CN102643885A - Starch sugar and method for recovering protein in derivative production process thereof - Google Patents
Starch sugar and method for recovering protein in derivative production process thereof Download PDFInfo
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- CN102643885A CN102643885A CN2012100955206A CN201210095520A CN102643885A CN 102643885 A CN102643885 A CN 102643885A CN 2012100955206 A CN2012100955206 A CN 2012100955206A CN 201210095520 A CN201210095520 A CN 201210095520A CN 102643885 A CN102643885 A CN 102643885A
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- albumen
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Abstract
The invention relates to starch sugar and a method for recovering protein in a derivative production process thereof. The method adopts the following steps of: (1) slurrying starch, (2) recovering cluster protein through a protein recovery device, (3) recovering protein through an ultrafiltration membrane, and (4) filter-pressing protein concentrated solution through a plate-and-frame filter press to recover protein. According to the method, the recovery rate of the protein is high, the quality of sugar liquor after protein recovery process is good, the burden of subsequent decoloration and desalinization sections is reduced, especially the hybridization operation time is prolonged, the produced hybridization waste water is less, the degree of automation is high, the labor intensity is reduced, the industrial production is easy to realize, the production efficiency is improved, and the service life of membrane equipment can be prolonged.
Description
Technical field
The present invention relates to the proteic method of a kind of recovery, be specifically related to reclaim in Dian Fentang and the verivate production process thereof proteic method.
Background technology
Now, the Dian Fentang industry has become one of relatively popular industry of China, the transformation of Along with people's consumption idea and the raising of the level of consumption, and the raising that importance of health is familiar with, and the demand of Dian Fentang increases day by day.
In order to improve the comprehensive utilization ratio of raw material, reduce the grain consumption, improve the dry recovery, the comprehensive utilization of waste vapour, waste water makes Dian Fentang and derivatives industry production model thereof meet the environmental requirement of low-carbon (LC), green more.Lot of domestic and international producer begins to pay attention to the comprehensive utilization of starch, reclaims the albumen in the starch complete processing one after another, in the hope of obtaining big profit, improves the competitive capacity of enterprise.
But be limited to state of the art, most of producers adopt the albumen in the filter press technology for recovery liquid glucose, and protein recovery is low, and the liquid glucose that reclaims behind the albumen is of poor quality, have increased the weight of the burden of back road workshop section.Also there is minority producer to adopt film device to reclaim albumen, though albumen reclaims back liquid glucose quality height; Because albumen does not pass through the pre-treatment of box albumen removal device in the liquefier; The enrichment factor of film device reduces greatly, causes the film device inefficiency, and; Too much albumen can cause the film core to stop up, and reduces the work-ing life of membrane cartridge; Also have only a few producer to adopt filter press to cooperate film device to carry out albumen recovery in the Dian Fentang production process; Back liquid glucose quality is good, protein recovery is high though albumen reclaims,, its facility investment is big; Floor space is big, and labor strength is big, the shopwork environment is poor.
Summary of the invention
The present invention provides and reclaims proteic method in a kind of Dian Fentang and the verivate production process thereof in order to overcome the deficiency of above technology.It may further comprise the steps: the liquefaction of (1) starch slurry: in starch slurry, add glycase, utilize Jet liquefier to liquefy, liquefying-point is 100 ℃-140 ℃, gets liquefied starch; (2) the albumen retrieving arrangement reclaims bulk albumen: said liquefied starch is reclaimed bulk albumen with box albumen retrieving arrangement, get coarse filtration liquid; (3) ultra-filtration membrane reclaims albumen: with said coarse filtration liquid, be cooled to 20-80 ℃, use ultrafiltration membrance filter, obtain protein concentrated solution; (4) plate-and-frame filter press press filtration protein concentrated solution reclaims albumen, filtrating repeating step (3).This method protein recovery liquid glucose quality high, that reclaim after albumen is handled is good, reduces the burden of follow-up decolouring, desalination workshop section; Particularly prolong from shipping line time, the ion exchange wastewater of generation is few; Level of automation is high, reduces labour intensity, is easy to realize suitability for industrialized production; Enhance productivity, can prolong film device work-ing life.
According to embodiments of the invention, the starch slurry among the present invention can add the water allotment by starch material and form, and transfers pH 5.8-6.2.
According to concrete examples more of the present invention, the starch material among the present invention can comprise purified starch, thick starch and starch-containing material, and wherein starch-containing material comprises W-Gum, wheat starch, tapioca(flour), sweet potato starch, sweet potato starch.
According to embodiments of the invention, the glycase among the present invention is high temperature resistant AMS.
According to embodiments of the invention, the weight ratio of starch content is 0.2-0.3g/Kg in glycase among the present invention and the starch slurry.
According to embodiments of the invention, the box albumen retrieving arrangement compass screen surface precision among the present invention is 0.5mm-1mm.Wherein box retrieving arrangement is incorporated it into this paper referring to the box retrieving arrangement described in the CN201120352456.6 through reference in full.
According to embodiments of the invention, the molecular retention amount of the ultra-filtration membrane among the present invention is 1-20 ten thousand.
According to concrete examples more of the present invention, the ultra-filtration membrane among the present invention comprises inorganic ceramic tubular membrane, organic rolled film and organic tubular membrane.
According to embodiments of the invention, albumen is reclaimed in the plate-and-frame filter press press filtration among the present invention, and temperature is 20, and pressure is 18-22MPa, filtrating repeating step (3).
Albumen recovery technology of the present invention and filter press reclaim the albumen compared with techniques, have the protein recovery height, to reclaim back liquid glucose quality good, advantage such as alleviate follow-up decolouring, desalination workshop section burden, labor strength is little, the Workshop Production environment is good; Reclaim the albumen compared with techniques with independent employing film device, it is big to have the film device enrichment factor, and production efficiency is high, advantages such as film device long service life; With cooperate film device to reclaim the albumen compared with techniques with filter press separately, compact equipment, advantage such as floor space is little, labor strength is little, and the shopwork environment is good.
Embodiment:
To do further describing below through embodiment to the present invention, the description of these embodiment is not that content of the present invention is done qualification.One skilled in the art will understand that to be equal to replacement to what content of the present invention was done, or corresponding the improvement, still belong within protection scope of the present invention.
Embodiment
Instance 1
(preparation malto-oligosaccharide)
(1) starch slurry liquefaction:
A) size mixing: earlier a certain amount of water is pumped in the jar of sizing mixing, start jar stirring of sizing mixing, progressively add starch, with the milk of starch of 15-22 ° of B ' e of starch furnishing, after stirring, utilizing 5%HCl solution and 5%NaOH solution to regulate pH is 5.8.
B) liquefaction: the starch slurry that will size mixing pumps into the preceding storage tank temporarily of liquefaction; Weight ratio by starch content in glycase and the starch slurry is that 0.25g/Kg adds high temperature resistant AMS; Stir, pump into intelligent HP steam Jet liquefier (million photo bio Engineering Co., Ltd make, model HYZ-7) and liquefy; Liquefying-point is 100 ℃, obtains the albumen liquefier preferably that flocculates.
(2) the albumen retrieving arrangement reclaims bulk albumen: step (1) gained liquefier is pumped into box albumen retrieving arrangement, filter bulk albumen, albumen retrieving arrangement compass screen surface precision is 0.5mm-1mm, gets coarse filtration liquid.According to material Tot Prot and recovery back Tot Prot rough calculation, protein recovery reaches 98%, handles back coarse filtration liquid and does not have naked eyes visible particle shape albumen.
(3) ultra-filtration membrane reclaims albumen: the coarse filtration liquid of gained in the step (2) is cooled to 58 ℃, pumps into ultrafiltration apparatus, film pressure at both sides difference is 0.4MPa; Ultra-filtration membrane molecular retention amount is 1-20 ten thousand, and ultrafiltration membrance filter liquid detects transmittance under the 440nm wavelength, can reach 98.3%; When being concentrated into 50 times, stop to filter, protein concentrated solution is got into the filter press operation.
(4) plate-and-frame filter press press filtration protein concentrated solution: gained protein concentrated solution in the step (3) is pumped into plate-and-frame filter press carry out press filtration; The press filtration temperature is 58 ℃, and pressure is 18-22MPa, after press filtration finishes; The sheet frame discharging; Reclaim the albumen filter cake, pressing filtering liquid returns step (3) and carries out ultrafiltration membrance filter, liquid glucose system Dian Fentang and verivate thereof after the filtration.
(5) malto-oligosaccharide is refining: the liquid glucose behind the ultrafiltration membrance filter is refining through IX, and the preparation malto-oligosaccharide.
Instance 2
(preparation oligomeric isomaltose)
(1) starch-liquefying:
A) size mixing: earlier a certain amount of water is pumped in the jar of sizing mixing, start jar stirring of sizing mixing, progressively add W-Gum, with the milk of starch of 15-22 ° of B ' e of W-Gum furnishing, after stirring, utilizing HCl and NaOH to regulate pH is 5.7.
B) liquefaction: the starch slurry that will size mixing pumps into the preceding storage tank temporarily of liquefaction; Weight ratio by starch content in glycase and the starch slurry is that 0.23g/Kg adds high temperature resistant AMS; Stir; Pump into Jet liquefier and liquefy, liquefying-point is 140 ℃, obtains the albumen liquefier preferably that flocculates.
(2) the albumen retrieving arrangement reclaims bulk albumen: step (1) gained liquefier is pumped into box albumen retrieving arrangement, filter bulk albumen, albumen retrieving arrangement compass screen surface precision is 0.5mm-1mm, gets coarse filtration liquid.According to material Tot Prot and recovery back Tot Prot rough calculation, protein recovery reaches 98.5%, handles back coarse filtration liquid and does not have naked eyes visible particle shape albumen.
(3) ultra-filtration membrane reclaims albumen: the coarse filtration liquid of gained in the step (2) is cooled to 65 ℃, pumps into ultrafiltration apparatus, film pressure at both sides difference is 0.4MPa; Ultra-filtration membrane molecular retention amount is 1-20 ten thousand; Ultrafiltration membrance filter liquid detects transmittance under the 440nm wavelength, can reach 98%, when being concentrated into 50 times; Stop to filter, protein concentrated solution is got into the filter press operation.
(4) plate-and-frame filter press press filtration protein concentrated solution: gained protein concentrated solution in the step (3) is pumped into plate-and-frame filter press carry out press filtration; The press filtration temperature is 65 ℃, and pressure is 18-22MPa, after press filtration finishes; The sheet frame discharging; Reclaim the albumen filter cake, pressing filtering liquid returns step (3) and carries out ultrafiltration membrance filter, liquid glucose system Dian Fentang and verivate thereof after the filtration.
(5) preparation oligomeric isomaltose: the liquid glucose behind the ultrafiltration membrance filter is added zymin transform the preparation oligomeric isomaltose.
Instance 3
(preparation sorbyl alcohol)
(1) starch-liquefying:
A) size mixing: earlier a certain amount of water is pumped in the jar of sizing mixing, start jar stirring of sizing mixing, progressively add the corn grain decortication, take off the Semen Maydis powder of directly pulverizing behind the embryo, with 15-17 ° of B ' e of Semen Maydis powder furnishing, after stirring, utilizing HCl and NaOH to regulate pH is 5.8.
B) liquefaction: the slurry that will size mixing pumps into the preceding storage tank temporarily of liquefaction; Weight ratio by dry powder content in glycase and the powder slurry is that 0.25g/Kg adds high temperature resistant AMS, stirs, and pumps into Jet liquefier and liquefies; Liquefying-point is 128 ℃, obtains the albumen liquefier preferably that flocculates.
(3) ultra-filtration membrane reclaims albumen: the coarse filtration liquid of gained in the step (2) is cooled to 80 ℃, pumps into ultrafiltration apparatus, film pressure at both sides difference is 0.4MPa; Ultra-filtration membrane molecular retention amount is 1-20 ten thousand; Ultrafiltration membrance filter liquid detects transmittance under the 440nm wavelength, can reach 97.5%, when being concentrated into 50 times; Stop to filter, protein concentrated solution is got into the filter press operation.
(4) plate-and-frame filter press press filtration protein concentrated solution: gained protein concentrated solution in the step (3) is pumped into plate-and-frame filter press carry out press filtration; The press filtration temperature is 80 ℃, and pressure is 18-22MPa, after press filtration finishes; The sheet frame discharging; Reclaim the albumen filter cake, pressing filtering liquid returns step (3) and repeats ultrafiltration membrance filter, liquid glucose system Dian Fentang and verivate thereof after the filtration.
(5) sorbyl alcohol preparation: the liquid glucose behind the ultrafiltration membrance filter is added zymin transform preparation glucose, generate sorbyl alcohol through the purification back end hydrogenation.
Claims (9)
1. reclaim proteic method in Dian Fentang and the verivate production process thereof, it is characterized in that may further comprise the steps:
(1) starch slurry liquefaction: in starch slurry, add glycase, utilize Jet liquefier to liquefy, liquefying-point is 100 ℃-140 ℃, gets liquefied starch,
(2) the albumen retrieving arrangement reclaims bulk albumen: said starch fluid is reclaimed bulk albumen with box albumen retrieving arrangement, get coarse filtration liquid,
(3) ultra-filtration membrane reclaims albumen: with said coarse filtration liquid, be cooled to 20-80 ℃, use ultrafiltration membrance filter, concentrate 50 times after, stop filtration, obtain protein concentrated solution,
(4) plate-and-frame filter press press filtration protein concentrated solution: the protein concentrated solution that utilizes plate-and-frame filter press that ultrafiltration membrance filter is obtained carries out press filtration and reclaims albumen, filtrating repeating step (3).
2. the proteic method of recovery according to claim 1 is characterized in that: the middle starch slurry of said step (1) adds the water allotment by starch material and forms, and transfers pH 5.8-6.2.
3. the proteic method of recovery according to claim 2 is characterized in that: said starch material comprises purified starch, thick starch and starch-containing comminuting matter.
4. the proteic method of recovery according to claim 1 is characterized in that: glycase is high temperature resistant AMS in the said step (1).
5. according to the proteic method of the arbitrary described recovery of claim 1-3, it is characterized in that: the weight ratio of starch content is 0.2-0.3g/Kg in middle glycase of said step (1) and the starch slurry.
6. according to the proteic method of the recovery described in the claim 1, it is characterized in that: the box albumen retrieving arrangement compass screen surface precision that adopts in the described step (2) is 0.5mm-1mm.
7. according to the proteic method of the recovery described in the claim 1, it is characterized in that: the molecular retention amount of ultra-filtration membrane is 1-20 ten thousand in the said step (3).
8. according to the albumen recovery method described in the claim 1, it is characterized in that: the ultra-filtration membrane in the described step (3) comprises inorganic ceramic tubular membrane, organic rolled film and organic tubular membrane.
9. according to the albumen recovery method described in the claim 1, it is characterized in that: in the described step (4)
The plate-and-frame filter press press filtration reclaim albumen, temperature is 20-80 ℃, pressure is 18-22MPa, filtrating repeating step (3).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
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| CN2012100955206A CN102643885A (en) | 2012-04-02 | 2012-04-02 | Starch sugar and method for recovering protein in derivative production process thereof |
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| CN2012100955206A CN102643885A (en) | 2012-04-02 | 2012-04-02 | Starch sugar and method for recovering protein in derivative production process thereof |
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| CN102643885A true CN102643885A (en) | 2012-08-22 |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109517861A (en) * | 2018-11-19 | 2019-03-26 | 山东盛泰生物科技有限公司 | Method for protein isolation and its separator in a kind of production of starch sugar |
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| US20020096473A1 (en) * | 2001-01-19 | 2002-07-25 | Ferro Larry S. | Potato wastewater treatment method |
| CN1618988A (en) * | 2004-10-12 | 2005-05-25 | 山东保龄宝生物技术有限公司 | Production technology of starch sugar |
| CN201250194Y (en) * | 2008-07-25 | 2009-06-03 | 甘肃省膜科学技术研究院 | Device for recovering protein in potato starch production waste water with membrane method |
| CN101701235A (en) * | 2009-12-10 | 2010-05-05 | 安徽农业大学 | Method for producing low DE value malt oligosaccharide syrup by potato starch |
| CN201586419U (en) * | 2009-12-31 | 2010-09-22 | 保龄宝生物股份有限公司 | Protein recovery plant in starch sugar production |
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2012
- 2012-04-02 CN CN2012100955206A patent/CN102643885A/en active Pending
Patent Citations (6)
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| US20020096473A1 (en) * | 2001-01-19 | 2002-07-25 | Ferro Larry S. | Potato wastewater treatment method |
| CN1618988A (en) * | 2004-10-12 | 2005-05-25 | 山东保龄宝生物技术有限公司 | Production technology of starch sugar |
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| CN101701235A (en) * | 2009-12-10 | 2010-05-05 | 安徽农业大学 | Method for producing low DE value malt oligosaccharide syrup by potato starch |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109517861A (en) * | 2018-11-19 | 2019-03-26 | 山东盛泰生物科技有限公司 | Method for protein isolation and its separator in a kind of production of starch sugar |
| CN109517861B (en) * | 2018-11-19 | 2021-05-04 | 山东盛泰生物科技有限公司 | Protein separation method and device in starch sugar production |
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Application publication date: 20120822 |