CN105646256B - A kind of extracting glutamic acid crystallization processes - Google Patents
A kind of extracting glutamic acid crystallization processes Download PDFInfo
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- CN105646256B CN105646256B CN201610155801.4A CN201610155801A CN105646256B CN 105646256 B CN105646256 B CN 105646256B CN 201610155801 A CN201610155801 A CN 201610155801A CN 105646256 B CN105646256 B CN 105646256B
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Abstract
The invention belongs to amino acids production field, discloses a kind of extracting glutamic acid crystallization processes, it is characterised in that the technique comprises the following steps：1）Disc centrifuge separates, and 2）Horizontal screw centrifuge separates, and 3）Disc centrifuge secondary separation, 4）Mixing, 5）Merge, 6）Concentration, 7）Deng electricity, 8）Stream plus concentrate, 9）Cooling, 10）Plate centrifuge centrifuges, and 11）Ion exchange, 12）Dry thalline.Present invention process energy-saving and emission-reduction, while ensure that glutamic acid quality and extract yield.
Description
Technical field
Patent of the present invention is related to a kind of extracting glutamic acid crystallization processes, belongs to amino acids production field.
Background technology
Glutamic acid, it is a kind of acidic amino acid.Intramolecular contains two carboxyls, and chemical name is alpha-amido glutaric acid.Paddy ammonia
Acid is that inner Suo Xun has found for 1856, is clear crystal, there is delicate flavour, is slightly soluble in water, and is dissolved in hydrochloric acid solution, isoelectric point 3.22.
Largely it is present in grain protein, content is also more in animal brain.During the protein metabolism of glutamic acid in vivo
Critical role is accounted for, participates in many important chemical reactions in animal, plant and microorganism.Monosodium glutamate is prepared by glutamic acid.
The conventional extraction process of domestic glutamic acid producer is to wait electricity, from extraction process is handed at present, i.e., by glutamic acid fermentation
Liquid cools and adjusts the pH of zymotic fluid to the isoelectric point 3.0-3.2 of glutamic acid, standing sedimentation, bottom with sulfuric acid and from handing over height to flow
Precipitation and centrifugal separation goes out glutamic acid, and supernatant liquor adjusts pH to 1.8 with sulfuric acid, is replaced with storng-acid cation exchange resin in clear liquid
Glutamic acid, then with ammoniacal liquor adjust supernatant pH to 10 eluted, the Gao Liuzai eluted is adjusted to pH to 1.5 with sulfuric acid, return
For waiting electricity regulation pH, handled from handing over workshop upper column clear liquid and washing post water and be delivered to sewage treatment plant, added into waste water
Flocculant is added to flocculate albumen, the clear liquid after removing protein after concentration make into fertilizer again by slurry-spraying pelletizing, and concentration and evaporation goes out
Condensed water handled into Aerobic Pond.But the technique there are, and sewage quantity is big and intractability is high, albumen quality is poor, product
The drawbacks such as quality is low, soda acid dosage is big.
This outer portion producer is using galvanic process such as continuous concentrations, and temperature control is in 42-45 after glutami acid fermentation liquor is concentrated
DEG C, stream be added to etc. in electric tank, the electric tank pH such as control to draw cold cooling in the cold tank of drawing after terminating 3.2 or so with sulfuric acid,
With centrifuge glutamic acid, centrifugal clear liquid is discharged into sewage treatment plant, and sewage caused by the technique is few, not from skill of handing over,
But the yield of glutamic acid and quality are low.
The content of the invention
In order to solve the above-mentioned technical problem, the present invention provides a kind of extracting glutamic acid crystallization processes, both can guarantee that glutamic acid
Quality, improve extract yield, improve albumen quality, moreover it is possible to reducing wastewater flow rate.
This law invention is realized in：A kind of extracting glutamic acid crystallization processes, it comprises the following steps：1）Disc-type from
Scheming separates, and 2）Horizontal screw centrifuge separates, and 3）Disc centrifuge secondary separation, 4）Mixing, 5）Merge, 6）Concentration, 7）Deng electricity,
8）Stream plus concentrate, 9）Cooling, 10）Plate centrifuge centrifuges, and 11）Ion exchange, 12）Dry thalline；
Specifically, comprise the following steps：
1）Disc centrifuge separates：Glutami acid fermentation liquor is separated with disc centrifuge, is centrifuged into two parts, and one
Part is the clear liquid A containing micro mycoprotein, mycoprotein content 0.1%（Volume ratio）, another part is to contain a large amount of mycoproteins
Protein liquid B, mycoprotein content 82%（Volume ratio）；
2）Horizontal screw centrifuge separates：Protein liquid B containing a large amount of mycoproteins is separated with horizontal screw centrifuge, is centrifuged into two
Point, a part is the clear liquid C containing a small amount of mycoprotein, mycoprotein content 0.45%（Volume ratio）, another part is in the pasty state
Albumen underflow D, albumen dry matter content are 35%（Mass ratio）；
3）Disc centrifuge secondary separation：With disc centrifuge separating step 2）Gained clear liquid C, is divided into two parts,
A part is the clear liquid E containing micro mycoprotein, and mycoprotein content is 0.1%（Volume ratio）, another part is to contain a large amount of thalline
The protein liquid F of albumen, protein content 80%（Volume ratio）；
4）Mixing：Step 3）Gained protein liquid F and the step 1 of next group feed liquid）The protein liquid containing a large amount of mycoproteins
Step 2 is carried out after mixing）Operation；
5）Merge：By step 1）Obtained clear liquid A and step 3）Obtained clear liquid E merges, and is then divided into clear liquid G and clear liquid
H two parts, clear liquid G are used for step 6）Operation, clear liquid H are used for step 7）Operation；Clear liquid G and clear liquid H volume ratio are 1:1 to 3:
2；
6）Concentration：Using plate-type evaporator concentration step 5）Gained clear liquid G, thickening temperature are 80 DEG C, and vacuum exists
0.06MPa, 2 times are concentrated, obtains concentrate I；
7）Deng electricity：With sulfuric acid by step 5）The clear liquid H reserved pH value is adjusted to glutamic acid isoelectric point 3.2, reduces per hour
Material liquid pH value 0.1-0.2, and feed liquid is progressively heated up, 2-3 DEG C of programming rate/h, feed temperature rises to 40 DEG C, maintains the temperature,
The feed liquid uses as female tank feed liquid；
8）Stream plus concentrate：To step 7）Female tank feed liquid in stream plus step 6）Obtained concentrate I, while add sulphur
Acid, maintain pH3.2 in tank, 40 DEG C of temperature；When material liquid volume accounts for the 90%-95% of tank body capacity, tank volume product is released from bottom
10%-15% feed liquid；
9）Cooling：By step 8）The feed liquid cooling of releasing is rapidly cooled to less than 15 DEG C；
10）Plate centrifuge centrifuges：By step 9）Feed liquid centrifuged using plate centrifuge, rotating speed 1000r/
Min, centrifugation time 10min, glutamic acid crystal and clear liquid J are separated；
11）Ion exchange：Step 10）The clear liquid J isolated adjusts pH to 1.5 with sulfuric acid, is entered by cationic ion-exchange resin
Line replacement, and eluted with ammoniacal liquor, the high flow liquid K under eluting can be used for step 8）The pH of the electric tanks such as regulation；
12）Dry thalline：By step 2）Obtained albumen underflow D is carried out drying to obtain mycoprotein powder with drying plant.
The technology of the present invention uses above-mentioned technique, compares, the advantage is that with conventional technology：
1st, clear liquid of the zymotic fluid after disc centrifuge centrifuges be used for etc. electricity extraction glutamic acid, reduced in electric process is waited
Influence of the mycoprotein to glutamic acid crystallization process, improve the quality of glutamic acid.
2nd, the glu thalline protein obtained after the albumen underflow drying that horizontal screw centrifuge is centrifuged out is without any addition
Thing, purity are high, quality better；
3rd, the feed liquid gone after removing protein is crossed from post is handed over, and is reduced influence of the impurity to resin, is improved the adsorption rate of resin,
And solves the defects of electric clear liquid such as continuous concentration can not be carried out from handing over.
4th, the clear liquid that disc centrifuge is centrifuged out is after concentration, and supernatant cumulative volume reduced to original 40% ~
50%, from the ionization such as contained glutamic acid total amount ratio in waste liquid after friendship hand over skill decline more than 50%, than directly concentrate etc. electric waste liquid paddy
Propylhomoserin total amount declines 80%, improves the total recovery of glutamic acid.
5th, the clear liquid that disc centrifuge is centrifuged out is after concentration, and supernatant cumulative volume reduced to original 40% ~
50%, from the ionization such as the soda acid amount ratio of friendship hand over skill decline more than 50%.
6. passing through above-mentioned technique, the purity of glutamic acid of the present invention can reach 97%（Mass ratio）More than, clear liquid Glutamic Acid contains
Measure 1.6-2.6 g/100mL.
Embodiment
The present invention will be further explained using specific embodiment, but be should not be construed as to this hair below
The bright limitation for creating new spirit.
Example one
A kind of extracting glutamic acid crystallization processes, it comprises the following steps：
1）Disc centrifuge separates：Glutami acid fermentation liquor is separated with disc centrifuge, is centrifuged into two parts, and one
Part is the clear liquid A 6000L containing micro mycoprotein, mycoprotein content 0.1%（Volume ratio）, another part is to contain a large amount of bacterium
The protein liquid B 1500L of body protein, mycoprotein content 82%（Volume ratio）；
2）Horizontal screw centrifuge separates：Protein liquid B 1500L containing a large amount of mycoproteins are separated with horizontal screw centrifuge, are centrifuged into
Two parts, a part are the clear liquid C 1135L containing a small amount of mycoprotein, mycoprotein content 0.45%（Volume ratio）, another part
It is albumen underflow D 389kg in the pasty state, albumen dry matter content is 35%（Mass ratio）；
3）Disc centrifuge secondary separation：With disc centrifuge separating step 2）Gained clear liquid C 1135L, are divided into two
Part, a part are the clear liquid E 908L containing micro mycoprotein, and mycoprotein content is 0.1%（Volume ratio）, another part is
Protein liquid F227L containing a large amount of mycoproteins, protein content 80%（Volume ratio）；
4）Mixing：Step 3）Gained mycoprotein liquid F 227L and the step 1 of next group feed liquid）Contain a large amount of mycoproteins
Protein liquid mixing after carry out step 2）Operation；
5）Merge：By step 1）Obtained clear liquid A 6000L and step 3）Obtained clear liquid E 908L merge common 6908L,
3908L clear liquids G is wherein taken to be used for step 6）Operation, 3000L clear liquid H are used for step 7）Operation；
6）Concentration：With concentrator concentration step 5）Obtained 3908L clear liquid G, using plate-type evaporator, thickening temperature is
80 DEG C, vacuum concentrates 2 times, obtains concentrate I 1954L in 0.06MPa；
7）Deng electricity：With sulfuric acid by step 5）The 3000L clear liquids H reserved pH value is adjusted to glutamic acid isoelectric point 3.2, per hour
Reduction material liquid pH value is 0.1-0.2, and feed liquid is progressively heated up, 2-3 DEG C of programming rate/h, and feed temperature rises to 40 DEG C, is maintained
The temperature, at 1 DEG C, the feed liquid uses temperature adjustment deviation amplitude as female tank feed liquid；
8）Stream plus concentrate：To step 7）Female tank feed liquid in stream plus step 6）Obtained concentrate I and 98% sulfuric acid, dimension
Hold pH3.2 in tank, 40 DEG C of temperature, pH value adjusting deviation amplitude is 0.1, and temperature adjustment deviation amplitude is at 1 DEG C；Treat that material liquid volume accounts for
During the 90%-95% of tank body capacity, the 10%-15% of tank volume product feed liquid is released from bottom, feed liquid cumulative volume must not be less than in tank
The 80% of tank appearance；
9）Cooling：By step 8）The feed liquid cooling of releasing is rapidly cooled to less than 15 DEG C；
10）Plate centrifuge centrifuges：By step 9）Feed liquid centrifuged using plate centrifuge, rotating speed 1000r/
Min, centrifugation time 10min, glutamic acid crystal and clear liquid J are separated；Purity can reach 97.6%；
11）Ion exchange：Step 10）The clear liquid J isolated adjusts pH to 1.5 with 98% sulfuric acid, passes through cationic ion-exchange resin
Enter line replacement, and eluted with ammoniacal liquor, the high flow liquid K under eluting can be used for step 8）The pH of the electric tanks such as regulation；
12）Dry thalline：By step 2）Obtained albumen underflow D is carried out drying to obtain mycoprotein powder with drying plant
160kg, drying plant use revolving roll drying machine and rotary cooler, and dryer entrance temperature is 600 DEG C, goes out material temperature
Spend for 100 DEG C, albumen enters cooler after discharging, and the drop temperature of cooler is 40 DEG C, and dried albumen moisture is 9.0% after drying.
Finally, it is also necessary to it is noted that listed above is only one of present invention specific embodiment.Obviously, originally
Invention is not limited to above example, can also there is many deformations.One of ordinary skill in the art can be from disclosed by the invention interior
Hold all deformations for directly exporting or associating, be considered as protection scope of the present invention.
Claims (2)
1. a kind of extracting glutamic acid crystallization processes, it is characterised in that the technique comprises the following steps：
1）Disc centrifuge separates：Glutami acid fermentation liquor is separated with disc centrifuge, is centrifuged into two parts, a part
It is the clear liquid A containing micro mycoprotein, mycoprotein content 0.1%, another part is the protein liquid B containing a large amount of mycoproteins, bacterium
Body protein content 82%, the thalline content is volume content；
2）Horizontal screw centrifuge separates：Protein liquid B containing a large amount of mycoproteins is separated with horizontal screw centrifuge, is centrifuged into two parts, and one
Part is the clear liquid C containing a small amount of mycoprotein, and mycoprotein content 0.45%, the content is volume content, and another part is to be in
The albumen underflow D of pasty state, albumen dry matter content are 35% according to mass content；
3）Disc centrifuge secondary separation：With disc centrifuge separating step 2）Gained clear liquid C, is divided into two parts, one
It is the clear liquid E containing micro mycoprotein to divide, and mycoprotein content is 0.1%, and another part is the protein liquid containing a large amount of mycoproteins
F, protein content 80%, the protein content are volume ratios；
4）Mixing：Step 3）Gained protein liquid F and the step 1 of next group feed liquid）Containing a large amount of mycoproteins protein liquid mixing
Step 2 is carried out afterwards）Operation；
5）Merge：By step 1）Obtained clear liquid A and step 3）Obtained clear liquid E merges, and is then divided into clear liquid G and clear liquid H two
Part, clear liquid G are used for step 6）Operation, clear liquid H are used for step 7）Operation；
6）Concentration：Using plate-type evaporator concentration step 5）Gained clear liquid G, thickening temperature are 80 DEG C, vacuum in 0.06MPa,
2 times of concentration, obtains concentrate I；
7）Deng electricity：With sulfuric acid by step 5）Gained clear liquid H pH value is adjusted to glutamic acid isoelectric point 3.2, reduces material liquid pH per hour
Value 0.1-0.2, and feed liquid is progressively heated up, 2-3 DEG C of programming rate/h, feed temperature rises to 40 DEG C, maintains the temperature, the feed liquid
Used as female tank feed liquid；
8）Stream plus concentrate：To step 7）Female tank feed liquid in stream plus step 6）Concentrate I, while add sulfuric acid, maintain tank
Interior pH3.2,40 DEG C of temperature；When material liquid volume accounts for the 90%-95% of tank body capacity, the 10%-15% of tank volume product is released from bottom
Feed liquid；
9）Cooling：By step 8）The feed liquid cooling of releasing is rapidly cooled to less than 15 DEG C；
10）Plate centrifuge centrifuges：By step 9）Feed liquid centrifuged using plate centrifuge, rotating speed 1000r/min, from
Heart time 10min, glutamic acid crystal and clear liquid J are separated；
11）Ion exchange：Step 10）The clear liquid J isolated adjusts pH to 1.5 with sulfuric acid, is put by cationic ion-exchange resin
Change, and eluted with ammoniacal liquor, elute to obtain high flow liquid K；
12）Dry thalline：By step 2）Obtained albumen underflow D is carried out drying to obtain mycoprotein powder with drying plant.
2. technique according to claim 1, it is characterised in that the step 5）In, clear liquid G and clear liquid H volume ratio are
1:1 to 3:2.
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Families Citing this family (6)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN110551041A (en) * | 2018-05-31 | 2019-12-10 | 卢松 | extraction and purification process of glutamic acid isoelectric supernatant |
| CN109988790A (en) * | 2019-04-09 | 2019-07-09 | 卢松 | The degerming and extracting method of glutami acid fermentation liquor |
| CN110128286B (en) * | 2019-05-23 | 2022-03-04 | 内蒙古阜丰生物科技有限公司 | Glutamic acid extraction and crystallization process |
| CN110526469A (en) * | 2019-09-10 | 2019-12-03 | 河北首朗新能源科技有限公司 | A kind of processing of fermentation waste water and mycoprotein recovery process and system |
| CN113336662A (en) * | 2021-04-18 | 2021-09-03 | 呼伦贝尔东北阜丰生物科技有限公司 | Process for improving extraction crystallization of threonine |
| CN115399466B (en) * | 2022-06-29 | 2024-02-06 | 呼伦贝尔东北阜丰生物科技有限公司 | Concentrating crystallization process of sodium glutamate |
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| EP0336818B1 (en) * | 1988-04-08 | 1994-08-31 | Sumitomo Chemical Company, Limited | Process for refining amino acids |
| CN102703537A (en) * | 2012-06-26 | 2012-10-03 | 呼伦贝尔东北阜丰生物科技有限公司 | Novel production method for glutamic acid |
| CN103224454A (en) * | 2013-03-18 | 2013-07-31 | 内蒙古阜丰生物科技有限公司 | Glutamic acid separating and extracting technology |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| BR0317778B1 (en) * | 2002-12-27 | 2014-09-02 | Ajinomoto Kk | Process for making an amino acid or a salt thereof |
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|---|---|---|---|---|
| EP0336818B1 (en) * | 1988-04-08 | 1994-08-31 | Sumitomo Chemical Company, Limited | Process for refining amino acids |
| CN102703537A (en) * | 2012-06-26 | 2012-10-03 | 呼伦贝尔东北阜丰生物科技有限公司 | Novel production method for glutamic acid |
| CN103224454A (en) * | 2013-03-18 | 2013-07-31 | 内蒙古阜丰生物科技有限公司 | Glutamic acid separating and extracting technology |
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