujo, Okayama | Non-reducing saccharide-forming enzyme, this coding DNA, and their preparations and uses |
| DE69505437T2 (en) * | 1994-03-01 | 1999-06-02 | Kabushiki Kaisha Hayashibara Seibutsu Kagaku Kenkyujo, Okayama | Crystalline maltotetraosyl glucoside, its production and use |
| DE69519532T2 (en) * | 1994-03-01 | 2001-05-31 | Hayashibara Biochem Lab | Crystalline maltosyl glucoside, process for its preparation and its use |
| US5556781A (en) * | 1994-03-07 | 1996-09-17 | Kabushiki Kaisha Hayashibara Seibutsu Kagaku Kenkyujo | DNA encoding enzyme, recombinant DNA and enzyme, transformant, and their preparations and uses |
| JP3557277B2 (en) * | 1994-06-25 | 2004-08-25 | 株式会社林原生物化学研究所 | Thermostable trehalose releasing enzyme, its production method and use |
| JP3662972B2 (en) | 1994-06-27 | 2005-06-22 | 株式会社林原生物化学研究所 | Non-reducing saccharides, production method and use thereof |
| JP3793590B2 (en) | 1994-06-27 | 2006-07-05 | 株式会社林原生物化学研究所 | Non-reducing saccharides, production method and use thereof |
| JP3650632B2 (en) | 1994-06-16 | 2005-05-25 | 株式会社林原生物化学研究所 | Recombinant enzyme that converts maltose to trehalose |
| US5763228A (en) * | 1994-06-16 | 1998-06-09 | Kabushiki Kaisha Hayashibara Seibutsu Kagaku Kenkyujo | Recombinant enzyme for converting maltose into trehalose from pimelobacter sp. |
| AU695080B2 (en) * | 1994-06-24 | 1998-08-06 | Kabushiki Kaisha Hayashibara Seibutsu Kagaku Kenkyujo | Thermostable non-reducing saccharide-forming enzyme, its production and uses |
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| KR20080049924A (en) * | 2006-12-01 | 2008-06-05 | 주식회사 신동방씨피 | Process for preparing high purity maltitol crystalline powder |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3565765A (en) * | 1966-12-27 | 1971-02-23 | Cpc International Inc | Preparation of high maltose conversion products |
| IT1050155B (en) * | 1967-06-30 | 1981-03-10 | Hayashibara Co | PROCESS FOR THE PRODUCTION OF HIGH PURITY MALTOSE |
| JPS5420578B1 (en) * | 1970-12-09 | 1979-07-24 | ||
| JPS5617078B1 (en) * | 1971-05-31 | 1981-04-20 | ||
| US3817787A (en) * | 1972-01-26 | 1974-06-18 | Suomen Sokeri Oy | Method for separating monosaccharides from mixtures including di-, and higher saccharides |
| JPS5246290B2 (en) * | 1973-06-05 | 1977-11-24 | ||
| JPS5186143A (en) * | 1975-01-21 | 1976-07-28 | Tokai Togyo Kk | Katono seizohoho |
| US4022637A (en) * | 1976-02-23 | 1977-05-10 | Standard Brands Incorporated | Method for separation of water soluble carbohydrates |
| US4109075A (en) * | 1976-06-09 | 1978-08-22 | Cpc International Inc. | Separation of saccharides by exclusion chromatography |
| FI772313A (en) * | 1976-08-02 | 1978-02-03 | Uop Inc | |
| JPS5246290A (en) * | 1976-09-17 | 1977-04-12 | Erepon Kakoki Kk | Ph control system of waste fluid |
| JPS5577896A (en) * | 1978-12-07 | 1980-06-12 | Meiji Seika Kaisha Ltd | Preparation of high-purity maltose |
| JPS5585395A (en) * | 1978-12-21 | 1980-06-27 | Nippon Shiryo Kogyo Kk | Preparation of crystalline maltose |
| JPS6026482B2 (en) * | 1980-07-31 | 1985-06-24 | 日本食品化工株式会社 | Method for producing cyclodextrin |
| JPS5759641A (en) * | 1980-09-26 | 1982-04-10 | Japan Organo Co Ltd | Regenerating method for strong acidic cation exchange resin |
| JPS57209000A (en) * | 1981-06-17 | 1982-12-22 | Organo Kk | Decomposition of maltose |
-
1981
- 1981-08-03 JP JP56121725A patent/JPS5823799A/en active Granted
-
1982
- 1982-08-02 DE DE19823228838 patent/DE3228838A1/en active Granted
- 1982-08-03 CA CA000408629A patent/CA1215361A/en not_active Expired
- 1982-08-03 FR FR8213526A patent/FR2510581B1/en not_active Expired
- 1982-08-03 GB GB08222390A patent/GB2106912B/en not_active Expired
-
1988
- 1988-06-06 US US07/202,249 patent/USRE33047E/en not_active Expired - Lifetime
Also Published As
| Publication number | Publication date |
|---|---|
| DE3228838A1 (en) | 1983-03-24 |
| USRE33047E (en) | 1989-09-05 |
| JPS5823799A (en) | 1983-02-12 |
| JPS6251120B2 (en) | 1987-10-28 |
| DE3228838C2 (en) | 1990-03-29 |
| GB2106912A (en) | 1983-04-20 |
| FR2510581B1 (en) | 1987-10-16 |
| FR2510581A1 (en) | 1983-02-04 |
| GB2106912B (en) | 1986-03-12 |
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