Method for production of microfibrillary pectin-containing cellulose fibres

FIELD: food industry.

SUBSTANCE: invention relates to production of sugar beet fibres and may be used during production of a rheological properties regulator, a structure-forming gent and a thickener in food industry. The method envisages preparation of pulp from sugar beet pressure cake or chips with cellular tissue content no less than 18%, expressed pulp addition into a solution of an alkali reagent in softened water, water duty equal to 1:15-1:40, pH equal to 10-12, water temperature being 30-60°C. One performs fractional introduction of hydrogen peroxide with gradual temperature increase. The total quality of hydrogen peroxide taken is 25 kg of hydrogen peroxide with concentration equal to 30% per 50 kg of pressure cake/chips. When the temperature is 65-70°C one performs pH correction with 5-10% water alkali solution until pH is 9.0-10.0. Then one reduces temperature to 70-90°C within 20-45 minutes. Total bleaching time is 1-3 hours. Then one performs expression using a decanter centrifuge. Then pulp is washed, first - with softened water, then - with osmotic water. After each washing stage pulp is subjected to expression. Then one supplies finely dispersed ozone with further addition of 2.0-6.0% solution of Na2S2O3; one performs stirring and pulp expression using a decanter centrifuge. Then one performs repeated additional washing with further expression using a decanter centrifuge. As a result, a grainy wet product is produced.

EFFECT: production of a product wherein pectin substances are bound with a cellulose matrix which ensures good damping of fibres and a high degree of structure forming.

6 cl, 11 ex

 

The invention relates to a method for microfibrillar pectin containing cellulose fibers from vegetable raw materials of different origin. The resulting material has wide applications in food and non-food industries.

Microfibrillar cellulose, also known as microcrystalline cellulose, or microfibrillar cellulose fiber, is used as a rheology controller, amendment and thickener in the food industry, and also has wide application in food industry.

The known method of microcrystalline cellulose, including the processing of the original cellulosic material with a high shearing force at a high temperature and high pressure reaction mixture consisting of cellulosic material, compounds containing active oxygen, and water, over a period of time effective for depolymerization of cellulosic material to an average degree of depolymerization is not more than 400, or where the pressure at the output of the product is in the range 137,9-10342,1 kPa, or where the pH value of the reaction mixture during extrusion is in the range of 8-2. As compounds containing active oxygen is hydrogen peroxide (RF patent No. 2343160, SW 15/00, SW 16/00, publ. 10.01.2009). This method allows to reduce supplies the d reagents and temporary production costs, however, requires a special extrusion equipment.

The known method of microcrystalline cellulose, including the initial hydrolysis of cellulosic material white up to 65% in sulfuric acid concentration of 5-10% at atmospheric pressure and a temperature of 100-105°C for 0.5-3 hours and subsequent bleaching of the material obtained by chlorine dioxide at a flow rate of 0.5 to 3.0% by weight of absolutely dry material at a temperature of 70°C for 1-3 hours until complete absorption of chlorine dioxide (RF patent No. 2298562, SW 15/02, D21C 1/04, publ. 10.05.2007). This method allows to reduce the consumption of reagents, however, requires the use of highly toxic reagents, and high-temperature processes result in termoretratil pectin.

A method of obtaining nutritional supplements by alkaline hydrolysis of plant materials, according to which the juice of the sugar beet roots or other plants are subjected to the action of hydrate of sodium oxide or potassium in saturated lime water at pH 13-14 (SV, ed. St. No. 1799252, 1993). The disadvantage of this method is that as a result of hydrolysis in tissue composition formed by a mixed sodium-calcium or potassium-calcium salt polianovich acids, resulting substance becomes very loose, formed small particles, impairing the filtering. In addition, in the line is the use of lime water in a given interval of pH occurs inactivation of pectin.

A method of producing microfibrillar cellulose, according to which the raw material, in particular sugar beet pulp, is subjected to acid or alkaline hydrolysis, resulting in the removal of pectin and hemicellulose. Acid hydrolysis is used deionized water, concentrated hydrochloric or sulfuric acid while keeping the temperature and time regimes. When alkaline hydrolysis using sodium hydroxide solution or potassium hydroxide. With the possible addition of sodium sulfite to prevent oxidation. From the resulting suspension is extracted solid residue and subjected to repeated alkaline hydrolysis with similar conditions, and then the resulting suspension is extracted solid residue by filtration and washed pulp. This is followed by a bleaching using sodium chlorite or sodium hypochlorite or hydrogen peroxide and repeatedly remove the solids by filtration and diluted with water to a solids content of 2-10%. Then spend homogenization. The result is a product containing 80% of primary cellulose fibres, simple carboxylic acids and salts. Thus obtained product forms stable suspensions and can be used in the food industry as a substitute for fat, one hundred is ilitator for emulsions, thickener for drinks, spreads, dairy desserts and meat products (patent US 5964983 (A), (1999). The disadvantages of this process are: the multi-stage process (acid hydrolysis, several alkaline gidrolizom, bleaching); the use of chemically active agents (chlorite and sodium hypochlorite), unsuitable for use in the food industry; the use of deionized water at all stages of the process, which increases the cost of the product; the resultant product to form a suspension, and not structure-forming gel, with rheological properties.

Described similar methods of obtaining microfibrillar cellulose by acid or alkaline hydrolysis with subsequent use of the obtained product in the oil industry (US patents 6348436 B1, 2002), food industry (US 6485767 B1, 2002).

Known methods for producing microfibrillated cellulose from various raw materials of vegetable origin by acidic and/or alkaline hydrolysis with possible stages of bleaching, drying and homogenization followed by application in the food and non-food industry (US 2004074615 (A1), 2004; US 7005514 (B2), 2006; US 5068121 (A), 1991; US 2003116289 (A1), 2003; US 7074300 (B2), 2006; US 20080146701 (A1), 2008).

A method of obtaining dietary fiber from beet pulp, providing retrieve the value of sugar and remove all soluble substances by washing the pulp with water, disinfection and probelly solution of hydrogen peroxide or ozone treatment or irradiation (CS 270967, A23L 1/21, 1991). The disadvantage of this method is the high cost of the method, the formation of substances that have adverse effects on the human body.

Closest to the invention to the technical essence and the achieved result in part of the method is a method of obtaining dietary fiber from beet pulp sugar beet production, including the pressing of the pulp, steam handling saturated steam with a temperature of 125-130°C for 15-20 minutes. Processed vegetable mass is extracted with 3-5%hydrogen peroxide solution for 15 to 20 minutes to problemone. After extraction, the fiber is pressed to a solids content 15,0-16,0%, dried and crushed to a powder (Patent RF №2175844, A23L 1/214, A23L 1/308, SS 3/00, publ. 20.11.2001). High temperature processing allows you to eliminate the smell of raw materials and solve the problem of microbiological purity of the product, however, leads to the destruction of pectin and reduce the degree of water retention of the pulp fibers.

The above-mentioned disadvantages of the known methods, each separately or all together, reduce process efficiency, increase the cost of production, causing difficulties in scaling up production, do not allow to obtain a product with sawlani and properties.

The objective of the invention is to develop a method of obtaining microfibrillar pectin containing cellulose fibers, which is characterized by the following set of essential features:

1) the minimum number of process steps;

2) use non-lethal reagents minimal;

3) scalability of production.

The technical result of the invention is to improve the quality of the finished product, with a range of important characteristics:

1) has a high biological value due to the high content of pectin substances (25-30% by weight of dry matter);

2) has a high degree of water retention, a measure of water retention is 13);

3) is the regulator for the rheology in the production of products with the desired viscosity and consistency with the formation of grid structures through intermolecular bonds;

4) has the organoleptic properties of fat product;

5) it is highly absorbent and absorbent properties;

6) fully preserves its structure and properties during drying;

7) the dried product is quickly restored (coefficient of recoverability is equal to 10).

The technical result is achieved by the fact that produce pulp from the pulp or chips of sugar beet with sod is a neigh fiber is not less than 18%, add the squeezed pulp in a pre-prepared solution containing the softened water with pH=8,9-12,0, alkalinity to phenolphthalein alkaline phosphatase/f=0.2-1.0 mg-EQ/DM3total alkalinity 0.5-1.5 mg-EQ/DM3total hardness of 10-50 μg-EQ/l, total dissolved solids 150-300 mg-EQ/DM3and alkaline reagent, at a water ratio of 1:15-1:40, pH=10-12, the water temperature 30-60°C, add 2/3 of the calculated quantity of hydrogen peroxide at a temperature of 40-45°C while continuously operating the stirrer speed 30-100 rpm, with slow controlled heating to a temperature of 50-55°C, add 1/6 of calculated quantity of hydrogen peroxide with a gradual increase of the temperature to 60-65°C, add the remaining 1/6 of the hydrogen peroxide, the measurement of pH at a temperature of 65-70°C, adjusting the pH of 5-10% aqueous alkaline solution to the desired pH level=9,0-10,0, increasing the temperature of 70-90°C for 20 to 45 minutes, with a total time of bleaching 1-3 hours, followed by spinning in a centrifuge-decanter, washing the pulp with the use of softened water level pH of 8.9 to 12.0, with a level of alkalinity to phenolphthalein Yf/f=0.2-1.0 mg-EQ/DM3when the level of alkalinity of 0.5-1.5 mg-EQ/DM3with the level of total hardness of 10-50 μg-EQ/l, with a total salt levels of 150-300 mg-EQ/DM3when the water ratio of 1:10-1:30, followed what CIMOM on the centrifuge-the decanter, gradually add the squeezed pulp in the reactor with mixer on "water pillow" when the water temperature is 60-80°C, the speed of rotation of the agitator 30-100 rpm, rotation time of 5-20 minutes after receipt of the first portion of the pulp, followed by spinning in a centrifuge-decanter, goatmilk pulp using osmotic water at a water ratio of 1:10-1:30, the water temperature 30-60°C, flow melkodispersnogo ozone diameter of the bubble 0.5 to about 30.0 μm in a stream of purified air within 15-45 minutes, adding water 2,0-6,0% solution of sodium servational Na2S2O3after cessation of ozone mixing within 5-20 minutes, followed by a time of rest for 15-30 minutes, an additional 5-10 revolutions of the stirrer, the measurement of the pH of the extraction slurry in the centrifuge-the decanter, the second goatmilk by filing squeezed pulp in the reactor with a stirrer in osmotic water at a water temperature of 30-60°C. for 5-20 minutes after receipt of the first portion of the pulp, the measurement and adjustment of pH with acetic acid concentration of 30-80% to the required pH=4,5-7,0 subsequent spin in the centrifuge-decanter, getting wet granular product.

The technical result is achieved due to:

1) select the optimum temperature and time indicators of technological stages;

2) technology is the logical optimization of the bleaching process, combined with alkaline hydrolysis;

3) fractional making reagents at specific temperatures on the phase of the combined bleaching;

4) the use of process water of different quality at different stages of production.

As raw materials in the proposed method using raw materials of different origin, including waste of sugar manufacture in the form of wet or dried sugar beet shavings, granular sugar beet pulp and wheat straw, in particular, buckwheat straw, potatoes, Jerusalem artichoke, Chinese cane, cake apples, baskets sunflower, corn stalks, perennial and annual herbs.

The method is implemented as follows.

In the production microfibrillar pectin containing cellulose fibers as a raw material is preferably used waste of sugar manufacture in the form of granulated sugar beet pulp, desugared in the form of dried chips of sugar beet or wet chips of sugar beet, with a fiber content of not less than 18% and a moisture content of 7-12%.

The feedstock is placed in a hammer mill (or any similar chopper, providing a fraction of the required size) and produce fragmentation. The resulting material diffuse into fractions. The size fraction required for further production is, should be in the range of 0.5-SMM, preferably 0.5 to 2 mm, or preferably 1-2 mm

Manufacturing technology includes 2 stages: (1) times the fraction with the three-laundering; (2) bleaching with three washing.

I Use faction with three washing.

The step of steaming the faction required to remove impurities, residual Sugars, proteins, water-soluble organic acids and other intermediate products of sugar production and storage of sugar beet pulp. In addition, the swelling of the pulp, which occurs when steaming, provides the technological achievement of the subsequent stages of production.

During steaming fraction as process water use potable water in accordance with GOST 2874, SanPiN 2.1.4.1074. Tested using softened, osmotic, and distilled drinking water. It was found that the use of different types of water did not affect the quality of the resulting steaming products, so based made use of drinking water that meets the requirements of GOST 2874, SanPiN 2.1.4.1074 to reduce energy costs and other costs in the production process.

During steaming faction should run conditions:

a) water ratio of 1:10-1:30, preferably 1:20-1:30, optimally 1:30; when using smaller hydro is odule not achieved the effect of steaming pulp and is insufficient removal of impurities; the maximum water ratio increases water consumption and energy consumption during production;

b) the temperature of the process water 30-60°C., preferably 40-50°C, optimally 40-45°C; at lower temperatures does not occur steaming pulp sufficiently when using higher temperature there is damage to the structure and change of properties of the obtained product, increased energy costs;

c) time of steaming 1-2,5 hours, preferably 1-2 hours, optimally 1.0-1.5 hours with occasional stirring with the mixer rotation speed of 30-100 rpm, preferably 30-80 rpm, optimum 30-40 rpm; with a minimum of time steaming, not the effect of steaming pulp and is insufficient removal of impurities, with a longer time steaming is the violation of the structure of matter and change properties of the obtained product.

Then produce a spin in the centrifuge-the decanter. In the pressing process separates water ratio in two phases: pressed pulp and waste water.

Next, produce flushing pressed pulp. Flushing occurs in three stages using the technology of drinking water in accordance with GOST 2874, SanPiN 2.1.4.1074 at a temperature of 40-45°C. the tests with the amount of leaching from 2 to 5, the basis adopted by the washing of pulp in three stages, the Kolka with fewer leaching is not achieved its purpose, with a larger number of washes is the violation of the structure of matter and decreases the degree of moisture content of the product. To achieve the desired result must also ensure that optimum temperature, time of performance, optimum water ratio and the optimal speed of rotation of the stirrer. The time of washing the pulp before pressing 5 to 25 minutes, preferably 5-20 minutes, optimally 5-15 minutes in the reactor with mixer, with the mixer rotation speed of 30-100 rpm, preferably 30-80 rpm, optimum 30-40 rpm At a lower speed, uneven mixing, seals are formed at the bottom of the reactor at higher revs there is a partial melirovanie substances, disrupted the structure, change the properties of the obtained product. After washing produce squeezing pulp to the centrifuge-the decanter. The operation of the leaching-extraction is repeated three times with similar conditions. Used the water ratio of 1:10-1:30, preferably 1:20-1:30, optimally 1:30.

For best results, you want stirrer specific geometry: length, structure and arrangement of the blades (angle of inclination to the axis of the shaft) must be such that during operation of the mixer had no "dead zones". This is achieved by cross-location l of the jaws, inclined at an angle of 15-45, preferably 25-45°, optimally 30°, the lower end of the agitator is deployed on 1-1,5 turnover to the shaft axis. To prevent funnel effect at the time of mixing required four symmetric bump on the walls of the reactor. The blades and chippers must be perforated, holes cut with smooth edges and a diameter of 3-BSM (preferably 4-5 .5 cm, optimally 5-5 .5 cm). If the size of the holes is less uneven mixing, the concentration of pulp in the corners of the bumpers. If the size of the holes more leads to slippage and lack of contact with the reagent.

II Combined bleaching with three washing. On stage combined bleaching achieved the following objectives:

a) remove pigments, which are formed during the caramelization of sugar in sharepointsite (discoloration);

(b) effect of mild alkaline hydrolysis with pH=9-11, preferably 9-10, optimally from 9.0 to 9.2 using an alkaline reagent NaOH, NH4OH, KOH, preferably NaOH, KOH, optimally CON needed to remove free hemicellulose, while the pH from 9.0 to 9.2 ensures the preservation of uniformity of the structure of finite substances - microfibrillar pectin containing cellulose fibers;

c) deep sterilization of the product due to atomic oxygen [O-]released in d is the query result of the decomposition of hydrogen peroxide and temperature conditions 45-95°C, preferably 45-90°C, optimally 65-75°C;

d) the final stage of disinfection product using short-term supply fine stream of ozonized air;

e) the destruction of residual hydrogen peroxide aqueous solution of hyposulphite of sodium pativedha Na2S2O3·SH2O (concentration of 2.0 to 6.0%, preferably 2.0 to 4.0 percent, optimally 2,4-2,5%);

f) conservation with the use of acetic acid solution (concentration of 30-80%, preferably 30-50%, optimally 45-50%) and bringing the pH to 4.5-5.

In the bleaching process pressed pulp after the third rinse after steaming is placed in a solution containing process water and an alkaline reagent NaOH, NH4OH, KOH, preferably NaOH, KOH, optimally CON. As a result of tests using NaOH, NH4OH, CON based was made using KOH as the alkali reagent that is technologically justified when used in combination with hydrogen peroxide in the established indicators of time and temperature conditions, these conditions are optimal for obtaining the product of the required quality. The use of NH4OH when receiving fibers microfibrillar cellulose is useless because the thus obtained product cannot be used in the food industry. In using the implement NaOH received coarser pulp, do not meet the stated properties of the finished product.

In the bleaching process for the over water ratio the following conditions: pH=10-12, preferably 10,0-11,5, optimally of 11.0 to 11.2 (in a more alkaline environment is the destruction of the fibers microfibrillar cellulose, lost structural properties, reduces the viscosity of the gel; when less alkaline coagulation takes place, decreases the viscosity, lost structural properties), the water ratio 1:15-1:40, preferably 1:15-1:30, optimally 1:25 (with less water ratio decreases the efficiency of bleaching and sterilization is not achieved the maximum efficiency of the process as a result of insufficient interaction of the slurry with the reagents; more water ratio requires greater consumption of reagents, which is impractical from an economic point of view), water temperature 30-60°C., preferably 40-50°C, optimally 40-45°C. At this stage as process water, forming water ratio, use softened water level pH of 8.9 to 12.0, preferably 8,9-11,0 optimum of 9.5 to 10.5, with the level of alkalinity to phenolphthalein Yf/f=0.2-1.0 mg-EQ/DM3, preferably 0.2 to 0.5 mg-EQ/DM3optimally 0.2 to 0.3 mg-EQ/DM at the level of alkalinity of 0.5-1.5 mg-EQ/DM3, preferably 0.5-1.0 mg-EQ/DM3optimally 0.5-0.7 mg-EQ/DM the level of total hardness of 10-50 μg-EQ/l, preferably 10-30 μg-EQ/l, optimally 10-15 μg-EQ/l total salt levels of 150-300 mg-EQ/DM3preferably 150-250 mg-EQ/DM3optimally 150-200 mg-EQ/DM3. If all these optimal requirements for the water greatly reduces the possibility of blocking salts of hardness and other ions of metals and nonmetals functionally active groups microfibrillar cellulose, providing the necessary structure.

After the formation of the water ratio at a temperature of 40-45°C and continuously operating the stirrer speed 30-100 rpm, preferably 30-80 rpm, optimum 30-40 rpm, making 2/3 of the calculated quantity of hydrogen peroxide, then make slow and controlled heating, observe the pricing (the foam layer should not exceed 3-10 cm) to a temperature of 50-55°C. the geometry of the mixer should be the same as during steaming.

When the temperature reaches 50-55°C contribute 1/6 calculated quantity of hydrogen peroxide, gradually increasing the temperature to 60-65°C, the tracking nature of the foam. In the case of unmanaged increasing temperature and foaming contribute to 0.25-1% of the volume of the reactor process water with an optimal temperature of 40-45°C. and Then make the remaining 1/6 part peroxide, bodoro the and. The phased introduction of hydrogen peroxide prevents the surface interaction of the peroxide and alkali and excessive pricing, contributes to a more uniform distribution of hydrogen peroxide in the reactor, to achieve maximum efficiency of bleaching and sterilization. Most of the hydrogen peroxide is introduced at lower temperatures, because the higher the temperature, the higher is the temperature the provocation and the peroxide decomposition.

When the temperature of 65-70°C measured pH, are adjusting 5-10% (preferably 6-8%, optimally 6-6,5%) aqueous solution of NaOH, NR4OH, KOH, preferably NaOH, KOH, optimally CON to the working pH=9,0-10,0, preferably pH=9,0-9,5, optimum pH of 9.0 to 9.2.

After adjusting the pH at a temperature of 65°C, which is the beginning of the bleaching process, continue to raise the temperature of 70-90°C., preferably 70-80°C, optimally 70-75°C for 20 to 45 minutes, preferably 20-35 minutes, optimally 20 to 30 minutes. The bleaching is carried out in 1-3 hours, preferably 1-2 hours, optimally 1.0 to 1.5 hours. After this time they spin in the centrifuge-the decanter.

Next, perform the washing of the pulp. The purpose of the cleaning - removal of decayed pigments, residue free hemicellulose and destroyed cellulose fibers.

When the washing process in the s use softened water with pH=8,9-12,0, preferably 8,9-11,0 optimum of 9.5 to 10.5, with the level of alkalinity to phenolphthalein alkaline phosphatase/f=0.2-1.0 mg-EQ/DM3, preferably 0.2 to 0.5 mg-EQ/DM3optimally 0.2 to 0.3 mg-EQ/DM3when the level of alkalinity of 0.5-1.5 mg-EQ/DM3, preferably 0.5-1.0 mg-EQ/DM3optimally 0.5-0.7 mg-EQ/DM3with the level of total hardness of 10-50 μg-EQ/l, preferably 10-30 μg-EQ/l, optimally 10-15 μg-EQ/l, with a total salt levels of 150-300 mg-EQ/DM3,is preferably 150-250 mg-EQ/DM3optimally 150-200 mg-EQ/DM3, water ratio of 1:10-1:30, preferably 1:20-1:30, optimally 1:30.

Pressed pulp is gradually fed into the reactor with mixer on "water pillow". When the water temperature is 60-80°C., preferably 60-75°C, optimally 65-75°C., the rotation speed of the stirrer 30-10 rpm, preferably 30-80 rpm, optimally 30-60 rpm, the rotation 5-20 minutes, preferably 5-15 minutes, optimally 5-10 minutes from receipt of the first portion of the pulp. After a specified time produce spin in the centrifuge-the decanter.

Then make two goatmilk.

The first goatmilk - enhancing effect of bleaching, disinfection, neutralization of atomic oxygen.

When you first goatmilk use of osmotic water, the water ratio of 1:10-1:30, preferably 1:20-1:30, optimally 1:15-1:30. The pulp is served in emotions the th water at a temperature of osmotic water 30-60°C., preferably 40-50°C, optimally 40-45°C, and begin to apply melkodispersionnyy ozone in a stream of purified air within 15-45 minutes, preferably 15-40 minutes, optimally 25-30 minutes. The diameter of the bubble ozone is 0.5 to about 30.0 μm, preferably 0.5 to 10.0 μm, optimally from 0.5 to 5.0 μm. Supply of ozone required for disinfection and enhance the effect of bleaching. For smaller bubble ozone satiation product with ozone, with a larger size of the bubble is not necessary disinfection. Before and after the filing of ozone measured pH level of the contents of the reactor.

After cessation of ozone contribute aqueous solution of sodium servational Na2S2O3(solution concentration of 2.0 to 6.0%, preferably 2.0 to 4.0 percent, optimally 2,4-2,5%) to inactivate the residual amount of atomic oxygen. Conduct stirring for 5-20 minutes, preferably 5-15 minutes, optimally 5-10 minutes and leave to rest for 15-30 minutes, that was the reaction of the reagent with hydrogen peroxide. Then produce 5-10 revolutions of the mixer, record the pH and produce squeezing pulp to the centrifuge-the decanter.

Then spend the second goatmilk. The goal of the second goatmilk is conservation. The obtained pressed pulp is fed into the reactor with a stirrer in osmotic water when the water temperature 30-0°C, preferably 40-50°C, optimally 40-45°C for 5-20 minutes, preferably 5-15 minutes, optimally 5-10 minutes from receipt of the first portion of the pulp, and then record the pH, if the pH>7,0, perform the adjustment with acetic acid (concentration of 30-80%, preferably 30-50%, optimally 45-50%) to the desired pH=4,5-7,0, preferably 4,5-5,5 optimum of 4.5-5.0. Then served on a centrifuge-decanter for extraction. The optimal temperature and optimal speed mixing allows to preserve the integrity of the structure and to prevent premature gelation.

The result is a moist granular product is white or light yellow color with a neutral taste, no odor, with the content of the mass fraction of moisture 85-95%, the content of pectic substances 25-30% by weight of dry matter, ash content not more than 5%, with a complete lack of Sugars. The size of the fibers of the product is in the cross-section of 0.1 to 1.0 μm, a length of 0.5 to 50 μm.

The resulting product may be subjected to additional stages of homogenization to obtain a gel-like product. To this end, the wet granular product is diluted with softened water to the desired solids content of 0.1 to 6.5%), which provides the viscosity of the gel required for specific examples of implementation, the AC shall're asked until smooth using a cutter, blender or any similar equipment providing smooth, then pass through a homogenizer, for example, APV, at a pressure of 200 to 300 atmospheres. Operation repeat 2-4 times, optimally 3 times (by repeating the operation less than three times is not reached the maximum viscosity of the gel). The result is a gel with high viscosity:

the viscosity of a 1.0% gel (water ratio 1:45) is more than 6500 centipoise;

the viscosity of a 1.5% gel (water ratio 1:40) is more than 7200 SDR;

the viscosity of 3.0% gel (water ratio 1:32) is more than 8500 centipoise;

the viscosity of 4.5% gel (water ratio 1:20) is more than 10,000 centipoise.

Ready wet dehomogenization product may be subjected to additional stages of a continuous infrared convection drying conveyor type purge with clean air at a temperature not above 35°C, eliminating the possibility of condensation of evaporated moisture from the product to a moisture content of product 6-30%. When drying the product to a moisture content less than 6% is significant destruction of pectin. The advantages of this type of drying are: the preservation of the structure of the fibers, the ability to restore the original properties of the product, saving pectin-cellulose complex, almost complete preservation of the original content of pectin (in the examples No. 3, 8, 9, 10 of the original content of pectin is 33%, after which the loud 27-29%), optional IR disinfection, increasing the shelf life of the product. The result of the finished dry product in the form of chips.

The obtained dry chips can be subjected to a further stage of grinding to the desired size fraction of 0.5-3 mm, the result is a dry powder homogeneous product.

The finished product in the form of dry microfibrillar pectin containing cellulose fibers (in the form of chips or powder) is quickly restored to the original properties of the wet product. During the restore process, the product pour the calculated amount of softened water temperature 40-45°C in accordance with the coefficient of restitution, is maintained at a given temperature for 20-40 minutes, optimally 30 minutes. The result is a moist granular product with an initial set of properties.

In the described method it is possible to exclude pre-grinding of raw materials and fractionation when used as a feedstock dried desugared form of chips of sugar beet.

When used in the described method as a source of raw material wet chips of sugar beet in addition to the exclusion of pre-grinding and fractionation instead of steaming with triple rinsing produce twice without washing will precede the high steaming.

Hereinafter the invention is described below do not limit the scope of the present invention examples. Example No. 1.

The raw material used granulated sugar beet fiber content of 18% and a moisture content of 12%. Made a grinding of pulp in a hammer mill and sieving into fractions. Produced steaming fraction of pulp 1.5-2.5 mm in the amount of 50 kg in the reactor 1400 liters of drinking water at 45°C for 1.5 hours under stirring. Produced squeezing pulp to the centrifuge-the decanter. The resulting slurry was applied to the reactor with the mixer in pre-cooked drinking water volume of 1100 l at a temperature of 45°C, made the washing of the pulp for 10 minutes and centrifuge the centrifuge-decanter. The operation of the leaching-extraction was repeated three times.

Pressed pulp is applied to the reactor with mixer in a pre-prepared solution consisting of 900 liters of softened water and potassium hydroxide necessary to ensure a pH of 11.5 at a temperature of 45°C. Gradually increasing the temperature in the reactor to 65°C, fractional contributed 25 kg hydrogen peroxide concentration of 33%. Made to measure pH and adjust to pH=9,0 using potassium hydroxide. After adjusting the pH continued to increase the temperature up to 75°C. the Total time of bleaching was 1.5 hours. Produced squeezing pulp to the centrifuge-the decanter.

Otia the second slurry is applied to the reactor with the mixer in pre-cooked softened water volume 650 l at a temperature of 70°C, made the washing of the pulp for 10 minutes and centrifuge the centrifuge-the decanter.

Pressed pulp is applied to the reactor with the mixer in pre-cooked osmotic water volume of 500 l at a temperature of 45°C and made a submission melkodispersnogo ozone for 30 minutes after which the reactor was made of a 2.5% aqueous solution of sodium thiosulfate in an amount necessary for complete inactivation of atomic oxygen. The pulp left in the reactor with mixer for 10 minutes and made a spin in the centrifuge-the decanter.

Pressed pulp is applied to the reactor with the mixer in pre-cooked osmotic water volume of 400 l at a temperature of 45°C, made the washing of the pulp for 10 minutes, then made to measure pH and adjust to pH of 4.5 with acetic acid. Produced squeezing pulp to the centrifuge-the decanter.

As a result of operations was obtained the product in the amount of 226 kg (yield of 56.5% in terms of absolute dry content, ACC), with a mass fraction of moisture 89%containing pulp fibers, the remains of hemicellulose and pectin (the content of pectic substances by weight of solids amounted to 29.3%).

The resulting product was diluted with softened water to a solids content of 5%, was mixed until smooth, missed three times through the homogenizer (APV) when d is a pressure of 250 atmospheres and a temperature of 20°C. The viscosity of the 5% gel microfibrillar pectin containing cellulose was 10350 SDR.

Example No. 2.

The raw material used granulated sugar beet fiber content of 18% and a moisture content of 12%. Made a grinding of pulp in a hammer mill and sieving into fractions. Produced steaming fraction of pulp size 1.0-2.0 mm in the amount of 50 kg in the reactor 1400 liters of drinking water at 45°C for 1 hour under stirring. Produced squeezing pulp to the centrifuge-the decanter.

The resulting slurry was applied to the reactor with the mixer in pre-cooked drinking water volume of 1100 l at a temperature of 45°C, made the washing of the pulp for 10 minutes and centrifuge the centrifuge-the decanter. The operation of the leaching-extraction was repeated three times.

Pressed pulp is applied to the reactor with mixer in a pre-prepared solution consisting of 900 liters of softened water and potassium hydroxide necessary to ensure a pH of 11.2, at a temperature of 45°C. Gradually increasing the temperature in the reactor to 65°C, fractional contributed 25 kg hydrogen peroxide concentration of 33%. Made to measure pH and adjust to pH=9,0 using potassium hydroxide. After adjusting the pH, which is the beginning of the bleaching continued to raise the temperature to 75°C. the Total time of bleaching was 1.5 hours. Produced squeezing pulp to the centrifuge-decant the re.

Pressed pulp is applied to the reactor with the mixer in pre-cooked softened water volume 650 l at a temperature of 70°C, made the washing of the pulp for 10 minutes and centrifuge the centrifuge-the decanter.

Pressed pulp is applied to the reactor with the mixer in pre-cooked osmotic water volume of 500 l at a temperature of 45°C and made a submission melkodispersnogo ozone for 30 minutes after which the reactor was made of a 2.5% aqueous solution of sodium thiosulfate in an amount necessary for complete inactivation of atomic oxygen. The pulp left in the reactor with mixer for 10 minutes and made a spin in the centrifuge-the decanter.

Pressed pulp is applied to the reactor with the mixer in pre-cooked osmotic water volume of 400 l at a temperature of 45°C, made the washing of the pulp for 10 minutes, then made to measure pH and adjust to pH of 4.5 with acetic acid. Produced squeezing pulp to the centrifuge-the decanter.

As a result of operations was obtained the product in the amount of 242 kg (output 55,0% in terms of ACC), with a mass fraction of moisture 90%containing pulp fibers, the remains of hemicellulose and pectin (the content of pectic substances by weight of dry matter was 30.2%).

The resulting product was diluted with softened water is on the dry matter content of 5%, mixed to a homogeneous mass, missed three times through the APV homogenizer at a pressure of 250 atmospheres and a temperature of 20°C. the viscosity of the 5% gel microfibrillar pectin containing pulp amounted to SDR 10500.

Example No. 3.

The raw material used dried desugared form of chips sugar beet fiber 19,0% and a moisture content of 8.6%. Grinding is not produced. Made zatarivanie chip in quantities of 50 kg in the reactor 1400 liters of drinking water at 45°C for 1.0 hour under stirring. Produced squeezing pulp to the centrifuge-the decanter.

The resulting slurry was applied to the reactor with the mixer in pre-cooked drinking water volume of 1100 l at a temperature of 45°C, made the washing of the pulp for 10 minutes and centrifuge the centrifuge-the decanter. The operation of the leaching-extraction was repeated three times.

Pressed pulp is applied to the reactor with mixer in a pre-prepared solution consisting of 900 liters of softened water and potassium hydroxide necessary to ensure a pH of 11.2, at a temperature of 45°C. Gradually increasing the temperature in the reactor to 65°C, fractional contributed 25 kg hydrogen peroxide concentration of 33%. Made to measure pH and adjust to pH=9,0 using potassium hydroxide. After adjusting the pH, which is the beginning of the bleaching continued to increase temperatureto 75°C. The total time of bleaching was 1.5 hours. Produced squeezing pulp to the centrifuge-the decanter.

Pressed pulp is applied to the reactor with the mixer in pre-cooked softened water volume 650 l at a temperature of 70°C, made the washing of the pulp for 10 minutes and centrifuge the centrifuge-the decanter.

Pressed pulp is applied to the reactor with the mixer in pre-cooked osmotic water volume of 500 l at a temperature of 45°C and made a submission melkodispersnogo ozone for 30 minutes after which the reactor was made of a 2.5% aqueous solution of sodium thiosulfate in an amount necessary for complete inactivation of atomic oxygen. The pulp left in the reactor with mixer for 10 minutes and made a spin in the centrifuge-the decanter.

Pressed pulp is applied to the reactor with the mixer in pre-cooked osmotic water volume of 400 l at a temperature of 45°C, made the washing of the pulp for 10 minutes, then made to measure pH and adjust to pH of 4.5 with acetic acid. Produced squeezing pulp to the centrifuge-the decanter.

As a result of operations was obtained the product in the amount of 221 kg (yield 63.0% in terms of ACC), with a mass fraction of moisture 87%containing pulp fibers, the remains of hemicellulose and pectin (the content of pectic substances is the mass of dry matter was 31.3%).

The resulting product was diluted with softened water to a solids content of 5%, was mixed until smooth, missed three times through the APV homogenizer at a pressure of 250 atmospheres and a temperature of +20°C. the viscosity of the 5% gel microfibrillar pectin containing cellulose was 10800 SDR.

Example No. 4.

The raw material used sugar-free fresh chips sugar beet fiber 21% (ACC) and a humidity of 93%. Grinding and steaming are not made. Made a rinsing the chip in quantities of 50 kg in the reactor at 1100 litre drinking water at 45°C for 10 minutes and centrifuge the centrifuge-the decanter. The operation of the leaching-extraction was repeated three times.

Pressed pulp is applied to the reactor with mixer in a pre-prepared solution consisting of 900 liters of softened water and potassium hydroxide necessary to ensure a pH of 11.2, at a temperature of 45°C. Gradually increasing the temperature in the reactor to 65°C, fractional contributed 25 kg hydrogen peroxide concentration of 33%. Made to measure pH and adjust to pH=9,0 using potassium hydroxide. After adjusting the pH, which is the beginning of the bleaching continued to raise the temperature to 75°C. the Total time of bleaching was 1.5 hours. Produced squeezing pulp to the centrifuge-the decanter.

Pressed pulp is applied to the reactor with the mixer in pre-cooked and grilled and cut the military softened water volume 650 l at a temperature of 70°C, made the washing of the pulp for 10 minutes and centrifuge the centrifuge-the decanter.

Pressed pulp is applied to the reactor with the mixer in pre-cooked osmotic water volume of 500 l at a temperature of 45 C and made a submission melkodispersnogo ozone for 30 minutes after which the reactor was made of a 2.5% aqueous solution of sodium thiosulfate in an amount necessary for complete inactivation of atomic oxygen. The pulp left in the reactor with mixer for 10 minutes and made a spin in the centrifuge-the decanter.

Pressed pulp is applied to the reactor with the mixer in pre-cooked osmotic water volume of 400 l at a temperature of 45°C, made the washing of the pulp for 10 minutes, then made to measure pH and adjust to pH of 4.5 with acetic acid. Produced squeezing pulp to the centrifuge-the decanter.

As a result of the operations was the product of 23 kg (65.0% in terms of ACC), with a mass fraction of moisture 90%containing pulp fibers, the remains of hemicellulose and pectin (the content of pectic substances by weight of dry matter 32.5%).

The resulting product was diluted with softened water to a solids content of 5%, was mixed until smooth, missed three times through the APV homogenizer at a pressure of 250 atmospheres and the temperature is e 20°C. The viscosity of the 5% gel microfibrillar pectin containing cellulose was 10850 SDR.

Example No. 5.

Same as example No. 1 except that two goatmilk after bleaching as process water was used for drinking water instead of osmotic.

As a result of operations was obtained the product in the amount of 224 kg (output 56,0% in terms of ACC), with a mass fraction of moisture 89%containing pulp fibers, the remains of hemicellulose and pectin (the content of pectic substances by weight of solids amounted to 23.6%).

The resulting product was diluted with softened water to a solids content of 5%, was mixed until smooth, missed three times through the APV homogenizer at a pressure of 250 atmospheres and a temperature of 20°C. the viscosity of the 5% gel microfibrillar pectin containing cellulose was 8820 SDR.

Example No. 6.

Same as example No. 1 except that the step of steaming as process water was used softened water instead of drinking.

As a result of operations was obtained the product in the amount of 222 kg (yield of 55.5% in terms of ACC), with a mass fraction of moisture 89%containing pulp fibers, the remains of hemicellulose and pectin (the content of pectic substances by weight of dry matter 29.8%).

The resulting product was diluted with softened water content from the XIX substances 5%, mixed to a homogeneous mass, missed three times through the APV homogenizer at a pressure of 250 atmospheres and a temperature of 20°C. the viscosity of the 5% gel microfibrillar pectin containing cellulose was 10200 SDR.

Example No. 7.

Same as example No. 1 except that when the user hovers water ratio on the stage bleaching process water was used osmotic water instead of softened.

As a result of operations was obtained the product in the amount of 225 kg (yield of 56.2% in terms of ACC), with a mass fraction of moisture 89%containing pulp fibers, the remains of hemicellulose and pectin (the content of pectic substances by weight of dry matter was 27.6%).

The resulting product was diluted with softened water to a solids content of 5%, was mixed until smooth, missed three times through the APV homogenizer at a pressure of 250 atmospheres and a temperature of 20°C. the viscosity of the 5% gel microfibrillar pectin containing cellulose was 10040 SDR.

Example No. 8.

The product obtained in example No. 3, was subjected to infrared convection drying.

Moisture content of the dried product amounted to 30%. The content of pectic substances by weight of dry matter was 29.4%.

The dried product was diluted with softened water, preheated to a temperature of 45°C. until the solids content of 5%survived when asked the Oh temperature for 30 minutes.

The recovered product three times missed through the APV homogenizer at a pressure of 250 atmospheres and a temperature of 20°C. the viscosity of the 5% gel microfibrillar pectin containing cellulose was 10520 SDR.

Example No. 9.

The product obtained in example No. 3, was subjected to infrared convection drying.

Moisture content of the dried product amounted to 12%. The content of pectic substances by weight of dry matter was 28.1%.

The dried product was diluted with softened water, preheated to a temperature of 45°C. until the solids content of 5%, stood at a given temperature for 30 minutes.

The recovered product three times missed through the APV homogenizer at a pressure of 250 atmospheres and a temperature of 20°C. the viscosity of the 5% gel microfibrillar pectin containing cellulose was 10400 SDR.

Example No. 10.

The product obtained in example No. 3, was subjected to infrared convection drying.

Moisture content of the dried product amounted to 6%. The content of pectic substances by weight of dry matter was 27.6%.

The dried product was diluted with softened water, preheated to a temperature of 45°C. until the solids content of 5%, stood at a given temperature for 30 minutes.

The recovered product three times missed through the APV homogenizer at a pressure of 250 atmospheres and a temperature of 20 the S. The viscosity of the 5% gel microfibrillar pectin containing cellulose was 10240 SDR.

Example No. 11.

The product obtained in example No. 3, was subjected to infrared convection drying.

Moisture content of the dried product amounted to 2.5%. The content of pectin substances to the mass of dry solids amounted to 10.4%.

The dried product was diluted with softened water, preheated to a temperature of 45°C. until the solids content of 5%, stood at a given temperature for 30 minutes.

The recovered product three times missed through the APV homogenizer at a pressure of 250 atmospheres and a temperature of 20°C. the viscosity of the 5% gel microfibrillar pectin containing cellulose was 7500 SDR.

1. The method of obtaining microfibrillar pectin containing cellulose fibers, comprising preparing a slurry of pulp or chips sugar beet fiber is not less than 18%, add the squeezed pulp in a pre-prepared solution containing the softened water with a pH of 8.9 to 12.0, the alkalinity to phenolphthalein Yf/f=0.2-1.0 mg-EQ/DM3total alkalinity 0.5-1.5 mg-EQ/DM3total hardness of 10-50 μg-EQ/l, total dissolved solids 150-300 mg-EQ/DM3and alkaline reagent, at a water ratio of 1:15-1:40, pH 10-12, water temperature 30-60°C, add 2/3 of the calculated quantity of hydrogen peroxide when the temperature is e 40-45°C while continuously operating the stirrer speed 30-100 rpm, with slow controlled heating to a temperature of 50-55°C, add 1/6 of calculated quantity of hydrogen peroxide with a gradual increase of the temperature to 60-65°C, add the remaining 1/6 of the hydrogen peroxide, the measurement of pH at a temperature of 65-70°C, adjusting the pH of 5-10% aqueous alkaline solution to the desired pH of 9.0 to 10.0, a temperature of 70-90°C for 20-45 minutes, with a total time of bleaching 1-3 hours, followed by spinning in a centrifuge-decanter, washing the pulp with the use of softened water with a pH of 8.9 to 12.0, with a level of alkalinity by the phenolphthalein Yf/f=0.2-1.0 mg-EQ/DM3when the level of alkalinity of 0.5-1.5 mg-EQ/DM3with the level of total hardness of 10-50 μg-EQ/l, with a total salt levels of 150-300 mg-EQ/DM3when the water ratio of 1:10-1:30, followed by spinning in a centrifuge-decanter, gradually add the squeezed pulp in the reactor with mixer on "water pillow" when the water temperature is 60-80°C, the speed of rotation of the agitator 30-10 rpm, rotation time of 5-20 minutes after receipt of the first portion of the pulp, followed by spinning in a centrifuge-decanter, goatmilk pulp using osmotic water at a water ratio of 1:10-1:30, the water temperature 30-60°C, flow melkodispersnogo ozone diameter of the bubble 0.5 to about 30.0 microns in a stream of purified air in for 15-45 m is h, add water 2,0-6,0%-aqueous solution of sodium servational Na2S2O3after cessation of ozone mixing within 5-20 min, followed by a rest time of 15-30 min, additional 5-10 revolutions of the stirrer, the measurement of the pH of the extraction slurry in the centrifuge-the decanter, the second goatmilk by filing squeezed pulp in the reactor with a stirrer in osmotic water when the water temperature 30-60°C for 5-20 min after receipt of the first portion of the pulp, the measurement and adjustment of pH with acetic acid concentration of 30-80% to the desired pH 4,5-7,0 subsequent spin in the centrifuge-decanter, getting wet granular product, the total number of hydrogen peroxide charge based on 50 kg of pulp/chip 25 kg hydrogen peroxide concentration of 33%.

2. The method according to claim 1, wherein preparing a slurry of the dried desugared form of chips of sugar beet by steaming at a water ratio of 1:10-1:30, the temperature of drinking water 30-60°C, time of steaming 1-2,5 hours, with occasional stirring with the mixer rotation speed of 30-100 rpm, followed by spinning in a centrifuge-decanter with separation of water ratio in the slurry and waste water and three times with washing pressed pulp drinking water when the water temperature 40-45°C for 5-25 min in the reactor included with the Noi stirrer, with the mixer rotation speed of 30-100 rpm, centrifuge the slurry in the centrifuge-the decanter after each washing step.

3. The method according to claim 1, characterized in that the pulp is prepared from sugar-free wet chips sugar beet humidity 7-12% by twice washing with drinking water when the water temperature 40-45°C for 5-25 min in the reactor with mixer, with the mixer rotation speed of 30-100 rpm, centrifuge the slurry in the centrifuge-the decanter after each washing step.

4. The method according to claim 1, characterized in that the pulp is prepared from granulated sugar beet pulp with a moisture content of 7-12% by crushing and fractionation to the size fraction of 0.5-3 mm.

5. The method according to claim 1, characterized in that the ready wet granular product is diluted with softened water to a solids content of 0.1 to 6.5%, and passed through the homogenizer at a pressure of 200 to 300 atmospheres, the operation is repeated 2-4 times, get a gel-like product.

6. The method according to claim 1, characterized in that the ready wet granular dehomogenization the product is placed in an infrared drying unit, is subjected to continuous infrared convection drying conveyor type purge with clean air at a temperature not above 35°C, eliminating the possibility of condensation of evaporated moisture from the product to a moisture content of product 6-30%, get ready the dry product in view of the chip or grind it to a powder, homogeneous state.



 

Same patents:

FIELD: chemistry.

SUBSTANCE: invention relates to food industry and can be used in producing pectin from vegetable material. The method involves hydrolysis and extraction of vegetable material in an electromagnetic field, separating the solid and liquid phases, concentrating, depositing pectin and drying the pectin. Hydrolysis and extraction of the vegetable material is carried out with aqueous solution of citric acid and succinic acid at temperature of 80-90°C and pH=2 in an electromagnetic field with frequency of 25-29 Hz for 55-90 minutes. The citric acid and succinic acid are taken in ratio of 3:2, respectively. Further, the material is concentrated to pectin substance concentration of 5% and coagulated with 96% ethyl alcohol for 10 minutes. The coagulate is subjected to infrared drying in a vacuum at pressure of 0.08±0.02 MPa and temperature of 35-40°C to moisture content of the end product of not more than 7%.

EFFECT: invention increases output of pectin and increases complexing capacity thereof.

3 ex, 1 tbl

FIELD: food industry.

SUBSTANCE: method for processing silver fir wood green envisages raw material milling, the raw material treatment with an alkali solution, the raw material filtering to remove the resultant solution, acids separation by way of extraction with an organic solvent. After milling the raw material is treated with 0.1-0.5% water solution of a mineral acid at a temperature of 50±5°C with the filtered raw material subsequent two-times washing with water. Then the blended acid filtrates are concentrated by way of water boiling out in a rotor evaporator at a temperature of 60°C. Polysaccharides are sedimented from the resultant concentrate with excessive ethanol. The raw material remaining after polysaccharides extraction is subjected to treatment with an alkali and an organic solvent to separate triterpenic acids.

EFFECT: invention enables silver fir wood green processing to produce polysaccharides and triterpenic acids and to increase the target products yield.

2 ex

FIELD: food industry.

SUBSTANCE: invention relates to technical biochemistry, in particular - to determination of pectin substances quantity in vegetal raw material. "Standardised" solutions of pectin substances fractions are prepared. The fractions solutions are sampled. Saponification of pectin substances fractions in the samples of the solutions being analysed is performed with 2.5 ml of 40% NaOH solution. The pectin substances fractions are sedimented with 2.5 ml of concentrated HCl. The solutions being analysed are centrifuged in 50 ml test tubes, rotation frequency being no less than 500 rpm, during 5-7 minutes. The sediments of pectin substances fractions are suspended in distilled water in a titration cup on a magnetic stirrer for at least 30 minutes. One performs conductometric titration of the suspension of pectin substances fractions sediment, stirring. Following the conductometric titration results, graphs are drawn, relying whereon one identifies the volume of the titrant spent on pectin acid titration. Pectin substances fractions weight percentage is calculated from the formula: ω=176×0,2×V10×200×100, where 176 - pectin acid equivalent; 0.2 - titrant normality; V - titrant volume spent on pectin acid titration, ml; 200 - volume of the solution of the corresponding pectin substances fraction taken for analysis, ml; 10 - conversion to acid milliequivalents (1 ml of 0.1n NaOH corresponding to 0.1 acid milliequivalent); 100 - percentage conversion factor.

EFFECT: invention enables obtainment of accurate data with high coincidence of parallel analyses and ensures labour and time expenditures saving at all the process stages.

6 dwg, 1 ex

FIELD: medicine, pharmaceutics.

SUBSTANCE: invention refers to methods for preparing low-molecular pectin and may be used in pharmaceutical industry for preparing new therapeutic and preventive drugs, low-molecular sorbents. The method provides pectin hydrolysis in an aqueous solution of mineral acid and liquid phase separation from an insoluble residue of pectin. The low-molecular products of pectin hydrolysis are recovered from the liquid phase by settling them in an organic solvent with water. A hydrolysis feed material is low-etherified pectin of ratio max. 30%. The hydrolysis process is continuous in a continuous-flow machine. Temperature in a working chamber of the machine is maintained at 70-100°C. Feeding speed of mineral acid into the chamber is calculated by specific formula. The prepared liquid phase is neutralized to pH min. 4.0. Thereafter, the prepared liquid phase is used to settle the low-molecular products of pectin hydrolysis.

EFFECT: invention enables producing low-molecular pectin with no process loss of the feed material, substantially reducing oligogalacturonide destruction accompanying the hydrolysis process, and thereby improving the end product yield.

5 cl, 1 dwg, 4 ex

FIELD: medicine, pharmaceutics.

SUBSTANCE: invention refers to methods for preparing low-molecular pectin and may be used in pharmaceutical industry for preparing new therapeutic and preventive drugs, low-molecular sorbents. The method provides pectin hydrolysis in an aqueous solution of mineral acid with heating and liquid phase separation from an insoluble residue of pectin. The low-molecular products of pectin hydrolysis are recovered from the liquid phase by settling them in an organic solvent with water. A hydrolysis feed material is low-etherified pectin of ratio max. 30%. The hydrolysis process is continuous in a continuous-flow machine. Temperature in a working chamber of the machine is maintained at 70-100°C. Feeding speed of mineral acid into the chamber is calculated by specific formula. The prepared liquid phase is exposed to additional heat treatment in a flow heat exchange following the hydrolysis process. Temperature of the additional heat treatment process coincides with hydrolysis temperature. Heat exchange section capacity is determined by specific formula. The prepared liquid phase is neutralised to pH min. 4.0. Thereafter, the prepared liquid phase is used to settle the low-molecular products of pectin hydrolysis.

EFFECT: invention enables producing low-molecular pectin with no process loss of the feed material, substantially reducing oligogalacturonide destruction accompanying the hydrolysis process, and thereby improving the end product yield.

5 cl, 1 dwg, 4 ex

FIELD: food industry.

SUBSTANCE: invention relates to food industry. The method envisages dry beet pulp swelling in 30-40°C water at a ratio of 1:20 during 30-40 minutes. Then pulp completely swollen is squeezed and twice washed with cold water. Then the washed pulp is poured with a 0.5-2.0% enzyme preparation solution with high cellulolytic activity. The weight ratio of beet pulp and the enzyme preparation is chosen within the range of 1 :(13-15). The mixture is maintained at a temperature of 40-42°C during 1-2 hours while continuously stirred. Then the mixture is separated. One pours the produced pulp with milk whey at a ratio of 1:(13-15) and performs hydrolysis extraction during 2-2.5 hours at a temperature of 95-98°C while continuously stirring. Then one performs hydrolysate separation and filtration. Then the final product is packed.

EFFECT: invention allows to produce a food pectin beet extract with good organoleptic indices and ensure a non-waste technology of sugar beet processing.

3 ex

FIELD: food industry.

SUBSTANCE: method envisages milling coniferous trees greens. Then one extracts the tree greens with ethyl acetate and chloroform. Then remains are extracted in three stages: with distilled water, with water acidified with hydrochloric acid, with water solution of potassium hydroxide. Then one proceeds with concentration and settlement with ethyl alcohol. Then the sediment is centrifuged, dissolved in water and dialysed against distilled water. One performs lyophilic drying of the target product.

EFFECT: invention allows to produce pectin polysaccharides and glucuron- oxylan class hemicellulases of coniferous trees greens with high yield and high purification degree.

7 cl, 1 dwg, 1 tbl, 4 ex

FIELD: chemistry.

SUBSTANCE: invention relates to methods of producing low-molecular pectin. The method involves hydrolysis of pectin in aqueous solution of mineral acid while heating. Further, the liquid phase is separated from the insoluble pectin residue and neutralised to pH lower than 4.0. Low-molecular pectin hydrolysis products are extracted through precipitation thereof using a water-miscible organic solvent. After precipitation, the obtained low-molecular pectin hydrolysis products are dried. The starting material used for hydrolysis is low-etherified pectin with etherification degree of not more than 30%. Hydrolysis is carried out in cycles. The duration of one cycle is calculated using a given formula.

EFFECT: invention enables to obtain low-molecular pectin without process loss of material and also significantly ensures destruction of oligogalacturonides, thus increasing ultimate output of the product.

2 cl, 6 ex

FIELD: chemistry.

SUBSTANCE: invention relates to methods of producing low-molecular pectin. The method involves hydrolysis of pectin in aqueous solution of mineral acid while heating. Further, the liquid phase is separated from the insoluble pectin residue and neutralised to pH lower than 4.0. Low-molecular pectin hydrolysis products are extracted through precipitation thereof using a water-miscible organic solvent. After precipitation, the obtained low-molecular pectin hydrolysis products are dried. The starting material used for hydrolysis is low-etherified pectin with etherification degree of not more than 30%. Hydrolysis is carried out in cycles. The duration of one cycle is calculated using a given formula. After separation from the pectin residue, the liquid phase undergoes further hydrolysis. The duration of one cycle of additional hydrolysis is calculated using a formula.

EFFECT: invention enables to obtain low-molecular pectin without process loss of material and also significantly ensures destruction of oligogalacturonides, thus increasing ultimate output of the product.

2 cl, 6 ex

FIELD: chemistry.

SUBSTANCE: invention relates to methods of obtaining pectine polysaccharides from waste wood and can be used in food, pharmaceutical, chemical and other industries. Siberian larch bark (Larix sibirica Ledeb.) and/or Dahurian larch bark (Gmelin) (Larix gmelinii Rupr. (Rupr.)) is prepared for complete extraction of pectine polysaccharides through successive treatment with acetylacetate, water and a solution of oxalic acid.The bark residue is then extracted with an ammonium oxalate solution at 60-70°C for 3-5 hours and then concentrated. The end product is then dropped into 96% ethanol and lyophilically dried.

EFFECT: disclosed method provides high output of up to 12% of pectine polysaccharides from larch bark, having membrane stabilising activity and capable of reducing silver ions from salt solutions to nanosize particles with zero valence, where during the reaction a nanobiocomposite is formed from silver nanoparticles with particle size of 3-27 nm, which are stabilised with an amorphous matrix - pectine.

4 cl, 2 dwg, 1 tbl, 6 ex

FIELD: food industry.

SUBSTANCE: invention relates to a technology for processing vegetables. The method envisages rutabaga preparation, cutting, convective drying till intermediate moisture content, additional drying in microwave field till dry substances content is equal to no less than 85%, impregnation with liquid carbon dioxide with simultaneous pressure boost, depressurisation to atmospheric value with simultaneous freezing of carbon dioxide, carbon dioxide subliming with simultaneous swelling of rutabaga, the latter packing into package fabricated of a polymer or combined material in an oxygen-free medium.

EFFECT: method allows to reduce losses of biologically active substances of initial raw materials.

FIELD: food industry.

SUBSTANCE: invention relates to a technology for processing vegetables. The method envisages yacon preparation, cutting, convective drying till intermediate moisture content, additional drying in microwave field till dry substances content is equal to no less than 85%, impregnation with liquid carbon dioxide with simultaneous pressure boost, depressurisation to atmospheric value with simultaneous freezing of carbon dioxide, carbon dioxide subliming with simultaneous swelling of yacon, the latter packing into package fabricated of a polymer or combined material in an oxygen-free medium.

EFFECT: method allows to reduce losses of biologically active substances of initial raw materials.

FIELD: food industry.

SUBSTANCE: invention relates to food industry and may be used for production of a high-quality biologically active additive applied in dietetic alimentation and for creation of food products of functional and specialised purpose. The biologically active food supplement having anti-inflammatory properties against gastrointestinal tract diseases represents a powder. The powder is produced of girasol tubers by way of their sorting, washing, rinsing with a water solution of carbon dioxide produced by way of carbon dioxide bubbling into water under a pressure equal to 0.1 MPa, girasol tubers dispersion into finely dispersed mass with particle size equal to 50-60 mcm. The produced mass is dried at a temperature of 60-70°C until the moisture content is 6-8%, dried material is cooled to 20-25°C and cooled dried material is milled into particles sized 30-35 mcm.

EFFECT: invention allows to produce, in accordance with the proposed modes, a biologically active food additive with high activity of anti-inflammatory properties against gastrointestinal tract diseases.

2 ex

FIELD: food industry.

SUBSTANCE: invention relates to food industry and can be used for production of high-quality biologically active additives applied for immediate food consumption by way of prophylactics or for creation of food products of specialised purpose. The biologically active food additive having hypoglycaemic properties represents a powder. The powder is produced of girasol tubers by way of their sorting, washing, rinsing with a water solution of carbon dioxide produced by way of carbon dioxide bubbling into water under a pressure equal to 0.1 MPa, girasol tubers dispersion into finely dispersed mass with particle size equal to 50-60 mcm. The produced mass is dried at a temperature of 60-70°C until the moisture content is 6-8%. Dried material is cooled to 20-25°C and cooled dried material is milled into particles sized 30-35 mcm.

EFFECT: invention enables production of a biologically active food additive having a high efficiency of hypoglycaemic properties due to the modes proposed.

2 ex

FIELD: food industry.

SUBSTANCE: invention relates to vegetables processing. The method envisages prepared stachys cutting, convective drying till intermediate moisture content, additional drying in microwave filed till dry substances content is equal to no less than 85%, impregnation with liquid carbon dioxide with simultaneous pressure boost, depressurisation to atmospheric value with simultaneous freezing of carbon dioxide, carbon dioxide subliming with simultaneous swelling of stachys. One performs the manufactured product packing it into a package fabricated of a polymer or combined material in an oxygen-free medium.

EFFECT: invention allows to reduce losses of biologically active substances of initial raw materials.

FIELD: food industry.

SUBSTANCE: invention relates to vegetables processing. The method envisages prepared parsnip root cutting, convective drying till intermediate moisture content, additional drying in microwave filed till dry substances content is equal to no less than 85%, impregnation with liquid carbon dioxide with simultaneous pressure boost, depressurisation to atmospheric value with simultaneous freezing of carbon dioxide, carbon dioxide subliming with simultaneous swelling of parsnip root. One performs the manufactured product packing it into a package fabricated of a polymer or combined material in an oxygen-free medium.

EFFECT: invention allows to reduce losses of biologically active substances of initial raw materials.

FIELD: food industry.

SUBSTANCE: invention relates to food industry, in particular, to functional vegetable food products manufacture. Girasol flakes manufacture involves sorting fresh girasol tubers in terms of quality and size, washing with cold running water in three serially installed washing machines until complete removal of soil contaminations. For reduction of microbiological contamination, enzymes activity and pH increase the tubers are blanched in 1% solution of citric acid. Girasol tuber re delivered into the grating grinder and milled to produce flakes. The flakes are sprinkled with 0.01% solution of ascorbic acid from a sprinkler or in a showering installation and delivered into the IR dryer. Drying lasts 3-4 hours at a temperature of 65°C until production of a product with residual moisture content equal to 12%.

EFFECT: method provides for production of girasol flakes according to a low waste technology.

1 tbl

FIELD: food industry.

SUBSTANCE: invention relates to food industry. The method envisages extraction, pressing, drying, crushing, sieve fractionation and ferric impurities removal. The extragent is represented by water acidified with citric acid till pH equal to 5.0 -5.2 at a ratio of the milled mass to extragent being 1: 1.5. Extraction is performed at a temperature of 80-85°C during 15 minutes. Drying of the presscake pressed after extraction is performed at a temperature of 100-105°C till residual moisture content is equal to 8.5-10%. Crushing is performed into powdery condition with subsequent sieve fractionation and ferric impurities removal.

EFFECT: method allows to create a simple and non-waste method for girasol tubers processing and ensures uniform charge of the technological line for production of food fibres during the year.

FIELD: food industry.

SUBSTANCE: invention relates to a technology for processing vegetables. The method envisages girasol preparation, cutting, convective drying till intermediate moisture content, additional drying in microwave field till dry substances content is equal to no less than 85%, impregnation with liquid carbon dioxide with simultaneous pressure boost, depressurisation to atmospheric value with simultaneous freezing of carbon dioxide, carbon dioxide subliming with simultaneous swelling of girasol, the latter packing into package fabricated of a polymer or combined material in an oxygen-free medium.

EFFECT: method allows to reduce losses of biologically active substances of initial raw materials.

FIELD: food industry.

SUBSTANCE: method envisages scorzonera preparation, cutting, convective drying till intermediate moisture content, additional drying in microwave field till dry substances content is equal to no less than 85%, impregnation with liquid carbon dioxide with simultaneous pressure boost, depressurisation to atmospheric value with simultaneous freezing of carbon dioxide, carbon dioxide subliming with simultaneous swelling of scorzonera, the latter packing into package fabricated of a polymer or combined material in an oxygen-free medium.

EFFECT: invention allows to reduce losses of biologically active substances of initial raw materials.

FIELD: food industry.

SUBSTANCE: invention relates to food industry. During the food product manufacture fruit raw materials are prepared; fruits are cut, strained and stirred. One adds ascorbic acid in an amount of 1-1.5% and a structure-forming component (in an amount of 3-5% of the weight of fruit puree) represented by pectin or modified starch or an extrusion product and performs stirring. One moulds a 1-1.5 cm thick stratum from the produced fruit puree and performs infrared drying at a temperature of 53-55°C during 20-24 minutes till moisture content is equal to 5-7%. The stratum is cut and packed in an oxygen-free medium into bags of combined material such as polymer-foil-polymer.

EFFECT: manufactured food product contains all the biologically active substances of the initial raw materials in the native form, has a consistency and appearance specific to chips but containing no by-side toxic substances including acrilamide generated in the process of thermal treatment.

5 cl, 1 tbl, 3 ex

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