CN108101744A - Inositol extraction method - Google Patents
Inositol extraction method Download PDFInfo
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- CN108101744A CN108101744A CN201711341127.XA CN201711341127A CN108101744A CN 108101744 A CN108101744 A CN 108101744A CN 201711341127 A CN201711341127 A CN 201711341127A CN 108101744 A CN108101744 A CN 108101744A
- Authority
- CN
- China
- Prior art keywords
- inositol
- liquid
- flash
- flash distillation
- fructus hordei
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
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- CDAISMWEOUEBRE-GPIVLXJGSA-N inositol Chemical compound O[C@H]1[C@H](O)[C@@H](O)[C@H](O)[C@H](O)[C@@H]1O CDAISMWEOUEBRE-GPIVLXJGSA-N 0.000 title claims abstract description 109
- CDAISMWEOUEBRE-UHFFFAOYSA-N scyllo-inosotol Natural products OC1C(O)C(O)C(O)C(O)C1O CDAISMWEOUEBRE-UHFFFAOYSA-N 0.000 title claims abstract description 109
- SQUHHTBVTRBESD-UHFFFAOYSA-N Hexa-Ac-myo-Inositol Natural products CC(=O)OC1C(OC(C)=O)C(OC(C)=O)C(OC(C)=O)C(OC(C)=O)C1OC(C)=O SQUHHTBVTRBESD-UHFFFAOYSA-N 0.000 title claims abstract description 108
- 229960000367 inositol Drugs 0.000 title claims abstract description 108
- 238000000605 extraction Methods 0.000 title abstract description 3
- 239000007788 liquid Substances 0.000 claims abstract description 142
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims abstract description 38
- 239000000463 material Substances 0.000 claims abstract description 33
- NWUYHJFMYQTDRP-UHFFFAOYSA-N 1,2-bis(ethenyl)benzene;1-ethenyl-2-ethylbenzene;styrene Chemical compound C=CC1=CC=CC=C1.CCC1=CC=CC=C1C=C.C=CC1=CC=CC=C1C=C NWUYHJFMYQTDRP-UHFFFAOYSA-N 0.000 claims abstract description 28
- 239000012528 membrane Substances 0.000 claims abstract description 25
- 239000000919 ceramic Substances 0.000 claims abstract description 20
- 239000003456 ion exchange resin Substances 0.000 claims abstract description 19
- 229920003303 ion-exchange polymer Polymers 0.000 claims abstract description 19
- 238000000108 ultra-filtration Methods 0.000 claims abstract description 19
- 239000013078 crystal Substances 0.000 claims abstract description 16
- 238000000926 separation method Methods 0.000 claims abstract description 15
- 238000001914 filtration Methods 0.000 claims abstract description 12
- 229920002521 macromolecule Polymers 0.000 claims abstract description 7
- 238000000034 method Methods 0.000 claims description 89
- 238000007701 flash-distillation Methods 0.000 claims description 79
- 230000008569 process Effects 0.000 claims description 66
- 239000000203 mixture Substances 0.000 claims description 40
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 38
- 240000004808 Saccharomyces cerevisiae Species 0.000 claims description 32
- 235000014680 Saccharomyces cerevisiae Nutrition 0.000 claims description 32
- 239000011347 resin Substances 0.000 claims description 28
- 229920005989 resin Polymers 0.000 claims description 28
- 239000012530 fluid Substances 0.000 claims description 26
- 238000002525 ultrasonication Methods 0.000 claims description 26
- 235000007340 Hordeum vulgare Nutrition 0.000 claims description 23
- 241000209219 Hordeum Species 0.000 claims description 22
- 108010011619 6-Phytase Proteins 0.000 claims description 18
- 229940085127 phytase Drugs 0.000 claims description 18
- 230000000694 effects Effects 0.000 claims description 15
- 239000003957 anion exchange resin Substances 0.000 claims description 14
- 238000003756 stirring Methods 0.000 claims description 14
- 108010051457 Acid Phosphatase Proteins 0.000 claims description 12
- 102000013563 Acid Phosphatase Human genes 0.000 claims description 12
- 239000003729 cation exchange resin Substances 0.000 claims description 12
- 238000009210 therapy by ultrasound Methods 0.000 claims description 11
- 238000002604 ultrasonography Methods 0.000 claims description 11
- GZCWLCBFPRFLKL-UHFFFAOYSA-N 1-prop-2-ynoxypropan-2-ol Chemical compound CC(O)COCC#C GZCWLCBFPRFLKL-UHFFFAOYSA-N 0.000 claims description 10
- 102000004190 Enzymes Human genes 0.000 claims description 10
- 108090000790 Enzymes Proteins 0.000 claims description 10
- 229940088598 enzyme Drugs 0.000 claims description 10
- 239000012141 concentrate Substances 0.000 claims description 9
- 239000003610 charcoal Substances 0.000 claims description 8
- 108010059892 Cellulase Proteins 0.000 claims description 6
- 239000002253 acid Substances 0.000 claims description 6
- 229940106157 cellulase Drugs 0.000 claims description 6
- 239000002893 slag Substances 0.000 claims description 6
- 238000009298 carbon filtering Methods 0.000 claims description 4
- 150000001768 cations Chemical class 0.000 claims description 4
- 150000001450 anions Chemical class 0.000 claims description 3
- 238000004061 bleaching Methods 0.000 claims description 3
- 150000002500 ions Chemical class 0.000 claims description 3
- 229910052760 oxygen Inorganic materials 0.000 claims description 3
- 239000001301 oxygen Substances 0.000 claims description 3
- 230000008859 change Effects 0.000 claims description 2
- 240000005979 Hordeum vulgare Species 0.000 claims 1
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims 1
- 229910052739 hydrogen Inorganic materials 0.000 claims 1
- 239000001257 hydrogen Substances 0.000 claims 1
- 238000001035 drying Methods 0.000 abstract description 7
- 229910052799 carbon Inorganic materials 0.000 abstract description 5
- 239000012535 impurity Substances 0.000 abstract description 3
- 238000002425 crystallisation Methods 0.000 abstract description 2
- 230000008025 crystallization Effects 0.000 abstract description 2
- 238000005374 membrane filtration Methods 0.000 abstract 2
- 238000011033 desalting Methods 0.000 abstract 1
- 239000000049 pigment Substances 0.000 abstract 1
- 150000003839 salts Chemical class 0.000 abstract 1
- 239000000047 product Substances 0.000 description 15
- 239000002585 base Substances 0.000 description 12
- 235000002949 phytic acid Nutrition 0.000 description 12
- IMQLKJBTEOYOSI-GPIVLXJGSA-N Inositol-hexakisphosphate Chemical compound OP(O)(=O)O[C@H]1[C@H](OP(O)(O)=O)[C@@H](OP(O)(O)=O)[C@H](OP(O)(O)=O)[C@H](OP(O)(O)=O)[C@@H]1OP(O)(O)=O IMQLKJBTEOYOSI-GPIVLXJGSA-N 0.000 description 11
- IMQLKJBTEOYOSI-UHFFFAOYSA-N Phytic acid Natural products OP(O)(=O)OC1C(OP(O)(O)=O)C(OP(O)(O)=O)C(OP(O)(O)=O)C(OP(O)(O)=O)C1OP(O)(O)=O IMQLKJBTEOYOSI-UHFFFAOYSA-N 0.000 description 11
- 229940068041 phytic acid Drugs 0.000 description 11
- 239000000467 phytic acid Substances 0.000 description 11
- 239000012452 mother liquor Substances 0.000 description 9
- 239000000126 substance Substances 0.000 description 7
- 230000002378 acidificating effect Effects 0.000 description 6
- 230000035784 germination Effects 0.000 description 6
- 235000016709 nutrition Nutrition 0.000 description 6
- 238000010583 slow cooling Methods 0.000 description 6
- -1 phospho phytate Chemical class 0.000 description 5
- PPBRXRYQALVLMV-UHFFFAOYSA-N Styrene Chemical compound C=CC1=CC=CC=C1 PPBRXRYQALVLMV-UHFFFAOYSA-N 0.000 description 4
- 238000001816 cooling Methods 0.000 description 4
- 230000035764 nutrition Effects 0.000 description 4
- 238000005406 washing Methods 0.000 description 4
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 3
- 125000003368 amide group Chemical group 0.000 description 3
- 238000005349 anion exchange Methods 0.000 description 3
- 230000008901 benefit Effects 0.000 description 3
- 238000005341 cation exchange Methods 0.000 description 3
- 230000007062 hydrolysis Effects 0.000 description 3
- 238000006460 hydrolysis reaction Methods 0.000 description 3
- 238000004519 manufacturing process Methods 0.000 description 3
- 244000005700 microbiome Species 0.000 description 3
- 239000002245 particle Substances 0.000 description 3
- 239000011148 porous material Substances 0.000 description 3
- 238000011084 recovery Methods 0.000 description 3
- BHPQYMZQTOCNFJ-UHFFFAOYSA-N Calcium cation Chemical compound [Ca+2] BHPQYMZQTOCNFJ-UHFFFAOYSA-N 0.000 description 2
- HEDRZPFGACZZDS-UHFFFAOYSA-N Chloroform Chemical compound ClC(Cl)Cl HEDRZPFGACZZDS-UHFFFAOYSA-N 0.000 description 2
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 description 2
- 238000010521 absorption reaction Methods 0.000 description 2
- LPQOADBMXVRBNX-UHFFFAOYSA-N ac1ldcw0 Chemical compound Cl.C1CN(C)CCN1C1=C(F)C=C2C(=O)C(C(O)=O)=CN3CCSC1=C32 LPQOADBMXVRBNX-UHFFFAOYSA-N 0.000 description 2
- 230000004103 aerobic respiration Effects 0.000 description 2
- 235000013405 beer Nutrition 0.000 description 2
- 238000009395 breeding Methods 0.000 description 2
- 230000001488 breeding effect Effects 0.000 description 2
- 229910001424 calcium ion Inorganic materials 0.000 description 2
- 229940023913 cation exchange resins Drugs 0.000 description 2
- 238000010612 desalination reaction Methods 0.000 description 2
- 238000001514 detection method Methods 0.000 description 2
- RTZKZFJDLAIYFH-UHFFFAOYSA-N ether Substances CCOCC RTZKZFJDLAIYFH-UHFFFAOYSA-N 0.000 description 2
- 150000004676 glycans Chemical class 0.000 description 2
- 239000004615 ingredient Substances 0.000 description 2
- 150000002605 large molecules Chemical class 0.000 description 2
- 238000002156 mixing Methods 0.000 description 2
- 229920001282 polysaccharide Polymers 0.000 description 2
- 239000005017 polysaccharide Substances 0.000 description 2
- 102000004169 proteins and genes Human genes 0.000 description 2
- 108090000623 proteins and genes Proteins 0.000 description 2
- 229940081969 saccharomyces cerevisiae Drugs 0.000 description 2
- 150000003335 secondary amines Chemical class 0.000 description 2
- 238000001179 sorption measurement Methods 0.000 description 2
- 239000000725 suspension Substances 0.000 description 2
- 230000001360 synchronised effect Effects 0.000 description 2
- 229940088594 vitamin Drugs 0.000 description 2
- 229930003231 vitamin Natural products 0.000 description 2
- 235000013343 vitamin Nutrition 0.000 description 2
- 239000011782 vitamin Substances 0.000 description 2
- HIXDQWDOVZUNNA-UHFFFAOYSA-N 2-(3,4-dimethoxyphenyl)-5-hydroxy-7-methoxychromen-4-one Chemical compound C=1C(OC)=CC(O)=C(C(C=2)=O)C=1OC=2C1=CC=C(OC)C(OC)=C1 HIXDQWDOVZUNNA-UHFFFAOYSA-N 0.000 description 1
- FRXSZNDVFUDTIR-UHFFFAOYSA-N 6-methoxy-1,2,3,4-tetrahydroquinoline Chemical compound N1CCCC2=CC(OC)=CC=C21 FRXSZNDVFUDTIR-UHFFFAOYSA-N 0.000 description 1
- 239000004215 Carbon black (E152) Substances 0.000 description 1
- PEDCQBHIVMGVHV-UHFFFAOYSA-N Glycerine Chemical compound OCC(O)CO PEDCQBHIVMGVHV-UHFFFAOYSA-N 0.000 description 1
- 239000004952 Polyamide Substances 0.000 description 1
- 239000004743 Polypropylene Substances 0.000 description 1
- 229910006069 SO3H Inorganic materials 0.000 description 1
- 230000009471 action Effects 0.000 description 1
- 239000003513 alkali Substances 0.000 description 1
- 150000001412 amines Chemical group 0.000 description 1
- 150000003863 ammonium salts Chemical group 0.000 description 1
- 238000009954 braiding Methods 0.000 description 1
- 239000011575 calcium Substances 0.000 description 1
- 229910052791 calcium Inorganic materials 0.000 description 1
- 125000003178 carboxy group Chemical group [H]OC(*)=O 0.000 description 1
- 230000001413 cellular effect Effects 0.000 description 1
- 238000004587 chromatography analysis Methods 0.000 description 1
- 235000009508 confectionery Nutrition 0.000 description 1
- 238000004132 cross linking Methods 0.000 description 1
- 239000012043 crude product Substances 0.000 description 1
- 239000003814 drug Substances 0.000 description 1
- 239000000428 dust Substances 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 235000019441 ethanol Nutrition 0.000 description 1
- 239000004744 fabric Substances 0.000 description 1
- 239000000835 fiber Substances 0.000 description 1
- 239000012065 filter cake Substances 0.000 description 1
- 239000000706 filtrate Substances 0.000 description 1
- 235000013305 food Nutrition 0.000 description 1
- 239000007789 gas Substances 0.000 description 1
- 229930195733 hydrocarbon Natural products 0.000 description 1
- 150000002430 hydrocarbons Chemical group 0.000 description 1
- 150000004001 inositols Chemical class 0.000 description 1
- 230000014759 maintenance of location Effects 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 210000003205 muscle Anatomy 0.000 description 1
- 230000007935 neutral effect Effects 0.000 description 1
- 230000009965 odorless effect Effects 0.000 description 1
- 229920002647 polyamide Polymers 0.000 description 1
- 229920000728 polyester Polymers 0.000 description 1
- 229920000642 polymer Polymers 0.000 description 1
- 229920001155 polypropylene Polymers 0.000 description 1
- 239000000843 powder Substances 0.000 description 1
- 150000003141 primary amines Chemical group 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 238000001953 recrystallisation Methods 0.000 description 1
- 238000007670 refining Methods 0.000 description 1
- 238000010025 steaming Methods 0.000 description 1
- 210000000498 stratum granulosum Anatomy 0.000 description 1
- 229920002994 synthetic fiber Polymers 0.000 description 1
- 239000012209 synthetic fiber Substances 0.000 description 1
- 150000003512 tertiary amines Chemical class 0.000 description 1
- 230000007704 transition Effects 0.000 description 1
- 150000003722 vitamin derivatives Chemical class 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C29/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring
- C07C29/74—Separation; Purification; Use of additives, e.g. for stabilisation
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C29/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring
- C07C29/74—Separation; Purification; Use of additives, e.g. for stabilisation
- C07C29/76—Separation; Purification; Use of additives, e.g. for stabilisation by physical treatment
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C29/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring
- C07C29/74—Separation; Purification; Use of additives, e.g. for stabilisation
- C07C29/76—Separation; Purification; Use of additives, e.g. for stabilisation by physical treatment
- C07C29/78—Separation; Purification; Use of additives, e.g. for stabilisation by physical treatment by condensation or crystallisation
-
- C—CHEMISTRY; METALLURGY
- C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
- C12P—FERMENTATION OR ENZYME-USING PROCESSES TO SYNTHESISE A DESIRED CHEMICAL COMPOUND OR COMPOSITION OR TO SEPARATE OPTICAL ISOMERS FROM A RACEMIC MIXTURE
- C12P7/00—Preparation of oxygen-containing organic compounds
- C12P7/02—Preparation of oxygen-containing organic compounds containing a hydroxy group
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Zoology (AREA)
- Life Sciences & Earth Sciences (AREA)
- Engineering & Computer Science (AREA)
- Wood Science & Technology (AREA)
- Microbiology (AREA)
- General Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Biotechnology (AREA)
- Crystallography & Structural Chemistry (AREA)
- Health & Medical Sciences (AREA)
- Biochemistry (AREA)
- Bioinformatics & Cheminformatics (AREA)
- General Engineering & Computer Science (AREA)
- General Health & Medical Sciences (AREA)
- Genetics & Genomics (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Preparation Of Compounds By Using Micro-Organisms (AREA)
Abstract
The invention discloses an inositol extraction method which comprises the following steps of preparing inositol material liquid, sequentially carrying out ceramic membrane filtration, ion exchange resin treatment, active carbon filtration, ultrafiltration membrane filtration, vacuum low-temperature concentration crystallization and crystal separation on the prefabricated inositol material liquid with the mass volume concentration of more than or equal to 60 g/L, and drying to obtain a finished product, wherein insoluble impurities in the inositol material liquid are filtered by using a ceramic membrane, desalting by using ion exchange resin to reduce the salt concentration in the inositol material liquid, removing pigments and peculiar smell in the inositol material liquid by using active carbon, and removing soluble macromolecular substances in the inositol material liquid by using an ultrafiltration membrane.
Description
Technical field
The present invention relates to the extraction production field of inositol, more particularly to a kind of extracting method of inositol.
Background technology
Inositol also known as bios Ⅰ are one kind in water-soluble (vitamin) B race.White crystalline powder, it is odorless, sweet,
Density 1.752g/ml, 225-227 DEG C of fusing point, is dissolved in water, insoluble in absolute ethyl alcohol, ether and chloroform, in water-soluble or alkali
Property.Inositol is the necessary material of people, animal and microorganism growth, is widely used in the industries such as medicine, food, feed.
The main or traditional high-temperature pressurizing Hydrolysis of Phytic Acid (phospho phytate) of the production of inositol at present.The process equipment material
Matter requirement is stringent, and one-time investment is big, and operating pressure can only be controlled in certain scope, limits carrying for utilization rate of raw materials
Height, and crude product process for refining is complicated, loss is more, and production cost is higher, it is difficult to meet the market demand.
The content of the invention
It is an object of the invention to solve at least the above, and provide the advantages of at least will be described later.
It is a still further object of the present invention to provide a kind of extracting methods of inositol, and the technique inositol yield is high, and inositol produces
Go out at the same can also synchronous output organic feed component, increase economic efficiency, avoid wastage of material.
In order to realize these purposes and further advantage according to the present invention, a kind of extracting method of inositol is provided, including
Following steps：
Prefabricated inositol feed liquid, by the inositol feed liquid of prefabricated mass-volume concentration >=60g/L successively through ceramic membrane filter, from
After sub-exchange resin processing, activated carbon filtering, ultrafiltration membrance filter, vacuum and low temperature condensing crystallizing and crystal separation it is dry obtain into
Product.
Preferably, the method for prefabricated inositol feed liquid is specifically further comprising the steps of：
1) count in parts by weight, 10 portions of barleys are prepared into fructus hordei germinatus I, wherein, sprout length≤4mm of fructus hordei germinatus I；
2) fructus hordei germinatus I is pulverized into rear ultrasonication, 20- is stood after being afterwards sufficiently mixed fructus hordei germinatus I and 3-5 volume of water
40min obtains mixture I, wherein, water temperature is 49-53 DEG C, pH value 5.6-5.9；
3) count in parts by weight, 1 portion of mixture I and 1-3 portions of barley is sufficiently mixed, be protected from light rush bud processing and be prepared into barley
Bud II, wherein, sprout length≤3mm of fructus hordei germinatus II；
4) fructus hordei germinatus II is pulverized into rear ultrasonication, be afterwards sufficiently mixed fructus hordei germinatus II with 3-4 times of volume of water rear quiet
It puts 10-15min, obtains II mixed liquor of fructus hordei germinatus, added into II mixed liquor of fructus hordei germinatus after phytase and acid phosphatase slowly
It stirs 100-120min and obtains mixture II, water temperature is 47-49 DEG C, and the enzyme activity of phytase is 6-6.5U/ml, acid phosphatase
Enzyme activity be 1-1.3U/ml, pH value 5.6-5.9；
5) mixture II is filtered, obtain filtered fluid I and crosses filter residue I；
6) by I instantaneous flash distillation process of filter residue, flash liquid I and flash distillation material I are obtained；
7) by the flash distillation material, Partial filtration slag I and water by volume 5：1：(5-10) is mixed after being sufficiently mixed
Object III adds in appropriate cellulase stirring at low speed processing 25-45min into mixture III, obtains zymolyte I, wherein, water temperature is
30-33℃；
8) isothermal holding 72-108h obtains Yeast Cultivation liquid after brewer's yeast is inoculated with into the zymolyte, during this period,
Low speed stirs and is at the uniform velocity passed through air；
9) by Yeast Cultivation liquid after ultrasonic disruption is handled, phytase progress enzymolysis processing is added in thereto and is digested
Object II；
10) zymolyte II is filtered and obtained filter residue II and filtered fluid II；
11) the quick-frozen rear instantaneous flash distillation process of filter residue II is obtained into flash distillation material II and flash liquid II；
12) inositol feed liquid is prepared into after remaining filtered fluid I, filtered fluid II, flash liquid I and flash liquid II being mixed concentration.
Preferably, the condition of the 2) ultrasonication is：Ultrasonic power is 720-780w, ultrasonic treatment time
For 20-30min, ultrasound works interval is than being 4S/1S；
6) condition of the ultrasonication is：Ultrasonic power is 500-550w, ultrasonic treatment time 20-
30min, ultrasound works interval is than being 2S/1S.
Preferably, instantaneous flash distillation process is further comprising the steps of：
Filter residue I will be crossed or cross filter residue II and be delivered in instantaneous flash distillation process device, and will be vacuumized in flash distillation process device
To vacuum degree≤15kPa；
Hot steam is passed through into flash distillation process device to pressurize 10-15s after pressure >=200kPa；
Will be down to pressure≤20kPa by the pressure in flash distillation process device in 2s, and collect flash liquid a；
Vacuum degree≤20kPa will be evacuated in flash distillation process device again；
Hot steam is passed through into flash distillation process device to pressurize 8-10s after pressure >=150kPa；
Will be down to pressure≤25kPa by the pressure in flash distillation process device in 4s, and collect flash liquid b；
Flash liquid I or flash liquid II are obtained after the flash liquid a of collection and flash liquid b is mixed.
Preferably, it is described 8) in, air 3min is passed through into the zymolyte at interval of 10-20min, is passed through institute every time
It is zymolyte described in 30ml/L to state the air capacity in zymolyte.
Preferably, the separation aperture of the ceramic membrane is 20~100nm, and inositol feed liquid obtains dense after ceramic membrane filter
Demagnification number is 5~10 times of concentrate.
Preferably, the ion exchange resin using positive resin and negative resin series connection by the way of upper prop or with the moon,
The mixed bed upper prop of positive resin, wherein, the ratio of positive resin and negative resin is 1:1~1.5, upper column quantity is the ion exchange resin
10~25Bv of volume.
Preferably, the resin cation uses hydro-strong acidic cation exchange resin, and anion exchange resin is adopted
With one kind in the strong-base anion-exchange resin or weak-base anion-exchange resin of hydrogen-oxygen type.
Preferably, the activated carbon uses medical charcoal or sugar charcoal, and activated carbon dosage is the inositol material liquid volume
0.2~1%W/V, bleaching temperature are 50~70 DEG C.
Preferably, the ultrafiltration retaining molecular weight is the macromolecular substances of 1000~5000Da.
The present invention includes at least following advantageous effect：
In the method for prefabricated inositol feed liquid：
1) a large amount of phytic acid are generated in I germinating of fructus hordei germinatus, resolves into inositol for the later stage and material base is provided；
2) by fructus hordei germinatus I after this step enzymolysis processing, the inositol feed liquid of first batch is obtained, that is to say mixture I；
3) part mixes I and second portion barley are sufficiently mixed, the inositol in mixture I effectively facilitates second portion
Barley germination improves germination percentage, shortens the germination duration of second portion barley；
4) after fructus hordei germinatus II being pulverized rear ultrasonication, phytic acid therein is released, and is carried out at sufficient enzymolysis
Reason, obtains the inositol feed liquid of second lot, that is to say mixture II；
Through above-mentioned 1) -7) after processing, barley partial hydrolysis generates a large amount of monose and polysaccharide, is inoculated with brewer's yeast simultaneously
Air is passed through, aerobic respiration and index breeding is carried out, accumulates microorganism phytic acid content；
Phytic acid is released after ultrasonic disruption 9), and then the enzymolysis for carrying out phytic acid again obtains the inositol of the 3rd batch
Feed liquid；Again through 10) -12) inositol feed liquid is fully extracted, while remaining filter residue I excessively and mistake filter residue II are more rich in fructus hordei germinatus
Kind of nutritional ingredient, and the protein of brewer's yeast and fat content are high, is organic feed component full of nutrition, great nutrition
Value and economic value.
Again by the inositol feed liquid of prefabricated mass-volume concentration >=60g/L successively through ceramic membrane filter, ion exchange resin
After processing, activated carbon filtering, ultrafiltration membrance filter, vacuum and low temperature condensing crystallizing and crystal separation it is dry obtain purity it is high into
Product：With ceramic membrane filter, except the insoluble impurities in inositol feed liquid, the cleaner liquid containing inositol is obtained；Filtering containing inositol
Liquid spent ion exchange resin desalination, obtains the desalinization liquor containing inositol；Desalinization liquor containing inositol adds in activated carbon decolorizing, filters
Activated carbon obtains destainer 1；Destainer 1 removes the soluble large molecule substance in feed liquid with ultrafiltration membrane, obtains containing inositol
Dialyzate；Inositol dialyzate is concentrated in vacuo, and obtains concentrate 1, and then decrease temperature crystalline is handled.
By the inositol feed liquid of prefabricated mass-volume concentration >=60g/L successively through ceramic membrane filter, ion exchange resin at
It is dry after reason, activated carbon filtering, ultrafiltration membrance filter, vacuum and low temperature condensing crystallizing and crystal separation to obtain finished product.
Filtering is by the inositol feed liquid containing certain content, and temperature maintains 50~75 DEG C, filters to remove brewer's yeast
Thalline and other insoluble macromolecular substances in liquid.Filtering is under the action of motive force, and the suspension positioned at one side (or contains
Dust and gas) in fluid flowed by the duct of porous media to opposite side, particle is then trapped, so as to fulfill fluid and particle
Separation operation process.The suspension filtered is also known as filter pulp, and stratum granulosum during filtering under retention is known as filter cake, the clear liquid of filtering
Referred to as filtrate.No matter using which kind of filter type, filter medium is always necessary, and filter medium is to enable flow through and particle
The porous media being trapped.The general character requirement of filter medium is porous, stable in physicochemical property, durable and can recycle.Mesh
Before may be used as filter medium material it is very much, such as formed by naturally occurring or synthetic fiber, wire braiding filter cloth and strainer,
Single thread strainer, ceramic membrane, high molecular polymer perforated membrane etc. made of the fibers such as polyamide, polyester or polypropylene.Ceramic membrane mistake
Filter preferably separates aperture as 20~100nm.
Cation exchange resin is divided into as two class of highly acid and faintly acid at present.Strongly acidic cation-exchange mainly contains
There is the reactive group of highly acid, such as sulfonic group (- SO3H), this ion exchange resin can exchange all cations.Weak-type sun
Ion exchange resin has weaker reactive group such as carboxyl (- COOH bases), the sun in the only commutative weak base of this ion exchange resin
Ion such as Ca2+、Mg2+, for such as Na of the ion in highly basic+、K+Etc. can not swap.Cation exchange resin of the present invention
For strongly acidic cation-exchange.More preferably JK008,732#, WA-2 or W-2 type ion exchange resin.Wherein, 732# types
Ion exchange resin also known as 001 × 7 type cation exchange resin refer to that gel-type strongly acidic styrene cation exchanges tree
Fat, the degree of cross linking 7%, skeleton carry very highdensity charge.732 type cation exchange resins are made after calcium ion makes the transition
732 type calcium cationic exchange resins.JK008 types ion exchange resin be equal hole strongly acidic styrene type cation exchange resin, property
Can be similar to 001 × 7 serial cation exchange resin, but with higher exchange capacity.Anion exchange resin is divided into be strong
Alkalescence and two class of alkalescent.(1) strong basic type anion-exchange resin：Mainly containing stronger reactive group, such as there is tetrahedron
Its-N+ (CH of ammonium salt functional group3)3, under hydrogen-oxygen form ,-+(CH3)3Hydroxyl ion in OH- can disengage rapidly, to carry out
It exchanges, strong basic type anion-exchange resin can swap removal with all anion, this resinoid contains strong basicity base
Group, such as quaternary amine base (also known as level Four amido)-NR3OH (R is hydrocarbon group), can dissociate OH in water-And in strong basicity.This
The positive charged group of kind resin can be combined with the Anion-adsorption in solution, so as to generate anion exchange effect.This resin
Dissociative is very strong, can be worked normally under different pH.It is regenerated with highly basic (such as NaOH).(2) weak base type anion is handed over
Change resin：Containing alkalescent group, such as primary amine groups (also known as level-one amido)-NH2, secondary amine (secondary amine)-NHR or tertiary amine
Base (three-level amido)-NR2, they can dissociate OH- and be in alkalescent in water.The positive charged group energy and solution of this resin
In Anion-adsorption combine, so as to generate anion exchange effect.This resin is in most cases will be whole in solution
A other acid molecules absorption.It can only work under neutral or acid part (such as pH1~9).Anion exchange tree of the present invention
Fat is preferably 717 types or A830 type ion exchange resin.
In conclusion the extracting method of inositol, the technique inositol yield is high, and inositol output simultaneously can also synchronous output
Organic feed component, increases economic efficiency, and avoids wastage of material.
Part is illustrated to embody by further advantage, target and the feature of the present invention by following, and part will also be by this
The research and practice of invention and be understood by the person skilled in the art.
Description of the drawings
The process flow chart of the extracting method of Fig. 1 inositols according to the present invention；
The prefabricated process flow chart of Fig. 2 inositol feed liquids according to the present invention.
Specific embodiment
The present invention is described in further detail below in conjunction with the accompanying drawings, to make those skilled in the art with reference to specification text
Word can be implemented according to this.
It should be appreciated that such as " having ", "comprising" and " comprising " term used herein do not allot one or more
The presence or addition of a other elements or its combination.
As shown in Figure 1, the present invention provides a kind of extracting method of inositol, comprise the following steps：Prefabricated, the general of inositol feed liquid
The inositol feed liquid of prefabricated mass-volume concentration >=60g/L is successively through ceramic membrane filter, ion exchange resin treatment, activated carbon mistake
It is dry after filter, ultrafiltration membrance filter, vacuum and low temperature condensing crystallizing and crystal separation to obtain finished product.
As shown in Fig. 2, in a preferred embodiment, the method for prefabricated inositol feed liquid is specifically further comprising the steps of：
1) count in parts by weight, 10 portions of barleys are prepared into fructus hordei germinatus I, wherein, sprout length≤4mm of fructus hordei germinatus I；
I germinating of fructus hordei germinatus generates a large amount of phytic acid, resolves into inositol for the later stage and provides material base；
2) fructus hordei germinatus I is pulverized into rear ultrasonication, 20- is stood after being afterwards sufficiently mixed fructus hordei germinatus I and 3-5 volume of water
40min obtains mixture I, wherein, water temperature is 49-53 DEG C, pH value 5.6-5.9；After this step enzymolysis processing, the is obtained
A batch of inositol feed liquid, that is to say mixture I；
3) count in parts by weight, 1 portion of mixture I and 1-3 portions of barley is sufficiently mixed, be protected from light rush bud processing and be prepared into barley
Bud II, wherein, sprout length≤3mm of fructus hordei germinatus II；Part mixes I and second portion barley are sufficiently mixed, mixture I
In inositol effectively facilitate second portion barley germination, improve germination percentage, shorten the germination duration of second portion barley；
4) fructus hordei germinatus II is pulverized into rear ultrasonication, be afterwards sufficiently mixed fructus hordei germinatus II with 3-4 times of volume of water rear quiet
It puts 10-15min, obtains II mixed liquor of fructus hordei germinatus, added into II mixed liquor of fructus hordei germinatus after phytase and acid phosphatase slowly
It stirs 100-120min and obtains mixture II, water temperature is 47-49 DEG C, and the enzyme activity of phytase is 6-6.5U/ml, acid phosphatase
Enzyme activity be 1-1.3U/ml, pH value 5.6-5.9；After fructus hordei germinatus II is pulverized rear ultrasonication, release therein
Phytic acid, and sufficient enzymolysis processing is carried out, the inositol feed liquid of second lot is obtained, that is to say mixture II；
5) mixture II is filtered, obtain filtered fluid I and crosses filter residue I；
6) by I instantaneous flash distillation process of filter residue, flash liquid I and flash distillation material I are obtained；By I instantaneous flash distillation process of filter residue,
Fully extract inositol feed liquid of the absorption in filter residue I is crossed；
7) by the flash distillation material, Partial filtration slag I and water by volume 5：1：(5-10) is mixed after being sufficiently mixed
Object III adds in appropriate cellulase stirring at low speed processing 25-45min into mixture III, obtains zymolyte I, wherein, water temperature is
30-33℃；
8) isothermal holding 72-108h obtains Yeast Cultivation liquid after brewer's yeast is inoculated with into the zymolyte, during this period,
Low speed stirs and is at the uniform velocity passed through air；Wherein, brewer's yeast refers to the yeast for beer brewing.Mostly saccharomyces cerevisiae (Sac-
Charomyces cerevisiae) different cultivars.Cellular morphology is identical with other culture yeasts, is subsphaeroidal ellipsoid,
It is different from wild yeasts.Brewer's yeast is common typical top fermenting yeast in Beer Brewage.Thalline vitamin, protein
Content is high, can eat, medicinal and fodder yeast.
9) by Yeast Cultivation liquid after ultrasonic disruption is handled, phytase progress enzymolysis processing is added in thereto and is digested
Object II；
10) zymolyte II is filtered and obtained filter residue II and filtered fluid II；
11) the quick-frozen rear instantaneous flash distillation process of filter residue II is obtained into flash distillation material II and flash liquid II；
12) inositol feed liquid is prepared into after remaining filtered fluid I, filtered fluid II, flash liquid I and flash liquid II being mixed concentration.
Through above-mentioned 1) -7) after processing, barley partial hydrolysis generates a large amount of monose and polysaccharide, is inoculated with brewer's yeast simultaneously
Air is passed through, aerobic respiration and index breeding is carried out, accumulates microorganism phytic acid content；
Phytic acid is released after ultrasonic disruption 9), and then the enzymolysis for carrying out phytic acid again obtains the inositol of the 3rd batch
Feed liquid；Again through 10) -12) inositol feed liquid is fully extracted, while remaining filter residue I excessively and mistake filter residue II are more rich in fructus hordei germinatus
Kind of nutritional ingredient, and the protein of brewer's yeast and fat content are high, is organic feed component full of nutrition, great nutrition
Value and economic value.
In one preferred embodiment, the condition of the 2) ultrasonication is：Ultrasonic power is 720-780w, at ultrasonic wave
The reason time is 20-30min, and ultrasound works interval is than being 4S/1S；
6) condition of the ultrasonication is：Ultrasonic power is 500-550w, ultrasonic treatment time 20-
30min, ultrasound works interval is than being 2S/1S.
In one preferred embodiment, instantaneous flash distillation process is further comprising the steps of：
Filter residue I will be crossed or cross filter residue II and be delivered in instantaneous flash distillation process device, and will be vacuumized in flash distillation process device
To vacuum degree≤15kPa；
Hot steam is passed through into flash distillation process device to pressurize 10-15s after pressure >=200kPa；
Will be down to pressure≤20kPa by the pressure in flash distillation process device in 2s, and collect flash liquid a；
Vacuum degree≤20kPa will be evacuated in flash distillation process device again；
Hot steam is passed through into flash distillation process device to pressurize 8-10s after pressure >=150kPa；
Will be down to pressure≤25kPa by the pressure in flash distillation process device in 4s, and collect flash liquid b；
Flash liquid I or flash liquid II are obtained after the flash liquid a of collection and flash liquid b is mixed.
In one preferred embodiment, it is described 8) in, air 3min is passed through into the zymolyte at interval of 10-20min, every time
The air capacity being passed through in the zymolyte is zymolyte described in 30ml/L.
Wherein, with ceramic membrane filter, except the insoluble impurities in inositol feed liquid, the cleaner liquid containing inositol is obtained；Contain
The cleaner liquid spent ion exchange resin desalination of inositol, obtains the desalinization liquor containing inositol；Desalinization liquor containing inositol adds in activity
Carbon decoloring I, filter activated carbon and obtain destainer 1；Destainer 1 removes the soluble large molecule substance in feed liquid with ultrafiltration membrane, obtains
To the dialyzate containing inositol；Inositol dialyzate is concentrated in vacuo, and obtains concentrate 1, then decrease temperature crystalline；Concentration after cooling
1, with the isolated wet crystal of sheet frame or centrifuge and a mother liquor；The wet crystal of isolated inositol through be dried to obtain inositol into
Product.
The concentrate mysoinositol content of vacuum and low temperature condensing crystallizing is controlled between 350~450g/L, after condensing crystallizing
Crystal separation is separated using centrifuge or flame filter press；The recyclable recrystallization processing of mother liquor, tool are obtained after Crystallization Separation
Body disposing mother liquor step is：
An isolated mother liquor adds in activated carbon and decolourizes, filters activated carbon and obtain destainer 2；
Destainer 2 is directly concentrated in vacuo, and obtains concentrate 2, decrease temperature crystalline；
Concentrate 2 after cooling is separated with sheet frame or centrifuge, and washing crystalline substance is added in separation process, obtains the wet crystalline substance of inositol
Body；
Isolated wet crystal is dried to obtain inositol finished product.
In one preferred embodiment, the separation aperture of the ceramic membrane is 20~100nm, and inositol feed liquid is after ceramic membrane filter
Obtain the concentrate that cycles of concentration is 5~10 times.
In one preferred embodiment, the ion exchange resin using positive resin and negative resin series connection by the way of upper prop or
It is the mixed bed upper prop with yin, yang resin, wherein, the ratio of positive resin and negative resin is 1:1~1.5, upper column quantity is the ion
10~25Bv of exchanger resin volume.
In one preferred embodiment, the resin cation uses hydro-strong acidic cation exchange resin, anion exchange
Resin is using one kind in the strong-base anion-exchange resin or weak-base anion-exchange resin of hydrogen-oxygen type.
In one preferred embodiment, the activated carbon uses medical charcoal or sugar charcoal, and activated carbon dosage is the inositol feed liquid
0.2~1%W/V of volume, bleaching temperature are 50~70 DEG C.
In one preferred embodiment, the ultrafiltration retaining molecular weight is the macromolecular substances of 1000~5000Da.
Embodiment 1
Prefabricated inositol feed liquid：
1) count in parts by weight, 10 portions of barleys are prepared into fructus hordei germinatus I, wherein, the sprout length 4mm of fructus hordei germinatus I；
2) fructus hordei germinatus I is pulverized into rear ultrasonication, is stood after fructus hordei germinatus I is sufficiently mixed with 3 volume of water afterwards
20min obtains mixture I, wherein, water temperature is 49 DEG C, pH value 5.6；
3) count in parts by weight, 1 portion of mixture I and 1-3 portions of barley is sufficiently mixed, be protected from light rush bud processing and be prepared into barley
Bud II, wherein, the sprout length 3mm of fructus hordei germinatus II；
4) fructus hordei germinatus II is pulverized into rear ultrasonication, is stood after fructus hordei germinatus II is sufficiently mixed with 3 times of volume of water afterwards
10min obtains II mixed liquor of fructus hordei germinatus, is slowly stirred after adding phytase and acid phosphatase into II mixed liquor of fructus hordei germinatus
100min obtains mixture II, and water temperature is 47 DEG C, and the enzyme activity of phytase is 6U/ml, and the enzyme activity of acid phosphatase is 1U/
Ml, pH value 5.6；
5) mixture II is filtered, obtain filtered fluid I and crosses filter residue I；
6) by I instantaneous flash distillation process of filter residue, flash liquid I and flash distillation material I are obtained；
7) by the flash distillation material, Partial filtration slag I and water by volume 5：1：5 be sufficiently mixed after obtain mixture III,
Appropriate cellulase stirring at low speed processing 25-45min is added in into mixture III, obtains zymolyte I, wherein, water temperature is 30 DEG C；
8) isothermal holding 72h obtains Yeast Cultivation liquid, during this period, low speed after brewer's yeast is inoculated with into the zymolyte
It stirs and is at the uniform velocity passed through air；
9) by Yeast Cultivation liquid after ultrasonic disruption is handled, phytase progress enzymolysis processing is added in thereto and is digested
Object II；
10) zymolyte II is filtered and obtained filter residue II and filtered fluid II；
11) the quick-frozen rear instantaneous flash distillation process of filter residue II is obtained into flash distillation material II and flash liquid II；
12) inositol feed liquid is prepared into after remaining filtered fluid I, filtered fluid II, flash liquid I and flash liquid II being mixed concentration.
Wherein, the condition of the 2) ultrasonication is：Ultrasonic power is 720w, ultrasonic treatment time 20min,
Ultrasound works interval is than being 4S/1S；
6) condition of the ultrasonication is：Ultrasonic power is 500w, ultrasonic treatment time 20min, ultrasound
Work interval ratio is 2S/1S.
Instantaneous flash distillation process is further comprising the steps of：Filter residue I will be crossed or cross filter residue II and be delivered to instantaneous flash distillation process device
It is interior, and vacuum degree 15kPa will be evacuated in flash distillation process device；Hot steam is passed through into flash distillation process device to pressure
Pressurize 10s after 200kPa；Will be down to pressure 20kPa by the pressure in flash distillation process device in 2s, and collect flash liquid a；Again
It is secondary to be evacuated to vacuum degree 20kPa in flash distillation process device；Hot steam is passed through into flash distillation process device to pressure 150kPa
Pressurize 8s afterwards；Will be down to pressure 25kPa by the pressure in flash distillation process device in 4s, and collect flash liquid b；By the sudden strain of a muscle of collection
Flash liquid I or flash liquid II are obtained after steaming liquid a and flash liquid b mixing.
It is described 8) in, air 3min is passed through into the zymolyte at interval of 10min, is passed through every time in the zymolyte
Air capacity is zymolyte described in 30ml/L.
After above-mentioned steps prepare inositol feed liquid, the feed liquid that 100L inositol contents are 92g/L is taken, pore size filter is
The ceramic membrane filter of 50nm obtains cleaner liquid, and cleaner liquid is crossed 12L anion-exchange resin columns, 10L cation exchange resin columns, obtained
To desalinization liquor 132L, adding in 70g sugar and decolourized with charcoal, obtain destainer 1, destainer 1 obtains dialyzate through ultrafiltration membrance filter,
Dialyzate is concentrated into inositol content as 395g/L, then decrease temperature crystalline, slow cooling to 8 DEG C, temperature fall time 10h separates, from
The isolated wet crystal 6477g of the heart, obtains inositol finished product 5830g after drying；One time mother liquor adds in 124g sugar carbon decolorings, obtains
Destainer 2, destainer 2 are concentrated into inositol content as 378g/L, decrease temperature crystalline.Slow cooling to 15 DEG C, temperature fall time 8h, from
The heart separates, and 500ml washing crystalline substances are added in separation process, wet crystal 1771g is obtained, inositol finished product 1596g is obtained after drying；Through liquid
The finished product content that is dried to obtain twice of chromatography detection is respectively 98.85% and 97.92%, total recovery 80.71%.
Embodiment 2
Prefabricated inositol feed liquid：
1) count in parts by weight, 10 portions of barleys are prepared into fructus hordei germinatus I, wherein, the sprout length 3mm of fructus hordei germinatus I；
2) fructus hordei germinatus I is pulverized into rear ultrasonication, is stood after fructus hordei germinatus I is sufficiently mixed with 4 volume of water afterwards
30min obtains mixture I, wherein, water temperature is 51 DEG C, pH value 5.8；
3) count in parts by weight, 1 part of mixture I and 2 portions of barleys are sufficiently mixed, be protected from light rush bud processing and be prepared into fructus hordei germinatus
II, wherein, the sprout length 2mm of fructus hordei germinatus II；
4) fructus hordei germinatus II is pulverized into rear ultrasonication, be afterwards sufficiently mixed fructus hordei germinatus II with 3-4 times of volume of water rear quiet
13min is put, obtains II mixed liquor of fructus hordei germinatus, is slowly stirred after adding phytase and acid phosphatase into II mixed liquor of fructus hordei germinatus
110min obtains mixture II, and water temperature is 48 DEG C, and the enzyme activity of phytase is 6.5U/ml, and the enzyme activity of acid phosphatase is
1.2U/ml, pH value 5.8；
5) mixture II is filtered, obtain filtered fluid I and crosses filter residue I；
6) by I instantaneous flash distillation process of filter residue, flash liquid I and flash distillation material I are obtained；
7) by the flash distillation material, Partial filtration slag I and water by volume 5：1：7 be sufficiently mixed after obtain mixture III,
Appropriate cellulase stirring at low speed processing 25-45min is added in into mixture III, obtains zymolyte I, wherein, water temperature is 32 DEG C；
8) isothermal holding 92h obtains Yeast Cultivation liquid, during this period, low speed after brewer's yeast is inoculated with into the zymolyte
It stirs and is at the uniform velocity passed through air；
9) by Yeast Cultivation liquid after ultrasonic disruption is handled, phytase progress enzymolysis processing is added in thereto and is digested
Object II；
10) zymolyte II is filtered and obtained filter residue II and filtered fluid II；
11) the quick-frozen rear instantaneous flash distillation process of filter residue II is obtained into flash distillation material II and flash liquid II；
12) inositol feed liquid is prepared into after remaining filtered fluid I, filtered fluid II, flash liquid I and flash liquid II being mixed concentration.
Wherein, the condition of the 2) ultrasonication is：Ultrasonic power is 75w, ultrasonic treatment time 25min,
Ultrasound works interval is than being 4S/1S；
6) condition of the ultrasonication is：Ultrasonic power is 530w, ultrasonic treatment time 25min, ultrasound
Work interval ratio is 2S/1S.
Instantaneous flash distillation process is further comprising the steps of：Filter residue I will be crossed or cross filter residue II and be delivered to instantaneous flash distillation process device
It is interior, and vacuum degree 11kPa will be evacuated in flash distillation process device；Hot steam is passed through into flash distillation process device to pressure
Pressurize 10-15s after 240kPa；Will be down to pressure 15kPa by the pressure in flash distillation process device in 2s, and collect flash liquid a；
Vacuum degree 15kPa will be evacuated in flash distillation process device again；Hot steam is passed through into flash distillation process device to pressure
Pressurize 8-10s after 170kPa；Will be down to pressure 30kPa by the pressure in flash distillation process device in 4s, and collect flash liquid b；
Flash liquid I or flash liquid II are obtained after the flash liquid a of collection and flash liquid b is mixed.
It is described 8) in, air 3min is passed through into the zymolyte at interval of 15min, is passed through every time in the zymolyte
Air capacity is zymolyte described in 30ml/L.
After above-mentioned steps prepare inositol feed liquid, the feed liquid that 150L inositol contents are 83g/L is taken, pore size filter is
The ceramic membrane filter of 100nm obtains cleaner liquid, and cleaner liquid crosses 15L anion-exchange resin columns, 11L cation exchange resin columns,
Desalinization liquor 201L is obtained, 90.45g medical charcoal is added in and decolourizes, obtain destainer 1, destainer 1 is obtained through ultrafiltration membrance filter
Liquid is analysed, the ultrafiltration membrane that molecular cut off is 3000Da is selected in ultrafiltration, and dialyzate is concentrated into inositol content as 375g/L, cooling knot
Then crystalline substance, slow cooling to 6 DEG C, temperature fall time 10h separate, are centrifugally separating to obtain wet crystal 7730g, flesh is obtained after drying
Alcohol finished product 6960g；Mother liquor 30.5L, one time mother liquor adds in 305g sugar carbon decolorings, obtains destainer 2, destainer 2 concentrates
To inositol content be 368g/L, decrease temperature crystalline.Slow cooling is centrifuged to 18 DEG C, temperature fall time 8h, is added in separation process
It is brilliant to enter 700ml washings, obtains wet crystal 2900g, inositol finished product 2610g is obtained after drying；It is done twice through liquid chromatograph detection
Dry obtained finished product content is respectively 98.52% and 97.43%, total recovery 76.87%.
Embodiment 3
Prefabricated inositol feed liquid：
1) count in parts by weight, 10 portions of barleys are prepared into fructus hordei germinatus I, wherein, the sprout length 2mm of fructus hordei germinatus I；
2) fructus hordei germinatus I is pulverized into rear ultrasonication, is stood after fructus hordei germinatus I is sufficiently mixed with 5 volume of water afterwards
40min obtains mixture I, wherein, water temperature is 53 DEG C, pH value 5.9；
3) count in parts by weight, 1 part of mixture I and 3 portions of barleys are sufficiently mixed, be protected from light rush bud processing and be prepared into fructus hordei germinatus
II, wherein, the sprout length 2mm of fructus hordei germinatus II；
4) fructus hordei germinatus II is pulverized into rear ultrasonication, is stood after fructus hordei germinatus II is sufficiently mixed with 4 times of volume of water afterwards
15min obtains II mixed liquor of fructus hordei germinatus, is slowly stirred after adding phytase and acid phosphatase into II mixed liquor of fructus hordei germinatus
120min obtains mixture II, and water temperature is 49 DEG C, and the enzyme activity of phytase is 6.5U/ml, and the enzyme activity of acid phosphatase is
1.3U/ml, pH value 5.9；
5) mixture II is filtered, obtain filtered fluid I and crosses filter residue I；
6) by I instantaneous flash distillation process of filter residue, flash liquid I and flash distillation material I are obtained；
7) by the flash distillation material, Partial filtration slag I and water by volume 5：1：10 be sufficiently mixed after obtain mixture III,
Appropriate cellulase stirring at low speed processing 45min is added in into mixture III, obtains zymolyte I, wherein, water temperature is 33 DEG C；
8) isothermal holding 108h obtains Yeast Cultivation liquid after brewer's yeast is inoculated with into the zymolyte, during this period, low
Speed stirs and is at the uniform velocity passed through air；
9) by Yeast Cultivation liquid after ultrasonic disruption is handled, phytase progress enzymolysis processing is added in thereto and is digested
Object II；
10) zymolyte II is filtered and obtained filter residue II and filtered fluid II；
11) the quick-frozen rear instantaneous flash distillation process of filter residue II is obtained into flash distillation material II and flash liquid II；
12) inositol feed liquid is prepared into after remaining filtered fluid I, filtered fluid II, flash liquid I and flash liquid II being mixed concentration.
Wherein, the condition of the 2) ultrasonication is：Ultrasonic power is 780w, ultrasonic treatment time 30min,
Ultrasound works interval is than being 4S/1S；
6) condition of the ultrasonication is：Ultrasonic power is 550w, ultrasonic treatment time 30min, ultrasound
Work interval ratio is 2S/1S.
Instantaneous flash distillation process is further comprising the steps of：Filter residue I will be crossed or cross filter residue II and be delivered to instantaneous flash distillation process device
It is interior, and vacuum degree 10kPa will be evacuated in flash distillation process device；Hot steam is passed through into flash distillation process device to pressure
Pressurize 15s after 280kPa；Will be down to pressure 13kPa by the pressure in flash distillation process device in 2s, and collect flash liquid a；Again
It is secondary to be evacuated to vacuum degree 12kPa in flash distillation process device；Hot steam is passed through into flash distillation process device to pressure 200kPa
Pressurize 10s afterwards；Will be down to pressure 10kPa by the pressure in flash distillation process device in 4s, and collect flash liquid b；By collection
Flash liquid I or flash liquid II are obtained after flash liquid a and flash liquid b mixing.
It is described 8) in, air 3min is passed through into the zymolyte at interval of 20min, is passed through every time in the zymolyte
Air capacity is zymolyte described in 30ml/L.
After above-mentioned steps prepare inositol feed liquid, the feed liquid that 500L inositol contents are 124.6g/L, pore size filter are taken
Cleaner liquid is obtained for the ceramic membrane filter of 100nm, cleaner liquid crosses 58.5L anion-exchange resin columns, 45L cation exchange resins
Column obtains desalinization liquor 672L, adds in 2688g sugar and is decolourized with charcoal, obtains destainer 1, destainer 1 is obtained through ultrafiltration membrance filter
The ultrafiltration membrane that molecular cut off is 2000Da is selected in dialyzate, ultrafiltration, and dialyzate is concentrated into inositol content as 415g/L, cooling knot
Then crystalline substance, slow cooling to 10 DEG C, temperature fall time 10h separate, are centrifugally separating to obtain wet crystal 41518g, are obtained after drying
Inositol finished product 38196g；Mother liquor 128L, one time mother liquor adds in the medicinal carbon decolorings of 1024g, obtains destainer 2, destainer 2 is dense
Inositol content is reduced to as 383g/L, decrease temperature crystalline.Slow cooling centrifuges, to 15 DEG C, temperature fall time 8h in separation process
It is brilliant to add in 11.52ml washings, obtains wet crystal 12810g, inositol finished product 11785g is obtained after drying；It is detected through liquid chromatograph
The finished product content being dried to obtain twice is respectively 98.83% and 98.05%, total recovery 80.23%.
Although the embodiments of the present invention have been disclosed as above, but its be not restricted in specification and embodiment it is listed
With it can be fully applied to various fields suitable for the present invention, for those skilled in the art, can be easily
Realize other modification, therefore without departing from the general concept defined in the claims and the equivalent scope, it is of the invention and unlimited
In specific details and shown here as the legend with description.
Claims (10)
1. a kind of extracting method of inositol, which is characterized in that comprise the following steps：
Prefabricated inositol feed liquid hands over the inositol feed liquid of prefabricated mass-volume concentration >=60g/L through ceramic membrane filter, ion successively
Change dry acquisition finished product after resin treatment, activated carbon filtering, ultrafiltration membrance filter, vacuum and low temperature condensing crystallizing and crystal separate.
2. the extracting method of inositol as described in claim 1, which is characterized in that the method for prefabricated inositol feed liquid specifically further includes
Following steps：
1) count in parts by weight, 10 portions of barleys are prepared into fructus hordei germinatus I, wherein, sprout length≤4mm of fructus hordei germinatus I；
2) fructus hordei germinatus I is pulverized into rear ultrasonication, 20- is stood after being afterwards sufficiently mixed fructus hordei germinatus I and 3-5 volume of water
40min obtains mixture I, wherein, water temperature is 49-53 DEG C, pH value 5.6-5.9；
3) count in parts by weight, 1 portion of mixture I and 1-3 portions of barley is sufficiently mixed, be protected from light rush bud processing and be prepared into fructus hordei germinatus
II, wherein, sprout length≤3mm of fructus hordei germinatus II；
4) fructus hordei germinatus II is pulverized into rear ultrasonication, 10- is stood after being afterwards sufficiently mixed fructus hordei germinatus II and 3-4 times of volume of water
15min obtains II mixed liquor of fructus hordei germinatus, is slowly stirred after adding phytase and acid phosphatase into II mixed liquor of fructus hordei germinatus
100-120min obtains mixture II, and water temperature is 47-49 DEG C, and the enzyme activity of phytase is 6-6.5U/ml, the enzyme of acid phosphatase
Vigor is 1-1.3U/ml, pH value 5.6-5.9；
5) mixture II is filtered, obtain filtered fluid I and crosses filter residue I；
6) by I instantaneous flash distillation process of filter residue, flash liquid I and flash distillation material I are obtained；
7) by the flash distillation material, Partial filtration slag I and water by volume 5：1：(5-10) obtains mixture III after being sufficiently mixed,
Appropriate cellulase stirring at low speed processing 25-45min is added in into mixture III, obtains zymolyte I, wherein, water temperature 30-33
℃；
8) isothermal holding 72-108h obtains Yeast Cultivation liquid, during this period, low speed after brewer's yeast is inoculated with into the zymolyte
It stirs and is at the uniform velocity passed through air；
9) by Yeast Cultivation liquid after ultrasonic disruption is handled, phytase is added in thereto and carries out enzymolysis processing acquisition zymolyte
Ⅱ；
10) zymolyte II is filtered and obtained filter residue II and filtered fluid II；
11) the quick-frozen rear instantaneous flash distillation process of filter residue II is obtained into flash distillation material II and flash liquid II；
12) inositol feed liquid is prepared into after remaining filtered fluid I, filtered fluid II, flash liquid I and flash liquid II being mixed concentration.
3. the extracting method of inositol as claimed in claim 2, which is characterized in that the condition of the 2) ultrasonication is：It is super
Acoustic power is 720-780w, and ultrasonic treatment time 20-30min, ultrasound works interval is than being 4S/1S；
6) condition of the ultrasonication is：Ultrasonic power is 500-550w, ultrasonic treatment time 20-30min, is surpassed
Sound work interval ratio is 2S/1S.
4. the extracting method of inositol as claimed in claim 2, which is characterized in that instantaneous flash distillation process is further comprising the steps of：
Filter residue I will be crossed or cross filter residue II and be delivered in instantaneous flash distillation process device, and will be evacuated in flash distillation process device true
Reciprocal of duty cycle≤15kPa；
Hot steam is passed through into flash distillation process device to pressurize 10-15s after pressure >=200kPa；
Will be down to pressure≤20kPa by the pressure in flash distillation process device in 2s, and collect flash liquid a；
Vacuum degree≤20kPa will be evacuated in flash distillation process device again；
Hot steam is passed through into flash distillation process device to pressurize 8-10s after pressure >=150kPa；
Will be down to pressure≤25kPa by the pressure in flash distillation process device in 4s, and collect flash liquid b；
Flash liquid I or flash liquid II are obtained after the flash liquid a of collection and flash liquid b is mixed.
5. the extracting method of inositol as claimed in claim 2, which is characterized in that it is described 8) in, at interval of 10-20min to institute
It states and air 3min is passed through in zymolyte, the air capacity being passed through every time in the zymolyte is zymolyte described in 30ml/L.
6. the extracting method of inositol as described in claim 1, which is characterized in that the separation aperture of the ceramic membrane for 20~
100nm, inositol feed liquid obtain the concentrate that cycles of concentration is 5~10 times after ceramic membrane filter.
7. the extracting method of inositol as described in claim 1, which is characterized in that the ion exchange resin using positive resin and
The mode upper prop or the mixed bed upper prop with yin, yang resin of negative resin series connection, wherein, the ratio of positive resin and negative resin is
1:1~1.5, upper column quantity is 10~25Bv of the ion exchange resin volume.
8. the extracting method of inositol as claimed in claim 3, which is characterized in that the resin cation uses hydrogen type strong acid
Cation exchange resin, anion exchange resin use the strong-base anion-exchange resin or weakly-basic anion of hydrogen-oxygen type
One kind in exchanger resin.
9. the extracting method of inositol as described in claim 1, which is characterized in that the activated carbon is used using medical charcoal or sugar
Charcoal, activated carbon dosage are 0.2~1%W/V of the inositol material liquid volume, and bleaching temperature is 50~70 DEG C.
10. the extracting method of inositol as described in claim 1, which is characterized in that the ultrafiltration retaining molecular weight is 1000
The macromolecular substances of~5000Da.
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