CN110407388B - Recycling treatment method of glutamic acid concentrated isoelectric extraction waste liquid - Google Patents
Recycling treatment method of glutamic acid concentrated isoelectric extraction waste liquid Download PDFInfo
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- C01C1/24—Sulfates of ammonium
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- 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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Abstract
The invention discloses a recycling treatment method of glutamic acid concentrated isoelectric extraction waste liquid, belonging to the technical field of industrial fermentation. The technical scheme of the invention comprises the following steps: the method comprises the steps of firstly treating glutamic acid concentrated isoelectric extraction waste liquid with an ultrafiltration membrane to obtain membrane concentrated liquid and membrane filtrate, filtering and drying the membrane concentrated liquid to obtain mycoprotein, decoloring the membrane filtrate with activated carbon, then performing electrodialysis treatment to obtain electrodialysis trapped fluid and electrodialysis permeate, and respectively performing evaporation concentration, cooling crystallization and separation recovery on the electrodialysis trapped fluid and the electrodialysis permeate to obtain glutamic acid and ammonium sulfate, so that the recycling treatment of the glutamic acid concentrated isoelectric extraction waste liquid is realized. By the treatment method, glutamic acid and ammonium sulfate are recovered, the economic benefit of each ton of monosodium glutamate is improved by 300-500 yuan, mycoprotein with high side value is obtained, and waste gas pollution generated in spray drying in the traditional process is eliminated.
Description
Technical Field
The invention relates to a recycling method of glutamic acid concentrated isoelectric extraction waste liquid, in particular to a method for treating extracted waste water generated by concentrated isoelectric processes and realizing waste water recycling by utilizing technical means such as electrodialysis, ultrafiltration membranes and the like, belonging to the technical field of industrial fermentation.
Background
At present, the scheme for producing glutamic acid in China mainly depends on a fermentation method, and after the fermentation is finished, a concentrated isoelectric extraction process is adopted as a main extraction process, and the concentrated isoelectric extraction process comprises the following steps: glutamic acid fermentation liquor is subjected to the working procedures of evaporation concentration, continuous isoelectric treatment, cooling crystallization, centrifugal separation treatment and the like, glutamic acid crystals are obtained by extraction, the extraction process yield is generally between 86 and 89 percent, and the yield is low. In addition, the obtained glutamic acid extraction waste liquid is called concentrated isoelectric extraction waste liquid, and the concentrated isoelectric extraction waste liquid contains a large amount of thalli, pigments and high-concentration inorganic salt impurities, and also contains high-concentration ammonium sulfate (about 90-140 g/L) and glutamic acid with the normal concentration of 20-38 g/L. Because of the existence of thalli, impurities and the like, glutamic acid in the waste liquid cannot be directly recovered, and meanwhile, the waste liquid cannot be subjected to biochemical treatment, so that the glutamic acid loss is caused, and the environment is greatly damaged.
At present, a method for treating concentrated isoelectric extraction waste liquid is to change waste water into fertilizer by adopting a concentration and spray drying method so as to reduce the pollution of the extracted waste water to the environment, but factors such as a large amount of waste gas generated in the fertilizer production process, low fertilizer efficiency of the fertilizer and the like limit the production and sale of the fertilizer, and meanwhile, the low extraction yield of glutamic acid causes the reduction of benefits of monosodium glutamate production enterprises and influences the healthy development of monosodium glutamate production enterprises. The prior art also reports a process for extracting substances or recycling glutamic acid extraction waste liquid, but the extracted substances are generally dilute acid (such as sulfuric acid, nitric acid, hydrochloric acid and the like) and ammonia, and are recycled in the steps of isoelectric crystallization or ion exchange and the like, and glutamic acid in mother liquor is not extracted, under the condition, due to the low economic value of the dilute acid and the like and the high cost of air blowing deamination, ammonia absorption, dilute acid separation and the like, the process is difficult to meet the requirements of enterprises, and particularly in Chinese patent applications CN102100353A and CN 102125252A.
Therefore, a method capable of recovering glutamic acid and other substances from an electric extraction waste liquid such as glutamic acid concentration without increasing the cost has been continuously sought.
Disclosure of Invention
[ problem ] to provide a method for producing a semiconductor device
The existing treatment method of the glutamic acid concentration isoelectric extraction waste liquid has the problems of incapability of recovering glutamic acid, high material extraction cost, waste gas pollution and the like.
[ technical solution ] A
In order to solve the problems, the invention provides a method for treating glutamic acid concentration and other electric extraction waste liquid by processes of ultrafiltration membrane, activated carbon decolorization, electrodialysis, evaporative crystallization and the like, so that the aim of recovering mycoprotein, ammonium sulfate and glutamic acid from the extraction waste liquid is fulfilled, and evaporated condensed water can be recycled in production, thereby finally realizing the aim of recycling the extraction waste liquid. The method not only obtains the mycoprotein with high side value, but also recovers a large amount of glutamic acid and ammonium sulfate, basically eliminates the pollution of high-concentration extraction waste liquid and waste gas to the environment, reduces the consumption of water resources due to the recycling of evaporation condensed water, realizes considerable economic benefit and has good environmental benefit.
Specifically, the technical scheme of the invention is as follows: a recycling treatment method of glutamic acid concentrated isoelectric extraction waste liquid comprises the following steps: the method comprises the steps of firstly treating glutamic acid concentrated isoelectric extraction waste liquid with an ultrafiltration membrane to obtain membrane concentrated liquid and membrane filtrate, filtering and drying the membrane concentrated liquid to obtain mycoprotein, decoloring the membrane filtrate with activated carbon, then performing electrodialysis treatment to obtain electrodialysis trapped fluid and electrodialysis permeate, and respectively performing evaporation concentration, cooling crystallization and separation recovery on the electrodialysis trapped fluid and the electrodialysis permeate to obtain glutamic acid and ammonium sulfate, so that the recycling treatment of the glutamic acid concentrated isoelectric extraction waste liquid is realized.
Furthermore, the evaporation condensed water obtained by evaporation concentration can be recycled for glutamic acid fermentation or glutamic acid extraction process.
Furthermore, the ultrafiltration membrane is one of a tubular ultrafiltration membrane and a ceramic ultrafiltration membrane.
Further, the operating parameters of the ultrafiltration membrane are as follows: the molecular weight cutoff is 10-300 kDa, the operating temperature is 15-40 ℃, the operating pressure is 0.15-0.3 MPa, and the membrane surface flow rate is 2-4 m/s.
Further, the membrane filtrate after the ultrafiltration membrane treatment is less than or equal to 25 NTU.
Further, the filtration is preferably a filter press, preferably a plate filter, for the filtration operation.
Further, in the activated carbon decoloring process, the activated carbon is powdered activated carbon; the addition amount of the activated carbon is 5-25 g/L; the operating parameters are as follows: the temperature is 40-70 ℃, and the decoloring time is 30-50 min.
Further, before electrodialysis treatment is carried out on the decolorized solution decolorized by activated carbon, separation is carried out to remove the activated carbon; the separation is filtration or microfiltration, wherein the mode of separation does not affect the practice of the invention.
Further, the membrane used for the electrodialysis treatment is a homogeneous membrane or a heterogeneous membrane, and the pH value of the feed liquid is controlled to be 3.0-3.3; when the membrane is a homogeneous membrane, the operating voltage of each pair of membranes is 0.6-1.2V, when the membrane is a heterogeneous membrane, the operating voltage of each pair of membranes is 0.3-0.6V, and the conductivity of the effluent of the electrodialysis trapped fluid is controlled to be less than or equal to 2600 mus/cm.
Further, the pH of the feed liquid at the time of the electrodialysis treatment is preferably 3.2.
Further, the retention solution of electrodialysis is used as the feed solution of electrodialysis treatment for circulation treatment.
Further, the evaporation concentration treatment of the electrodialysis trapped fluid is to adopt a negative pressure single-effect evaporator or a negative pressure double-effect evaporator to carry out evaporation concentration to 6-15 times, and the absolute pressure of the last-effect evaporator is controlled at 15-35 kPa.
Further, the electrodialysis permeate is evaporated and concentrated to 3-6 times by adopting a pressure-reducing multi-effect evaporator, then evaporated and concentrated to 3-5 times by adopting a negative-pressure single-effect forced external circulation evaporator, and the absolute pressure of the ineffective evaporator is controlled to be 15-30 kPa; wherein, any one of 2-4 effect evaporators can be adopted as the multi-effect evaporator.
Further, the cooling crystallization and separation operation of the concentrated solution obtained after the electrodialysis trapped fluid is evaporated and concentrated is as follows: controlling the cooling rate to be 0.5-4 ℃/h, cooling and crystallizing, controlling the stirring speed to be 20-100 r/min, controlling the final cooling temperature to be 8-18 ℃, and then carrying out crystal growth, sedimentation and separation to obtain the glutamic acid crystal.
Further, the cooling crystallization and separation operation of the concentrated solution obtained after the electrodialysis permeate is evaporated and concentrated is as follows: controlling the cooling rate to be 0.5-2 ℃/h, cooling and crystallizing, controlling the stirring speed to be 30-60 r/min, controlling the final cooling temperature to be 50-65 ℃, and separating to obtain ammonium sulfate crystals.
Further, the separation means that the crystallized crystal slurry is separated by one of a centrifuge, a belt filter, a plate frame and the like to obtain glutamic acid crystals or ammonium sulfate crystals, and the implementation of the patent is not affected by adopting a centrifugal separation mode other than the above-mentioned centrifugal separation mode.
Further, the glutamic acid concentrated isoelectric extraction waste liquid is obtained by concentrating, continuously isoelectric, cooling, crystallizing and centrifugally separating glutamic acid fermentation liquid, wherein the concentration of glutamic acid in the glutamic acid extraction waste liquid is 20-38 g/L, and the pH value is 3.0-3.3.
The invention has the following beneficial technical effects:
1. according to the invention, 40-75% of glutamic acid and 70-95% of ammonium sulfate in the glutamic acid concentrated isoelectric extraction waste liquid can be recovered, and the economic benefit of each ton of monosodium glutamate is improved by 300-500 yuan;
2. the invention can eliminate the traditional spray drying process and eliminate the waste gas pollution caused by the traditional spray drying process;
3. the invention realizes the reclamation of the extracted wastewater, reduces the wastewater pollution and saves water resources.
Drawings
FIG. 1 is a general flow diagram of a recycling method of glutamic acid concentrated isoelectric extraction waste liquid.
Detailed Description
The method for measuring the content of the glutamic acid comprises the following steps: the measurement was carried out using the biosensor SBA-40.
The invention will now be further described, by way of example, with reference to figure 1:
example 1
(1) 6600mL of glutamic acid concentrated isoelectric extraction waste liquid is taken, the concentration of the glutamic acid is 27g/L, the ammonium sulfate is 105g/L, the waste liquid is processed by a tubular ultrafiltration membrane with the molecular weight cutoff of 200kDa, the operation temperature is controlled at 30 ℃, the operation pressure is 0.15MPa, the waste liquid is washed by clear water to obtain 6500mL of membrane filtration liquid with 20NTU, and the concentrated liquid is filtered, squeezed and dried to obtain mycoprotein.
(2) Adding 39g of activated carbon (the addition amount of the activated carbon is 6g/L) into 6500mL of membrane filtrate, decolorizing at 60 ℃ for 35min, and filtering to remove the activated carbon to obtain decolorized solution.
(3) The decolored solution enters a homogeneous membrane electrodialysis treatment system, the pH of the decolored solution is 3.2, and the decolored solution is treated under the condition that the operating voltage of each pair of membranes is 1.1V, so that electrodialysis permeate and trapped fluid with the conductivity of 1800 mu s/cm are obtained respectively.
(4) And (4) passing the electrodialysis trapped fluid through a single-effect evaporation system, and evaporating and concentrating to 8 times under the condition that the vacuum degree is 20 kPa.
(5) And (3) feeding the concentrated solution into a cooling crystallization tank, controlling the cooling speed to be 2.2 ℃/h and the stirring speed to be 55r/min, finally cooling to 12 ℃, stirring for 5h, and then performing settling separation to obtain 92.7g of glutamic acid crystals, wherein the recovered glutamic acid is 52%.
(6) The electrodialysis permeate passes through a double-effect reduced pressure evaporation system, and is evaporated and concentrated to 4 times under the condition that the ineffective vacuum degree is 25 kPa; then transferring the mixture into a single-effect forced evaporation crystallizer with the vacuum degree of 20kPa for concentration by 4 times. And (3) the concentrated solution enters a cooling crystallization tank, the cooling speed is controlled to be 1 ℃/h, the stirring speed is 55r/min, the concentrated solution is finally cooled to 55 ℃, the concentrated solution is stirred for 2h, then the concentrated solution is separated by a cone blue type centrifuge, 589g of ammonium sulfate crystals are obtained, and the recovered ammonium sulfate reaches 85%.
(7) Wherein, the condensed water produced in the evaporation concentration is partially used in the cleaning process in the glutamic acid extraction process, thereby realizing the recycling.
Example 2
(1) 5000mL of glutamic acid concentrated isoelectric extraction waste liquid is taken, the concentration of the glutamic acid is 36g/L, the ammonium sulfate is 110g/L, the glutamic acid concentrated isoelectric extraction waste liquid is treated by a tubular ultrafiltration membrane with the molecular weight cutoff of 100kDa, the operation temperature is controlled to be 40 ℃, the operation pressure is 0.2MPa, and the glutamic acid concentrated isoelectric extraction waste liquid is washed by clear water to obtain 5000mL of membrane filtrate.
(2) 60g of activated carbon (the addition amount of the activated carbon is 12g/L) is added into 5000mL of the membrane filtrate, decolorization is carried out for 30min at the temperature of 65 ℃, and then the activated carbon is removed by filtration to obtain decolorized liquid.
(3) The decolored solution enters an heterogeneous membrane electrodialysis treatment system, the pH of the decolored solution is 3.2, and the decolored solution is treated under the condition that the operating voltage of each pair of membranes is 0.3V, so that electrodialysis permeate and trapped fluid with the conductivity of 880 mu s/cm are obtained.
(4) And (4) passing the electrodialysis trapped fluid through a single-effect evaporation system, and evaporating and concentrating to 10 times under the condition that the vacuum degree is 15 kPa.
(5) And (3) feeding the concentrated solution into a cooling crystallization tank, controlling the cooling speed to be 1 ℃/h and the stirring speed to be 50r/min, finally cooling to 6 ℃, stirring for 4h, and then performing settling separation to obtain 111.7g of glutamic acid crystals, wherein the recovered glutamic acid content is 62%.
(6) The electrodialysis permeate passes through a double-effect reduced pressure evaporation system, and is evaporated and concentrated to 4.5 times under the condition that the ineffective vacuum degree is 25 kPa; then transferring the mixture into a single-effect forced evaporation crystallizer with the vacuum degree of 20kPa for concentration by 4 times. And (3) feeding the concentrated solution into a cooling crystallization tank, controlling the cooling speed to be 2 ℃/h and the stirring speed to be 50r/min, finally cooling to 60 ℃, stirring for 3h, and separating by using a cone blue type centrifuge to obtain 517.3g of ammonium sulfate crystals, wherein the recovered ammonium sulfate is 94%.
(7) Wherein, the condensed water generated during the evaporation and concentration is used for the cleaning in the glutamic acid extraction process and the ultrafiltration membrane treatment and cleaning process, thereby realizing the recycling.
Example 3
(1) 7000mL of glutamic acid concentrated isoelectric extraction waste liquid is taken, the concentration of the glutamic acid is 30g/L, the ammonium sulfate is 95g/L, the glutamic acid concentrated isoelectric extraction waste liquid is treated by a tubular ultrafiltration membrane with the molecular weight cutoff of 50kDa, the operation temperature is controlled to be 32 ℃, the operation pressure is 0.3MPa, and the glutamic acid concentrated isoelectric extraction waste liquid is washed by clear water to obtain 7000mL of membrane filtrate.
(2) 63g of activated carbon (the addition amount of the activated carbon is 9g/L) is added into 7000mL of membrane filtrate, decolorization is carried out for 50min at 55 ℃, and then the activated carbon is removed by filtration to obtain decolorized solution.
(3) The decolored solution enters an heterogeneous membrane electrodialysis treatment system, the pH of the decolored solution is 3.3, and the decolored solution is treated under the condition that the operating voltage of each pair of membranes is 0.6V, so that electrodialysis permeate and trapped fluid with the conductivity of 1200 mu s/cm are obtained. .
(4) And (4) carrying out evaporation concentration on the electrodialysis trapped fluid to 7 times by a single-effect evaporation system under the condition that the vacuum degree is 23 kPa.
(5) And (3) feeding the concentrated solution into a cooling crystallization tank, controlling the cooling speed to be 3.5 ℃/h and the stirring speed to be 60r/min, finally cooling to 10 ℃, stirring for 5h, and then performing settling separation to obtain 92.6g of glutamic acid crystals, wherein the recovered glutamic acid is 44%.
(6) The electrodialysis permeate passes through a double-effect reduced pressure evaporation system, and is evaporated and concentrated to 3.5 times under the condition that the ineffective vacuum degree is 20 kPa; then transferring the mixture into a single-effect forced evaporation crystallizer with the vacuum degree of 20kPa for concentration by 3.5 times. And (3) feeding the concentrated solution into a cooling crystallization tank, controlling the cooling speed to be 1 ℃/h, stirring at the rotating speed of 55r/min, finally cooling to 58 ℃, stirring for 1h, separating by using a cone blue type centrifuge to obtain 572.1g of ammonium sulfate crystals, and recovering 86% of ammonium sulfate.
(7) Wherein, the condensed water generated during evaporation and concentration, 15 percent of condensed water replaces corresponding ingredient water for glutamic acid fermentation, the fermentation result has no influence, and the recycling is realized.
Comparative example 1
The molecular cut-off of the ultrafiltration membrane selected in the step (1) is 600kDa, the turbidity of the obtained filtrate is 52NTU under the operation pressure of 0.5MPa, and the rest conditions and steps are the same as those in the example 1. 64.1g of glutamic acid crystals and 540.4g of ammonium sulfate were finally obtained, and the recovery rate of glutamic acid was only 36%, and the recovery rate of ammonium sulfate was only 78%, which was lower than that of glutamic acid and ammonium sulfate in example 1 under the optimum conditions.
Comparative example 2
In example 1, no ultrafiltration membrane treatment or activated carbon decolorization treatment was used, and the remaining conditions and steps were the same as in example 1. The final glutamic acid recovery rates are all less than 8%, which is far lower than the glutamic acid recovery rate of example 1 under the optimized conditions.
Comparative example 3
In the step (3), the pH of the feed liquid during the electrodialysis treatment was adjusted to 4.8, and the permeability conductivity was controlled to 4500. mu.s/cm, and the other conditions and steps were the same as those in example 1. The final yield of glutamic acid crystals was 33.1g, the recovery of glutamic acid was only 18.6%, which is much lower than the total extraction yield of example 1 under optimized conditions, while the extraction yield of ammonium sulfate was not much affected.
Comparative example 4
In the step (4), the concentration multiple is changed into 4 times in the concentration process, the concentration multiple of the single-effect forced evaporation crystallizer in the step (6) is changed into 2 times, the rest conditions and the steps are the same as those of the embodiment 1, 22.4g of glutamic acid crystals and 376.2g of ammonium sulfate crystals are obtained, the recovery rate of the glutamic acid is only 12.6 percent, the recovery rate of the ammonium sulfate is 54.3 percent, and the total extraction yield is far lower than that of the embodiment 1 under the optimized conditions.
Although the present invention has been described with reference to the preferred embodiments, it should be understood that various changes and modifications can be made therein by those skilled in the art without departing from the spirit and scope of the invention as defined in the appended claims.
Claims (30)
1. A recycling treatment method of glutamic acid concentrated isoelectric extraction waste liquid is characterized by comprising the following steps: treating the glutamic acid concentrated isoelectric extraction waste liquid with an ultrafiltration membrane to obtain membrane concentrated liquid and membrane filtrate, filtering and drying the membrane concentrated liquid to obtain mycoprotein, decoloring the membrane filtrate with activated carbon, performing electrodialysis treatment to obtain electrodialysis trapped fluid and electrodialysis permeate, and performing evaporation concentration, cooling crystallization and separation recovery on the electrodialysis trapped fluid and the electrodialysis permeate to obtain glutamic acid and ammonium sulfate, so that the glutamic acid concentrated isoelectric extraction waste liquid is recycled; the turbidity of a membrane filtrate treated by the ultrafiltration membrane is less than or equal to 25NTU, the pH of an electrodialysis treatment feed liquid is controlled to be 3.0-3.3, the conductivity of outlet water of an electrodialysis trapped liquid is controlled to be less than or equal to 2600 microseconds/cm, the glutamic acid concentrated isoelectric extraction waste liquid is waste liquid obtained by concentrating, continuously isoelectric, cooling, crystallizing and centrifugally separating glutamic acid fermentation liquid, and the glutamic acid concentration in the waste liquid is 20-38 grams per liter.
2. The method for recycling glutamic acid concentrated isoelectric extraction waste liquid according to claim 1, wherein the evaporation condensate obtained by evaporation concentration is recycled for glutamic acid fermentation or glutamic acid extraction process.
3. The resource treatment method of the glutamic acid concentrated isoelectric extraction waste liquid according to claim 1 or 2, characterized in that the operating parameters of the ultrafiltration membrane are as follows: the molecular weight cutoff is 10-300 kDa, the operating temperature is 15-40 ℃, the operating pressure is 0.15-0.3 MPa, and the membrane surface flow rate is 2-4 m/s.
4. The resource treatment method of the glutamic acid concentrated isoelectric extraction waste liquid according to claim 1 or 2, characterized in that in the activated carbon decolorization process, the activated carbon is powdered activated carbon; the adding amount of the activated carbon is 5-25 g/L; the operating parameters are as follows: the temperature is 40-70 ℃, and the decoloring time is 30-50 min.
5. The resource treatment method of the glutamic acid concentrated isoelectric extraction waste liquid according to claim 3, characterized in that in the activated carbon decolorization process, the activated carbon is powdered activated carbon; the adding amount of the activated carbon is 5-25 g/L; the operating parameters are as follows: the temperature is 40-70 ℃, and the decoloring time is 30-50 min.
6. The method for recycling glutamic acid concentrated isoelectric extraction waste liquid according to any one of claims 1, 2 and 5, wherein the membrane used for the electrodialysis treatment is a homogeneous membrane or a heterogeneous membrane; when the membrane is a homogeneous membrane, the operating voltage of each pair of membranes is 0.6-1.2V, and when the membrane is a heterogeneous membrane, the operating voltage of each pair of membranes is 0.3-0.6V.
7. The method for recycling glutamic acid concentrated isoelectric extraction waste liquid according to claim 3, wherein the membrane used for the electrodialysis treatment is a homogeneous membrane or a heterogeneous membrane; when the membrane is a homogeneous membrane, the operating voltage of each pair of membranes is 0.6-1.2V, and when the membrane is a heterogeneous membrane, the operating voltage of each pair of membranes is 0.3-0.6V.
8. The method for recycling glutamic acid concentrated isoelectric extraction waste liquid according to claim 4, wherein the membrane used for the electrodialysis treatment is a homogeneous membrane or a heterogeneous membrane; when the membrane is a homogeneous membrane, the operating voltage of each pair of membranes is 0.6-1.2V, and when the membrane is a heterogeneous membrane, the operating voltage of each pair of membranes is 0.3-0.6V.
9. The method for recycling glutamic acid concentrated isoelectric extraction waste liquid according to any one of claims 1, 2, 5, and 7-8, wherein the evaporation concentration treatment of the electrodialysis retentate is performed by adopting a negative pressure single-effect evaporator or a negative pressure double-effect evaporator to 6-15 times.
10. The method for recycling glutamic acid concentrated isoelectric extraction waste liquid according to claim 3, wherein the evaporation concentration treatment of the electrodialysis retentate is to carry out evaporation concentration to 6-15 times by using a negative pressure single-effect evaporator or a negative pressure double-effect evaporator.
11. The resource treatment method of the glutamic acid concentrated isoelectric extraction waste liquid according to claim 4, wherein the evaporation concentration treatment of the electrodialysis trapped fluid is to adopt a negative pressure single-effect evaporator or a negative pressure double-effect evaporator to carry out evaporation concentration to 6-15 times.
12. The method for recycling glutamic acid concentrated isoelectric extraction waste liquid according to claim 6, wherein the electrodialysis retentate is evaporated and concentrated to 6-15 times by using a negative pressure single-effect evaporator or a negative pressure double-effect evaporator.
13. The method for recycling glutamic acid-concentrated electric extraction waste liquid according to any one of claims 1, 2, 5, 7 to 8 and 10 to 12, wherein the evaporation and concentration treatment of the electrodialysis permeate is carried out by evaporating and concentrating to 3 to 6 times by using a pressure-reducing multi-effect evaporator and then evaporating and concentrating to 3 to 5 times by using a negative-pressure single-effect forced external circulation evaporator.
14. The method for recycling glutamic acid concentrated isoelectric extraction waste liquid according to claim 3, wherein the evaporation concentration treatment of the electrodialysis permeate is to perform evaporation concentration to 3-6 times by using a reduced-pressure multi-effect evaporator, and then perform evaporation concentration to 3-5 times by using a negative-pressure single-effect forced external circulation evaporator.
15. The method for recycling glutamic acid concentrated isoelectric extraction waste liquid according to claim 4, wherein the evaporation concentration treatment of the electrodialysis permeate is to perform evaporation concentration to 3-6 times by using a reduced-pressure multi-effect evaporator, and then perform evaporation concentration to 3-5 times by using a negative-pressure single-effect forced external circulation evaporator.
16. The method for recycling glutamic acid concentrated isoelectric extraction waste liquid according to claim 6, wherein the evaporation concentration treatment of the electrodialysis permeate is to perform evaporation concentration to 3-6 times by using a reduced-pressure multi-effect evaporator, and then perform evaporation concentration to 3-5 times by using a negative-pressure single-effect forced external circulation evaporator.
17. The method as claimed in claim 9, wherein the electrodialysis permeate is evaporated and concentrated to 3-6 times by using a reduced-pressure multi-effect evaporator, and then evaporated and concentrated to 3-5 times by using a negative-pressure single-effect forced external circulation evaporator.
18. The method for recycling glutamic acid concentrated isoelectric extraction waste liquid according to any one of claims 1, 2, 5, 7-8, 10-12, and 14-17, wherein the cooling crystallization of the concentrated solution obtained after the electrodialysis trapped fluid is evaporated and concentrated is as follows: controlling the cooling rate to be 0.5-4 ℃/h, cooling and crystallizing, controlling the stirring speed to be 20-100 r/min, and controlling the final cooling temperature to be 8-18 ℃.
19. The method for recycling glutamic acid concentrated isoelectric extraction waste liquid according to claim 3, wherein the cooling crystallization of the concentrate obtained after the electrodialysis retentate is evaporated and concentrated is as follows: controlling the cooling rate to be 0.5-4 ℃/h, cooling and crystallizing, controlling the stirring speed to be 20-100 r/min, and controlling the final cooling temperature to be 8-18 ℃.
20. The method for recycling glutamic acid concentrated isoelectric extraction waste liquid according to claim 4, wherein the cooling crystallization of the concentrate obtained after the electrodialysis retentate is evaporated and concentrated is as follows: controlling the cooling rate to be 0.5-4 ℃/h, cooling and crystallizing, controlling the stirring speed to be 20-100 r/min, and controlling the final cooling temperature to be 8-18 ℃.
21. The method for recycling glutamic acid concentrated isoelectric extraction waste liquid according to claim 6, wherein the cooling crystallization of the concentrate obtained after the electrodialysis retentate is evaporated and concentrated is as follows: controlling the cooling rate to be 0.5-4 ℃/h, cooling and crystallizing, controlling the stirring speed to be 20-100 r/min, and controlling the final cooling temperature to be 8-18 ℃.
22. The method for recycling glutamic acid concentrated isoelectric extraction waste liquid according to claim 9, wherein the cooling crystallization of the concentrate obtained after the electrodialysis retentate is evaporated and concentrated is as follows: controlling the cooling rate to be 0.5-4 ℃/h, cooling and crystallizing, controlling the stirring speed to be 20-100 r/min, and controlling the final cooling temperature to be 8-18 ℃.
23. The method for recycling glutamic acid concentrated isoelectric extraction waste liquid according to claim 13, wherein the cooling crystallization of the concentrate obtained after the electrodialysis retentate is evaporated and concentrated is: controlling the cooling rate to be 0.5-4 ℃/h, cooling and crystallizing, controlling the stirring speed to be 20-100 r/min, and controlling the final cooling temperature to be 8-18 ℃.
24. The method for recycling a glutamic acid-concentrated electric extraction waste liquid according to any one of claims 1, 2, 5, 7 to 8, 10 to 12, 14 to 17, and 19 to 23, wherein a cooling crystallization of a concentrated solution obtained by evaporating and concentrating the electrodialysis permeate is: controlling the cooling rate to be 0.5-2 ℃/h, cooling and crystallizing, controlling the stirring speed to be 30-60 r/min, and controlling the final cooling temperature to be 50-65 ℃.
25. The method for recycling glutamic acid concentrated isoelectric extraction waste liquid according to claim 3, wherein the cooling crystallization of the concentrated solution obtained by evaporating and concentrating the electrodialysis permeate is as follows: controlling the cooling rate to be 0.5-2 ℃/h, cooling and crystallizing, controlling the stirring speed to be 30-60 r/min, and controlling the final cooling temperature to be 50-65 ℃.
26. The method for recycling glutamic acid concentrated isoelectric extraction waste liquid according to claim 4, wherein the cooling crystallization of the concentrated solution obtained by evaporating and concentrating the electrodialysis permeate is as follows: controlling the cooling rate to be 0.5-2 ℃/h, cooling and crystallizing, controlling the stirring speed to be 30-60 r/min, and controlling the final cooling temperature to be 50-65 ℃.
27. The method for recycling glutamic acid concentrated isoelectric extraction waste liquid according to claim 6, wherein the cooling crystallization of the concentrate obtained by evaporating and concentrating the electrodialysis permeate is as follows: controlling the cooling rate to be 0.5-2 ℃/h, cooling and crystallizing, controlling the stirring speed to be 30-60 r/min, and controlling the final cooling temperature to be 50-65 ℃.
28. The method for recycling glutamic acid concentrated isoelectric extraction waste liquid according to claim 9, wherein the cooling crystallization of the concentrate obtained by evaporating and concentrating the electrodialysis permeate is: controlling the cooling rate to be 0.5-2 ℃/h, cooling and crystallizing, controlling the stirring speed to be 30-60 r/min, and controlling the final cooling temperature to be 50-65 ℃.
29. The method for recycling glutamic acid concentrated isoelectric extraction waste liquid according to claim 13, wherein the cooling crystallization of the concentrate obtained by evaporating and concentrating the electrodialysis permeate is: controlling the cooling rate to be 0.5-2 ℃/h, cooling and crystallizing, controlling the stirring speed to be 30-60 r/min, and controlling the final cooling temperature to be 50-65 ℃.
30. The method for recycling glutamic acid concentrated isoelectric extraction waste liquid according to claim 18, wherein the cooling crystallization of the concentrate obtained by evaporating and concentrating the electrodialysis permeate is: controlling the cooling rate to be 0.5-2 ℃/h, cooling and crystallizing, controlling the stirring speed to be 30-60 r/min, and controlling the final cooling temperature to be 50-65 ℃.
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| 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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| Publication number | Priority date | Publication date | Assignee | Title |
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| 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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