JP4690741B2 - Method for producing non-polymer catechins composition - Google Patents

Description

  The present invention relates to a non-polymer catechin composition having an improved flavor and a reduced caffeine content, without degrading the composition before purification of the non-polymer catechins from the water-soluble extract composition of green tea leaves. The present invention relates to a production method obtained with high yield.

  As an effect of catechins, α-amylase activity inhibitory action and the like have been reported (Patent Document 1). In order to express such physiological effects, it is necessary to drink 4 to 5 cups of tea per day for adults. A technique for blending concentrations has been desired.

As one of the methods, a method of adding catechins to a beverage in a dissolved state using a water-soluble extract composition such as a concentrate of green tea extract is used. However, depending on the type of beverage for which catechins are to be blended at a high concentration, for example, when catechins are added to black tea extracts or carbonated beverages, the remaining caffeine and green tea-derived flavors may increase the commercial value of the beverage. It is known that it will greatly damage.
In order to solve this problem, when a method of adding a highly purified non-polymer catechin composition is used, any of the conventional purification methods can be applied to non-polymer catechins before and after purification of a water-soluble extract composition. Therefore, there is a problem that the physiological effect verified with the water-soluble extract composition before purification cannot be guaranteed after the composition change due to purification. Moreover, in order to reduce caffeine which is not preferable in terms of physiological activity, there has been a problem that further treatment such as chloroform treatment is required.

Against this background, among the conventional purification methods, many attempts have been made to adsorb the water-soluble extract composition extracted from green tea leaves using water once onto an adsorbent and then desorb and recover it with a solvent or the like. (Patent Documents 2 to 6). However, Patent Document 2 is a method of purification using a hydroxypropylated dextran gel or a hydrophilic vinyl polymer gel. However, since the concentration of the organic solvent used for desorption is always as high as 20% or more, There was a problem that the amount of caffeine increased. Further, Patent Document 3 is a method of purification using styrene-divinylbenzene or methacrylic acid ester. However, since the concentration of the organic solvent used for desorption is finally about 60%, a separate chloroform treatment is performed after the column treatment. It was necessary to carry out a decaffeination treatment. Similarly, in Patent Documents 3 to 5, since the organic solvent has a concentration of 30%, 40% or more, or 50% or more, it was in the same purified state. Moreover, the reduction method of caffeine by cation exchange resin is also known (patent documents 7-9). However, in Patent Documents 7 and 8, since the extract extracted from green tea leaves is brought into direct contact with the cation exchange resin, salt exchange of potassium or sodium occurs, and the regeneration frequency of the cation exchange resin increases. In Patent Document 9, there are many water-soluble polymers such as proteins and polysaccharides that cause starch generation, and there is a problem that the flavor of the resulting non-polymer catechins-containing liquid is lowered.
Japanese Patent Laid-Open No. 3-133828 JP-A-1-175978 Japanese Patent Laid-Open No. 2-311474 Japanese Patent Laid-Open No. 10-67771 JP-A-4-182479 JP-A-6-9607 JP-A-11-228565 JP 11-292870 A JP 2004-305012 A

  The object of the present invention is to reduce the amount of caffeine and improve the flavor from a water-soluble extract composition extracted from green tea leaves using water without impairing the composition before the purification treatment. It is providing the manufacturing method which obtains a composition with a high yield.

  The present inventors have studied to reduce the amount of caffeine in a water-soluble extract composition extracted from green tea leaves using water, and as a result, the water-soluble extract composition extracted from green tea leaves using water is hydrophobic. Adsorb to a column packed with adsorbent, wash the hydrophobic adsorbent with water, and then perform the first step of elution by passing an aqueous ethanol solution and bringing the eluate into contact with the cation exchange resin. At this time, the caffeine content is lower than the conventional one by reducing the salt concentration and the electric conductivity sufficiently, and performing the second step of passing the liquid after the pH is changed from weakly acidic to neutral by washing with water. It has been found that a non-polymer catechin composition having a reduced selenium can be obtained.

  That is, in the present invention, the water-soluble extract composition of green tea leaves is adsorbed on a column packed with a hydrophobic adsorbent, washed with water, and then 10 to 50% by volume of an aqueous ethanol solution is added to the hydrophobic adsorbent. In the first stage step of elution by passing 0.5 to 20 [v / v] volume per packed volume, and when the eluate obtained in the first stage is brought into contact with the cation exchange resin, The cation exchange resin is replaced so that the salt concentration of water in the ion exchange resin is less than 0.2% by weight and the electric conductivity is less than 0.5 [S / m], and then the pH of the washing water is 4 or more. The present invention provides a method for producing a non-polymer catechin composition having a second stage process in which a cation exchange resin that has been washed with water and a first stage process eluate are brought into contact with each other.

  According to the present invention, it is possible to obtain a non-polymer catechin composition in which the composition is not changed as compared with the conventional method, the amount of caffeine is reduced, and the flavor is improved, in a high yield.

  Non-polymer catechins in the present invention are non-epimeric catechins such as catechin, gallocatechin, catechin gallate, and gallocatechin gallate, and epicatechins such as epicatechin, epigallocatechin, epicatechin gallate, and epigallocatechin gallate. Is a collective term.

  The non-polymer catechin gallate body in the present invention is a general term including catechin gallate, gallocatechin gallate, epicatechin gallate, epigallocatechin gallate and the like. The non-polymer gallo form is a general term including gallocatechin, gallocatechin gallate, epigallocatechin, epigallocatechin gallate and the like.

  Examples of green tea leaves used in the present invention include Camellia genus such as C.I. sinensis, C.I. Examples include tea leaves produced from tea leaves obtained from assamica and Yabuki species or their hybrids. The tea leaves produced can be all used as long as they are non-fermented teas, but steamed tea leaves such as ordinary sencha, deep steamed sencha, gyokuro, kabuse tea, tama green tea and bancha are preferred.

  The water-soluble extraction composition used in the present invention is produced under normal green tea extraction conditions using water. The temperature of water when extracting from green tea leaves is preferably 70 to 100 (boiling water) ° C., more preferably 80 to 100 (boiling water) ° C. from the viewpoint of increasing the extraction efficiency of non-polymer catechins. The amount of water at the time of extraction from green tea leaves is preferably 5 to 60 times by weight, more preferably 5 to 40 times by weight with respect to green tea leaves. The extraction time from green tea leaves is preferably 1 to 60 minutes, more preferably 1 to 40 minutes, and still more preferably 1 to 30 minutes. If the extraction time is too short, elution of the non-polymer catechins is insufficient, and if it is too long, the heat-denatured isomerization reaction of the non-polymer catechins proceeds.

  The water-soluble extract composition used in the present invention is a concentrate of a so-called green tea extract, for example, JP-A-59-219384, JP-A-4-20589, JP-A-5-260907, JP-A-5-26095. You may use what was prepared by the method illustrated in detail in 306279 gazette, Unexamined-Japanese-Patent No. 2003-304811, Unexamined-Japanese-Patent No. 2003-219800, etc. Examples of commercially available products include “Polyphenone”, Mitsui Norin Co., Ltd., “Theafranc”, ITO EN Co., Ltd., and “Sunphenon”, Taiyo Kagaku Co., Ltd. In addition, a column purified product and a chemically synthesized product may be used. As the form of the tea extract concentrate here, various forms such as solids, aqueous solutions, and slurries can be mentioned. In the treatment of the present invention, the concentrate of the tea extract is prepared in the state of an aqueous solution in advance. .

Examples of the hydrophobic adsorbent packed in the column of the first step in the production method of the present invention include an adsorbent obtained by hydrophobically modifying the surface of an inorganic substance, and a polymeric hydrophobic adsorbent. As the adsorbent, from the viewpoint of adsorptive power, a polymeric hydrophobic adsorbent is preferable, and more specifically, a styrene-divinylbenzene, modified styrene-divinylbenzene, or methyl methacrylate as a base is mentioned. . Examples of styrene-divinylbenzene-based hydrophobic adsorbents include trade names Diaion HP-20, HP-21, Sepabeads SP70, SP700, SP825, SP-825, manufactured by Mitsubishi Chemical Corporation, and Organo Corporation (supplier: USA). Rum & Haas) Amberlite XAD4, XAD16HP, XAD1180, XAD2000, Sumitomo Chemical (supplier: Rohm & Haas, USA) Duolite S874, S876, and the like. Examples of the modified styrene-divinylbenzene-based hydrophobic adsorbent include those obtained by nuclear substitution of bromine atoms to increase the adsorptive power, for example, trade names such as Sepabeads SP205, SP206, and SP207 manufactured by Mitsubishi Chemical Corporation. It is done. Examples of the methyl methacrylate-based hydrophobic adsorbent include Sepa beads HP1MG and HP2MG manufactured by Mitsubishi Chemical Corporation, XAD7HP manufactured by Organo Corporation, and Duolite S877 manufactured by Sumitomo Chemical.
Of the hydrophobic adsorbents, modified polystyrene-divinylbenzene-based hydrophobic adsorbents and methyl methacrylate-based hydrophobic adsorbents are particularly preferable. The former is preferable because it has a higher adsorption capacity than polystyrene-divinylbenzene-based hydrophobic adsorbent and has a high specific gravity, so that an upflow liquid can be passed in the process. Moreover, although the latter has a small amount of adsorption, it is advantageous for adsorption of highly polar organic substances.

  Specific preferred examples include modified polystyrene-divinylbenzene-based hydrophobic adsorbents such as SP207 (Mitsubishi Chemical Corporation) and methyl methacrylate-based hydrophobic adsorbents (Mitsubishi Chemical Corporation) such as HP2MG. For the above reasons, SP207 and HP2MG are more preferable, and SP207 is more preferable.

In the first step of the present invention, the water-soluble extraction composition is passed through a column (1) packed with a hydrophobic adsorbent, and SV (space velocity) = 1 to 10 [h ⁻¹ ], The hydrophobic adsorbent was washed with 95% by volume (hereinafter referred to as [v / v]%) ethanol aqueous solution under a flow rate of 2 to 10 [v / v] as the flow rate of the hydrophobic adsorbent. It is preferable to remove the raw material monomer and impurities in the raw material monomer. In addition, SV (space velocity) uses the value measured by dividing the liquid flow rate by the liquid flow time. Then, washing with water is performed under conditions of SV = 1 to 10 [h ⁻¹ ] and a flow rate of 1 to 10 [v / v] as the flow rate of the hydrophobic adsorbent, ethanol is removed to remove the hydrophobic adsorbent. The ability to adsorb non-polymer catechins is improved by substituting the aqueous solution with water.

The condition for passing the water-soluble extraction composition through the column filled with the hydrophobic adsorbent is preferably 0.5 to 20 [v / v] as the liquid passing ratio with respect to the hydrophobic adsorbent. Is preferably SV (space velocity) = 0.5 to 10 [h ⁻¹ ]. Adsorption of non-polymer catechins may be insufficient when the flow rate exceeds 10 [h ^-1 ] or the flow rate exceeds 20 [v / v].

Furthermore, it is preferable to perform water washing after adsorbing the water-soluble extraction composition to the hydrophobic adsorbent, and it is particularly preferable to carry out water washing at a liquid passage ratio of 1 to 10 [v / v] with respect to the hydrophobic adsorbent. preferable. At this time, the liquid passing speed is preferably SV = 0.5 to 10 [h ⁻¹ ]. By this water washing, gallic acid and impurities attached to the hydrophobic adsorbent are removed. Non-polymer catechins may be eluted when washed with water at a flow rate exceeding 10 [h ^-1 ] or a water flow rate exceeding 10 [v / v], and less than 1 [v / v] If the amount of water is a multiple of the flow rate, removal of gallic acid, which is undesirable in terms of flavor, is insufficient.

The conditions for eluting the water-soluble extraction composition of the first stage of the present invention with an aqueous ethanol solution after adsorption to a column and washing with water are 10-50 [v / v]% ethanol aqueous solution per volume of hydrophobic adsorbent packed. When 0.5 to 20 [v / v] is passed, the weight ratio of caffeine and non-polymer catechins can be reduced, and the load of the caffeine removal process in the second stage cation exchange resin treatment can be reduced. In view of the above, an ethanol aqueous solution of 10 to 30 [v / v]% is particularly preferable.
Here, in the case of elution with an ethanol aqueous solution of less than 10 [v / v]%, the ratio of caffeine to non-polymer catechins decreases, but the liquid passage ratio with respect to the hydrophobic adsorbent exceeds 20 times. And the recovery rate of non-polymer catechins is low. On the other hand, when elution is performed with an ethanol aqueous solution exceeding 50 [v / v]%, the separation of caffeine and non-polymer catechins is worsened, and the second stage cation exchange resin treatment step is loaded. Therefore, it is preferable to reduce the weight ratio of the caffeine content and the non-polymer catechin composition content in the eluate to less than 0.15.

  The hydrophobic adsorbent used for the treatment in the first step can be reused by the following method. Specifically, in addition to a method that removes adsorbed caffeine by passing high-concentration ethanol of about 95 [v / v]%, an aqueous alkali solution such as sodium hydroxide is passed and washed. Then, all the aqueous solution composition components remaining on the hydrophobic adsorbent are desorbed.

  As the cation exchange resin used in the second step of the present invention, a resin having a sulfonic acid group, a carboxyl group, a phosphoric acid group, or the like is used. Specifically, the SK series including Diaion SK1B, the PK series including Diaion PK208 (manufactured by Mitsubishi Chemical), and the 100th series including Amberlite IR116 (manufactured by Rohm and Hirsch) And chelating resins such as Dowex 50W / X1 and W series (Dow Chemical Co.) and Diaion CR10 (Mitsubishi Chemical Co., Ltd.). SK-1B having a sulfonic acid group having cation exchange ability and SK-1BH in which hydrogen ion exchange has been performed in advance are preferable.

  The method of contacting the eluate obtained in the first step of the present invention with a cation exchange resin can be carried out batchwise, semi-batch, semi-continuous, or continuous. It is good to let it pass through from the viewpoint of caffeine removal efficiency. Hereinafter, the second stage process may be described as a process using a column.

  The strong cation exchange resin having a sulfonic acid group of the present invention is roughly classified into a metal ion type such as sodium ion and potassium ion and a hydrogen ion type, and the hydrogen ion type is preferable from the viewpoint of the adsorption efficiency of caffeine. When the eluate obtained in the first stage is brought into contact with the cation exchange resin packed in the column, the salt concentration in the column is less than 0.2% by weight, and the electric conductivity is 0.5 [S / m. If the metal ion is sufficiently removed from the cation exchange resin and the solution is not passed through, sufficient caffeine adsorption ability cannot be obtained. In particular, when using a metal ion type cation exchange resin, it is necessary to exchange hydrogen ions below the above-mentioned salinity and electrical conductivity by passing hydrochloric acid or the like. Specifically, by passing 1,000 to 5,000 mL of 2 mol / L hydrochloric acid at SV = 50 to 100 with respect to 100 mL of the metal ion type strong cation cation exchange resin, Washing water having a salt concentration of less than 0.2% by weight and an electric conductivity of less than 0.5 [S / m] is obtained.

  Usually, when water is passed through a column that has been cation-exchanged into the hydrogen ion type, the pH of the passing solution is lowered to about 1.0 to 3.0. However, before contacting the eluate obtained in the first stage, the column is washed with water, and the pH of the washing water is 4 or more, preferably 4.5 to 6.0, more preferably 5.0 to 5.5. Then, the sourness of the non-polymer catechin composition obtained in the second stage of the present invention is improved.

  The concentration of the aqueous ethanol solution when the eluate obtained in the first stage is brought into contact with the cation exchange resin of the present invention is 0 to 30 [v / v]% from the viewpoint of caffeine adsorption efficiency with respect to the cation exchange resin. preferable. If the caffeine adsorption capacity is not sufficiently obtained, the ethanol concentration is preferably reduced to about 0 to 20 [v / v]% by concentrating or diluting the eluate obtained in the first stage with water. Caffeine removal efficiency is improved when it is brought into contact with water. Further, when the concentration operation is performed and the aqueous system is replaced, the caffeine adsorption ability is improved by increasing the solid content concentration and then bringing it into contact with the strong ion cation exchange resin of the present invention.

As a condition for bringing the eluate obtained in the first stage into contact with the column packed with the cation exchange resin of the present invention, 0.5 to 100 [v / v] as a liquid passage ratio with respect to the cation exchange resin is used. Preferably, the liquid passing speed at this time is SV = 0.5 to 20 [h ⁻¹ ]. If the flow rate exceeds 20 [h ⁻¹ ] or the flow rate exceeds 100 [v / v], the caffeine adsorption efficiency may be insufficient.

  In the present invention, the water-soluble extract composition extracted from green tea leaves using water in the first stage is brought into contact with the hydrophobic adsorbent, and the non-polymer catechins composition and caffeine as adsorbing components are adsorbed. Sodium, potassium, magnesium and calcium contained in the extract are previously removed from the hydrophobic adsorbent. For this reason, when the eluate obtained in the first step is brought into contact with the cation exchange resin in the second step, the metal ions are sufficiently reduced, so that the adsorption efficiency of caffeine is improved and the regeneration of hydrogen ion exchange is improved. And the production efficiency is improved.

  The cation exchange resin used in the second stage of the present invention can be reused by using a predetermined method after the purification treatment. Specifically, in addition to the method of removing adsorbed caffeine by passing high-concentration ethanol of about 95 [v / v]%, recycle reuse by ion exchange to hydrogen type with hydrochloric acid and water washing Perform the operation.

  The weight ratio of the caffeine content to the non-polymer catechin content in the non-polymer catechin composition produced according to the present invention is less than 0.08, more preferably 0.09 to 0, more preferably 0.08. A value of -0.01 is preferable in terms of stability because caffeine is sufficiently reduced.

  The recovery rate of the non-polymer catechins of the non-polymer catechin composition produced according to the present invention is 70% by weight or more, more preferably 70 to 90% by weight, and more preferably 70 to 90% by weight. Non-category catechin gallate in non-polymer catechins is a change in concentration of non-polymer catechin gallate in the combined catechins is less than 10% by weight, more preferably 9 to 1% by weight, more preferably 8 to 2% by weight. It is preferable that the concentration change of the body fraction is less than 10% by weight, more preferably 9 to 1% by weight, and more preferably 8 to 2% by weight because the composition change of natural non-polymer catechins is small.

  The non-polymer catechin composition obtained in the second step of the present invention may be used as it is, and ethanol may be removed by a method such as vacuum concentration or thin film concentration. When used for blending into a normal beverage, it is preferable to completely remove ethanol. In addition, when a powder is desirable as a product form of the non-polymer catechin composition, it can be pulverized by a method such as spray drying or freeze drying.

  The non-polymer catechin composition obtained in the present invention can be blended in a packaged beverage. Containers to be used are provided in ordinary forms such as molded containers (so-called PET bottles) mainly composed of polyethylene terephthalate, metal cans, paper containers combined with metal foil or plastic film, bottles, etc., as with general beverages. be able to. The term “packaged beverage” as used herein means a beverage that can be drunk without dilution.

  Moreover, said container-packed drink is manufactured on the sterilization conditions prescribed | regulated to the food hygiene law, for example, when it can heat-sterilize after filling a container like a metal can. For PET bottles and paper containers that cannot be sterilized by retort, sterilize under the same conditions as above, for example, after sterilizing at a high temperature and short time with a plate heat exchanger, etc. The method is adopted. Moreover, you may mix | blend another component with the filled container under aseptic conditions.

(Measurement of catechins and caffeine)
Packed columns for octadecyl group-introduced liquid chromatographs using a high-performance liquid chromatograph (model SCL-10AVP) manufactured by Shimadzu Corporation, which is filtered with a filter (0.8 μm) and then diluted with distilled water. -Column TM ODS (4.6 mmφ x 250 mm: manufactured by Chemical Substance Evaluation Research Organization) was attached, and measurement was performed by a gradient method at a column temperature of 35 ° C. The mobile phase A solution was a distilled aqueous solution containing 0.1 mol / L of acetic acid, the B solution was an acetonitrile solution containing 0.1 mol / L of acetic acid, the sample injection amount was 20 μL, and the UV detector wavelength was 280 nm. (Normally, the concentrations of catechins and caffeine are expressed in weight / volume% ([w / v]%), but the contents in the examples are expressed by weight by multiplying the liquid amount).

(Measurement of electrical conductivity and salinity)
The electrical conductivity meter DS-51 manufactured by HORIBA, Ltd. was used, and the electrical conductivity [S / m] and the salt concentration (% by weight), which were values converted to 25 ° C., were used.

(Flavor evaluation after sterilization)
The non-polymer catechin composition obtained in each example was diluted with deionized water so that the catechin content was 0.175 [w / v]%, and 40 mL thereof was placed in a 50 mL pressure-resistant glass container. It was. Thereto was added 0.1% by weight of sodium ascorbate, the pH was adjusted to 6.4 with a 5% by weight aqueous sodium bicarbonate solution, nitrogen substitution was performed, and the mixture was sterilized by heating at 121 ° C. for 10 minutes in an autoclave. After that, five taste panelists confirmed the green tea-derived taste and odor.

(Evaluation method of precipitation)
The evaluation sample contained in the pressure-resistant glass container was placed in a constant temperature bath at 55 ° C., and the occurrence of turbidity after 2 weeks was confirmed. The state of the contents was observed on an illuminator, and the time when starch was observed was defined as the starch production date.

Example 1
Extract 1,200 g of Kenya CTC green tea with 24,000 g of deionized water at 95 ° C. for 10 minutes, cool and squeeze, filter through a wire mesh, remove fine particles with a Laval centrifuge, extract 19, 120 g was obtained. The extract contained 156.3 g of non-polymer catechins, and had a gallate body ratio of 53.1% and a gallo body ratio of 76.3%. Moreover, 30.9g of caffeine was contained, and the weight ratio of caffeine / non-polymer catechins was 0.198.

(First stage process)
Subsequently, 5,192 mL of hydrophobic adsorbent Sepabead SP-207 (Mitsubishi Chemical Corporation) packed in a stainless steel column (inner diameter 72.3 mm × height 1,600 mm, volume 5,745 mL) was previously set to SV = 6. Washing was performed with 95 [v / v]% ethanol 25,960 mL at 9 [h ⁻¹ ], and then with 25,960 mL water at SV = 6.9 [h ⁻¹ ].

The total amount of the extract (4.3 times volume to hydrophobic adsorbent) was passed at SV = 4.6 [h ⁻¹ ], the passing liquid was discarded, and SV = 4.6 [h ⁻¹ ] was 20, Washing was performed with 760 mL (4 volumes vs. hydrophobic adsorbent) of water. The total of the passing liquid and the washing liquid contained 2.0 g of non-polymer catechins, and there was almost no elution of non-polymer catechins by adsorption and water washing.

Then, 29,320 mL of 20 [v / v]% ethanol water was passed through SV = 4.6 [h ⁻¹ ] (5.65 times volume to hydrophobic adsorbent). After 3,000 mL of residual water in the column was cut off, 25,320 mL of eluate was recovered.

(Second stage process)
SV = 70 [h ⁻¹ ] was previously added to 1038.4 mL of ion exchange resin SK-1B (manufactured by Mitsubishi Chemical Corporation) packed in a stainless steel column (inner diameter 72.3 mm × height 3,200 mm, volume 1,302 mL). Then, hydrogen ion exchange was carried out with 29,075 mL of 2 mol / L hydrochloric acid, and then washed with 51,920 mL of ion exchange water at SV = 70 [h ⁻¹ ]. The salt concentration after hydrogen ion substitution was reduced to 0.10% by weight, and the electrical conductivity was reduced to 0.23 [S / m]. Further, the pH of the cleaning solution was 5.12, and the flavor was confirmed, so that neither acidity nor saltiness was felt.

Next, the entire amount of the eluate obtained in the first step was passed through the column subjected to hydrogen substitution at SV = 4.6 [h ⁻¹ ]. The obtained eluate was concentrated under reduced pressure, and ethanol was distilled off to obtain a non-polymer catechin composition. The concentrate contains 133.3 g of non-polymer catechins, the recovery rate of non-polymer catechins from the extract is 85.3% by weight, and the gallate content of the non-polymer catechins composition is 46.9% by weight, and the percentage of gallium in the non-polymer catechins was 82.3% by weight. Further, it contained 4.27 g of caffeine, and the weight ratio of caffeine / non-polymer catechins was 0.032.

Example 2
The 20 [v / v]% ethanol solution obtained in the first step was concentrated under reduced pressure and then subjected to the same operation as in Example 1 except that water substitution was carried out. The composition of the non-polymer catechins of the present invention I got a thing.

Example 3
A non-polymer catechin composition of the present invention was obtained in the same manner as in Example 1 except that a 40 [v / v]% ethanol solution was used in the first step.

Comparative Example 1
In the second step, the same operation as in Example 1 was performed except that 2 mol / L hydrochloric acid and water washing were not performed.

Comparative Example 2
The same operation as in Example 1 was performed except that the first step was not performed.

  Table 1 shows the analysis and evaluation results.

  Further, in any of Examples 1 to 3, compared with the comparative example, the recovery rate of non-polymer catechins before and after the treatment was high, and the change in the non-polymer catechin gallate rate and the non-polymer catechin gallo-body rate was small. A non-polymer catechin composition with reduced inn could be obtained. In addition, in the flavor evaluation after sterilization using a packaged beverage as a model system, no sourness or off-flavor or odor derived from green tea was felt, and no starch was produced after storage at 55 ° C.

Claims (5)

The water-soluble extract composition of green tea leaves is adsorbed on a column filled with a hydrophobic adsorbent, washed with water, and then 10 to 20% by volume of an aqueous ethanol solution is added to the hydrophobic adsorbent in an amount of 0. 5 to 20 [v / v] times the first stage of the step of elution and elution,
When the eluate obtained in the first step is brought into contact with the cation exchange resin, the salt concentration of water in the cation exchange resin is less than 0.2% by weight, and the electric conductivity is 0.5 [S / m]. In the second stage, the cation exchange resin is subjected to hydrogen ion substitution so that the pH is less than 4, and then washed with water so that the pH of the washing water becomes 4 or more, and the first stage process eluate is brought into contact. The manufacturing method of the non-polymer catechin composition which has a process. In the second step, the cation exchange resin is packed in the column so that the salinity of the water at the outlet of the column is less than 0.2% by weight and the electric conductivity is less than 0.5 [S / m]. The non-heavy product according to claim 1, wherein the cation exchange resin is replaced with hydrogen ions , washed with water so that the pH of water at the outlet of the column is 4 or more, and then the eluate is brought into contact with the cation exchange resin. A method for producing a combined catechin composition.   The non-polymer catechin composition according to claim 1 or 2, wherein when the eluate obtained in the first stage is brought into contact with the cation exchange resin in the second stage, the ethanol concentration in the eluate is 0 to 30% by volume. Manufacturing method. The non- polymer catechin according to any one of claims 1 to 3, wherein a weight ratio of the caffeine content to the non-polymer catechin content in the produced non- polymer catechin composition is less than 0.08. A method for producing a composition.   The recovery rate of the non-polymer catechins in the produced non-polymer catechins composition is 70% by weight or more, the concentration change of the non-polymer catechin gallate in the non-polymer catechins is less than 10% by weight and The method for producing a non-polymer catechin composition according to any one of claims 1 to 4, wherein the concentration change of the non-polymer catechin gallo body ratio in the combined catechins is less than 10% by weight.