CN101491323A - New production technique of sodium glutamate - Google Patents
New production technique of sodium glutamate Download PDFInfo
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- CN101491323A CN101491323A CNA2008101596914A CN200810159691A CN101491323A CN 101491323 A CN101491323 A CN 101491323A CN A2008101596914 A CNA2008101596914 A CN A2008101596914A CN 200810159691 A CN200810159691 A CN 200810159691A CN 101491323 A CN101491323 A CN 101491323A
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Abstract
The invention discloses a novel process for producing monosodium glutamate, which comprises the following key points: performing two stages of membrane filtrations on a glutamic acid fermentation broth obtained through fermentation so as to eliminate mycoproteins and other macromolecular substances; performing decolorization through active carbons, sheet frame filtration, alkali neutralization and concentration on the fermentation broth; performing ammonia blowoff recycling in the process of the concentration; performing further decolorization through a particle carbon column; and performing concentration and crystallization to prepare the final product of the monosodium glutamate. The process achieves the procedure of converting the glutamic acid fermentation broth into sodium glutamate directly without extracting the glutamic acid, has the advantages of simple operation, short production period, low cost, less pollution, high added value of by-products, and the like, and solves the problems that the production of the monosodium glutamate by the prior art has over-dependence on sulphuric acid, high yield of wastewater and lower quality of the by-products.
Description
Technical field
The invention belongs to the glutamate production technical field, be specifically related to a kind of glutamate production new technology.
Background technology
Monosodium glutamate, the chemical name sodium glutamate is a kind of amino acid production by ferment method flavouring of output maximum.China's monosodium glutamate industrial development in recent years is rapid, and the monosodium glutamate sales volume increases year by year.According to statistics, China's msg output was 1,190,000 tons in 2003, had reached 191.3 ten thousand tons by 2007, accounted for world's monosodium glutamate total output more than 70%.
At present the production of gourmet powder flow process is: the glutami acid fermentation liquor that microbial fermentation obtains, and adopt " isoelectric point and ion-exchange " to extract monosodium glutamate precursor substance glutamic acid in the zymotic fluid, add the alkali neutralization then, concentrate, crystallization obtains monosodium glutamate.Promptly by the transformation mode of " monoammonium glutamate is converted into glutamic acid and is converted into sodium glutamate again ".Though this technology is very ripe, has following insoluble problem, is to influence the bottleneck that the monosodium glutamate industry develops to green, environmental protection direction.
1, sulfuric acid consumption is big, increases extra cost.All by reducing the extraction that glutamic acid solubility realizes glutamic acid, sulfuric acid commonly used is regulated the isoelectric point that zymotic fluid pH value reaches glutamic acid to prior art in this process, and this moment, its solubility was minimum, and it is separated out from zymotic fluid.But regulating zymotic fluid pH value active ingredient is the hydrogen ion of sulfuric acid only, and sulfate radical is present in the zymotic fluid, combines with other cations to form sulfate, mainly is ammonium sulfate, becomes the central impurity component of feed liquid.According to statistics, produce 1 ton of monosodium glutamate and need consume 850 kilograms of left and right sides sulfuric acid, account for 15% of glutamate production cost.
2. ion-exchange produces a large amount of waste water, and environmental pollution is serious.For improving product yield, often adopt the residual glutamic acid in the electric clear liquid of ion-exchange equity to extract once more.General the glutamic acid yield can reach about 95% through ion-exchange, and therefore " isoelectric point+ion-exchange " extraction glutamic acid is well received in the monosodium glutamate industry.In ion exchange process, need to consume a large amount of liquefied ammonia and regulate pH as eluant, eluent.According to statistics, produce 1 ton of monosodium glutamate and need consume liquefied ammonia about 450 kilograms, wherein as 380 kilograms in nitrogenous source, 70 kilograms of ion-exchanges account for 25% of glutamate production cost.The waste water that ion-exchange produces accounts for more than 60% of gustatory production wastewater generation, is the difficult point and the emphasis of environment protection treating.
3, the accessory substance grade is lower, and economic benefit is difficult to performance.Prior art is to adopt flocculence that mycoprotein in the feed liquid is extracted, as feed.But, pass through etc. that electricity extracts, contain a large amount of sulfate radicals in the mycoprotein after the ion-exchange, cause product quality not high, be difficult to realize higher value application.Ammonium sulfate is the main accessory substance of liquid waste processing in the glutamate production process, but because market price depression, profit is lower, becomes the burden that glutamate production enterprise is difficult to abandon.
Summary of the invention
The objective of the invention is to solve the prior art glutamate production to the depending on unduly of sulfuric acid, the waste water generation is big, the accessory substance quality is lower technical problem, provide a kind of with short production cycle, technology simple, the new technology of saving energy, lowering energy consumption and reducing pollutants discharge outstanding effect glutamate production.
The new technology of glutamate production of the present invention is a raw material with starch, obtains glutami acid fermentation liquor through fermentation; Its main points are according to the following steps zymotic fluid to be purified:
1), with zymotic fluid micro-filtration and ultrafiltration two-stage membrane filtration, at first adopt ceramic micro filter film to remove thalline in the zymotic fluid, the feed liquid printing opacity reaches 40～50%% behind the micro-filtration, dry clearance 1.2%, feed liquid is handled with ceramic super-filtering film behind the micro-filtration, and the feed liquid printing opacity is 80～85% after the ultrafiltration, dry clearance 0.5%, the micro-filtration residue is made high-quality protein feed, and ultrafiltration residue spray-drying is made organic fertilizer;
2), the feed liquid in the step 1) is heated to 50～80 ℃, use powdered activated carbon decoloring, 50～80 ℃ of bleaching temperatures, bleaching time 0.5～3h, decolouring pH4.0～8.0, the feed liquid light transmittance after the decolouring is 88%～95%;
3), the feed liquid after the decolouring is in plate-frame filtering is placed on the closed container that has stirring, by glutamic acid: alkali be 1: 1.0～1.1 mol ratio adding solid sodium hydroxide react sodium glutamate feed liquid;
4), the feed liquid in the step 3) is concentrated into feed concentration through the multiple-effect cryogenic vacuum is 25～29 ° of B é, by retracting device, makes liquefied ammonia with blow-off method, it is recycling to get back to fermentation procedure;
5), with the concentrate in the step 4) with the decolouring of particle charcoal post, the feed liquid light transmittance after the decolouring reaches 93%～100%;
6), the feed liquid after will decolouring changes in the crystallizer, continues to be concentrated into 30～32 ° of B é of concentration, adds the crystal seed graining then, continues to concentrate again, and gets the product monosodium glutamate through centrifugation.
The present invention compared with prior art, changed the transformation mode of " monoammonium glutamate is converted into glutamic acid and is converted into sodium glutamate again " in the existing production technology, be converted into sodium glutamate from monoammonium glutamate, avoided waiting the ionization preface of handing over, have following outstanding advantage:
1, shortened technological process, the production cycle shortens, and has improved production efficiency;
2, greatly reduce the consumption of sulfuric acid and liquefied ammonia, not only reduced production cost, but also avoided the generation of a large amount of sulfate;
3, reduce sewage emissions, greatly alleviated the environmental protection pressure of enterprise;
4, adopt two-stage membrane technology fox extracting thallus protein, not only improved the quality of feed liquid, but also improved the quality of byproduct, increased value-added content of product.
In addition, the ammonia stripping reclaims in the concentration process, has realized ammonia recycling in the glutamate production system, the environmental protection pressure that has not only reduced production cost but also avoided high ammonia-nitrogen wastewater to bring.
Glutamate production new technology of the present invention, need not to extract glutamic acid, but be converted into sodium glutamate, the electron ion exchange process such as thoroughly eliminated, compared with existing technology that can to shorten the production cycle about 1/3, reduced sulfuric acid consumption about 15%, save liquefied ammonia use amount about 20%, reduce sewage discharge more than 60%, produce 1 ton of monosodium glutamate and reduce cost approximately 8%, be roughly equal to 550 yuan.China produced about 1,900,000 tons of monosodium glutamate per year in 2007, if adopt new technology the saving cost was dropped into about 1,000,000,000 yuan, and this new technology has great economic benefit, social benefit and environmental benefit.
The specific embodiment
Conventional method is that fermenting raw materials is produced glutamic acid with starch, obtain glutami acid fermentation liquor, behind micro-filtration and ultrafiltration two-stage membrane filtration, activated carbon decolorizing, plate-frame filtering, alkali neutralization, low-temperature reduced-pressure concentrate, utilize the ammonia in the ammonia stripping retracting device recovery concentration process again, and then preparation liquefied ammonia, utilize particle charcoal post further to decolour again, make monosodium glutamate through condensing crystallizing.
Embodiment 1 starch material is put jar and is obtained 9.7m after the ferment tank maturation
3Zymotic fluid, glutamic acid content 11.6% adopts the two-stage membrane filtration to remove mycoprotein and big molecular impurity, at first adopts ceramic micro filter film to remove thalline in the zymotic fluid, the feed liquid printing opacity reaches 43% behind the micro-filtration, dry clearance 1.2%, the ceramic hyperfiltration treatment of feed liquid behind the micro-filtration, the feed liquid printing opacity is 84% after the ultrafiltration, dry clearance 0.5%, the micro-filtration residue is made high-quality protein feed, and ultrafiltration residue spray-drying is made organic fertilizer, and feed liquid behind the two-stage membrane filtration becomes 12.3m owing to increase the wash water volume
3, content 9.08%, product loss rate 0.7%; Then with the 12.3m behind the membrane filtration
3Feed liquid is decoloured in bleacher, adds powdered activated carbon, and 65 ℃ are stirred decolouring 1.5h, plate-frame filtering carbon removal, powdery carbon decolouring back feed liquid printing opacity 96.4%; Filtering back feed liquid stirring at normal temperature adds among the NaOH 314kg and the generation of the glutamic acid in feed liquid monosodium glutamate, in and feed liquid low-temperature reduced-pressure in 2nd effect evaporator concentrate, make separating of ammonia and feed liquid, feed liquid is concentrated into 27 ° of B é of concentration discharging, and the ammonia and the condensed water of generation reclaim by recovery system; The ammonia that reclaims obtains liquefied ammonia 100.5kg after compression, and liquefied ammonia returns fermentation and supplies thalli growth as nitrogenous source; With the decolouring of particle charcoal post, the feed liquid printing opacity reaches 99.5% again, and feed liquid enters concentration pan and continues to be concentrated into 31 ° of B é of concentration, adds crystal seed, concentrated, crystallization, centrifugation again obtains msg product 1216kg, the monosodium glutamate leading indicator is a content 99.58% after testing, printing opacity 99.1%, sulfate 0.01%.
Embodiment 2 is put jar and is obtained 100m according to embodiment 1
3Zymotic fluid, glutamic acid content 11% adopts the two-stage membrane filtration to remove mycoprotein and big molecular impurity, at first adopts micro-filtration membrane to remove thalline in the zymotic fluid, the feed liquid printing opacity reaches 40% behind the micro-filtration, dry clearance 1.1%, feed liquid is carried out hyperfiltration treatment behind the micro-filtration, and the feed liquid printing opacity is 85% after the ultrafiltration, dry clearance 0.5%, the micro-filtration residue is made high-quality protein feed, and ultrafiltration residue spray-drying is made organic fertilizer, and feed liquid behind the two-stage membrane filtration becomes 120m owing to increase the wash water volume
3, content 8.7%, product loss rate 0.5%; Feed liquid 120m behind the membrane filtration
3, in bleacher, decolour, add powdered activated carbon, 65 ℃ are stirred decolouring 1h, plate-frame filtering carbon removal, powdery carbon decolouring back feed liquid printing opacity 95%; Feed liquid behind the membrane filtration, stirring at normal temperature add among the NaOH 2821kg and the glutamic acid in the feed liquid, generate monosodium glutamate; In and feed liquid low-temperature reduced-pressure in triple effect evaporator concentrate, ammonia is separated with feed liquid, feed liquid is concentrated into 28 ° of B é of concentration and gets final product discharging; The ammonia and the condensed water that produce reclaim by recovery system, and the ammonia of recovery obtains liquefied ammonia 940kg after compression, return fermentation and supply thalli growth as nitrogenous source; Use the particle carbon decoloring again, the feed liquid printing opacity reaches 99.3%, and feed liquid enters concentration pan and continues to be concentrated into 31 ° of B é of concentration, adds crystal seed, and concentrated again, crystallization obtain msg product 11275kg through centrifugation; The monosodium glutamate leading indicator is a content 99.56% after testing, printing opacity 98.7%, sulfate 0.01%.
Annotate: related material % in the specification is weight %.
Claims (1)
1, a kind of glutamate production new technology is a raw material with starch, obtains glutami acid fermentation liquor through fermentation; It is characterized in that according to the following steps zymotic fluid being purified:
1), with zymotic fluid micro-filtration and ultrafiltration two-stage membrane filtration, at first adopt ceramic micro filter film to remove thalline in the zymotic fluid, the feed liquid printing opacity reaches 40～50% behind the micro-filtration, dry clearance 1.2%, feed liquid is handled with ceramic super-filtering film behind the micro-filtration, and the feed liquid printing opacity is 80～85% after the ultrafiltration, dry clearance 0.5%, the micro-filtration residue is made protein feed, and ultrafiltration residue spray-drying is made organic fertilizer;
2), the feed liquid in the step 1) is heated to 50～80 ℃, use powdered activated carbon decoloring, 50～80 ℃ of bleaching temperatures, bleaching time 0.5～3h, decolouring pH4.0～8.0, the feed liquid light transmittance after the decolouring is 88%～95%;
3), the feed liquid after the decolouring is in plate-frame filtering is placed on the closed container that has stirring, by glutamic acid: alkali be 1: 1.0～1.1 mol ratio adding solid sodium hydroxide react sodium glutamate feed liquid;
4), the feed liquid in the step 3) is concentrated into feed concentration through the multiple-effect cryogenic vacuum is 25～29 ° of B é, by retracting device, makes liquefied ammonia with blow-off method, it is recycling to get back to fermentation procedure;
5), with the concentrate in the step 4) with the decolouring of particle charcoal post, the feed liquid light transmittance after the decolouring reaches 93%～100%;
6), the feed liquid after will decolouring changes in the crystallizer, continues to be concentrated into 30～32 ° of B é of concentration, adds the crystal seed graining then, continues to concentrate again, and gets the product monosodium glutamate through centrifugation.
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Cited By (13)
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| CN102533884A (en) * | 2011-12-30 | 2012-07-04 | 宝鸡阜丰生物科技有限公司 | Method for cleanly producing glutamic acid, gamma-polyglutamic acid and organic fertilizer |
| CN103288932A (en) * | 2013-06-13 | 2013-09-11 | 天津科技大学 | Method for separating and extracting pediocin PA-1 from fermentation solution |
| CN104212870A (en) * | 2014-09-28 | 2014-12-17 | 呼伦贝尔东北阜丰生物科技有限公司 | Process for fermentation production of lysine hydrochloride |
| CN104386875A (en) * | 2014-09-27 | 2015-03-04 | 呼伦贝尔东北阜丰生物科技有限公司 | Sodium glutamate fermentation waste liquid treatment process |
| CN105349591A (en) * | 2015-12-18 | 2016-02-24 | 内蒙古阜丰生物科技有限公司 | Natural food additive sodium glutamate and preparation technology thereof |
| CN106566852A (en) * | 2016-08-31 | 2017-04-19 | 安徽珍味奇调味食品有限公司 | Sodium glutamate separation and purification method |
| CN107337611A (en) * | 2017-06-07 | 2017-11-10 | 成都连接流体分离科技有限公司 | A kind of method that glutami acid fermentation liquor prepares sodium glutamate |
| CN107801971A (en) * | 2017-10-19 | 2018-03-16 | 宁波远利化工有限公司 | A kind of production method of healthy monosodium glutamate |
| CN109797176A (en) * | 2017-11-17 | 2019-05-24 | 卢松 | A kind of environment-protective process preparing monosodium glutamate |
| CN110551040A (en) * | 2018-05-31 | 2019-12-10 | 卢松 | Method for refining monosodium glutamate by adopting macroporous strong base anion resin |
| CN112457208A (en) * | 2020-12-30 | 2021-03-09 | 赵兰坤 | Continuous crystal growth process for sodium glutamate |
| CN112708645A (en) * | 2020-11-04 | 2021-04-27 | 呼伦贝尔东北阜丰生物科技有限公司 | Method for efficiently producing monosodium glutamate |
| CN113545470A (en) * | 2021-08-06 | 2021-10-26 | 呼伦贝尔东北阜丰生物科技有限公司 | Production method for high-quality monosodium glutamate |
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| CN1099746A (en) * | 1993-08-30 | 1995-03-08 | 无锡轻工业学院 | Method for extracting glutaminic acid from fermentation liquor |
| CN1282424C (en) * | 2005-07-01 | 2006-11-01 | 江南大学 | Production of gourmet powder |
| CN101033478B (en) * | 2007-04-12 | 2010-08-25 | 江南大学 | Process of producing sodium glutamate |
| CN101120766B (en) * | 2007-07-30 | 2011-08-10 | 山东阜丰生物科技开发有限公司 | Monosodium glutamate green manufacturing technology |
| CN101103800A (en) * | 2007-07-30 | 2008-01-16 | 山东阜丰生物科技开发有限公司 | Green making technology for monosodium glutanmate |
| CN101103802A (en) * | 2007-07-30 | 2008-01-16 | 山东阜丰生物科技开发有限公司 | Isoelectric separating new technology for glutamic acid |
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- 2008-11-12 CN CN2008101596914A patent/CN101491323B/en not_active Expired - Fee Related
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| CN102533884B (en) * | 2011-12-30 | 2014-01-22 | 宝鸡阜丰生物科技有限公司 | Method for cleanly producing glutamic acid, gamma-polyglutamic acid and organic fertilizer |
| CN102533884A (en) * | 2011-12-30 | 2012-07-04 | 宝鸡阜丰生物科技有限公司 | Method for cleanly producing glutamic acid, gamma-polyglutamic acid and organic fertilizer |
| CN103288932A (en) * | 2013-06-13 | 2013-09-11 | 天津科技大学 | Method for separating and extracting pediocin PA-1 from fermentation solution |
| CN103288932B (en) * | 2013-06-13 | 2015-04-15 | 天津科技大学 | Method for separating and extracting pediocin PA-1 from fermentation solution |
| CN104386875B (en) * | 2014-09-27 | 2016-04-27 | 呼伦贝尔东北阜丰生物科技有限公司 | A kind for the treatment of process of Sodium Glutamate fermented waste fluid |
| CN104386875A (en) * | 2014-09-27 | 2015-03-04 | 呼伦贝尔东北阜丰生物科技有限公司 | Sodium glutamate fermentation waste liquid treatment process |
| CN104212870A (en) * | 2014-09-28 | 2014-12-17 | 呼伦贝尔东北阜丰生物科技有限公司 | Process for fermentation production of lysine hydrochloride |
| CN105349591B (en) * | 2015-12-18 | 2019-08-30 | 内蒙古阜丰生物科技有限公司 | A kind of natural additive for foodstuff sodium glutamate and its preparation process |
| CN105349591A (en) * | 2015-12-18 | 2016-02-24 | 内蒙古阜丰生物科技有限公司 | Natural food additive sodium glutamate and preparation technology thereof |
| CN106566852A (en) * | 2016-08-31 | 2017-04-19 | 安徽珍味奇调味食品有限公司 | Sodium glutamate separation and purification method |
| CN107337611A (en) * | 2017-06-07 | 2017-11-10 | 成都连接流体分离科技有限公司 | A kind of method that glutami acid fermentation liquor prepares sodium glutamate |
| CN107801971A (en) * | 2017-10-19 | 2018-03-16 | 宁波远利化工有限公司 | A kind of production method of healthy monosodium glutamate |
| CN109797176A (en) * | 2017-11-17 | 2019-05-24 | 卢松 | A kind of environment-protective process preparing monosodium glutamate |
| CN110551040A (en) * | 2018-05-31 | 2019-12-10 | 卢松 | Method for refining monosodium glutamate by adopting macroporous strong base anion resin |
| CN112708645A (en) * | 2020-11-04 | 2021-04-27 | 呼伦贝尔东北阜丰生物科技有限公司 | Method for efficiently producing monosodium glutamate |
| CN112457208A (en) * | 2020-12-30 | 2021-03-09 | 赵兰坤 | Continuous crystal growth process for sodium glutamate |
| CN113545470A (en) * | 2021-08-06 | 2021-10-26 | 呼伦贝尔东北阜丰生物科技有限公司 | Production method for high-quality monosodium glutamate |
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