CN110407388A - A kind of electricity such as glutamic acid concentration extract the recycling processing method of waste liquid - Google Patents
A kind of electricity such as glutamic acid concentration extract the recycling processing method of waste liquid Download PDFInfo
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- C01—INORGANIC CHEMISTRY
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- C01C1/00—Ammonia; Compounds thereof
- C01C1/24—Sulfates of ammonium
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- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
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- C02F1/28—Treatment of water, waste water, or sewage by sorption
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- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
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- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
- C02F1/444—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by ultrafiltration or microfiltration
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- C02F1/46—Treatment of water, waste water, or sewage by electrochemical methods
- C02F1/469—Treatment of water, waste water, or sewage by electrochemical methods by electrochemical separation, e.g. by electro-osmosis, electrodialysis, electrophoresis
- C02F1/4693—Treatment of water, waste water, or sewage by electrochemical methods by electrochemical separation, e.g. by electro-osmosis, electrodialysis, electrophoresis electrodialysis
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- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
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- C02F2103/00—Nature of the water, waste water, sewage or sludge to be treated
- C02F2103/34—Nature of the water, waste water, sewage or sludge to be treated from industrial activities not provided for in groups C02F2103/12 - C02F2103/32
- C02F2103/36—Nature of the water, waste water, sewage or sludge to be treated from industrial activities not provided for in groups C02F2103/12 - C02F2103/32 from the manufacture of organic compounds
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Abstract
The invention discloses the recycling processing methods that a kind of electricity such as glutamic acid concentration extract waste liquid, belong to industrial fermentation technology field.Technical solution of the present invention comprises the steps of: that the electricity such as glutamic acid concentration, which are extracted waste liquid, first passes through ultrafiltration membrane treatment acquisition film concentrate and membrane filtration clear liquid, film concentrate is by filtering, dry acquisition mycoprotein, the membrane filtration clear liquid carries out electrodialysis process after decolorizing with activated carbon, obtain electrodialysis trapped fluid and electrodialysis permeate, the electrodialysis trapped fluid and electrodialysis permeate obtain glutamic acid and ammonium sulfate by evaporation and concentration, crystallisation by cooling and separation and recovery respectively, to realize the recycling treatment that the electricity such as glutamic acid concentration extract waste liquid.By processing method of the invention, glutamic acid and ammonium sulfate are recycled, the economic benefit of monosodium glutamate per ton promotes 300~500 yuan, and obtains the mycoprotein of higher pair value, also eliminates the exhaust emission generated when being spray-dried in traditional handicraft.
Description
Technical field
The present invention relates to the recycling processing methods that a kind of electricity such as glutamic acid concentration extract waste liquid, and in particular to a kind of utilization
The galvanic process extraction waste water generated and the methods for realizing waste water reclaiming such as the processing concentration of the technological means such as electrodialysis, ultrafiltration membrane,
Belong to industrial fermentation technology field.
Background technique
Currently, the scheme of domestic production glutamic acid mainly relies on fermentation method, after fermentation, main extraction process is adopted
" concentration etc. electric extraction process ", it is described " the electric extraction process such as concentration " are as follows: by glutami acid fermentation liquor by being concentrated by evaporation,
Continuous to wait the processes such as electricity, crystallisation by cooling, centrifuging treatment, extraction obtains glutamic acid crystal, and extraction process yield is generally in 86-
Between 89%, yield is lower.In addition, the glutamate extraction waste liquor obtained, which is referred to as the electricity such as concentration, extracts waste liquid, the electricity such as concentration
The inorganic salt impurities in waste liquid containing a large amount of thallus, pigment and high concentration are extracted, in addition to this, also contain high-concentration sulfuric acid ammonium
(about 90~140g/L) and concentration are normally 20~38g/L glutamic acid.Due to the presence of thallus and impurity etc., cause in waste liquid
Glutamic acid can not directly recycle, while waste liquid can not also carry out biochemical treatment, not only glutamic acid be caused to lose, and return environment and make
It is destroyed at great.
Currently, it is to use concentration and spray drying process will that more method is used in the processing for extracting waste liquid for the electricity such as concentration
Waste water becomes fertilizer, to reduce the pollution for extracting waste water to environment, but produces generation large quantity of exhaust gas and fertilizer fertilizer during fertilizer
It imitates low factor and limits the production and sale of fertilizer, while also leading to glutamate production enterprise because extracting glutamic acid yield is low
Benefit reduces, and influences the sound development of glutamate production enterprise.It also reported in the prior art and substance is carried out to glutamate extraction waste liquor
The technique of extraction or circulating and recovering, but the substance extracted is usually diluted acid (such as sulfuric acid, nitric acid, hydrochloric acid) and ammonia, reuse
In isoelectric point crystallization or ion exchange and etc. in, the glutamic acid in mother liquor is not extracted, in such cases, due to diluted acid
Deng economic value is not high and air stripping ammonia, ammonia absorb, the high cost of diluted acid separation etc. so that it is difficult to meet enterprise
Needs, be specifically shown in Chinese patent application CN102100353A and CN102125252A.
Therefore, recycling glutamic acid in waste liquid can be extracted from electricity such as glutamic acid concentrations, recycle other objects by continually looking for one kind
Matter and the method that not will increase cost.
Summary of the invention
[technical problem]
The processing method presence that the electricity such as existing glutamic acid concentration extract waste liquid can not recycle glutamic acid, substance extraction cost
The problems such as high and exhaust gas pollution.
[technical solution]
To solve the above-mentioned problems, the present invention provides a kind of using ultrafiltration membrane, decolorizing with activated carbon, electrodialysis, evaporation knot
The techniques such as crystalline substance realize come the method for handling the electricity extraction waste liquid such as glutamic acid concentration and recycle mycoprotein, sulphur from extraction waste liquid
The purpose of sour ammonium and glutamic acid, meanwhile, the condensed water of evaporation, which is recycled into, to be used in production, and final realize extracts effluent resource
Purpose.The method of the present invention not only obtains the mycoprotein of higher pair value, has also recycled a large amount of glutamic acid and ammonium sulfate, and basic
It eliminates high concentration and extracts the pollution of waste liquid, exhaust gas to environment, also reduce water resource because of the circulating and recovering of evaporation condensed water
Consumption, not only realizing considerable economic benefit also has good environmental benefit.
Specifically, the technical solution of the present invention is as follows: a kind of glutamic acid concentration etc. electricity extract waste liquid recycling processing method,
The method are as follows: the electricity such as glutamic acid concentration are extracted into waste liquid and first pass through ultrafiltration membrane treatment acquisition film concentrate and membrane filtration clear liquid, film
Concentrate carries out electrodialysis process after decolorizing with activated carbon, obtains by filtering, dry acquisition mycoprotein, the membrane filtration clear liquid
To electrodialysis trapped fluid and electrodialysis permeate, the electrodialysis trapped fluid and electrodialysis permeate respectively by being concentrated by evaporation,
Crystallisation by cooling and separation and recovery obtain glutamic acid and ammonium sulfate, to realize the recycling that the electricity such as glutamic acid concentration extract waste liquid
Processing.
Further, the evaporation condensed water obtained that is concentrated by evaporation is recycled into for glutamic acid fermentation or glutamic acid
Among extraction process.
Further, the ultrafiltration membrane is one of tubular ultra-filtration membrane, ceramic super-filtering film.
Further, the operating parameter of the ultrafiltration membrane is: 10~300kDa of molecular cut off, and operation temperature is 15~40
DEG C, operating pressure is 0.15~0.3MPa, and crossflow velocity is 2~4m/s.
Further, membrane filtration clear liquid≤25NTU after the ultrafiltration membrane treatment.
Further, the filtering is preferably filters pressing, and preferably plate filter is filtered operation.
Further, during the decolorizing with activated carbon, the active carbon is powder activated carbon；The additive amount of activated carbon
For 5~25g/L；Operating parameter are as follows: temperature is 40~70 DEG C, and bleaching time is 30~50min.
Further, before the destainer after decolorizing with activated carbon carries out electrodialysis process, separation need to be first passed through to remove
Active carbon；It is described to be separated into filtering or micro-filtration, wherein separate mode does not influence implementation of the invention.
Further, the film that the electrodialysis process uses is homogeneous membrane or heterogeneous membrane, the pH control of feeding liquid 3.0~
Between 3.3；When for homogeneous membrane, the operation voltage of each pair of film is 0.6~1.2V, when for heterogeneous membrane, the operation electricity of each pair of film
Pressure is 0.3~0.6V, conductivity≤2600 μ s/cm of control electrodialysis trapped fluid water outlet.
Further, the pH of the feeding liquid when electrodialysis process is preferably 3.2.
Further, the electrodialytic trapped fluid carries out circular treatment as the feeding liquid of electrodialysis process.
Further, the evaporation and concentration processing of the electrodialysis trapped fluid is using negative pressure single effect evaporator or negative pressure economic benefits and social benefits
Evaporator, which is evaporated, is concentrated into 6~15 times, and last evaporator absolute pressure is controlled in 15~35kPa.
Further, the evaporation and concentration processing of the electrodialysis permeate is first to be evaporated using decompression multi-effect evaporator
3~6 times are concentrated into, then forces external circulation evaporator to be evaporated 3~5 times of concentration using negative pressure single-action, does not imitate evaporator
Absolute pressure is controlled in 15~30kPa；Wherein, any one of 2~4 effect evaporators can be used in the multi-effect evaporator.
Further, the crystallisation by cooling and lock out operation of electrodialysis trapped fluid gained concentrate after being concentrated by evaporation
Are as follows: control cooling rate is that 0.5~4 DEG C/h carries out cooling down crystallization, and speed of agitator is controlled in 20~100r/min, final cold
But temperature control obtains glutamic acid crystal using educating brilliant sedimentation, separating at 8~18 DEG C.
Further, the crystallisation by cooling and lock out operation of electrodialysis permeate gained concentrate after being concentrated by evaporation
Are as follows: control cooling rate is that 0.5~2 DEG C/h carries out cooling down crystallization, and speed of agitator is controlled in 30~60r/min, final cold
But temperature control obtains ammonia sulfate crystal using separation at 50~65 DEG C.
Further, the separation refers to that crystallization magma is carried out by one of centrifuge, band filter, sheet frame etc.
Separation obtains glutamic acid crystal or ammonia sulfate crystal, does not influence this patent implementation using the centrifuge separation mode except above-mentioned.
Further, the electricity such as glutamic acid concentration extract waste liquid refer to glutami acid fermentation liquor by the electricity such as concentration, continuous,
It is obtained after crystallisation by cooling, centrifuge separation, extracting glutamic acid waste water Glutamic Acid concentration is 20~38g/L, and pH is 3.0~3.3.
The advantageous effects that the present invention obtains:
1, the electricity such as recyclable glutamic acid concentration of the present invention extracts 40~75% glutamic acid and 70~95% in waste liquid
Ammonium sulfate, the economic benefit of monosodium glutamate per ton improves 300~500 yuan；
2, the present invention can be achieved to eliminate traditional spray drying process, eliminate its brought exhaust emission；
3, the present invention, which realizes, will extract waste water reclaiming, reduce contaminated wastewater, save water resource.
Detailed description of the invention
Fig. 1 is the overall procedure signal for the recycling processing method that a kind of electricity such as glutamic acid concentration of the present invention extract waste liquid
Figure.
Specific embodiment
Content of glutamic acid measuring method: it is measured using biosensor SBA-40.
The present invention will be further described in the form of embodiment in conjunction with Fig. 1 below:
Embodiment 1
(1) electricity such as 6600mL glutamic acid concentration are taken to extract waste liquid, aminoglutaric acid concentration 27g/L, ammonium sulfate 105g/L pass through
The tubular ultra-filtration membrane that molecular cut off is 200kDa is handled, and control operation temperature is 30 DEG C, and operating pressure 0.15MPa is used in combination
Clear water washing obtains the membrane filtration clear liquid of 6500mL, 20NTU, and concentrate obtains mycoprotein by filtering, squeezing, drying.
(2) 39g activated carbon (activated carbon additive amount is 6g/L) is added into membrane filtration clear liquid 6500mL, is taken off under the conditions of 60 DEG C
Color 35min, then filtering removes activated carbon and obtains destainer.
(3) destainer enters homogeneous membrane electrodialysis process system, and destainer pH is 3.2, and is in each pair of membrane operations voltage
It is handled under the conditions of 1.1V, obtains electrodialysis permeate and conductivity respectively as the trapped fluid of 1800 μ s/cm.
(4) electrodialysis trapped fluid passes through single-effect evaporation system, under the conditions of vacuum degree is 20kPa, is concentrated by evaporation to 8 times.
(5) concentrate enters crystallisation by cooling tank, and control cooling velocity is 2.2 DEG C/h, speed of agitator 55r/min, finally
12 DEG C are cooled to, 5h is stirred for, then passes through sedimentation separation, obtains glutamic acid crystal 92.7g, recycling glutamic acid reaches 52%.
(6) electrodialysis permeate is evaporated dense under the conditions of not imitating vacuum degree is 25kPa by two effect reduction vaporization systems
It is reduced to 4 times；Then it is transferred to again in the single-action forced evaporation crystallizer that vacuum degree is 20kPa and is concentrated 4 times.Concentrate enters cooling knot
Brilliant tank, control cooling velocity are 1 DEG C/h, and speed of agitator 55r/min is finally cooled to 55 DEG C, is stirred for 2h, then by cone
Basket centrifuge separation, obtains ammonia sulfate crystal 589g, and recycling ammonium sulfate reaches 85%.
(7) condensate portion that generates is real in the cleaning process during extracting glutamic acid when being wherein concentrated by evaporation
Circulating and recovering is showed.
Embodiment 2
(1) electricity such as 5000mL glutamic acid concentration are taken to extract waste liquid, aminoglutaric acid concentration 36g/L, ammonium sulfate 110g/L pass through
The tubular ultra-filtration membrane that molecular cut off is 100kDa is handled, and control operation temperature is 40 DEG C, operating pressure 0.2MPa, and with clearly
Water washing obtains 5000mL membrane filtration clear liquid.
(2) 60g activated carbon (activated carbon additive amount is 12g/L) is added into membrane filtration clear liquid 5000mL, under the conditions of 65 DEG C
Decolourize 30min, and then filtering removes activated carbon and obtains destainer.
(3) destainer enters heterogeneous membrane electrodialysis process system, and destainer pH is 3.2, and is in each pair of membrane operations voltage
It is handled under the conditions of 0.3V, obtains electrodialysis permeate and conductivity as the trapped fluid of 880 μ s/cm.
(4) electrodialysis trapped fluid passes through single-effect evaporation system, under the conditions of vacuum degree is 15kPa, is concentrated by evaporation to 10 times.
(5) concentrate enters crystallisation by cooling tank, and control cooling velocity is 1 DEG C/h, speed of agitator 50r/min, final cold
But to 6 DEG C, it is stirred for 4h, then passes through sedimentation separation, obtains glutamic acid crystal 111.7g, recycling glutamic acid reaches 62%.
(6) electrodialysis permeate is evaporated dense under the conditions of not imitating vacuum degree is 25kPa by two effect reduction vaporization systems
It is reduced to 4.5 times；Then it is transferred to again in the single-action forced evaporation crystallizer that vacuum degree is 20kPa and is concentrated 4 times.Concentrate enters cooling
Crystallizing tank, control cooling velocity are 2 DEG C/h, and speed of agitator 50r/min is finally cooled to 60 DEG C, is stirred for 3h, then passes through
Basket centrifuge separation is bored, ammonia sulfate crystal 517.3g is obtained, recycling ammonium sulfate reaches 94%.
(7) when being wherein concentrated by evaporation the condensed water that generates for during extracting glutamic acid cleaning and ultrafiltration membrane treatment it is clear
During washing, circulating and recovering is realized.
Embodiment 3
(1) electricity such as 7000mL glutamic acid concentration are taken to extract waste liquid, aminoglutaric acid concentration 30g/L, ammonium sulfate 95g/L pass through
The tubular ultra-filtration membrane that molecular cut off is 50kDa is handled, and control operation temperature is 32 DEG C, operating pressure 0.3MPa, and with clearly
Water washing obtains 7000mL membrane filtration clear liquid.
(2) 63g activated carbon (activated carbon additive amount is 9g/L) is added into membrane filtration clear liquid 7000mL, is taken off under the conditions of 55 DEG C
Color 50min, then filtering removes activated carbon and obtains destainer.
(3) destainer enters heterogeneous membrane electrodialysis process system, and destainer pH is 3.3, and is in each pair of membrane operations voltage
It is handled under the conditions of 0.6V, obtains electrodialysis permeate and conductivity as the trapped fluid of 1200 μ s/cm.
(4) electrodialysis trapped fluid passes through single-effect evaporation system, under the conditions of vacuum degree is 23kPa, is concentrated by evaporation to 7 times.
(5) concentrate enters crystallisation by cooling tank, and control cooling velocity is 3.5 DEG C/h, speed of agitator 60r/min, finally
10 DEG C are cooled to, 5h is stirred for, then passes through sedimentation separation, obtains glutamic acid crystal 92.6g, recycling glutamic acid reaches 44%.
(6) electrodialysis permeate is evaporated dense under the conditions of not imitating vacuum degree is 20kPa by two effect reduction vaporization systems
It is reduced to 3.5 times；Then it is transferred to again in the single-action forced evaporation crystallizer that vacuum degree is 20kPa and is concentrated 3.5 times.Concentrate enters cold
But crystallizing tank, control cooling velocity are 1 DEG C/h, and speed of agitator 55r/min is finally cooled to 58 DEG C, is stirred for 1h, then passes through
The separation of cone basket centrifuge is crossed, ammonia sulfate crystal 572.1g is obtained, recycling ammonium sulfate reaches 86%.
(7) condensed water generated when being wherein concentrated by evaporation, 15% condensed water replace corresponding ingredient water to be used for glutamic acid
Fermentation, fermentation results do not influence, and realize circulating and recovering.
Comparative example 1
It is turbid to obtain cleaner liquid in operating pressure 0.5MPa by the molecule interception 600kDa for the ultrafiltration membrane selected in step (1)
Degree is 52NTU, remaining condition and step are same as Example 1.It is final to obtain glutamic acid crystal 64.1g, ammonium sulfate 540.4g, paddy
The rate of recovery of propylhomoserin only has 36%, and the ammonium sulfate rate of recovery only has 78%, lower than the glutamic acid and sulphur of embodiment 1 under optimal condition
The rate of recovery of sour ammonium.
Comparative example 2
Ultrafiltration membrane treatment is not used in embodiment 1 or does not use decolorizing with activated carbon to handle, remaining condition and step and implementation
Example 1 is identical.The rate of recovery of final glutamic acid is respectively less than 8%, far below the recycling of the glutamic acid of embodiment 1 under optimal condition
Rate.
Comparative example 3
The feeding liquid pH during electrodialysis process is adjusted to 4.8 in step (3), the control of transmitance conductivity is 4500 μ
S/cm, remaining condition and step are same as Example 1.Final to obtain glutamic acid crystal 33.1g, the rate of recovery of glutamic acid only has
18.6%, far below total extract yield of embodiment 1 under optimal condition, and ammonium sulfate extract yield influences less.
Comparative example 4
In step (4), cycles of concentration is changed to 4 times in concentration process, single-action forced evaporation crystallizer is dense in step (6)
Demagnification number is changed to 2 times, remaining condition and step are same as Example 1, obtains glutamic acid crystal 22.4g, ammonia sulfate crystal
376.2g, the rate of recovery of glutamic acid only have 12.6%, and the rate of recovery of ammonium sulfate is 54.3%, real far below under optimal condition
Apply total extract yield of example 1.
Although the present invention has been described by way of example and in terms of the preferred embodiments, it is not intended to limit the invention, any to be familiar with this skill
The people of art can do various change and modification, therefore protection model of the invention without departing from the spirit and scope of the present invention
Enclosing subject to the definition of the claims.
Claims (10)
1. the recycling processing method that a kind of electricity such as glutamic acid concentration extract waste liquid, which is characterized in that the method are as follows: by paddy ammonia
The electric waste liquid that extracts such as sour concentration first passes through ultrafiltration membrane treatment acquisition film concentrate and membrane filtration clear liquid, and film concentrate passes through filtering, does
Dry acquisition mycoprotein, the membrane filtration clear liquid carry out electrodialysis process after decolorizing with activated carbon, obtain electrodialysis trapped fluid and
Electrodialysis permeate, the electrodialysis trapped fluid and electrodialysis permeate by evaporation and concentration, crystallisation by cooling and separate back respectively
Receipts obtain glutamic acid and ammonium sulfate, to realize the recycling treatment that the electricity such as glutamic acid concentration extract waste liquid.
2. a kind of electricity such as glutamic acid concentration according to claim 1 extract the recycling processing method of waste liquid, feature exists
In the evaporation condensed water obtained that is concentrated by evaporation is recycled to be used in glutamic acid fermentation or extraction technology of glutamic acid.
3. a kind of electricity such as glutamic acid concentration according to claim 1 or 2 extract the recycling processing method of waste liquid, feature
Be, the operating parameter of the ultrafiltration membrane is: 10~300kDa of molecular cut off, operation temperature are 15~40 DEG C, operating pressure
For 0.15~0.3MPa, crossflow velocity is 2~4m/s.
4. a kind of electricity such as glutamic acid concentration according to claim 3 extract the recycling processing method of waste liquid, feature exists
In membrane filtration clear liquid≤25NTU after the ultrafiltration membrane treatment.
5. a kind of electricity such as glutamic acid concentration according to any one of claims 1 to 4 extract the recycling processing method of waste liquid,
It is characterized in that, during the decolorizing with activated carbon, the active carbon is powder activated carbon；The additive amount of activated carbon be 5~
25g/L；Operating parameter are as follows: temperature is 40~70 DEG C, and bleaching time is 30~50min.
6. a kind of electricity such as any described glutamic acid concentration extracts the recycling processing method of waste liquid according to claim 1~5,
It is characterized in that, the film that the electrodialysis process uses is homogeneous membrane or heterogeneous membrane, and the pH of feeding liquid is controlled between 3.0~3.3；
When for homogeneous membrane, the operation voltage of each pair of film is 0.6~1.2V, when for heterogeneous membrane, the operation voltage of each pair of film for 0.3~
0.6V, conductivity≤2600 μ s/cm of control electrodialysis trapped fluid water outlet.
7. a kind of electricity such as any described glutamic acid concentration extracts the recycling processing method of waste liquid according to claim 1~6,
Be characterized in that, the processing of the evaporation and concentration of the electrodialysis trapped fluid for using negative pressure single effect evaporator or negative pressure double effect evaporator into
Row is concentrated by evaporation to 6~15 times, does not imitate the control of evaporator absolute pressure in 15~35kPa.
8. a kind of electricity such as any described glutamic acid concentration extracts the recycling processing method of waste liquid according to claim 1~7,
It is characterized in that, the evaporation and concentration processing of the electrodialysis permeate is concentrated into 3 to be first evaporated using decompression multi-effect evaporator
~6 times, then external circulation evaporator is forced to be evaporated 3~5 times of concentration using negative pressure single-action, last evaporator absolute pressure
Control is in 15~30kPa.
9. a kind of electricity such as any described glutamic acid concentration extracts the recycling processing method of waste liquid according to claim 1~8,
It is characterized in that, the crystallisation by cooling of electrodialysis trapped fluid gained concentrate after being concentrated by evaporation are as follows: controlling cooling rate is
0.5~4 DEG C/h carries out cooling down crystallization, and speed of agitator control is in 20~100r/min, and final cooling temperature control is 8~18
℃。
10. a kind of electricity such as any described glutamic acid concentration extracts the recycling processing method of waste liquid according to claim 1~9,
It is characterized in that, the crystallisation by cooling of electrodialysis permeate gained concentrate after being concentrated by evaporation are as follows: control cooling rate
Carry out cooling down crystallization for 0.5~2 DEG C/h, speed of agitator control in 30~60r/min, final cooling temperature control 50~
65℃。
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Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US20080102502A1 (en) * | 2006-10-25 | 2008-05-01 | Brian Foody | Inorganic salt recovery during processing of lignocellulosic feedstocks |
| CN102086159A (en) * | 2009-12-07 | 2011-06-08 | 江南大学 | Glutamic acid extraction method |
| CN104311337A (en) * | 2014-10-19 | 2015-01-28 | 内蒙古阜丰生物科技有限公司 | Method for producing liquid fertilizer by using glutamic acid wastewater |
| CN109232338A (en) * | 2018-11-09 | 2019-01-18 | 禄丰天宝磷化工有限公司 | A kind of isolation and purification method of methionine hydroxy analog |
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Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US20080102502A1 (en) * | 2006-10-25 | 2008-05-01 | Brian Foody | Inorganic salt recovery during processing of lignocellulosic feedstocks |
| CN102086159A (en) * | 2009-12-07 | 2011-06-08 | 江南大学 | Glutamic acid extraction method |
| CN104311337A (en) * | 2014-10-19 | 2015-01-28 | 内蒙古阜丰生物科技有限公司 | Method for producing liquid fertilizer by using glutamic acid wastewater |
| CN109232338A (en) * | 2018-11-09 | 2019-01-18 | 禄丰天宝磷化工有限公司 | A kind of isolation and purification method of methionine hydroxy analog |
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