CN111500794A - Production method of water-containing glucose - Google Patents
Production method of water-containing glucose Download PDFInfo
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- CN111500794A CN111500794A CN202010297236.1A CN202010297236A CN111500794A CN 111500794 A CN111500794 A CN 111500794A CN 202010297236 A CN202010297236 A CN 202010297236A CN 111500794 A CN111500794 A CN 111500794A
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- activated carbon
- aqueous glucose
- ion exchange
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- WQZGKKKJIJFFOK-GASJEMHNSA-N Glucose Natural products OC[C@H]1OC(O)[C@H](O)[C@@H](O)[C@@H]1O WQZGKKKJIJFFOK-GASJEMHNSA-N 0.000 title claims abstract description 38
- 239000008103 glucose Substances 0.000 title claims abstract description 38
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 28
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 title claims abstract description 17
- 238000001914 filtration Methods 0.000 claims abstract description 105
- 239000006188 syrup Substances 0.000 claims abstract description 41
- 235000020357 syrup Nutrition 0.000 claims abstract description 41
- 238000005342 ion exchange Methods 0.000 claims abstract description 27
- 238000001035 drying Methods 0.000 claims abstract description 21
- 238000001704 evaporation Methods 0.000 claims abstract description 19
- 238000000034 method Methods 0.000 claims abstract description 17
- 238000002425 crystallisation Methods 0.000 claims abstract description 16
- 230000008025 crystallization Effects 0.000 claims abstract description 16
- 229920002472 Starch Polymers 0.000 claims abstract description 11
- 239000008107 starch Substances 0.000 claims abstract description 11
- 235000019698 starch Nutrition 0.000 claims abstract description 11
- 235000013336 milk Nutrition 0.000 claims abstract description 10
- 239000008267 milk Substances 0.000 claims abstract description 10
- 210000004080 milk Anatomy 0.000 claims abstract description 10
- 238000005119 centrifugation Methods 0.000 claims abstract description 8
- 230000008020 evaporation Effects 0.000 claims abstract description 8
- 238000002347 injection Methods 0.000 claims abstract description 7
- 239000007924 injection Substances 0.000 claims abstract description 7
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 84
- 239000007788 liquid Substances 0.000 claims description 26
- 102000004169 proteins and genes Human genes 0.000 claims description 21
- 108090000623 proteins and genes Proteins 0.000 claims description 21
- 235000012907 honey Nutrition 0.000 claims description 16
- 239000004743 Polypropylene Substances 0.000 claims description 15
- -1 polypropylene Polymers 0.000 claims description 15
- 229920001155 polypropylene Polymers 0.000 claims description 15
- 238000005406 washing Methods 0.000 claims description 15
- 239000013078 crystal Substances 0.000 claims description 14
- 238000004042 decolorization Methods 0.000 claims description 14
- 150000001768 cations Chemical class 0.000 claims description 12
- 239000012452 mother liquor Substances 0.000 claims description 11
- 238000000746 purification Methods 0.000 claims description 10
- 239000011148 porous material Substances 0.000 claims description 8
- 238000005189 flocculation Methods 0.000 claims description 4
- 230000016615 flocculation Effects 0.000 claims description 4
- 238000005507 spraying Methods 0.000 claims description 4
- 235000013162 Cocos nucifera Nutrition 0.000 claims description 3
- 244000060011 Cocos nucifera Species 0.000 claims description 3
- 239000003957 anion exchange resin Substances 0.000 claims description 3
- 239000003729 cation exchange resin Substances 0.000 claims description 3
- 238000002156 mixing Methods 0.000 claims description 3
- 230000009290 primary effect Effects 0.000 claims description 3
- 239000010420 shell particle Substances 0.000 claims description 3
- 230000001105 regulatory effect Effects 0.000 abstract 1
- 239000012528 membrane Substances 0.000 description 21
- 239000000243 solution Substances 0.000 description 10
- 229920002678 cellulose Polymers 0.000 description 9
- 238000001179 sorption measurement Methods 0.000 description 9
- 229910052799 carbon Inorganic materials 0.000 description 8
- 238000001816 cooling Methods 0.000 description 8
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 description 7
- 238000005349 anion exchange Methods 0.000 description 6
- 238000005341 cation exchange Methods 0.000 description 6
- 238000004383 yellowing Methods 0.000 description 6
- 239000000126 substance Substances 0.000 description 5
- 239000012535 impurity Substances 0.000 description 4
- 239000006004 Quartz sand Substances 0.000 description 3
- 150000001450 anions Chemical class 0.000 description 3
- 238000006243 chemical reaction Methods 0.000 description 3
- 239000011347 resin Substances 0.000 description 3
- 229920005989 resin Polymers 0.000 description 3
- 238000000926 separation method Methods 0.000 description 3
- 239000004677 Nylon Substances 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 239000000463 material Substances 0.000 description 2
- 239000010413 mother solution Substances 0.000 description 2
- 229920001778 nylon Polymers 0.000 description 2
- 230000004075 alteration Effects 0.000 description 1
- 230000000903 blocking effect Effects 0.000 description 1
- 238000001514 detection method Methods 0.000 description 1
- 238000005374 membrane filtration Methods 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000003541 multi-stage reaction Methods 0.000 description 1
- 239000002357 osmotic agent Substances 0.000 description 1
- 238000004806 packaging method and process Methods 0.000 description 1
- 239000002245 particle Substances 0.000 description 1
- 239000000843 powder Substances 0.000 description 1
- 239000002510 pyrogen Substances 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 238000007670 refining Methods 0.000 description 1
- 229920006395 saturated elastomer Polymers 0.000 description 1
- 230000009291 secondary effect Effects 0.000 description 1
- 239000007921 spray Substances 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
- 230000009293 tertiary effect Effects 0.000 description 1
- 238000009423 ventilation Methods 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C13—SUGAR INDUSTRY
- C13K—SACCHARIDES OBTAINED FROM NATURAL SOURCES OR BY HYDROLYSIS OF NATURALLY OCCURRING DISACCHARIDES, OLIGOSACCHARIDES OR POLYSACCHARIDES
- C13K1/00—Glucose; Glucose-containing syrups
- C13K1/06—Glucose; Glucose-containing syrups obtained by saccharification of starch or raw materials containing starch
- C13K1/08—Purifying
-
- C—CHEMISTRY; METALLURGY
- C13—SUGAR INDUSTRY
- C13K—SACCHARIDES OBTAINED FROM NATURAL SOURCES OR BY HYDROLYSIS OF NATURALLY OCCURRING DISACCHARIDES, OLIGOSACCHARIDES OR POLYSACCHARIDES
- C13K1/00—Glucose; Glucose-containing syrups
- C13K1/10—Crystallisation
Landscapes
- Chemical & Material Sciences (AREA)
- Health & Medical Sciences (AREA)
- Emergency Medicine (AREA)
- General Health & Medical Sciences (AREA)
- Life Sciences & Earth Sciences (AREA)
- Biochemistry (AREA)
- Organic Chemistry (AREA)
- Crystallography & Structural Chemistry (AREA)
- Jellies, Jams, And Syrups (AREA)
Abstract
The invention relates to the technical field of production of aqueous glucose, and discloses a production method of aqueous glucose, which comprises the following steps of firstly processing the aqueous glucose through starch milk → one-time injection → a column type liquefier, and performing subsequent treatment: s1 pre-filtering, S2 decolorizing and filtering, S3 regulating the pH value, S4 decolorizing dilute syrup, S5 ion exchange, S6 low-temperature evaporation, S7 thick syrup decolorizing, S8 crystallization, S9 centrifugation and S10 drying; the method improves the traditional process for producing the water-containing glucose product, has low requirement on matched production equipment, can effectively improve the problem of filtration rate, improves the filtration rate, and meets the market requirements at home and abroad.
Description
Technical Field
The invention relates to the technical field of production of aqueous glucose, in particular to a production method of aqueous glucose.
Background
At present, the domestic medical water-containing glucose market reaches the nearly saturated condition, and the foreign medical osmotic agent and other fields still have market demands for the product. After most of domestic customers purchase water-containing glucose products, the water-containing glucose products are treated by activated carbon and then used as pharmaceutical raw and auxiliary materials; the foreign customers basically cancel the active carbon filtration and directly apply the active carbon filtration after the active carbon filtration is processed by adopting a membrane filtration mode, so the corresponding product quality also faces greater examination.
The foreign company uses a 0.22 micron filter element to respectively filter the hydrous glucose product solution of the domestic company and another glucose product solution of the foreign company, the difference of the service lives of the two solutions is large, the filter element used for filtering the product of the domestic company has a short service life and can only filter 12000L, the filter element used for filtering the product of the foreign company has a long service life and can filter 84000L, in addition, the color of the filter element becomes black after the filter element is filtered, the color of the filter element becomes yellow after the filter element is filtered, and a method capable of solving the filtering speed of the hydrous glucose is urgently needed for improving the product competitiveness.
Disclosure of Invention
The technical problem to be solved by the invention is to provide a production method of aqueous glucose, improve the traditional process for producing aqueous glucose products, and the process has low requirements on matched production equipment, can effectively improve the problem of filtration rate, improves the filtration rate, and meets the market requirements at home and abroad.
In order to solve the technical problems, the technical scheme of the invention is as follows:
a production method of water-containing glucose, in the production process of the water-containing glucose, the processing flow of starch milk → one-time spraying → column type liquefier is needed, and the subsequent treatment comprises the following steps:
s1 pre-filtering: in the starch milk liquefaction process, primarily separating flocculation protein generated after primary injection and liquefaction to obtain liquefied liquid with the protein content of less than 0.15%, and then saccharifying to obtain saccharified liquid;
s2 decolorization and filtration: blending the saccharified liquid with 40-55 wt% of centrifugal honey washing mother liquor, and decoloring and filtering to obtain dilute syrup;
s3, pH value adjustment: adjusting the pH value of the dilute syrup to 4.2-4.8;
s4 decolorization of dilute syrup: decoloring the dilute syrup after adjusting the pH by S3 by using powdered activated carbon;
s5 ion exchange: performing ion exchange on the diluted syrup decolorized by S4 to obtain refined syrup;
s6 low-temperature evaporation: evaporating the refined syrup under the condition of negative pressure and low temperature to obtain concentrated syrup;
s7 decolorization of concentrated syrup: adsorbing and filtering the concentrated syrup by adopting activated carbon, and decoloring;
s8 crystallization: crystallizing the concentrated syrup decolorized by S7 by using 25-35 wt% of crystallized massecuite as wet seed crystal;
s9 centrifugation: crystallizing the concentrated syrup by S8 to obtain massecuite, centrifuging, and adding an air filter in a centrifugal purification room for air collection;
s10, drying: and (4) drying the massecuite after centrifugation in the S9, adding an air filter at a wind collecting position of a clean room, and drying to obtain a finished product of the water-containing glucose.
As a preferred embodiment, the filtration in S2 is performed by a plate filter press.
In a preferred embodiment, the powdered activated carbon in S4 is 303 type powdered activated carbon, and the addition amount is 1.8-2.5 kg/TDS, and the decoloring time is 30 min.
In a preferred embodiment, the ion exchange process in S5 is carried out by using two pairs of cation and anion exchange resin beds in series.
In a preferred embodiment, a polypropylene filter is added after ion exchange, and filtration is carried out; two polypropylene filters are additionally arranged, namely a 0.45 micron pore size polypropylene filter and a 0.22 micron pore size polypropylene filter.
In a preferred embodiment, the negative pressure in S6 is-0.1 MPa, and the temperature is 75-85 ℃.
In a preferred embodiment, the activated carbon in S7 is coconut shell particle activated carbon column.
In a preferred embodiment, the decolorization in S7 is performed at 78-83 ℃ for 15min, and a 0.22 μm pore size polypropylene filter is disposed after the decolorization for filtration.
In a preferred embodiment, the air filters in S9 and S10 are primary, secondary, tertiary and quaternary sub-high efficiency filters.
By adopting the technical scheme, insoluble protein and soluble protein in the starch milk are removed, so that the composite reaction in the saccharification process and various reactions in a high-temperature environment are reduced, and the subsequent filtration pressure is effectively reduced; the quality of the materials after refining procedures at all levels can be effectively ensured by the filters at all levels; granular active carbon is used for decoloring the concentrated syrup before crystallization, so that active carbon omission is effectively avoided; the air intake is additionally provided with the filters at all stages, so that the phenomenon that impurities in the air are sucked into a centrifuge to pollute wet sugar due to pressure difference in the centrifugal process and the phenomenon that the impurities in the air are mixed with the product to influence the product quality in the drying process are avoided; on the whole, the filtering speed of the aqueous glucose is effectively improved, compared with the filtering speed of the aqueous glucose without the method, the filtering speed is obviously improved under the same condition, and the treatment capacity is improved by more than 6 times.
Detailed Description
The following further describes the embodiments of the present invention. It should be noted that the description of the embodiments is provided to help understanding of the present invention, but the present invention is not limited thereto. In addition, the technical features involved in the embodiments of the present invention described below may be combined with each other as long as they do not conflict with each other.
The present invention is further described to enable those skilled in the art to better practice the invention.
The existing production process flow of the aqueous glucose comprises the following steps: starch milk → primary injection (105-110 ℃) → column type liquefier → secondary injection (135-145 ℃) → column type liquefier (laminar flow tube) → saccharification → protein deslagging and filtering → decolorization → ion exchange → evaporation → concentrated syrup decolorization → pre-crystallization → crystallization (horizontal crystallizer) → centrifugation → drying → packaging → finished product.
The invention relates to a production method of water-containing glucose, which comprises the following steps of starch milk → primary spray → column type liquefier in the production process of the water-containing glucose:
a production method of water-containing glucose, in the production process of the water-containing glucose, the processing flow of starch milk → one-time spraying → column type liquefier is needed, and the subsequent treatment comprises the following steps:
s1 pre-filtering: in the starch milk liquefaction process, primarily separating flocculation protein generated after primary injection and liquefaction to obtain liquefied liquid with the protein content of less than 0.15%, and then saccharifying to obtain saccharified liquid; a flocculation protein separation device in starch sugar production is adopted in the separation process;
s2 decolorization and filtration: blending saccharified liquid with 40-55 wt% of centrifugal honey washing mother liquor, decoloring and filtering to obtain dilute syrup; because most of protein is removed in the previous process, the filtration efficiency is improved, and a plate type filter press is adopted for filtration;
s3, pH value adjustment: adjusting the pH value of the dilute syrup to 4.2-4.8, and separating out a small amount of soluble protein at the isoelectric point;
s4 decolorization of dilute syrup: the dilute syrup after the pH is adjusted by S3 is decolorized by powdered activated carbon, insoluble impurities, colored substances, precipitated soluble protein and the like are removed; the powdered activated carbon is 303 type powdered activated carbon, the addition amount is 1.8-2.5 kg/TDS, and the decoloring time is 30 min.
S5 ion exchange: ion exchange is carried out on the diluted syrup decolorized by S4 to obtain refined syrup;
the ion exchange adopts two pairs of cation and anion exchange resin beds which are connected in series for use, and the ion exchange process is carried out;
adding a polypropylene filter after ion exchange, and filtering; two polypropylene filters are additionally arranged, namely a 0.45 micron pore size polypropylene filter and a 0.22 micron pore size polypropylene filter.
S6 low-temperature evaporation: evaporating the refined syrup under the condition of negative pressure and low temperature to obtain concentrated syrup; the negative pressure low temperature evaporation reduces the Maillard reaction and the caramelization reaction; the negative pressure is-0.1 MPa, and the temperature is 75-85 ℃.
S7 decolorization of concentrated syrup: adsorbing and filtering the concentrated syrup by adopting active carbon, and decoloring; removing impurities, colored substances and pyrogen in sugar solution generated in the evaporation process by adopting activated carbon adsorption; the active carbon adopts coconut shell particle active carbon columns;
decoloring for 15min at 78-83 deg.C, and filtering with 0.22 μm polypropylene filter.
S8 crystallization: crystallizing the concentrated syrup decolorized by S7 by using 25-35 wt% of crystallized massecuite as wet seed crystal; a pre-crystallization tower which is commonly used in the traditional process is omitted, and the quality of the seed crystal is ensured;
s9 centrifugation: crystallizing the concentrated syrup by S8 to obtain massecuite, centrifuging, and air-collecting in a centrifugal purification room and adding an air filter; respectively recycling the centrifugal honey separation sugar solution and the honey washing sugar solution;
s10, drying: and (4) drying the massecuite centrifuged by the S9, adding an air filter at a wind collecting position of a clean room, and drying to obtain a finished product of the water-containing glucose.
The air filters in S9 and S10 are primary-effect, secondary-effect, tertiary-effect and quaternary-sub-high-efficiency filters.
Example one
Filtering a normally produced saccharification liquid by using diatomite, adding 55% of washing honey mother liquor, adjusting pH, decoloring by using 303 type powdered activated carbon at 68 ℃, performing series connection treatment by using a group of cation and anion column ion exchange columns and a precision filter thereof, evaporating at 75 ℃ and 0.1MPa, performing circulating filtration by using a granular activated carbon adsorption column for 20min, feeding the obtained product into a crystallization tank containing 30% of wet seed crystals, keeping the temperature at 45 ℃ for 8h, cooling to 25 ℃ within 50h, centrifuging and drying in a purification room with qualified wind collection, dissolving a dried finished product to prepare 35% by weight of sugar liquid, filtering by using a 0.22 mu m cellulose ester mixed membrane at 20 ℃ and 0.1MPa, recording the filtration time once per 100m L volume of filtration, filtering at a filtration speed of 2.84m L/s after 2000ml, slightly yellowing the filter membrane, filtering by using a precision filter after 18h of ion exchange, and intercepting substances containing a small amount of quartz sand and resin, containing a large amount of white floccule, and detecting the content of fat protein of 3.96% and 3.25% of 3.25%.
Example two
Filtering a normally produced saccharification liquid by using diatomite, adding 55% of washing honey mother liquor, adjusting pH, decoloring by using 303 type powdered activated carbon at 68 ℃, performing series connection treatment by using a group of cation and anion column ion exchange columns and a precision filter thereof, evaporating at 80 ℃ and 0.1MPa, performing circulating filtration by using a granular activated carbon adsorption column for 20min, feeding the obtained product into a crystallization tank containing 30% of wet seed crystals, keeping the temperature for 8h at 45 ℃, cooling to 25 ℃ within 50h, centrifuging and drying in a purification room with qualified wind collection, dissolving a dried finished product to prepare 35% by weight of sugar liquid, filtering by using a 0.22 mu m mixed cellulose ester membrane at 20 ℃ and 0.1MPa, recording the filtration time once per 100m L volume of filtration, filtering at a filtration speed of 2.56m L/s after 2000ml, slightly yellowing a filter membrane, filtering by using a precision filter after 18h after ion exchange, and blocking the filtration of substances, which contain a small amount of quartz sand and resin, contain a large amount of flocculent content of 34.29%, 34.26% of fat protein and 3.26% of 27.15% by detection.
EXAMPLE III
Filtering a normally produced saccharification liquid by using diatomite, adding 55% of washing honey mother liquor, adjusting pH, decoloring by using 303 type powdered activated carbon at 68 ℃, performing series connection treatment by using a group of cation and anion column ion exchange columns and a precision filter thereof, evaporating at 85 ℃ and 0.1MPa, performing circulating filtration by using a granular activated carbon adsorption column for 20min, feeding the obtained product into a crystallization tank containing 30% of wet seed crystals, keeping the temperature at 45 ℃ for 8h, cooling to 25 ℃ within 50h, centrifuging and drying in a purification room with qualified wind collection, dissolving a dried finished product to prepare 35% by weight of sugar liquid, filtering by using a 0.22 mu m cellulose ester mixed membrane at 20 ℃ and 0.1MPa, recording the filtration time once per 100m L volume of filtration, filtering at a filtration speed of 1.98m L/s after 2000ml, slightly yellowing the filter membrane, filtering by using a precision filter after 18h of ion exchange, and intercepting a small amount of quartz sand and resin in substances containing a large amount of white floccule, and detecting the content of fat protein of 35.96%, 89.26% and 89.85%.
Example four
Adding 55% of honey washing mother liquor into a saccharified liquid after protein spraying, adjusting the pH value to 4.8, decoloring by using 303 type powdered activated carbon at the temperature of 68 ℃, performing series treatment by two groups of positive and negative column ion exchange columns and a precision filter thereof, evaporating at 75 ℃ and 0.1MPa, performing circulating filtration for 20min by using a granular activated carbon adsorption column, putting into a crystallization tank containing 30% of wet seed crystals, keeping the temperature for 8h at 45 ℃, cooling to 25 ℃ within 50h, centrifuging and drying in a purification room qualified by wind collection, dissolving a dried finished product to prepare 35% by weight of sugar liquid, filtering by using a 0.22 mu m mixed cellulose ester membrane at the temperature of 20 ℃ and 0.1MPa, recording the filtration time once per 100m L volume of filtration, after 2000ml, the filtration speed is 4.56m L/s, slightly yellowing the filter membrane, operating the precision filter for more than 48h after ion exchange, and obviously reducing white floccules.
EXAMPLE five
Filtering the saccharified liquid after being sprayed and deproteinized by diatomite, adding 55% of honey washing mother liquor, adjusting the pH to 4.8, decoloring by 303 type powdered activated carbon at 68 ℃, performing serial treatment by two groups of cation and anion exchange columns and a precision filter thereof, evaporating at 80 ℃ and under 0.1MPa, performing circulating filtration by a granular activated carbon adsorption column for 20min, entering a crystallization tank containing 30% of wet seed crystals, keeping the temperature for 8h at 45 ℃, cooling to 25 ℃ within 50h, centrifuging and drying in a ventilation qualified purification room, dissolving a dried finished product to prepare 35% by weight of sugar liquid, filtering by a 0.22 mu m mixed cellulose ester membrane at 20 ℃ and under 0.1MPa, recording the filtration time once per 100m L volume of filtration, after 2000ml, the filtration speed is 4.61m L/s, slightly yellowing the filter membrane, operating the precision filter for more than 48h after ion exchange, and obviously reducing white floccules.
EXAMPLE six
Adding 55% of honey washing mother liquor into the saccharified liquid after being sprayed for protein removal, adjusting the pH value to 4.8, decoloring by using 303 type powdered activated carbon at the temperature of 68 ℃, performing serial treatment by two groups of positive and negative column ion exchange columns and a precision filter thereof, evaporating at 85 ℃ and 0.1MPa, performing circulating filtration for 20min by using a particle activated carbon adsorption column, putting into a crystallization tank containing 30% of wet seed crystals, keeping the temperature for 8h at 45 ℃, cooling to 25 ℃ within 50h, centrifuging and drying in a purification room qualified by wind collection, dissolving a dried finished product to prepare 35% by weight of sugar liquid, filtering by using a 0.22 mu m mixed cellulose ester membrane at the temperature of 20 ℃ and 0.1MPa, recording the filtration time once per 100m L volume of filtration, after 2000ml, the filtration speed is 4.12m L/s, slightly yellowing the filter membrane, operating the precision filter for more than 48h after ion exchange, and obviously reducing white floccules.
EXAMPLE seven
Adding the saccharified solution after being sprayed with the protein into 55 percent of honey washing mother solution, adjusting the pH value to 4.8, decoloring by using 303 type powdered activated carbon at the temperature of 68 ℃, performing series treatment by using a group of cation and anion exchange columns and a precision filter thereof, filtering by using a 0.22 mu m organic nylon membrane at the temperature of 20 ℃ and under the pressure of-0.1 MPa, recording the filtering time once for each filtering volume of 100m L, filtering 2000m L, and then, the filtering speed is 4.24m L/s, and the effective filtering area of the filter membrane is yellow.
Example eight
Adding the saccharified solution after being sprayed with the protein into 55 percent of honey washing mother solution, adjusting the pH value to 4.8, decoloring by using 303 type powdered activated carbon at the temperature of 68 ℃, performing serial treatment by two groups of cation and anion exchange columns and a precision filter thereof, filtering by using a 0.22 mu m organic nylon membrane at the temperature of 20 ℃ and under the pressure of-0.1 MPa, recording the filtering time once for each filtering volume of 100m L, filtering 2000m L, and then, the filtering speed is 4.68m L/s, and the effective filtering area of the filter membrane has slight color change.
Example nine:
adding 55% of honey washing mother liquor into the saccharified liquid which is subjected to protein removal after being sprayed, adjusting the pH value to 4.8, decoloring by using 303 type powdered activated carbon at the temperature of 68 ℃, performing series treatment by two groups of cation and anion exchange columns and a precision filter thereof, evaporating at 80 ℃ and 0.1MPa, decoloring by 767 type needle powder activated carbon for 20min, putting into a crystallization tank with 30% of wet seed crystals, keeping the temperature for 8h at 45 ℃, cooling to 25 ℃ within 50h, centrifuging and drying in a qualified wind collection purification room, dissolving a dried finished product to prepare 35% by weight of sugar solution, filtering by using a 0.22 mu m mixed cellulose ester membrane at the temperature of 20 ℃ and 0.1MPa, recording the filtering time once per 100m L volume of filtering, after 2000ml, the filtering speed is 4.15m L/s, and the effective filtering area of the filtering membrane is black and the activated carbon is left out.
Example ten
Adding 55% of honey washing mother liquor into the saccharified liquid which is subjected to protein removal after being sprayed, adjusting the pH value to 4.8, decoloring by using 303 type powdered activated carbon at the temperature of 68 ℃, performing series treatment by two groups of cation and anion exchange columns and a precision filter thereof, evaporating at 80 ℃ and 0.1MPa, performing circulating filtration for 20min by using a granular activated carbon adsorption column, feeding into a crystallization tank containing 30% of wet seed crystals, preserving the temperature for 8h at 45 ℃, cooling to 25 ℃ within 50h, centrifuging and drying in a space without a filter in wind collection, dissolving a dried finished product to prepare 35% by weight of sugar solution, filtering by using a 0.22 mu m mixed cellulose ester membrane at the temperature of 20 ℃ and 0.1MPa, recording the filtration time once per 100m L volume of filtration, filtering at the speed of 3.89m L/s after 2000ml, and slightly graying the filter membrane.
The method and the device of the embodiment are utilized to separate out protein in the primary injection liquefied liquid, 55 percent of washing honey mother liquid is recycled after saccharification, the pH value is adjusted to 4.8 to the isoelectric point of the protein, 303 type powdered activated carbon is utilized for decolorization, two groups of cation and anion exchange columns are used for serially connecting to process sugar liquid, concentrated syrup obtained after evaporation concentration under the conditions of-0.1 MPa and 75 ℃ is filtered by a granular activated carbon adsorption column, 30 percent of weight wet seed crystal is adopted for crystal growth for 8h and is cooled to 25 ℃ within 50h, centrifugation and drying are carried out in the environment of a primary effect, secondary medium effect, tertiary medium effect and four-level sub-high efficiency filter is additionally arranged at the wind production place, the obtained finished product is filtered by a 0.22 mu m mixed cellulose ester membrane, and the filtering speed is improved by 5-6 times compared with the filtering speed of the finished product obtained without the above-mentioned treatment.
The embodiments of the present invention have been described in detail, but the present invention is not limited to the described embodiments. It will be apparent to those skilled in the art that various changes, modifications, substitutions and alterations can be made in these embodiments without departing from the principles and spirit of the invention, and the scope of protection is still within the scope of the invention.
Claims (9)
1. A production method of water-containing glucose is characterized in that in the production process of the water-containing glucose, the processing flow of starch milk → one-time spraying → a column type liquefier is needed, and the subsequent treatment comprises the following steps:
s1 pre-filtering: in the starch milk liquefaction process, primarily separating flocculation protein generated after primary injection and liquefaction to obtain liquefied liquid with the protein content of less than 0.15%, and then saccharifying to obtain saccharified liquid;
s2 decolorization and filtration: blending the saccharified liquid with 40-55 wt% of centrifugal honey washing mother liquor, and decoloring and filtering to obtain dilute syrup;
s3, pH value adjustment: adjusting the pH value of the dilute syrup to 4.2-4.8;
s4 decolorization of dilute syrup: decoloring the dilute syrup after adjusting the pH by S3 by using powdered activated carbon;
s5 ion exchange: performing ion exchange on the diluted syrup decolorized by S4 to obtain refined syrup;
s6 low-temperature evaporation: evaporating the refined syrup under the condition of negative pressure and low temperature to obtain concentrated syrup;
s7 decolorization of concentrated syrup: adsorbing and filtering the concentrated syrup by adopting activated carbon, and decoloring;
s8 crystallization: crystallizing the concentrated syrup decolorized by S7 by using 25-35 wt% of crystallized massecuite as wet seed crystal;
s9 centrifugation: crystallizing the concentrated syrup by S8 to obtain massecuite, centrifuging, and adding an air filter in a centrifugal purification room for air collection;
s10, drying: and (4) drying the massecuite after centrifugation in the S9, adding an air filter at a wind collecting position of a clean room, and drying to obtain a finished product of the water-containing glucose.
2. The method for producing aqueous glucose according to claim 1, characterized in that: the filtration in S2 was carried out using a plate filter press.
3. The method for producing aqueous glucose according to claim 1, characterized in that: the powdered activated carbon in S4 is 303 type powdered activated carbon, the addition amount is 1.8-2.5 kg/TDS, and the decoloring time is 30 min.
4. The method for producing aqueous glucose according to claim 1, characterized in that: the ion exchange in S5 adopts two pairs of cation and anion exchange resin beds which are connected in series for use to carry out the ion exchange process.
5. The method for producing aqueous glucose according to claim 4, characterized in that: adding a polypropylene filter after ion exchange, and filtering; two polypropylene filters are additionally arranged, namely a 0.45 micron pore size polypropylene filter and a 0.22 micron pore size polypropylene filter.
6. The method for producing aqueous glucose according to claim 1, characterized in that: in S6, the negative pressure is-0.1 MPa, and the temperature is 75-85 ℃.
7. The method for producing aqueous glucose according to claim 1, characterized in that: the activated carbon in S7 is coconut shell particle activated carbon column.
8. The method for producing aqueous glucose according to claim 1, characterized in that: and (3) decolorizing for 15min at the temperature of 78-83 ℃ in S7, and filtering by arranging a 0.22 micron pore size polypropylene filter after decolorizing.
9. The method for producing aqueous glucose according to claim 1, characterized in that: the air filters in the S9 and S10 are primary-stage primary-effect, secondary-stage intermediate-effect, tertiary-stage intermediate-effect and quaternary-stage sub-high-efficiency filters.
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|---|---|---|---|---|
| CN101787385A (en) * | 2010-03-10 | 2010-07-28 | 中南林业科技大学 | Preparation method for medical glucose with ultrahigh purity |
| CN102703547A (en) * | 2012-06-14 | 2012-10-03 | 万福生科(湖南)农业开发股份有限公司 | Method for producing glucose bulk drug for injection by using rice |
| CN103060402A (en) * | 2013-01-07 | 2013-04-24 | 安徽友勇生物科技有限公司 | Production method of starch syrup |
| CN103725731A (en) * | 2013-12-30 | 2014-04-16 | 河南飞天农业开发股份有限公司 | Crystalline dextrose special for sodium gluconate and preparation method of crystalline dextrose |
| CN110835657A (en) * | 2019-11-15 | 2020-02-25 | 河南飞天农业开发股份有限公司 | Production process of low-oligosaccharide edible glucose |
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Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101787385A (en) * | 2010-03-10 | 2010-07-28 | 中南林业科技大学 | Preparation method for medical glucose with ultrahigh purity |
| CN102703547A (en) * | 2012-06-14 | 2012-10-03 | 万福生科(湖南)农业开发股份有限公司 | Method for producing glucose bulk drug for injection by using rice |
| CN103060402A (en) * | 2013-01-07 | 2013-04-24 | 安徽友勇生物科技有限公司 | Production method of starch syrup |
| CN103725731A (en) * | 2013-12-30 | 2014-04-16 | 河南飞天农业开发股份有限公司 | Crystalline dextrose special for sodium gluconate and preparation method of crystalline dextrose |
| CN110835657A (en) * | 2019-11-15 | 2020-02-25 | 河南飞天农业开发股份有限公司 | Production process of low-oligosaccharide edible glucose |
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