CN1615722A - Method for preparing soybean separate protein by ultra-filter film separation technology - Google Patents
Method for preparing soybean separate protein by ultra-filter film separation technology Download PDFInfo
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Abstract
The preparation process of separate soybean protein includes the following steps: low temperature defatting bean, the first leaching, separating protein liquid from bean dregs, the second leaching, separating protein liquid from bean dregs, deairing, acid depositing, filterig with ultrafiltering film to obtain concentrated liquid, water washing, neutralizing, sterilizing, spray drying and spraying phospholipid to obtain the separate soybean protein product.
Description
Affiliated technical field
The invention belongs to the soybean deep processing technology field, exactly is to utilize hyperfiltration technique to realize the preparation of soybean protein isolate.
Background technology
The extraction that present domestic production soybean protein isolate mainly utilizes horizontal spiral seperator or vertical butterfly sheet seperator to finish protein liquid and curdled milk separates, its weak point is that the separation accuracy of protein liquid and whey is not high enough, make yield of soy protein isolate be affected, protein content improves in the whey, has brought the difficulty of subsequent product purification and the environmental issue of sewage discharge simultaneously.In addition, the operation continuity of traditional seperator is undesirable, shuts down the cleaning frequency height, and might cause when stream time is long mixing up in the finished product has the burnt impurity of sticking with paste.
Ultrafiltration is the membrane separation technique that a kind of RECENT DEVELOPMENTS is got up, and uses to some extent in biochemistry industry is extracted.It has realized the separating substances of molecular level, separates to belong to physical process, does not have phase transformation, and materials quality is protected greatly, and the operation continuity is strong, the yield height, and material concentration can control arbitrarily in relative broad range.At present, the domestic production that does not utilize this technology to realize soybean protein isolate as yet, in view of the various advantages of hyperfiltration technique and in the applicability of soybean protein isolate industry, this preparation method will have development potentiality.
Summary of the invention
The objective of the invention is to overcome the weak point that exists in the soybean protein isolate technology, a kind of method of utilizing hyperfiltration technique to produce soybean protein isolate is provided.
In order to achieve the above object, the technical solution used in the present invention is:
(1) low temperature defatting bean
Get quantitative low temperature defatting bean and drop into batch extractor.
(2) once leach
Low temperature beans sheet is dissolved in 48 ℃ of-52 ℃ of water.At first 48 ℃-52 ℃ water is pressed ratio of water to material 20: 1-8: 1 adds in the batch extractor, with NaOH (NaOH, concentration is 10%-30%) the pH value of water and low temperature beans sheet is transferred to 6.8-9.0, at the uniform velocity stir, kept above process conditions 20-40 minute, and be and once leach protein liquid.
(3) protein liquid and bean dreg separation
Soluble protein, carbohydrate and salt are separated from leachate, separated with seperator, separating the back liquid phase is the protein liquid that once leaches, and solid phase is for once leaching bean dregs, and once leaching protein liquid concentration is 6%-20%.
(4) secondary leaches
To once leach bean dregs and be dissolved in the secondary batch extractor, between water temperature kept 48 ℃-52 ℃, ratio of water to material was 12: 1-5: 1, water is added in the batch extractor, the pH value keeps nature, does not manually adjust, and secondary leaches the leachate that maintenance was leached for secondary after 10-30 minute.
(5) secondary separation of bean dregs and protein liquid
Soluble protein, carbohydrate and salt are separated from leachate.Separating the back liquid phase is that secondary leaches protein liquid, and it is 6-20% that separation back secondary leaches protein liquid concentration.
(6) degassing
Once leach protein liquid and secondary after the separation and leach protein liquid and squeeze into degassing tank, add defoamer, addition be the 6-12 kilogram/hour.
(7) neutralization
Protein liquid enters neutralizing tank through pump, adds hydrochloric acid (HCl, concentration is 10%-30%) the pH value of protein liquid is transferred to 6.0-7.5.
(8) ultra-filtration and separation
Protein liquid after the neutralization enters the plate-type hyperfiltration membrane system through pump, and control system pressure is 5bar.Concentrating after the separation is protein concentrate liquid mutually, and its solid concentration is 15%-25%, and dilution is whey mutually, its centrefuge experiment sediment≤0.05ml/15ml.
(9) heat treatment
Protein concentrate liquid after separating is carried out sterilization, and sterilization temperature is 80 ℃-90 ℃, and material, is got to high-pressure pump by homogenizer and carried out spray-drying to homogenizer through pump.
(10) spray-drying, lecithin spraying
Adopt press atomization, heated-air drying, the high-pressure pump outlet pressure reaches more than the 500bar, drying tower material inlet amount be the 2-4 ton/hour, outlet temperature is 80 ℃-90 ℃, evaporated quantity of water be the 2-4 ton/hour, material is delivered to high-pressure pump through filter at the process homogenizer earlier and is sloughed moisture again in drying tower, be located at the interior nozzle of tower simultaneously to the material spraying lecithin, the lecithin quantity for spray is the 0.5%-2% of dry, nozzle exit pressure 300-400kg/cm
2, the tower outlet temperature is 80 ℃-90 ℃, dry powder forwards subsequent processing to through cooling.
(11) puddle and pack
Product after the spray-drying sprays phosphatide in fluid bed, after puddling device and puddling, pack.
Advantage of the present invention:
1, the present invention has improved local flavor, the color and luster of soybean protein isolate effectively, has improved solubility.Because of hyperfiltration technique is the separation process that utilizes pressure to realize for driving force, there is not heating, material properties there is not influence, so product quality obtains guarantee largely.
2, reduced preparation cost.Because ultrafiltration system has been realized the original position cleaning, has shortened downtime, will separate, wash, concentrate and finish simultaneously; reduced equipment investment; shortened the production cycle, water consumption is few in the production, and these inherent characteristicses have all determined this preparation method's cost relatively the end of than.
3, realized the operation continuity in the preparation process.Utilize seperator to separate in the traditional mode of production, shut down the cleaning frequency height, equipment is installed complicated, when stream time is long, cause sometimes mixing up in the product having and burntly stick with paste impurity, and the ultrafiltration apparatus contamination resistance is strong, can realize for a long time operation continuously.
4, main performance index
Thick protein (butt %) 〉=92
PH value 6.0-7.5
NSI(％) ≥91
Dispersion stabilization (%) 〉=90
Emulsion stability (%) 〉=90
Emulsifying capacity (ml/g) 〉=500
Dissolubility: gentle agitation, all dissolving
Dispersed: as not have caking, in water, disperse rapidly
The specific embodiment
Below embodiments of the invention are done and described in further detail
(1) low temperature defatting bean
Get quantitative low temperature defatting bean and drop into batch extractor.
(2) once leach
Low temperature beans sheet is dissolved in 48 ℃ of-52 ℃ of water.At first 48 ℃-52 ℃ water is pressed ratio of water to material 20: 1-8: 1 adds in the batch extractor, with NaOH (NaOH, concentration is 10%-30%) the pH value of water and low temperature beans sheet is transferred to 6.8-9.0, at the uniform velocity stir, kept above process conditions 20-40 minute, and be and once leach protein liquid.
(3) protein liquid and bean dreg separation
Soluble protein, carbohydrate and salt are separated from leachate, separated with seperator, separating the back liquid phase is the protein liquid that once leaches, and solid phase is for once leaching bean dregs, and once leaching protein liquid concentration is 6%-20%.
(4) secondary leaches
To once leach bean dregs and be dissolved in the secondary batch extractor, between water temperature kept 48 ℃-52 ℃, ratio of water to material was 12: 1-5: 1, water is added in the batch extractor, the pH value keeps nature, does not manually adjust, and secondary leaches the leachate that maintenance was leached for secondary after 10-30 minute.
(5) secondary separation of bean dregs and protein liquid
Soluble protein, carbohydrate and salt are separated from leachate.Separating the back liquid phase is that secondary leaches protein liquid, and it is 6-20% that separation back secondary leaches protein liquid concentration.
(6) degassing
Once leach protein liquid and secondary after the separation and leach protein liquid and squeeze into degassing tank, add defoamer, addition be the 6-12 kilogram/hour.
(7) neutralization
Protein liquid enters neutralizing tank through pump, adds hydrochloric acid (HCl, concentration is 10%-30%) the pH value of protein liquid is transferred to 6.0-7.5.
(8) ultra-filtration and separation
Protein liquid after the neutralization enters the plate-type hyperfiltration membrane system through pump, and control system pressure is 5bar.Concentrating after the separation is protein concentrate liquid mutually, and its solid concentration is 15%-25%, and dilution is whey mutually, its centrefuge experiment sediment≤0.05ml/15ml.
(9) heat treatment
Protein concentrate liquid after separating is carried out sterilization, and sterilization temperature is 80 ℃-90 ℃, and material, is got to high-pressure pump by homogenizer and carried out spray-drying to homogenizer through pump.
(10) spray-drying, lecithin spraying
Adopt press atomization, heated-air drying, the high-pressure pump outlet pressure reaches more than the 500bar, drying tower material inlet amount be the 2-4 ton/hour, outlet temperature is 80 ℃-90 ℃, evaporated quantity of water be the 2-4 ton/hour, material is delivered to high-pressure pump through filter at the process homogenizer earlier and is sloughed moisture again in drying tower, be located at the interior nozzle of tower simultaneously to the material spraying lecithin, the lecithin quantity for spray is the 0.5%-2% of dry, nozzle exit pressure 300-400kg/cm
2, the tower outlet temperature is 80 ℃-90 ℃, dry powder forwards subsequent processing to through cooling.
(11) puddle and pack
Product after the spray-drying sprays phosphatide in fluid bed, after puddling device and puddling, pack.
Embodiment 1
(1) low temperature defatting bean
Get quantitative low temperature defatting bean and drop into batch extractor.
(2) once leach
Low temperature beans sheet is dissolved in 50 ℃ of water.At first 50 ℃ water is pressed ratio of water to material and added at 18: 1 in the batch extractor, use NaOH (NaOH, concentration is 30%) that the pH value of water and low temperature beans sheet is transferred to 7.5, at the uniform velocity stir, kept above process conditions 30 minutes, be and once leach protein liquid.
(3) protein liquid and bean dreg separation
Soluble protein, carbohydrate and salt are separated from leachate, separated with seperator, separating the back liquid phase is the protein liquid that once leaches, and solid phase is for once leaching bean dregs, and once leaching protein liquid concentration is 12%.
(4) secondary leaches
To once leach bean dregs and be dissolved in the secondary batch extractor, between water temperature kept 50 ℃, ratio of water to material was 7: 1, and water is added in the batch extractor, and the pH value keeps nature, does not manually adjust, and secondary leaches the leachate that maintenance was leached for secondary after 20 minutes.
(5) secondary separation of bean dregs and protein liquid
Soluble protein, carbohydrate and salt are separated from leachate.Separating the back liquid phase is that secondary leaches protein liquid, and it is 8% that separation back secondary leaches protein liquid concentration.
(6) degassing
Once leach protein liquid and secondary leaching protein liquid after the separation and squeeze into degassing tank, add defoamer, addition is 10 kilograms/hour.
(7) neutralization
Protein liquid enters neutralizing tank through pump, adds hydrochloric acid (HCl, concentration is 30%) the pH value of protein liquid is transferred to 7.0.
(8) ultra-filtration and separation
Protein liquid after the neutralization enters the plate-type hyperfiltration membrane system through pump, and control system pressure is 5bar.Concentrating after the separation is protein concentrate liquid mutually, and its solid concentration is 15%, and dilution is whey mutually, its centrefuge experiment sediment≤0.05ml/15ml.
(9) heat treatment
Protein concentrate liquid after separating is carried out sterilization, and sterilization temperature is 90 ℃, and material, is got to high-pressure pump by homogenizer and carried out spray-drying to homogenizer through pump.
(10) spray-drying, lecithin spraying
Adopt press atomization, heated-air drying, the high-pressure pump outlet pressure reaches 520bar, drying tower material inlet amount is 2.5 tons/hour, and outlet temperature is 80 ℃, and evaporated quantity of water is 2.3 tons/hour, material is delivered to high-pressure pump through filter at the process homogenizer earlier and is sloughed moisture again in drying tower, be located at the interior nozzle of tower simultaneously to the material spraying lecithin, the lecithin quantity for spray is 1% of a dry, nozzle exit pressure 400kg/cm
2, the tower outlet temperature is 80 ℃, dry powder forwards subsequent processing to through cooling.
(11) puddle and pack
Product after the spray-drying sprays phosphatide in fluid bed, after puddling device and puddling, pack.
Embodiment 2
(1) low temperature defatting bean
Get quantitative low temperature defatting bean and drop into batch extractor.
(2) once leach
Low temperature beans sheet is dissolved in 48 ℃ of water.At first 48 ℃ water is pressed ratio of water to material and added at 16: 1 in the batch extractor, use NaOH (NaOH, concentration is 20%) that the pH value of water and low temperature beans sheet is transferred to 7.5, at the uniform velocity stir, kept above process conditions 30 minutes, be and once leach protein liquid.
(3) protein liquid and bean dreg separation
Soluble protein, carbohydrate and salt are separated from leachate, separated with seperator, separating the back liquid phase is the protein liquid that once leaches, and solid phase is for once leaching bean dregs, and once leaching protein liquid concentration is 12.5%.
(4) secondary leaches
To once leach bean dregs and be dissolved in the secondary batch extractor, between water temperature kept 48 ℃, ratio of water to material was 10: 1, and water is added in the batch extractor, and the pH value keeps nature, does not manually adjust, and secondary leaches the leachate that maintenance was leached for secondary after 20 minutes.
(5) secondary separation of bean dregs and protein liquid
Soluble protein, carbohydrate and salt are separated from leachate.Separating the back liquid phase is that secondary leaches protein liquid, and it is 7.5% that separation back secondary leaches protein liquid concentration.
(6) degassing
Once leach protein liquid and secondary leaching protein liquid after the separation and squeeze into degassing tank, add defoamer, addition is 10 kilograms/hour.
(7) neutralization
Protein liquid enters neutralizing tank through pump, adds hydrochloric acid (HCl, concentration is 20%) the pH value of protein liquid is transferred to 7.0.
(8) ultra-filtration and separation
Protein liquid after the neutralization enters the plate-type hyperfiltration membrane system through pump, and control system pressure is 5bar.Concentrating after the separation is protein concentrate liquid mutually, and its solid concentration is 16%, and dilution is whey mutually, its centrefuge experiment sediment≤0.05ml/15ml.
(9) heat treatment
Protein concentrate liquid after separating is carried out sterilization, and sterilization temperature is 90 ℃, and material, is got to high-pressure pump by homogenizer and carried out spray-drying to homogenizer through pump.
(10) spray-drying, lecithin spraying
Adopt press atomization, heated-air drying, the high-pressure pump outlet pressure reaches more than the 500bar, drying tower material inlet amount is 2.5 tons/hour, and outlet temperature is 80 ℃, and evaporated quantity of water is 2.3 tons/hour, material is delivered to high-pressure pump through filter at the process homogenizer earlier and is sloughed moisture again in drying tower, be located at the interior nozzle of tower simultaneously to the material spraying lecithin, the lecithin quantity for spray is 1% of a dry, nozzle exit pressure 400kg/cm
2, the tower outlet temperature is 80 ℃, dry powder forwards subsequent processing to through cooling.
(11) puddle and pack
Product after the spray-drying sprays phosphatide in fluid bed, after puddling device and puddling, pack.
Claims (1)
1, a kind of method of utilizing the milipore filter isolation technics to prepare soybean protein isolate, its characteristic is:
(1) low temperature defatting bean
Get quantitative low temperature defatting bean and drop into batch extractor.
(2) once leach
Low temperature beans sheet is dissolved in 48 ℃ of-52 ℃ of water.At first 48 ℃-52 ℃ water is pressed ratio of water to material 20: 1-8: 1 adds in the batch extractor, with NaOH (NaOH, concentration is 10%30%) the pH value of water and low temperature beans sheet is transferred to 6.8-9.0, at the uniform velocity stir, kept above process conditions 20-40 minute, and be and once leach protein liquid.
(3) protein liquid and bean dreg separation
Soluble protein, carbohydrate and salt are separated from leachate, separated with seperator, separating the back liquid phase is the protein liquid that once leaches, and solid phase is for once leaching bean dregs, and once leaching protein liquid concentration is 6%-20%.
(4) secondary leaches
To once leach bean dregs and be dissolved in the secondary batch extractor, between water temperature kept 48 ℃-52 ℃, ratio of water to material was 12: 1-5: 1, water is added in the batch extractor, the pH value keeps nature, does not manually adjust, and secondary leaches the leachate that maintenance was leached for secondary after 10-30 minute.
(5) secondary separation of bean dregs and protein liquid
Soluble protein, carbohydrate and salt are separated from leachate.Separating the back liquid phase is that secondary leaches protein liquid, and it is 6-20% that separation back secondary leaches protein liquid concentration.
(6) degassing
Once leach protein liquid and secondary after the separation and leach protein liquid and squeeze into degassing tank, add defoamer, addition be the 6-12 kilogram/hour.
(7) neutralization
Protein liquid enters neutralizing tank through pump, adds hydrochloric acid (HCl, concentration is 10%-30%) the pH value of protein liquid is transferred to 6.0-7.5.
(8) ultra-filtration and separation
Protein liquid after the neutralization enters the plate-type hyperfiltration membrane system through pump, and control system pressure is 5bar.Concentrating after the separation is protein concentrate liquid mutually, and its solid concentration is 15%-25%, and dilution is whey mutually, its centrefuge experiment sediment≤0.05ml/15ml.
(9) heat treatment
Protein concentrate liquid after separating is carried out sterilization, and sterilization temperature is 80 ℃-90 ℃, and material, is got to high-pressure pump by homogenizer and carried out spray-drying to homogenizer through pump.
(10) spray-drying, lecithin spraying
Adopt press atomization, heated-air drying, the high-pressure pump outlet pressure reaches more than the 500bar, drying tower material inlet amount be the 2-4 ton/hour, outlet temperature is 80 ℃-90 ℃, evaporated quantity of water be the 2-4 ton/hour, material is delivered to high-pressure pump through filter at the process homogenizer earlier and is sloughed moisture again in drying tower, be located at the interior nozzle of tower simultaneously to the material spraying lecithin, the lecithin quantity for spray is the 0.5%-2% of dry, nozzle exit pressure 300-400kg/cm
2, the tower outlet temperature is 80 ℃-90 ℃, dry powder forwards subsequent processing to through cooling.
(11) puddle and pack
Product after the spray-drying sprays phosphatide in fluid bed, after puddling device and puddling, pack.
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| Application Number | Priority Date | Filing Date | Title |
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| CN 200310107703 CN1615722A (en) | 2003-11-14 | 2003-11-14 | Method for preparing soybean separate protein by ultra-filter film separation technology |
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| Application Number | Priority Date | Filing Date | Title |
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| CN 200310107703 CN1615722A (en) | 2003-11-14 | 2003-11-14 | Method for preparing soybean separate protein by ultra-filter film separation technology |
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| CN1615722A true CN1615722A (en) | 2005-05-18 |
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| CN101965897A (en) * | 2010-10-19 | 2011-02-09 | 浙江大学 | Processing method for mussel isolated protein |
| CN102781255A (en) * | 2009-12-30 | 2012-11-14 | 索莱有限责任公司 | Soy whey protein compositions and methods for recovering same |
| CN103769608A (en) * | 2014-02-20 | 2014-05-07 | 北京碧水源膜科技有限公司 | Nano-silver sol separating method |
| CN103864886A (en) * | 2013-01-29 | 2014-06-18 | 临邑禹王植物蛋白有限公司 | Process for extracting soybean protein isolates at high extraction rate |
| CN104710637A (en) * | 2015-03-16 | 2015-06-17 | 常熟理工学院 | Method for improving oxygen resistance of isolated soy protein film |
| CN105432934A (en) * | 2014-08-07 | 2016-03-30 | 中粮营养健康研究院有限公司 | Method for preparing soybean protein isolate |
| CN105533118A (en) * | 2016-01-20 | 2016-05-04 | 山东禹王生态食业有限公司 | Technology for refining soybean protein according to membrane method |
| CN106518906A (en) * | 2016-09-24 | 2017-03-22 | 合肥信达膜科技有限公司 | Membrane-method extraction process for soybean lecithin |
| CN107348094A (en) * | 2017-08-30 | 2017-11-17 | 山东禹王生态食业有限公司 | A kind of production method of soybean protein isolate |
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| US10555542B2 (en) | 2006-03-03 | 2020-02-11 | Specialty Protein Producers, Inc. | Methods of separating fat from non-soy plant materials and compositions produced therefrom |
| WO2009111987A1 (en) * | 2008-03-12 | 2009-09-17 | Yin Xuebin | Method for preparing organic selenium proteins |
| CN102781255B (en) * | 2009-12-30 | 2015-11-25 | 索莱有限责任公司 | Soybean whey protein composition and recovery method thereof |
| CN102781255A (en) * | 2009-12-30 | 2012-11-14 | 索莱有限责任公司 | Soy whey protein compositions and methods for recovering same |
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| CN101965897B (en) * | 2010-10-19 | 2012-06-06 | 浙江大学 | Processing method for mussel isolated protein |
| CN103864886A (en) * | 2013-01-29 | 2014-06-18 | 临邑禹王植物蛋白有限公司 | Process for extracting soybean protein isolates at high extraction rate |
| CN103769608A (en) * | 2014-02-20 | 2014-05-07 | 北京碧水源膜科技有限公司 | Nano-silver sol separating method |
| CN105432934A (en) * | 2014-08-07 | 2016-03-30 | 中粮营养健康研究院有限公司 | Method for preparing soybean protein isolate |
| CN104710637B (en) * | 2015-03-16 | 2018-02-13 | 常熟理工学院 | A kind of method for improving soybean separation protein tunica albuginea oxygen resistance |
| CN104710637A (en) * | 2015-03-16 | 2015-06-17 | 常熟理工学院 | Method for improving oxygen resistance of isolated soy protein film |
| CN105533118A (en) * | 2016-01-20 | 2016-05-04 | 山东禹王生态食业有限公司 | Technology for refining soybean protein according to membrane method |
| CN106518906A (en) * | 2016-09-24 | 2017-03-22 | 合肥信达膜科技有限公司 | Membrane-method extraction process for soybean lecithin |
| CN107348094A (en) * | 2017-08-30 | 2017-11-17 | 山东禹王生态食业有限公司 | A kind of production method of soybean protein isolate |
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