EP1058693A1 - Procede de fabrication de produits de pectine fractionnee - Google Patents

Procede de fabrication de produits de pectine fractionnee

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Publication number
EP1058693A1
EP1058693A1 EP99965032A EP99965032A EP1058693A1 EP 1058693 A1 EP1058693 A1 EP 1058693A1 EP 99965032 A EP99965032 A EP 99965032A EP 99965032 A EP99965032 A EP 99965032A EP 1058693 A1 EP1058693 A1 EP 1058693A1
Authority
EP
European Patent Office
Prior art keywords
calcium
pectin
csp
upper limit
lower limit
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.)
Withdrawn
Application number
EP99965032A
Other languages
German (de)
English (en)
Inventor
Donald Joye
Gary Luzio
Joergen Soederberg
Maurits P. Taytelbaum
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
CP Kelco ApS
Original Assignee
Hercules LLC
Priority date (The priority date 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 date listed.)
Filing date
Publication date
Application filed by Hercules LLC filed Critical Hercules LLC
Publication of EP1058693A1 publication Critical patent/EP1058693A1/fr
Withdrawn legal-status Critical Current

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Classifications

    • C—CHEMISTRY; METALLURGY
    • C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
    • C08B—POLYSACCHARIDES; DERIVATIVES THEREOF
    • C08B37/00—Preparation of polysaccharides not provided for in groups C08B1/00 - C08B35/00; Derivatives thereof
    • C08B37/0006—Homoglycans, i.e. polysaccharides having a main chain consisting of one single sugar, e.g. colominic acid
    • C08B37/0045—Homoglycans, i.e. polysaccharides having a main chain consisting of one single sugar, e.g. colominic acid alpha-D-Galacturonans, e.g. methyl ester of (alpha-1,4)-linked D-galacturonic acid units, i.e. pectin, or hydrolysis product of methyl ester of alpha-1,4-linked D-galacturonic acid units, i.e. pectinic acid; Derivatives thereof
    • C08B37/0048—Processes of extraction from organic materials

Definitions

  • the present invention relates to a process for extracting fractionated pectin compositions directly from plant starting material in which pectin is bound.
  • a typical pectin process comprises the steps of: (1) aqueous extraction from plant starting material,
  • plant material is typically treated with dilute acids such as nitric-, sulfuric-, hydrochloric- or other inorganic or organic acids at somewhat elevated temperatures (70-90°C is specified) to remove the pectin from the cellulose components of the plant starting material.
  • dilute acids such as nitric-, sulfuric-, hydrochloric- or other inorganic or organic acids at somewhat elevated temperatures (70-90°C is specified)
  • Commonly used plant starting materials are citrus peels left over from juice production and apple pomace left over from apple juice and cider production. Extraction conditions are selected such that a major part of the pectin molecules contained in the plant starting material is transferred from the cell walls of the plant starting material to the extraction medium.
  • a mixture of solid plant material and liquid that contains the pectin remains. This mixture is then separated by filtration, centrifugation or other conventional separation steps known to those skilled in the art.
  • the wet solids cake can be re-extracted or neutralized and sold as cattle feed. Re-extractions can be done in another stage or multi-stage or continuous countercurrent extractors common to the art.
  • the extract juice is treated to precipitate pectin by addition of an appropriate alcohol. This renders the pectin insoluble in the resulting mixture of an alcohol and water.
  • the insolubilized pectin is separated from the alcohol/water mixture by appropriate means such as filtration, centrifugation, etc.
  • the resulting pectin cake is dried and milled to the desired particle size.
  • pectins are made up primarily of polygalacturonic acid chains in which rhamnose may be found. Neutral sugars may be attached to the rhamnose units. To qualify as pectin the anhydrogalacturonic acid must make up at least 65% of the ash-free dry matter in commercial type pectins.
  • the galacturonic acid units in the pectin are naturally partly esterified with methyl alcohol. According to convention, pectins with more than 50% of the carboxylic acid groups esterified with methyl alcohol are referred to as high methoxyl pectins; whereas, pectins with less than 50% of the carboxylic acid groups esterified with methyl alcohol are called low methoxyl pectins.
  • the extract as obtained by the commercial production is composed of those molecules that are soluble under the conditions of pH, temperature, and time used during the extraction.
  • the extract is composed of a mixture of molecules which differ according to molecular weight, distribution of molecular weight, and degree of esterification. In most instances, the extract is composed of high methoxyl pectins.
  • SUBST ⁇ UTE SHEET accomplished by blending different extracts and diluting with acceptable diluent such as sugar, dextrose, fructose, etc., but control of specific pectin properties is limited by this approach.
  • acceptable diluent such as sugar, dextrose, fructose, etc.
  • high methoxyl pectin is not a well-defined molecule but is actually a complex mixture of different types of pectin molecules. Individual types of high methoxyl pectins can have very useful properties.
  • One of the main functional variations between high methoxyl pectins is their sensitivity to the presence of varying concentration of polyvalent cations such as calcium ions. Sensitivity to the presence of calcium ion is defined here as calcium sensitivity.
  • US Patent No. 5,567,462 discloses a process for preparing a pecto- cellulose composition from a pectin-containing plant raw material by treating comminuted citrus peel in an acidified aqueous solution to solubilize pectin. The pectin is then recovered in the cellulosic matrix of the citrus peel by adjusting the pH of the solution and dried. The resulting pecto-cellulose product is incorporated in food and other products.
  • first extraction step mild pH conditions are used to extract a pectin fraction having a low level of calcium sensitivity. This first fraction is known as non-calcium sensitive pectin or NCSP.
  • second extraction step more acidic conditions are used to extract a pectin fraction having a high level of calcium sensitivity. This second fraction is known as calcium sensitive pectin, or CSP.
  • this invention is directed to a process comprising treating pectin starting material under conditions sufficient to form an aqueous phase rich in NCSP.
  • This invention also comprehends an aqueous composition comprising a non calcium sensitive pectin having a pH greater than 2.5 containing less than 2% by weight of alcohol.
  • this invention relates to a process comprising (1 ) treating pectin starting material under conditions sufficient to form modified pectin material rich in CSP and (2) treating the modified pectin material under conditions sufficient to form an aqueous phase rich in CSP.
  • An aqueous composition is also provided comprising a calcium sensitive pectin having a pH less than 2.5 containing less than 2% by weight of alcohol.
  • a peel composition is also embraced by this invention comprising a peel in which the ratio of CSP to the sum of CSP and NCSP is enriched. The process of this invention does not require isopropyl alcohol
  • IPA soluble calcium salt
  • Fig. 1 shows a block diagram of the process of the invention.
  • Fig. 2 shows an embodiment of the present invention using a single extractor.
  • Fig. 3 shows a multi-stage, multi-celled, countercurrent flow process embodiment of the present invention.
  • CSP can be extracted from NCSP from a source of pectin starting material using only a simple process based on differential pH acidities.
  • CSP and NCSP can be extracted directly from the pectin starting material in-situ, thus eliminating the need for first removing both fractions together in a solution and then using isopropyl alcohol and a source of cation for separating and then using filtering equipment.
  • the fractional extraction process of the present invention uses two solvents in sequence to extract the pectin fractions from the pectin starting material.
  • the first solvent contains a relatively weak acid solution and optionally may contain a small amount of a cation salt under certain conditions for extracting the NCSP while fixing the CSP in place.
  • the second solvent is a relatively strong acid solution which then extracts the remaining CSP. It has been found that the weak and strong acid solvents have pH ranges greater than 2.5 for the weak acid and less than 2.5 for the strong acid.
  • the present invention relates to a process of sequentially extracting two kinds of pectin, distinguished by their calcium sensitivity in solution, from the same plant starting material.
  • the invention described herein is a two-step extraction process, which uses a different pH in each step.
  • Pectins are generally extracted on an industrial scale using only a single step process.
  • the first step is performed under mild acid pH conditions greater than pH 2.5 and the second step is performed under strong acid pH conditions less than pH 2.5.
  • Any inorganic acid can be used.
  • the preferred acid is nitric acid.
  • Organic acids can be used also, if they are capable of the pH requirements of the invention.
  • the low pH required for the second step extraction of the present invention rules out most organic acids for this step.
  • the first step has been found to extract a non-calcium sensitive pectin or NCSP which exhibits a calcium sensitivity of 0 to 20 cps in a 0.5 weight percent (wt%) solution at 25° C. It is more preferred that the NCSP has a calcium sensitivity of 0 to 10 cps.
  • the second step has been found to extract a calcium sensitive pectin or CSP which exhibits a calcium sensitivity of greater than 20 cps in a 0.5 wt% solution at 25° C. CSP with calcium sensitivities of between 100 and 1000 cps as measured by calcium sensitivity test defined hereinafter is particularly useful.
  • calcium sensitivity is intended to mean that property of a pectin product related to an increase in the viscosity of a solution of the pectin product under appropriate conditions using the procedure as described below in the section labeled "Analytical Procedures.” Since calcium sensitivity is a strong indicator of sensitivity to other multi-valent cations, the present invention covers sensitivity to such other cations also, for example, magnesium, copper, iron, zinc, aluminum, manganese, and barium.
  • degree of esterification is intended to mean the extent to which free carboxylic acid groups contained in the polygalacturonic acid chain have been esterified (e.g., by methylation) or in other ways rendered non-acidic (e.g., by amidation).
  • degree of esterification of pectin fractions produced by the fractional extraction technique of the present invention varies from about 60% to about 80%.
  • the NCSP has typically higher DE than the CSP material. For example, NCSP has DE of 70-80%, whereas CSP has a DE of 60-70%.
  • the calcium content in the NCSP and CSP fractions of the present invention has been found to be important for their use in acid-milk stabilization properties of the pectin.
  • the preferred calcium level in the CSP pectin especially is less than 1500 ppm on a weight basis. It is preferred to have the calcium content less than 750 ppm, and more preferred less than 500 ppm. This is achieved by means common to the art, for example, ion exchange. If conversion of NCSP to low DE pectins is desired then the preferred calcium content of NCSP should also be less than 1500 ppm, preferred less than 750 ppm, and more preferred less than 500 ppm.
  • processes in accordance with the present invention comprise the treatment of plant starting material containing extractable pectin.
  • This typically includes citrus peel such as lemon, orange, grapefruit, lime, but could also include other fruits such as apple, or other vegetable matter such as sugar beets or sunflower heads.
  • FIRST STEP EXTRACTION In the first step peel, water and acid are charged to a reactor. Sufficient acid is added to the reactor in the first step to adjust the pH to a value of 2.5 to 4.0.
  • the pH of the reaction medium influences the rate at which pectin can be extracted as well as the amount. It is clear from this invention that pH also influences the type or fraction of pectin extracted.
  • pectin can be extracted under any acidic conditions from plant starting material, from pH 0 - 7, NCSP can only be extracted at pH in the range of 2.5-4.0 and at temperatures in the range of 70° C to 90°C. Above 3.3 NCSP yields are lessened, and at pH 2.7 or lower small amounts of CSP start to be extracted in the first step.
  • the lower limit of the pH range be 2.7, more preferably 2.8.
  • the preferred upper limit of the pH range is 3.0 with the most preferred pH being 3.3.
  • the resident time of extraction in the first step has a lower limit of 0.5 hour, preferably 0.75 hour, with the most preferred time being 1.0 hour.
  • the upper limit of the resident time for extraction is 5.0 hours, preferably 4.0 hours, more preferably 3.0 hours.
  • the pH is less aggressive, for example 3.0 or higher
  • no calcium addition is necessary to prevent extraction of CSP.
  • the most preferred pH range is 3.0 to 3.3.
  • the first step extraction is done under more aggressive acid conditions of pH 2.5 up to 3.0, or at more elevated temperatures than usual, for example, temperatures of 75 to 90°C, it is advantageous to add a small amount of the preferred calcium salt to the acid mixture used for the extraction.
  • the addition of calcium under more aggressive extraction conditions has been found to inhibit the release of CSP in this step.
  • the divalent cation concentration can be varied over a relatively narrow range in the first step extraction, for example from 1 to 50 millimolar (mM) concentration of calcium ion in the acid solution.
  • the preferred lower limit of this range is 3 mM with the most preferred lower limit being 5 mM.
  • the preferred upper limit of this range is 33 mM with a more preferred upper limit being 25 mM and the most preferred upper limit being 20 mM.
  • This added calcium is above that which naturally is in the plant starting material, which can be, typically, about 1% of dry weight basis. The optimal amounts of calcium ion or other divalent cation depend
  • SUBSTTTUTE SHEET (RULE 26) on pH and temperature and are a matter of simple optimization within defined parameters.
  • the pH of the first step extraction can be as low as 2.5, in which case a calcium ion concentration in the acid added to the vegetable starting material of about 20 mM was found to be advantageous.
  • the most preferred pH range is from 2.7 to 3.0.
  • Calcium salts which could be used in the first step extraction under aggressive conditions include calcium hydroxide, calcium chloride and calcium oxide.
  • the more preferred salts are calcium nitrate, calcium acetate, calcium propionate, calcium gluconate and calcium lactate.
  • the most preferred calcium salt is calcium carbonate. Lime can also be used as a source of calcium carbonate.
  • Salts of other polyvalent cations such as iron, barium, magnesium, copper and aluminum in particular, can also be used.
  • the temperature of the first step reaction is also an important variable. Pectin must be extracted at temperatures between 70 and 90°C in order to be labeled pectin. Extractions could be performed at lower temperatures, for example, 50-70°C, but the products cannot be called pectin. It is advantageous and most economical to extract the pectin at a
  • SUBSTTTUTE SHEET (RULE 26) temperature of 70°C normally. Extraction at higher temperature can hasten the release of pectin from vegetable starting material, and thus shorten the process time. However, at elevated temperatures, extraction of undesirable CSP in the first step extraction can occur, and this must be guarded against in such an operation. Extraction at elevated temperatures also has a deleterious effect on the molecular weight of the pectin. The most preferred temperature range is 70 to 75° C for the first step extraction.
  • the juice containing the NCSP is separated from the peel which still contains CSP.
  • the separation of the peel and juice is done by vacuum filtration or other such means well known in the art.
  • the aqueous composition that is separated is a NCSP pectin solution having a pH greater than 2.5 containing less than 2% by weight of alcohol. It should be understood that although no alcohol is used in this simple process, minor amounts could be in the system either as a contaminant or could be formed during the extraction; therefore, to cover these extrinsic amounts of alcohol, the term less than 2% by weight is used.
  • the juice from the first step extraction, which contains NCSP is processed under conditions normally and conventionally used for pectin isolation.
  • the remaining peel after the removal of the NCSP is CSP enriched peel that possibly can be used where a source of fiber and CSP is required. Notwithstanding, this CSP peel is typically sent to the second stage reaction vessel for further processing.
  • SUBST ⁇ JTE SHEET (RULE 26)
  • the second step extraction is performed under more acidic conditions.
  • the major difference is that the NCSP has been removed from the peel and the pectin extracted in the second step is relatively pure CSP.
  • Sufficient acid is added in the second step extraction to adjust the pH to a value of between 1.5 and 2.2.
  • the preferred upper limit of the pH range is 2.1 with the more preferred pH being 2.0.
  • Various temperatures may be used for the second extraction step ranging from 70 to 90° C, but the preferred temperature range for this second step is 70 to 75° C with no calcium added for the second step. It would be counterproductive to add calcium to this second step, where extraction of CSP is desired, because calcium has the effect of gelling or binding the CSP in the peel. Extractions could be performed at lower temperatures, for example, 50-70 C, but the products cannot be labeled as pectin.
  • the resident time of extraction in the second step has a lower limit of 0.5 hour, preferably 0.75 hour, with the most preferred time being 1.0 hour.
  • the upper limit of the resident time for extraction is 5.0 hours, preferably 4.0 hours, more preferably 3.0 hours
  • peel and liquid are separated by filtration or other means common to the art.
  • the CSP fraction is then precipitated from aqueous solution by addition of isopropyl alcohol (IPA).
  • IPA isopropyl alcohol
  • the NCSP fraction can be treated in the same way, which is conventional in the art, or can be used as aqueous solution for other processing, for example amidation or total de-esterification to produce low methoxyl grades of pectin.
  • Converting the pectin fractions to solid form and readying them for sale is carried out by conventional techniques. Drying is accomplished by conventional techniques, e.g., atmospheric or reduced-pressure ovens, to a moisture content of preferably less than 10%.
  • the drying temperature should be maintained below the temperature at which the pectin starts to lose its properties, e.g., color, molecular weight, etc. Milling techniques are well known and any known technique can be used to mill the pectin product to the desired particle size. It is most preferred that the final product be in dry, powder form, with a moisture content of 10% or less. Dry, powder form is intended to mean that the product be pourable without substantial caking. This is preferred for ease of use. In accordance with the present invention, any type of conventional equipment can be used in the present invention.
  • each of the steps can be multiple steps; this means that the two steps of this invention only refer to the two different distinct acidity pH ranges required for removing the different fractions of the pectin.
  • the equipment can be a fixed bed that moves between the stages or a fixed reactor that is stirred for intimate contact or a fixed bed that percolates the solvent through the bed. The only requirement is that the stages be so designed so that intimate contact is made in a sufficient time period in order to make the separation. Therefore, a multistage process can be used because the more stages, the more thorough the contact and separation. Processes in accordance with the present invention could be either continuous or batch, with continuous being preferred.
  • Fig. 1 shows a block diagram of the invention in its broadest sense for illustration purposes to demonstrate the simplicity of the instant invention.
  • Fig. 1 shows that water, acid, and optional cation salt is added to vessel (1) that is operated at a temperature of about 70°C for at least one hour for extracting NCSP from citrus fruit peel that has been chopped up into small pieces for this process.
  • NCSP solution with other products that are normally present in citrus fruit peel is removed and is sent to an ion exchanger (2) so that the cation is removed to an amount below 1500 ppm.
  • the NCSP solution is then sent to an evaporator (3) for removing the water from the NCSP; this evaporator can be distilled at normal distillation temperatures either under vacuum or at atmospheric pressure.
  • the NCSP is then precipitated with a cation in vessel (4) and this precipitate is sent to a drier (5) and grinding apparatus (6) where the NCSP is then dried into particles and ground to the desired sizes and the particulate product is then bagged for use.
  • the NCSP is substantially removed from the peel (that can be ascertained by sampling)
  • the CSP enriched citrus peel is then sent to the second stage (7) for CSP extraction.
  • the extracted solution containing the CSP and other side products is then sent to an ion exchanger (8) so that the cation is removed to an amount below 1500 ppm.
  • the CSP solution is then sent to an evaporator (9) for removing the water from the CSP.
  • This evaporator can be distilled at normal distillation temperatures either under vacuum or at atmospheric pressure.
  • the CSP is then precipitated in vessel (10) with a cation and this precipitate is sent to a drier (11) and grinding apparatus (12) and the particulate product is then bagged for use.
  • the spent solid citrus peel removed from the second stage (7) is then removed and disposed of by conventional disposal means; normally, it is sold to farmers for use as animal feed such as for cattle or hogs.
  • Fig. 2 illustrates a more detailed embodiment of the present invention using a single, jacketed (15), cylindrical vessel (extractor) (10) having a removable top and a porous support (11 ) for supporting a peel bed (12) positioned near the bottom of the vessel and a distributor (13) for distributing over the bed of peel the extraction fluid for percolating through the bed; both stages of the extraction takes place in extractor (10).
  • extractor or extractant fluid, is then pumped through an insulated
  • the liquid passes over the distributor (13) and drains through the bed (12) and back into the first receiver (20).
  • the recirculation loop is continued until it is indicated that substantially all of the fraction has been extracted.
  • the bed can be drained by opening the drain line as indicated by line (6).
  • Valves V1 and V4 are open while valves V2, V3, V5, V6 and V7 are closed for the first extraction; valves V2 and V3 are open while the other valves are closed for the second extraction. In this way, the bed of vegetable material can be extracted in sequence.
  • the second receiver (30) receives the CSP fraction.
  • the extraction solvent is introduced to the system through receiver (20) or (30) depending on the cycle. This is done to make sure that the extraction fluid is at the correct temperature before going to the extractor so that the system operates more efficiently.
  • the temperatures of the extractor (10) during both of the extractions are controlled by the circulation of an ethylene glycol/water mixture through the jacket (15) by way of the jacket heater and recirculator (16).
  • the jacket valves, J1 , J2, J3, and J4 control the flow of the heating fluid.
  • the flow is parallel to the receivers and in series with the extractor.
  • the temperature can be carefully monitored with probes (not shown) located in all vessels (10), (20), and (30).
  • the pressure drop across the bed of vegetable material can be controlled by the liquid level above the bed.
  • valves J1 and J4 are closed while valves J2 and J3 are opened for circulating and recirculating the heating fluid.
  • valves J1 and J4 are opened and J2 and J3 are closed. The receiver and the extractor for each of the cycles are maintained at the
  • countercurrent extractors are preferred because they recover more of the available pectin that is hydrolyzed from the vegetable material.
  • the preferred embodiment of the invention is a continuous countercurrent process equipment typical of the art.
  • a horizontal extractor in which the solids move along a conveyor belt is common geometry, or a rotary countercurrent extractor such as a Rotacel® extractor can be used.
  • the extraction battery must be adapted for introduction of two different solvents in sequence, and provision made to draw off the appropriate product.
  • Fig. 3 shows a countercurrent flow extractor (100) having two stages, the first (101 ) for extracting NCSP and the second (102) for extracting CSP.
  • first (101 ) for extracting NCSP
  • second (102) for extracting CSP.
  • different extraction fluids are used in the different stages.
  • Each stage is divided into cells (a,b,c,d,e,f,g,h,i,j)(or segments); the number of cells will depend on the design of the equipment and the desired effect that would be designed into the unit by artisan in the art.
  • This design permit for a more thorough removal of all of the NCSP from the first stage (101) and CSP from the second stage (102).
  • fillers can be used with the vegetable material to increase the rate of flow of the extracting fluid through the bed (105) or (106) as it moves along perforated the conveyor belt (103) or (104).
  • the filler material is inert to the extraction fluid adding support to the bed and creating voids for liquid percolation.
  • Natural materials such as peanut hulls, sunflower hulls, wood fiber, or mixtures thereof, are the preferred fillers.
  • Non-corrosive packing material, such as Rashig rings, wire coils or the like can also be used.
  • the fixed bed travels on a perforated conveyor belt (103) or (104) while the extracting fluid (111 or 112) moves through the bed in the opposite direction.
  • the fluid is removed along with the extracted materials and are used as the extracting fluid for a porous cell in each of the stages.
  • the extracted materials along with the extractant fluid after moving through series of cells in each stage are removed from each stage at the bottom of cell a or f via lines 107 or 108.
  • the extracting fluid and extracted materials are moved countercurrent to the bed (105 or 106) by pumps (109 or 110) and introduced to a proceedinging stage by springer means (113 or 114).
  • this embodiment has been illustrated as a bed moving on a linear conveyor belt, it could also be in the form of a rotary multistage system such as a Rotacel percolation extractor or any form well known in the art.
  • a main consideration in this system is that the beds remain substantially fixed throughout the process in each of the stages during the extraction process so as to enable intimate contact between the extracting fluid and vegetable material with minimal disturbance of the bed so that no or substantially less particulate materials are in the extract.
  • the compositions described herein offer unique performance characteristics heretofore not obtained.
  • High methoxyl CSP has the ability to imbibe more water than a corresponding material of lower degree of esterification because it has a more open structure. This results in a softer, more deformable gel which is important for many applications in food, cosmetics, etc. The gel is easily reduced to desirable small particles, and its improved deformability results in better mouth feel and creaminess.
  • the products of this invention can be used as a fat substitute because of their fat-like organoleptic properties, they can also be added to foods that normally do not contain fat just to impart the fat-like organoleptic properties.
  • CSP composition according to the present invention is more efficient in many applications, for example, up to two times more efficient in stabilizer applications for acidified protein systems, such as acidified milk drinks and yoghurt products.
  • a YOG assay as described in the analytical section hereinafter
  • Non-fractionated pectins typically have YOG values of from about 100 to about 140.
  • the CSP fraction of the pectin has a YOG value of greater than 150, preferably greater than 160, more preferably greater than 180, and most preferably greater than 200. The higher the YOG value the greater the stabilizing power of the pectin in the final product.
  • NCSP compositions according to the present invention provide better performance in those applications requiring pectin that is not reactive with cations.
  • the NCSP according to the present invention, has the advantage that it will not form gels in the presence of calcium, can be readily dissolved in solutions below 10°C, and can be dissolved in solutions
  • Products of the present invention are particularly applicable to meat, poultry, fish products, dairy products such as milk, ice cream, yoghurt,
  • SUBST ⁇ TUTE SHEET (RULE 26) cheese, pudding, and flavored dairy drinks, baked foods such as bread, cake, cookies, crackers, biscuits, pies, donuts, pretzels, and potato chips, non-dairy spreads, mayonnaise, soups, sauces, dips, dressings, frozen confections, fruit preparations, jams and jellies, beverages, water gels, confectionery jelly, and low fat spreads.
  • pectins produced by process of the present invention are applicable to sun tan lotions, sun screen compositions, creams which include emollients such as isopropylmyristate, silicone oils, mineral oils, and vegetable oils which give rise to a tactile response in the form of an increase in skin lubricity, and skin coolants such as menthol, menthyl lactate, menthyl pyrrolidone carboxylate N-ethyl-p-menthane-3-carboxamide and other derivatives of menthol, all of which give rise to a tactile response in the form of a cooling sensation on the skin, perfumes, deodorants other than perfumes, whose function is to reduce the level of, or eliminate microflora at the skin surface, especially those responsible for the development of body odor, antiperspirant actives, whose function is to reduce or eliminate the appearance of perspiration at the skin surface
  • CS Calcium Sensitivity
  • SUBSTTTUTE SHEET (RULE 26) Five (5) ml of a solution containing 250 mM calcium chloride is added to the 145 g pectin solution to give a final concentration of 8.3 mM calcium.
  • the magnet is taken out, and the glass is left at room temperature (25 C) until the next day, when the viscosity is measured at 25 C with a Brookfield viscometer.
  • the contribution by the calcium ions to the viscosity of the calcium containing solution can be calculated by subtracting the value for the calcium free solution or CS- from the value for the calcium containing solution or CS+. This value is called the CS value (in the table it is referred to as delta CS). For pectin samples with very low calcium sensitivity (CS), this difference is typically less than 20 cps.
  • results reported in the examples are the difference between measured viscosity with and without the addition of calcium. If the difference in viscosity is less than 20 cps then this is classified as a non- calcium sensitive pectin or NCSP. If the difference in viscosity is greater than 20 cps then this is classified as a calcium sensitive pectin or CSP. Viscosities of CSP types typically are greater than 100 cps.
  • To the distillation flask add 20 ml of a 1-in-10 sodium hydroxide solution, seal the connections, and then begin heating carefully to avoid excessive foaming. Continue heating until 80-120 ml of distillate has been collected. Add a few drops of methyl red TS to the receiving flask, and titrate the excess acid with 0.1 sodium hydroxide TS,
  • SUBSTTTUTE SHEET (RULE 26) recording the volume required, in ml, as S. Perform a blank determination on 20.0 ml of 0.1 jN hydrochloric acid TS, and record the volume required, in ml, as B. Record the amide titre (B-S) as V 3 .
  • the mg of galacturonic acid obtained in this way is the content of one-tenth of the weight of the washed and dried sample.
  • % galacturonic acid on a moisture-and-ash-free basis multiply the number of mg obtained by 1000/x, x being the weight in mg of the washed and dried sample.
  • Solutions of pectin with different concentrations are mixed with yoghurt, homogenized and heat treated at 70°C for 10 minutes. The amount of sediment and the viscosity are measured after cooling to 5°C.
  • Viscosimiter glasses (inner diameter: 50 mm, inner length: 110 mm)
  • Control Method 708 Yoghurt production - 17% MSNF.
  • Stabilizing Power 1 Prepare an X% pectin solution in deionized water using a Silverson mixer. Mix for 5 min. Heat to 70°C for 10 min. for dissolution of the pectin, cool and adjust for evaporated water. Calculate X as:
  • a weight attached to a computer with calculation program may be used with advantage.
  • Example #1 differs only in experimental conditions or peel source.
  • Example #2 various experimental conditions were used with one peel source.
  • Example #2 the same experimental conditions were used with different peel sources.
  • Table 1 The results for both examples are shown in Table 1. All experiments were carried out using a 12-liter, jacketed glass reaction vessel. Hot liquid circulated in the jacket to maintain reaction temperature at 70C, which was measured by a thermocouple. The reactor was provided with a stirrer which operated at mild stirring conditions sufficient to lift the peel to the surface. Acid solution of the proper concentration was prepared in the reactor and heated to temperature. Nitric acid was used in these experiments. Peel was received in shredded, dried form and contained about 12% moisture.
  • peel was then charged and the extraction allowed to proceed for a pre-determined time. Peel weight was typically 400 g. The pH was measured and adjusted during the time period, since the peel has buffering action. After the reaction was complete, the reactor contents were drained into a bucket and filtered in a large Buechner funnel or crock using filter cloth and vacuum. The wet peel was then either placed back into the reactor for the second step extraction under different pH conditions or re-extracted in a large beaker adapted for stirring and temperature control (hot plate) under the same pH conditions or with water to increase the yield of the first fraction. The extract was ion- exchanged, evaporated to concentrate the liquor, and then precipitated with IPA. The precipitate was washed with IPA/water solution and dried in a vacuum oven with nitrogen sweep. The resulting pectin material was then ground to pass through an 80 (US) Mesh screen and sent for analyses and further testing.
  • US 80
  • Example 1 Several extractions are described in this example. All experiments in this example used a single peel source designated A. In runs 4A and 11 A no additional calcium was added to the reactor. Increasing levels of calcium were added in runs 5A and 8A. Calcium was added as calcium nitrate salt. Runs 4A and 5A show similar results, both having high calcium sensitivity numbers over 600 cps for the CSP fraction and very low delta CS for the NCSP fraction. A low delta CS for the NCSP fraction indicates there is no CSP in that fraction. The overall yields and molecular weights of each fraction are similar, but the split is somewhat different.
  • Run 8A done under more aggressive acid but increased calcium addition showed similar results in some instances to runs 4A and 5A, except the calcium sensitivity of the CSP fraction was significantly less, below 600, and the split was somewhat more even.
  • the amount of NCSP in the extracted pectin varies with peel source, among other things, but the expected maximum is about 45% of the total pectin.
  • Run 11 A done under aggressive acid conditions but no added calcium shows a split higher than 40%, but also show a high delta CS for the NCSP fraction. This indicates bleed through of the CSP into the NCSP fraction, and therefore indicates undesirable run conditions. Thus runs 8A and 11 A are not preferred conditions, whereas runs 4A and 5A are.
  • the galacturonic acid content of all extracted pectin samples are typical, between 70 and 80%.
  • the degree of esterification is higher for the NCSP fraction (74-77%) than for the CSP fraction (64-68%).
  • the dilution ratios are on the basis of peel charged, for example 20 indicates 20 times as much liquid as peel on a weight basis, thus for 100 g of dried peel charged, 2 liters of liquid would be used. Additional acid solution was used in the re-extracts at a 10/1 basis.
  • Example 2 In this example different peel sources were used to extract fractionated pectins under the same conditions. From Table 1 , it is clear that the results are similar, with the splits being somewhat different, as might be expected. All peel sources were from citrus fruit (dried lemon peel) from South America.
  • the preferred pH of the second extraction is between 1.7 and 2.0, which is very typical of normal acid extraction of pectin anyway.
  • the preferred pH range for the first extraction is between 2.9 and 3.3, although this could be extended to 2.7-3.5 in our judgment.
  • a pH of 1.5 is too aggressive for the second stage, and a pH of 2.5 is too aggressive for the first stage, even though its effects can be countered by adding additional calcium, it is not preferred to do so.
  • This process uses batch extraction equipment typically found in a pectin plant rather than elaborate stagewise extraction equipment and therefore should be easy to implement. Because of its relative simplicity, this process should be more cost effective than alternative methods used to extract non- calcium and calcium sensitive pectin fractions.

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Abstract

Cette invention concerne un procédé de fabrication de pectine fractionnée à partir d'une matière de départ végétale. Le procédé fait intervenir l'extraction de matière végétale qui se déroule en deux étapes: la première étape consiste à mettre la matière végétale en contact avec une solution faiblement acide à une température et pour une durée permettant de prélever une fraction de pectine non sensible au calcium (PNSC), puis à séparer le jus extrait de la matière végétale; la seconde étape consiste à mettre la matière végétale ainsi séparée en contact avec une solution plus acide à une température et pour une durée permettant de prélever une fraction de pectine sensible au calcium (PSC).
EP99965032A 1998-12-28 1999-11-29 Procede de fabrication de produits de pectine fractionnee Withdrawn EP1058693A1 (fr)

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US22411698A 1998-12-28 1998-12-28
US224116 1998-12-28
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JP3941772B2 (ja) * 1999-01-19 2007-07-04 不二製油株式会社 根菜類由来ペクチンを含む安定剤、並びにそれを使用した酸性蛋白食品及びその製造法
JP3511952B2 (ja) * 1999-01-19 2004-03-29 不二製油株式会社 ペクチン及びその製造法並びにそれを使用した酸性蛋白食品及びその製造法
US6699977B1 (en) 2000-06-09 2004-03-02 Cp Kelco Aps Low methoxyl pectins, processes thereof, and stabilized aqueous systems comprising the same
EP1294773B1 (fr) * 2000-06-09 2006-08-23 CP KELCO ApS Pectines possedant une teneur limitee en methoxyle, procedes correspondants et systemes aqueux stabilises les contenant
EP1546209A2 (fr) * 2002-09-02 2005-06-29 CP Kelco ApS Procede ameliore pour traiter de la matiere vegetale contenant de la pectine
KR100754658B1 (ko) 2004-03-12 2007-09-03 삼성전자주식회사 통신 시스템에서 복합 재전송 운용 방법
MY159105A (en) 2009-10-30 2016-12-15 Cj Cheiljedang Corp Process for economically manufacturing xylose from hydrolysate using electrodialysis and direct recovery method
PL2628396T3 (pl) 2010-10-13 2020-03-31 Cargill, Incorporated Mieszanka w proszku
CN102033050B (zh) * 2011-01-13 2012-07-04 广东中烟工业有限责任公司 植物样品中果胶含量的测定方法
US8592575B2 (en) * 2011-06-06 2013-11-26 Cp Kelco Aps Process for extraction of pectin
CA2878399C (fr) 2012-07-13 2021-01-19 Kabushiki Kaisha Yakult Honsha Boisson lactee acide contenant de la pectine et son procede de fabrication
RU2527296C2 (ru) * 2012-12-21 2014-08-27 Федеральное государственное бюджетное образовательное учреждение Высшего профессионального образования КАБАРДИНО-БАЛКАРСКАЯ ГОСУДАРСТВЕННАЯ СЕЛЬСКОХОЗЯЙСТВЕННАЯ АКАДЕМИЯ ИМЕНИ В.М. КОКОВА Способ получения пектина из створок зеленого гороха
GB201322454D0 (en) * 2013-12-18 2014-02-05 Dupont Nutrition Biosci Aps Process
CN109306026B (zh) * 2018-07-24 2021-04-09 江西莱檬生物科技有限责任公司 柑橘类果胶的分级提取方法及应用

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US2020572A (en) * 1929-07-29 1935-11-12 Fruit Growers Exchange Ca Method of extracting pectin
JPS6178501A (ja) * 1984-09-27 1986-04-22 Kawasaki Steel Corp Ｈ形鋼の製造方法
US6143346A (en) * 1993-12-02 2000-11-07 Hercules Incorporated Pectin process and composition
US5627269A (en) * 1994-06-22 1997-05-06 Hercules Incorporated Process for the extraction of soluble polysaccharides
EP0991669B1 (fr) * 1997-06-23 2001-09-05 Danisco A/S Procedes d'extraction de fractions selectionnees de pectine, fractions ainsi obtenues et leur utilisation

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JP2002533533A (ja) 2002-10-08
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PL201281B1 (pl) 2009-03-31
KR20010041405A (ko) 2001-05-15
UA73471C2 (en) 2005-08-15
ID26580A (id) 2001-01-18
CN100381470C (zh) 2008-04-16
AU3103500A (en) 2000-07-31
RU2272812C2 (ru) 2006-03-27
IL138106A0 (en) 2001-10-31
PL342496A1 (en) 2001-06-04

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