CN1285615C - Inulin extraction process - Google Patents
Inulin extraction process Download PDFInfo
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- CN1285615C CN1285615C CN 200410073338 CN200410073338A CN1285615C CN 1285615 C CN1285615 C CN 1285615C CN 200410073338 CN200410073338 CN 200410073338 CN 200410073338 A CN200410073338 A CN 200410073338A CN 1285615 C CN1285615 C CN 1285615C
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- JYJIGFIDKWBXDU-MNNPPOADSA-N inulin Chemical compound O[C@H]1[C@H](O)[C@@H](CO)O[C@@]1(CO)OC[C@]1(OC[C@]2(OC[C@]3(OC[C@]4(OC[C@]5(OC[C@]6(OC[C@]7(OC[C@]8(OC[C@]9(OC[C@]%10(OC[C@]%11(OC[C@]%12(OC[C@]%13(OC[C@]%14(OC[C@]%15(OC[C@]%16(OC[C@]%17(OC[C@]%18(OC[C@]%19(OC[C@]%20(OC[C@]%21(OC[C@]%22(OC[C@]%23(OC[C@]%24(OC[C@]%25(OC[C@]%26(OC[C@]%27(OC[C@]%28(OC[C@]%29(OC[C@]%30(OC[C@]%31(OC[C@]%32(OC[C@]%33(OC[C@]%34(OC[C@]%35(OC[C@]%36(O[C@@H]%37[C@@H]([C@@H](O)[C@H](O)[C@@H](CO)O%37)O)[C@H]([C@H](O)[C@@H](CO)O%36)O)[C@H]([C@H](O)[C@@H](CO)O%35)O)[C@H]([C@H](O)[C@@H](CO)O%34)O)[C@H]([C@H](O)[C@@H](CO)O%33)O)[C@H]([C@H](O)[C@@H](CO)O%32)O)[C@H]([C@H](O)[C@@H](CO)O%31)O)[C@H]([C@H](O)[C@@H](CO)O%30)O)[C@H]([C@H](O)[C@@H](CO)O%29)O)[C@H]([C@H](O)[C@@H](CO)O%28)O)[C@H]([C@H](O)[C@@H](CO)O%27)O)[C@H]([C@H](O)[C@@H](CO)O%26)O)[C@H]([C@H](O)[C@@H](CO)O%25)O)[C@H]([C@H](O)[C@@H](CO)O%24)O)[C@H]([C@H](O)[C@@H](CO)O%23)O)[C@H]([C@H](O)[C@@H](CO)O%22)O)[C@H]([C@H](O)[C@@H](CO)O%21)O)[C@H]([C@H](O)[C@@H](CO)O%20)O)[C@H]([C@H](O)[C@@H](CO)O%19)O)[C@H]([C@H](O)[C@@H](CO)O%18)O)[C@H]([C@H](O)[C@@H](CO)O%17)O)[C@H]([C@H](O)[C@@H](CO)O%16)O)[C@H]([C@H](O)[C@@H](CO)O%15)O)[C@H]([C@H](O)[C@@H](CO)O%14)O)[C@H]([C@H](O)[C@@H](CO)O%13)O)[C@H]([C@H](O)[C@@H](CO)O%12)O)[C@H]([C@H](O)[C@@H](CO)O%11)O)[C@H]([C@H](O)[C@@H](CO)O%10)O)[C@H]([C@H](O)[C@@H](CO)O9)O)[C@H]([C@H](O)[C@@H](CO)O8)O)[C@H]([C@H](O)[C@@H](CO)O7)O)[C@H]([C@H](O)[C@@H](CO)O6)O)[C@H]([C@H](O)[C@@H](CO)O5)O)[C@H]([C@H](O)[C@@H](CO)O4)O)[C@H]([C@H](O)[C@@H](CO)O3)O)[C@H]([C@H](O)[C@@H](CO)O2)O)[C@@H](O)[C@H](O)[C@@H](CO)O1 JYJIGFIDKWBXDU-MNNPPOADSA-N 0.000 title claims abstract description 233
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- Polysaccharides And Polysaccharide Derivatives (AREA)
Abstract
本发明公开了一种菊粉的提取工艺，利用菊苣鲜根作原料，将鲜根妥善处理，能实现菊粉的长年生产；生产的菊粉产品多样，如生产聚合度小于9的可以用于功能性饮料的添加物，改善其口感；生产聚合度分布在10～45且含量75%以上的高效菊粉，用于碳水化合物代谢紊乱的治疗；可以生产聚合度在20-45之间的菊粉，用于脂肪的替代品或纤维食品，和用于化工业或制药工业作赋形剂的聚合度在45以上的菊粉；可以生产不易结块和凝块的精制菊粉及稀释性降级、溶解度提高的特定聚合度的菊粉。
The invention discloses an inulin extraction process. The fresh chicory roots are used as raw materials. The fresh roots are properly processed to achieve the long-term production of inulin. Various inulin products are produced, such as inulin with a degree of polymerization less than 9 which can be used as an additive for functional beverages to improve their taste; inulin with a degree of polymerization of 10 to 45 and a content of more than 75% can be produced for the treatment of carbohydrate metabolic disorders; inulin with a degree of polymerization between 20 and 45 can be produced for fat substitutes or fiber foods, and inulin with a degree of polymerization of more than 45 can be used as an excipient in the chemical industry or the pharmaceutical industry; refined inulin that is not easy to agglomerate and coagulate and inulin with a specific degree of polymerization with reduced dilution and improved solubility can be produced.
Description
Technical field
The invention belongs to chemical industry and extract field, particularly a kind of extraction process of inulin.
Background technology
Inulin (inulin) be by between the residue of fructose (F) with β-2, the 1-glycosidic link connects and end has the straight-chain polysaccharide that is connected with glucosyl residue (G), also contains the promptly terminal Polylevulosan that does not connect glucosyl residue of a spot of another kind of Polylevulosan (inulonose) in addition in the inulin.Inulin is present in each kind of plant widely, and especially content is higher in the feverfew root, as jerusalem artichoke 15-20%, and witloof 13-20% (it is heavy to account for bright root).Different production technique, different plants, different breeding times, the inulin mean polymerisation degree difference that plant produced under the different weather condition.Polymerization degree difference, its thing physics is then different with chemical property, its function is also different, the inulin of difference in functionality to the polymerization degree require different.Inulin is widely used in food, functional drinks, health care industry, healthcare products industry and some chemical industries etc. at present.
The inulin extractive technique, China just enters this field in late nineteen nineties, and technology is imperfection also.At present main production method is as follows: publication number is the method that the straight film of the Chinese patent of CN1389468A is produced inulin, oligofructose, the advantage of this invention is: the preprocessing process of raw material is simplified greatly, the production process cleaning, non-pollutant discharge, obtain the purity height of product, advantages such as the production process power consumption is low, and production process is easy to control.Its shortcoming is costing an arm and a leg of filter membrane, and is easily contaminated, needs periodic replacement, the production cost height, and, realize fully that replacing other all Technologies by filter membrane needs time in China from the technical situation that present filter membrane itself is produced.Publication number is the working method of the patent inulin of CN 1422547A, advantage is that working method is simple, cost is not high, but contain impurity such as other organism, various thalline, virus in the inulin, and the inulin that extracts contains fructose, glucose, oligofructose and the polymerization degree greater than 9 inulin, the easy moisture absorption of this inulin, caking, be difficult for preserving, therefore the inulin poor quality that obtains influences the performance of inulin function.Granted publication number is component, its preparation method of the novel inulin of patent of CN1163157C and the food that contains described inulin component, and this method and technology is perfect, and the inulin quality product of production is higher, as seeks out the inulin of specific aggregation degree, relatively difficulty.
Summary of the invention
The objective of the invention is to, a kind of attractive technically and economically technology that can produce the high-quality inulin of different performance, different polymerization degree scope is provided.
To achieve these goals, technical solution of the present invention is that a kind of extraction process of inulin is characterized in that, comprises the following steps:
1), removes and pulverize behind the foreign material or the section after drying is preserved and treated with post-treatment with fresh witloof raw material Rapid Cleaning; The witloof sheet of preserving for the section after drying adds man-hour with the organic solvent lixiviate, to remove synanthrin other organism in addition, volatilizes solvent; Organic solvent selection concentration content is the ethanolic soln (V/V) more than 60%, or selects the discrepant organic solvent gradient extraction of polarity for use;
2) raw material after the mechanical disintegration is soaked, 10 ℃-45 ℃ of the water temperatures that bright root soaks, the time is 20-30min; For the hot-water soak of the witloof sheet that volatilizes solvent through 30-95 ℃, the time is 20-60min; Be heated to 75 ℃-100 ℃ then, the time is 40min, carries out three adverse current lixiviates, and a washery slag operation is last, press filtration or the centrifugal crude extract that obtains being rich in inulin;
3) crude extract that is rich in inulin that obtains is carried out thermal treatment earlier, its method is that crude extract is delivered to sterilization in the disinfection tank, germ-resistant purpose is killed the arbitrary bacterium in the crude extract and is made enzyme denaturation, make protein coagulating, 90 ℃～110 ℃ of Heating temperatures, time 5-15min, or select the higher temperature instantaneous sterilization, make protein coagulating, later cooling immediately; After extracting solution is cooled to 40-50 ℃, add Ca (OH)
2: CaCl
2=1: 1 the alkaline reagents Deproteinization and the class material that removes photoresist; Adopt membrane filtration to remove thalline, water-soluble protein, pigment and other insolubles at last; Can obtain the clarifying refining extracting solution that is rich in inulin;
4) obtain preparing the pure inulin liquid of efficient inulin after the above-mentioned refining extracting solution that is rich in inulin is handled by the combined ionic exchange process, or handle by alcohol and to obtain precipitating inulin and behind pure recrystallization, to obtain α-form inulin, or obtain β-form inulin by deepfreeze;
5) the above-mentioned pure inulin liquid that obtains, α-form inulin and β-further decolouring of form inulin, desalination and removal of impurities are handled, preparing efficient inulin adopts temperature, pressure to control continuous two-stage concentrating and separating method, adopt gradient ethanol to precipitate to α-form inulin in conjunction with the temperature controlling classification, adopt cellulose column or ion-exchange cellulose post in conjunction with the nanofiltration membrane separation method to β-form inulin, produce the dry inulin of different specific aggregation degree.
The extraction process of inulin of the present invention can not only utilize the bright root of witloof to make raw material, and under the situation of output that does not influence inulin and quality, bright root is dealt carefully with, and can realize the production all the year round of inulin; The inulin product of producing is various, less than 9 the additive that can be used for functional drinks, improves its mouthfeel as the production polymerization degree; The production distribution of polymerization degree is used for the treatment of disturbance of carbohydrate metabolism 10～45 and the efficient inulin of content more than 75%; Can the inulin of the production polymerization degree between 20-45, be used for the substitute or the fiber food of fat and be used for chemical industry or pharmaceutical industry is made the polymerization degree of vehicle at the inulin more than 45; Can produce the inulin of the specific aggregation degree that the refining inulin of prevented from caking and grumeleuse and dilution degradation, solubleness improves.
Description of drawings
Fig. 1 is that technology of the present invention is extracted the route block diagram;
Fig. 2 is that the technology of producing efficient inulin is extracted the route block diagram;
Fig. 3 is that α-form inulin preparation and separating technology extract the route block diagram; Technology is extracted the route block diagram;
Fig. 4 is that the production technique of β-form inulin is extracted the route block diagram.
Below in conjunction with drawings and Examples technology of the present invention is described in further detail.
Embodiment
The present invention is the raw material production inulin with the witloof, and its production technology route is referring to Fig. 1.
1. witloof raw material:
The present invention comes the special functional inulin of separation of produced from polymerization degree angle, raw material sources, the sowing time of plant, temperature, growth and development stage, gather in the crops the pitch time of handling with starting material, and the different treatment of each process procedure of extraction production inulin etc., the distribution range of the inulin polymerization degree and the ratio that accounts for all influenced.
In order to obtain the comparatively ideal inulin of the polymerization degree, the field production witloof, Chinese northern area should be advisable sowing the 4-5 month to gather in the crops in the 9-12 month.The principle of foundation is: can carry out inulin production since vegetative period with root of Herba Cichorii greater than three months, until add the end of duration, do not trigger EFH gene (gene that DP is diminished) temperature in the root of Herba Cichorii when cold condition occurs and be not less than 0 ℃ and preferably be not less than 3 ℃.SST and FFT gene are to promote inulin synthetic gene in the root simultaneously.The SST gene makes Polylevulosan synthetic initial, and the FFT gene can make the prolongation of chain, has the specificity of space and etap but express.SST's is active high during young root, and the substrate sucrose concentration is low, the concentration height of product glucose, oligofructose showed increased.Between 5-6 month of vegetative period, sucrose and high-polymerization degree fructose content rise, and glucose level descends, and the large percentage that accounts for of high-polymerization degree is a best period so produce inulin between 5-6 month of vegetative period.Fructose concentration in February from December to the next year greatly increases, and Polylevulosan content descends, and EFH expresses stronger, and the inulin polymerization degree DP that produce this moment is minimum.Preferably in 60 days, finish from gathering in the crops to the pitch time of processing, be no more than 90 days at most.
2. the storage of witloof raw material:
Obtain inulin, must in two months, finish the results and the processing of plant piece root, otherwise will resolve into fructose.According to suitable time sowing that the front is sayed, results and processing then are difficult at short notice the root of Herba Cichorii of disposable results is processed, and can not carry out whole year production.Production phase, weak point can not have better economic benefit.For the starting material of producing inulin are arranged at any time, so proposed the treatment process of balance and preservation inulin plant.Therefore the method for the present invention's design not only realizes the long-term production of inulin, and does not influence inulin output and quality:
At first, the fresh root of Herba Cichorii of harvesting will be excavated, Rapid Cleaning in cleaning machine, remove earth, Shi Sha and other foreign material etc., the time of soaking and washing is short as much as possible, because along with the prolongation of soak time, the sugar degree in the wash water liquid increases, the loss of sugar is big more, preferably is no more than 30min on the time.
The chiccory root tuber that can't finish processing the short period of time after the cleaning, section, rapidly drying treatment is stored, perhaps the high temperature dry storage again of going out behind the enzyme.The section purpose allows big as far as possible area contact water, is easy to lixiviate, notices that the thickness of section is preferably between the 0.5-1cm, and maximum is no more than 2cm, approaches excessively to be unfavorable for filtering; The content that makes water is that the original 10%-30% of raw material is advisable.
Notice during heating that controlled temperature more than 75 ℃, when temperature rises to 50-60 ℃, skip as much as possible rapidly, prevent that inulinase is activated, cause a large amount of degradeds of inulin, cause the loss of inulin.Heating or rapidly drying can make the inulinase inactivation, make simultaneously that inulin exists with solid form in the enchylema.
For cleaning Manufactured witloof dry plate in the process of storing, can adhere to a large amount of impurity such as dust, express 2-15min, can leach a part of pigment, the loss of sugar also seldom, if the time lengthening of embathing is to 15min, though the elutant color burn, but remove partial pigment, the loss excessive (more than 10%) of sugar, water-soluble physiologically active substance also can lose, so the cleaning of witloof dry plate is best with 2-10min.
3. inulin extracts:
1. exsiccant witloof sheet is handled: at first with the organic solvent lixiviate to remove other organism of removing the synanthrin, the ethanolic soln (V/V) of any concentration of lixiviate first-selection more than 60% of organic solvent also can select for use the discrepant organic solvent gradient of polarity to extract.This method can be removed monose, disaccharide, the part oligose in the witloof, bitter substance, and a large amount of pigments and other impurity volatilize solvent, and inulin then remains in the witloof sheet slag.
(2) extraction of witloof sheet slag and bright root inulin: at first soak, 10 ℃-45 ℃ of the water temperatures (enzyme that do not go out, if water temperature is high, inulinase is activated, and can cause the degraded of inulin) that bright root soaks, the time is 20-30min; The sheet root soaks after volatilizing solvent, and soaking water temperature is 30-95 ℃; Time is that 20-60min gets final product.Heating, lixiviate then: temperature is preferably 75 ℃-100 ℃, and the time is 40min, generally carries out three adverse current lixiviates, a washery slag operation.The adverse current lixiviate can produce maximum concentration difference, and lixiviate is carried out effectively.At last, press filtration or the centrifugal crude extract that obtains being rich in inulin.
4. the crude extract of inulin is handled:
(1) go out enzyme, sterilization: the extracting solution that will be rich in inulin is delivered to sterilization in the disinfection tank, germ-resistant purpose is killed the arbitrary bacterium in the feed liquid and is made enzyme denaturation, solidifying protein, Heating temperature is more than 90 ℃, below 110 ℃, time 5-15min also can select more high-temperature instantaneous sterilization, and germ-resistant principle is the suitable high protein coagulating that extremely enough makes of temperature, pressure.For preventing the thermolysis of inulin, cooling immediately later.
(2) material such as the alkali lye Deproteinization and the class of removing photoresist: contain a large amount of glue classes, macromolecular protein in the inulin crude extract, influence the quality and the filtration of inulin, add alkaline matter, can make protein denaturation on the one hand, thereby accelerate precipitation, can make pectin and alkali generate salts substances such as calcium pectinate on the other hand, and the organic acid of trace forms insoluble calcium salt etc. and be filtered or centrifugal removing, unnecessary salts substances such as calcium are by adding CO
2Be removed, residual salt ion and other ion are removed in subsequent technique together in the system.
Method is after crude extract is cooled to 40-50 ℃, adds alkali type reagent: first-selected Ca (OH)
2: CaCl
2=1: 1; Having of other: milk of lime, Na
2CO
3, NaOH, K
2CO
3, KOH, NH
4CO
3, NH
4OH, Ca (OH)
2, Mg (OH)
2, Ba (OH)
2, Sr (OH)
2Deng, regulate PH8-13.5, make these macromole post precipitations, feed CO
2Handle the unnecessary sedimentary basic solution that generates, filtered while hot is removed all precipitations again, filters to obtain the inulin extracting solution.The inulin extracting solution that leaves standstill is pumped in the clear whizzer, centrifugal suspension foul, particle and the solid removed, the attention extracting solution need filter under the temperature of higher (less than 100 ℃) or be centrifugal, otherwise inulin can be separated out precipitation.
(3) membrane filtration is removed thalline, water-soluble protein, pigment and other insolubles: preferred aperture is at 0.05-0.2 μ m, preferably select the tubular fibre inorganic ultra-filtration membrane of aperture at 0.05-0.1 μ m, remove thalline fully, solidify and water-soluble protein, colloid, pigment and other insolubles, obtain the clarifying refining extracting solution that is rich in inulin.This extracting solution is carried out the analysis of the inulin polymerization degree, and used method is high performance liquid chromatography (HPLC), if the polymerization degree of 10% above inulin below 5, be carried out the adjustment of pH value, makes PH control to 7.
Adopt alkali lye precipitation-centrifugation-integrated impurity removal method of ultra-filtration membrane, give full play to advantage separately, reduced the pollution of film, reduced cost, improved quality.
5. long-chain inulin preparation:
(1) efficient inulin preparation: can directly carry out desalination by the inulin extracting solution, decolour, obtain clarifying the refined soln that is rich in inulin.
Stage division utilizes the classification of temperature, pressure control method of enrichment.
Method one: refined soln 200mg room temperature is placed crystallization in 48 hours, and 50 ℃, the time is no more than 1 hour, is evaporated to concentration and is 40% sol particle;
Method two: refined soln 200mg room temperature is placed crystallization in 6 hours, and 100 ℃, it is 55% sol particle that about 30min of time, normal atmosphere are concentrated into concentration.
Method three: under the refined soln 200mg normal pressure, 120 ℃, 1 hour time, 80% sol particle that is evaporated to concentration and is.
The inulin polymerization degree 1-4 that obtains by above-mentioned three kinds of methods is less than 5%, and polymerization degree 5-9 accounts for 5%, the polymerization degree 6-45 greater than 75%, the polymerization degree is less than 10% greater than 45 inulin content.
After 50 ℃ of two weeks of preservation, it is 15% solution that centrifuging obtains inulin concentration with above-mentioned refined soln.Solution after filtering is handled with following two kinds of methods.
Method one: the solution of getting 200ml was at room temperature placed 6 hours, and 50 ℃ of concentrating under reduced pressure 1min obtain to contain the solution of 25% sol particle.
Method two: the solution of getting 200ml reduced pressure 5 hours the inulin solution of the solubility of acquisition 40% for 80 ℃.
The distribution of polymerization degree scope that obtains inulin by above-mentioned two kinds of methods is: polymerization degree 1-4 is less than 10%, polymerization degree 5-9 less than 40%, the polymerization degree 6-45 greater than 50%, the polymerization degree is greater than 45 inulin trace.
(2) preparation of α-form inulin: long-chain inulin can be separated out in the organic solvent of high density in precipitated filtration, first-selected ethanol of organic solvent and methyl alcohol, Virahol etc.Method is that the aqueous extract that is rich in inulin is concentrated into below 1/2 of former extracting solution, add 95% alcohol (V/V) that 1-5 doubly measures then, after adding alcohol, the pure content of solution is not less than 60% (V/V), leaves standstill 2-5h, suction filtration or centrifugation, solution reclaims alcohol, precipitation is used a spot of water dissolution again, repeatedly pure recrystallization, and precipitation volatilizes solvent and promptly obtains α-form inulin.The solubleness of the inulin that this method obtains in cold water is not as the solubleness height of inulin in cold water of β-form.
(3) inulin of β-form: the inulin of β-form can directly cool off 0-3 ℃ by the inulin extracting solution, and 24-48 hour, collecting precipitation obtained; In the crystalline process, can add a small amount of inulin crystal seed, quicken the inulin crystallization and separate out, only need to separate out in 10-20 hour precipitation; Or the cooling elutriant, a part of inulin crystallizes out, collecting precipitation, and remaining solution for vacuum concentration xln is separated out; Or the whole solution of concentrating under reduced pressure is original 30-50%, with this heavy solution heating, crystallisation by cooling.Or inulin content is to place at low temperatures 48 hours in 24% o'clock in the extracting solution, separates out inulin and is heated to 90-95 ℃, and the cooling precipitation at room temperature filters to isolate inulin, and remaining solution pressurization obtains new precipitation inulin when being concentrated to the 45% original left and right sides.The solubleness of inulin in cold water that obtains this form is higher.
6. various inulin decolouring, desalination removal of impurities are handled:
(1) desalination bleaching of efficient inulin: use highly acidic resin, the ion exchange method decolouring desalination of basic resin and weakly acidic resin combination, just can reach good effect at normal temperatures, not only can slough the pigment of extracting solution, and in decolouring, the ion in the extracting solution be removed.
(2) the desalination bleaching removal of impurities of α-form inulin: by ethanol repeatedly recrystallization removed impurity such as most pigment, but containing residual pigment need remove, in addition, in heat-sterilization process, the spore and the part bacterium that may not kill are still arranged, therefore the preferred film bore dia is the impurity such as ultra-filtration membrane deionizing, low molecule organic matter of 0.01-0.05 μ m, reaches that desalination is decoloured again and spissated effect, obtains purified α-form inulin.
(3) the desalination bleaching removal of impurities of β-form inulin: ultrafiltration and polymeric adsorbent logotype refining beta-form inulin: macroporous adsorbent resin is to adsorb semipolar small molecules with electrostatic attraction from inulin solution, macromolecular inulin can not see through the resin mesh or can not be adsorbed too by force with aqueous solution avidity, like this impurity such as the pigment in the inulin solution, bitter taste is adsorbed separation; Nonionic adsorption resin adsorbs by electric charge, realizes ion-exchange, and the ionic species composition is adsorbed, and inulin is made with extra care.
Modern membrane separation technique is to utilize the aperture feature of film, separate with the molecule of physical means different sizes, sepn process is not heated, stable components, separation rate height, power consumption are low, and non-secondary pollution has very big advantage to the removal of particulate and the separation of water-soluble macromolecule.Can remove particulate, pyrogen, microorganism well as ultra-filtration membrane 6000-10000 molecular weight ultra-filtration membrane, the quality of raising preparation and stability thereof, security.But cost an arm and a leg, need protection meticulously to use.
In the polymeric adsorbent use, the declining meeting of resin comes off with form of chips in the purified process, produces secondary pollution, has a strong impact on the security of preparation, and can the come off removing of fragment of membrane filtration improves the security that polymeric adsorbent is used.On the other hand, behind the inulin solution resin purification, the composition of polluted membrane being reduced greatly, is that effectively pretreatment process is used in ultrafiltration.Both combinations can be given full play to advantage separately, and complementary the other side's deficiency more has an economic benefit than independent use film.
The present invention will again through the ion exchange column desalination, remove residual particulate, pyrogen, microorganism etc. with inulin through ultra-filtration membrane then by after the macroporous adsorbent resin decolouring earlier, finally obtain high-quality β-form inulin.
7. the separation of the inulin of different polymerization degree:
(1) efficient inulin adopts temperature, pressure to control continuous two-stage concentrating and separating method: inulin liquid is carried out the continuous two-stage handle: with inulin liquid concentrating under reduced pressure at once, temperature is 60 ℃, and being concentrated to inulin concentration is 40%; Then under a normal atmosphere, to be concentrated to inulin concentration be 75% to temperature in order to be 120 ℃.This moment, the high-efficient liquid phase analysis result was that DP is 70% at the inulin of 10-40.
(2) α-form inulin adopts gradient ethanol to precipitate in conjunction with the temperature controlling classification: inulin is dissolved into saturated inulin solution with distilled water, deionized water or ozonated water, then with adding ethanol precipitation gradually, reach 20%, 40%, 60%, 80%, 100% ethanol as concentration of ethanol, respectively collecting precipitation.Concentration of ethanol is to change, and can adjust alcohol concn according to the desired molecule amount, and for better effects if, the temperature that can make solvent is below 10 ℃.
(3) β-form inulin adopts cellulose column or ion-exchange cellulose post in conjunction with the nanofiltration membrane separation method: cellulose column or ion-exchange cellulose post can both well separate monose, disaccharide, oligose and polysaccharide.Utilize mixing sugar solution, flow through in advance with the cellulose column of another kind of solvent (as ethanol) suspendible, polysaccharide is separated out precipitation on this porous medium, with rare alcohol of successively decreasing wash-out progressively, separates out various sugar again.
8. various product dryings are handled:
The final inulin that obtains the required polymerization degree or molecular weight that separates passes through earlier to concentrate, and carries out drying then.Temperature controlling when noting drying, under the decompression situation, 50-100 ℃ concentrates, or 100-120 ℃ of normal pressure is concentrated, and the time is no more than 1 hour.
General can obtain crystallization or powdery product at last by spraying drying, forced air drying, drying bu sublimation.
With the witloof is example, can more know the preferred method of the present invention by embodiment given below:
Embodiment 1: produce efficient inulin
Referring to Fig. 2, with the root of Herba Cichorii dry plate 10kg after the drying treatment, soak 20～40min down at 25～30 ℃, 85 ℃ of lixiviates, filter, remove impurity, 90～95 ℃ of sterilizations of vat liquor remove by filter collagen protein, obtain to be rich in the inulin seminal fluid, use highly acidic resin, basic resin and weakly acidic resin combined ionic exchange process decolouring desalination obtains the water white inulin liquid that is rich in, and is that fast decompression is concentrated under 60 ℃ the condition in temperature, inulin concentration reaches 40% and can stop, at once it is carried out the processing of subordinate phase: normal pressure, 120 ℃, concentrate fast, when reaching 75%, inulin concentration stops.This moment, the inulin polymerization degree DP that obtains accounted for 75% at 10-40.This inulin liquid is carried out drying with the forced air drying method obtain moisture 12% inulin 4.324kg.
Embodiment 2: α-preparation of form inulin and separation
Concrete technical process is got the bright root 10kg of witloof referring to Fig. 3, and 30 ℃ are soaked 20min, perhaps root of Herba Cichorii dry plate 10kg60 ℃ is soaked the 30min mixing, is heated to 90 ℃ of hot water lixiviates, centrifugation then, removes slag, obtain the inulin extracting solution, above-mentioned inulin extracting solution is concentrated into inulin concentration 18%, logical co
2Add milk of lime and transfer PH to 10～11, filter, abandon its slag, obtain rich inulin filtrate, obtain clarifying inulin liquid behind the ultrafiltration membrance filter (aperture 0.1 μ m), be concentrated into about 50% of original volume then, add the dehydrated alcohol precipitation, obtain the inulin crystal; Dissolved in distilled water, centrifugation ethanol periodic crystallisation, obtain α-form inulin, to promptly get saturated inulin solution after α-form inulin ultra-filtration membrane removal of impurities (aperture 0.01 μ m), respectively with the dehydrated alcohol precipitation separation of 35%, 55%, 75% concentration, temperature is 8 ℃ of drying bu sublimations, and the white purified oligose inulin 0.75%, DP that can obtain DP＜9 is at 10～45 the inulin 87.81% and the inulin 11.44% of DP＞45.
The production of example 3: β-form inulin
Concrete technical process is referring to Fig. 4, get 10 kilograms the identical treatment process of bright root and embodiment 1, obtain the clarifying hot water extraction liquid that is rich in inulin, be evaporated to the inulin that contains in the solution about 50%, heat this thick solution (90～95 ℃ of temperature), be cooled to room temperature, filter, get the inulin throw out, make saturated inulin solution, through the macroporous adsorbent resin decolouring, the condensed water elutriant obtains the pure solution of inulin, utilizes the dimethylaminoethyl cellulose column to separate, and each elutriant concentrates respectively, obtain 0.261 kilogram of monose, 0.087 kilogram of sucrose, 0.144 kilogram of the inulin of polymerization degree 3-7,0.542 kilogram of the inulin of polymerization degree 8-30,0.374 kilogram of polymerization degree 30-40 inulin, the polymerization degree is greater than 0.212 kilogram of 40 inulin.
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| BRPI0710972B1 (en) * | 2006-04-28 | 2018-02-14 | Bayer Intellectual Property Gmbh | VERY HIGH CHAIN LENGTH INULIN, ITS USES AND THEIR OBTAINING PROCESS, FOOD GENDER, FOOD SUPPLEMENT, COSMETIC PREPARATION, AND WATER PASTE AND ITS USE |
| CN101432313B (en) * | 2006-04-28 | 2013-08-07 | 拜尔作物科学股份公司 | Inulin of very high chain length |
| CN101331924B (en) * | 2007-06-28 | 2011-01-12 | 定西市陇海乳品有限责任公司 | Method for producing inulin syrupy using waste fluid of producing inulin |
| BRPI0822085B1 (en) * | 2007-12-17 | 2017-05-02 | Bayer Cropscience Ag | process for isolating inulin from inulin-containing plant material |
| CN101214040B (en) * | 2008-01-04 | 2012-07-25 | 纽威公司 | Momordica grosvenori sweetening agent and preparation thereof |
| CN101628949B (en) * | 2009-08-07 | 2011-12-14 | 烟台海岸带可持续发展研究所 | Method for manufacturing high-quality inulin |
| CN102153679B (en) * | 2011-02-14 | 2012-08-22 | 大连工业大学 | Method for grading inulin |
| WO2013011566A1 (en) * | 2011-07-19 | 2013-01-24 | 日本甜菜製糖株式会社 | Method for producing inulin |
| CN105384851A (en) * | 2015-11-10 | 2016-03-09 | 军株（大连）生物产业有限公司 | Extraction method for producing inulin by cichorium intybus |
| CN105968233A (en) * | 2016-05-12 | 2016-09-28 | 青岛大学 | Burdock root inulin and preparation method thereof |
| CN106035211A (en) * | 2016-06-04 | 2016-10-26 | 金寨县峰远黑猪养殖专业合作社 | Method for recycling pig excrement to improve pork quality |
| CN106418539A (en) * | 2016-10-12 | 2017-02-22 | 多（大连）生物产业有限公司 | Method for producing original taste inulin |
| CN106889625B (en) * | 2017-02-27 | 2020-12-04 | 深圳市华利康纤生物科技有限公司 | Preparation method of inulin particles |
| CN112552427B (en) * | 2020-07-01 | 2024-06-04 | 吉林省石油化工设计研究院 | Molecular-grade production process and device of inulin |
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