CN109422661A - A method of leucine is extracted using corn protein powder - Google Patents
A method of leucine is extracted using corn protein powder Download PDFInfo
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- CN109422661A CN109422661A CN201710737885.7A CN201710737885A CN109422661A CN 109422661 A CN109422661 A CN 109422661A CN 201710737885 A CN201710737885 A CN 201710737885A CN 109422661 A CN109422661 A CN 109422661A
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- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C227/00—Preparation of compounds containing amino and carboxyl groups bound to the same carbon skeleton
- C07C227/38—Separation; Purification; Stabilisation; Use of additives
- C07C227/40—Separation; Purification
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Abstract
The present invention relates to a kind of methods for extracting leucine using corn protein powder, it is characterised in that the following steps are included: step 1: the hydrolysis stage of corn protein powder；Step 2: I preparatory phase of leucine crude product；Step 3: II preparatory phase of leucine crude product；Step 4: leucine finished product preparatory phase.The present invention utilizes corn protein powder as a raw material for production using the method that corn protein powder extracts leucine, and price is cheaper, substantially reduces production cost.Product purity made from method of the invention simultaneously is very high, and the process conditions of production are relatively simple, are more suitable for use of large-scale production.
Description
Technical field
The invention belongs to chemical technology field more particularly to a kind of methods for extracting leucine using corn protein powder.
Background technique
Leucine is a kind of main biogenetic products, is widely used in fields such as medicine, food.Leucine is generally multi-purpose
In bread, dough product；Prepare amino acid transfusion and comprehensive amino acid preparation, Hypoylycemic agents, plant growth promoter；It can be used as
Fragrance can improve flavour of food products.In pharmaceuticals industry, L-Leu is that the compound amino acid intravenous fluid of Clinical Selection is indispensable
Few raw material, for maintaining the nutritional need of urgent patient, the life for rescuing patient plays positive effect；Leucine is also being adjusted
It plays an important role in terms of section amino acid and protein metabolism.The study found that leucine is uniquely adjusted in skeletal muscle and cardiac muscle
The amino acid of Protein Turnover.In addition, also some researches show that leucine can promote the synthesis of skeletal muscle protein.Leucine
One ketoisocaproate of metabolite also has the function of the metabolism of regulatory protein matter, and the market prospects of leucine are boundless.
Currently, the manufacturing condition for extracting leucine is all more complicated, the reaction time is long, high production cost, right
It is low in the utilization rate of raw material.It is had not been reported simultaneously about the technique for extracting leucine using corn protein powder.
Summary of the invention
The present invention devises a kind of method for extracting leucine using corn protein powder, and its purpose is to provide a kind of utilizations
The reactant of this relative low price of corn protein powder as raw material, meanwhile, reaction condition requires simple, and production cost is low,
Product purity is high, is suitable for the extracting method of the leucine of large-scale promotion.
To achieve the goals above, present invention employs following scheme:
A method of leucine is extracted using corn protein powder, it is characterised in that the following steps are included:
Step 1: the hydrolysis stage of corn protein powder；
Step 2: I preparatory phase of leucine crude product；
Step 3: II preparatory phase of leucine crude product；
Step 4: leucine finished product preparatory phase.
The hydrolysis stage of corn protein powder described in step 1 is that hydrochloric acid is first added into reaction vessel, adds corn egg
White powder opens steam valve heating, and vapour pressure is not more than 0.2Mpa, and keeping temperature is 105 DEG C -115 DEG C, complete to corn protein powder
Start to calculate hydrolysis time after dissolution, carry out heat preservation hydrolysis, the time of hydrolysis is -10 hours 6 hours, hydrolysis
After, starting vacuum pump carries out catching up with acid, and catching up with the sour time is -3 hours 1 hour, cooling treatment is carried out after catching up with acid, when hydrolysis liquid cooling
But to after 40 DEG C or less, turn off coolant valve, hydrolyzate is squeezed into plate and frame filter press and is filtered, after having filtered, use 300L-
The tap water of 500L rushes first filter residue, and flushing water merges hydrolyzate and is pumped into tone pitch tank.
I preparatory phase of leucine crude product described in step 2 is a N-process, and a N-process is that will walk
Rapid one hydrolyzate filtrate and the flushing water for rinsing filter residue are put into after tone pitch tank plus ammonium hydroxide adjusts pH value to 2.8-3.0, control temperature
Degree is 40 DEG C -50 DEG C；Then the hydrolyzate after tone pitch is sucked into concentration tank, opens steam valve, heating, Steam pressure control
0.15Mpa-0.2Mpa, it is to be concentrated to stop concentration to after there is mass crystallization, a concentrate is squeezed into cooling tank, starting is stirred
It mixes, opens cooling water, a concentrate is cooled to room temperature；A concentrate for being cooled to room temperature is pumped into plate and frame filter press to carry out
Filtering, removing the resulting solid of filtrate is leucine crude product I.
II preparatory phase of leucine crude product described in step 3 includes a decolorization and secondary N-process.
Decolorization of the step 3 is to put into leucine crude product I in bleacher, according to leucine crude product
Mass content is salt acid for adjusting pH value to be added to 0.5-1.0, the hydrochloric acid molar concentration should be after water is added in 35% ratio
0.6mol-1.0mol；Be completely dissolved leucine crude product I, and measure material liquid volume, open steam valve be heated to 60 DEG C-
65 DEG C, the additional amount of the activated carbon after purification is added, the purification active carbon is every 1000L solution 30kg-80kg, keeps the temperature 30 points
Zhong Hou, filtering, filtrate are shallow dark brown；
The secondary N-process of the step 3 is that the filtrate after primary decoloration is put into secondary neutralizing tank, is passed through into tank
Concentration is the ammonium hydroxide of 8mol-12mol, and temperature control is 42 DEG C -47 DEG C, adjusts pH value to 4.5-4.8, the secondary neutralization when
Between be -4 hours 3 hours, after being then cooled to room temperature secondary neutralizer, be pumped into plate and frame filter press and be filtered, remove filtrate
The bagging and weighing after being centrifuged and doing of solid afterwards is leucine crude product II.
Leucine finished product preparatory phase described in step 4 includes secondary decolourization process, fine work concentration process and post-processed
Journey；The secondary decolourization process is that leucine crude product II and water are added into bleacher, described according to leucine crude product II
Additional amount with water is that the mass concentration of control leucine crude product II is 6.0%；Open steam valve heating, stirring, temperature control
System is at 40 DEG C -45 DEG C, after leucine crude product II is completely dissolved, liquid sodium hydroxide is added into tank and adjusts pH to 6.0-7.0,
The liquid sodium hydroxide mass concentration is 30%-42%, and measures material liquid volume, and refined using active carbon is then added, described
Refine active carbon additional amount be every 1000L solution 4kg-30kg, when be back to liquid it is limpid when, sampling analysis solution light transmission
Filtrate is put to high-order material-storage jar when light transmittance reaches 100%, crosses anion-exchange column, remove impurity by rate；
The fine work concentration process is that will be put into reacting tank body by the feed liquid of anion-exchange column processing, control material
Liquid height is reacting tank body 2/3；Steam valve is opened, control vapour pressure is not more than 0.2Mpa, it is dense to be warming up to 80 DEG C of -85 DEG C of progress
Contracting closes steam when the intracorporal material liquid volume of tank is concentrated into original volume 1/10, closes cooling water, closes vacuum, opens exhaust-valve, will
Fine work enriched product is transferred in crystallization cylinder；
The last handling process is to cover after fine work enriched product is transferred to completely in crystallization cylinder, open cooling water
Crystallisation by cooling, it is described by the transferred product after crystallization to centrifuge when the feed liquid temperature in crystallization cylinder is down to 45 DEG C -50 DEG C
600-900 revs/min of centrifuge speed, centrifugation time is -20 minutes 10 minutes, after centrifugation is dry, deionized water such as is added to wash repeatedly
It washs；Finished product of the washing after qualified is moved into double-cone vacuum drier, holding vacuum degree is -0.06--0.08Mpa, opens steam valve
Door, pressure control should be not more than 0.1Mpa, and heating, keeping temperature is 60 DEG C -65 DEG C, after -2.5 hours 2 hours dry, discharging；
After product is cooled to room temperature, 12-15 mesh is crossed, obtains leucine finished product according to product requirement weighing packaging.
It is carried out in hydrolytic process described in step 1 plus vapour is handled, in first 4 hours plus vapour frequency of hydrolysis
For 10-15 minutes plus straight-through vapour was primary, was every time 5-10 seconds；Afterwards 4 hours every 15-20 minutes it is straight-through plus vapour is primary, be every time 6-8
Second, hydrolysis liquid level keeps slightly boiled and stirs state.
Corn protein powder described in step 1 and hydrochloric acid are according to 1 ton of corn protein powder: the ratio of the hydrochloric acid of 1.5 cubic meter volumes
Example feeds intake.
It for adjusting pH value to obtain the concentration of ammonium hydroxide be mass concentration is 15%-22% ammonium hydroxide described in step 2.
It is primary at interval of feed supplement in 6 hours in fine work concentration process described in step 4, guarantee that the intracorporal feed liquid height of tank is
Reacting tank body 2/3；
In the crystallization process of last handling process described in step 4, need to wash crystallized product the water to centrifugation without nitre
Sour silver reaction.
This is had the advantages that using the method that corn protein powder extracts leucine
The present invention utilizes corn protein powder as a raw material for production using the method that corn protein powder extracts leucine, and price is more
Add cheap, substantially reduces production cost.Product purity made from method of the invention simultaneously is very high, and the process conditions of production are more
Simply, it is more suitable for use of large-scale production.
It is carried out in hydrolytic process described in step 1 plus vapour is handled, in first 4 hours plus vapour frequency of hydrolysis
For 10-15 minutes plus straight-through vapour was primary, was every time 5-10 seconds；Afterwards 4 hours every 15-20 minutes it is straight-through plus vapour is primary, be every time 6-8
Second, hydrolysis liquid level keeps slightly boiled and stirs state.In the present invention plus vapour is that air is added in hydrolytic decomposition pot using air compressor machine, mesh
Be in order to stir the hydrolysis material in tank using compressed air, be allowed to uniformly hydrolyze thoroughly, improve yield.
Specific embodiment
Combined with specific embodiments below, the present invention will be further described.
Embodiment
The invention discloses a kind of methods for extracting leucine using corn protein powder, it is characterised in that including following step
It is rapid: step 1: the hydrolysis stage of corn protein powder；Step 2: I preparatory phase of leucine crude product；Step 3: leucine crude product II
Preparatory phase；Step 4: leucine finished product preparatory phase.
The hydrolysis stage of the corn protein powder of step 1 is that hydrochloric acid is first added into reaction vessel, adds zein
Powder, corn protein powder and hydrochloric acid described in step 1 are according to 1 ton of corn protein powder: the ratio of the hydrochloric acid of 1.5 cubic meter volumes into
Row feeds intake.Steam valve heating is opened, vapour pressure is not more than 0.2Mpa, and keeping temperature is 105 DEG C -115 DEG C, complete to corn protein powder
Start to calculate hydrolysis time after fully dissolved, carry out heat preservation hydrolysis, the time of hydrolysis is -10 hours 6 hours, and hydrolysis is anti-
After answering, starting vacuum pump carries out catching up with acid, and catching up with the sour time is -3 hours 1 hour, carries out cooling treatment after catching up with acid, works as hydrolyzate
After being cooled to 40 DEG C or less, turn off coolant valve, hydrolyzate is squeezed into plate and frame filter press and is filtered, filtrate is continued to employ.Feed liquid mistake
After having filtered, first filter residue is rushed with 400L or so tap water, flushing water merges hydrolyzate and is pumped into tone pitch tank.
I preparatory phase of leucine crude product described in step 2 is a N-process, and a N-process is that will walk
Rapid one hydrolyzate filtrate and the flushing water for rinsing filter residue are put into after tone pitch tank plus ammonium hydroxide adjusts pH value to 2.8-3.0, step 2
Described for adjusting pH value to obtain the concentration of ammonium hydroxide be mass concentration is 15%-22% ammonium hydroxide.Controlled at 40 DEG C -50 DEG C；
Then the hydrolyzate after tone pitch is sucked into concentration tank, opens steam valve, heating, Steam pressure control 0.15Mpa-
0.2Mpa, it is to be concentrated to stop concentration to after there is mass crystallization, a concentrate is squeezed into cooling tank, starting stirring is opened cold
Concentrate is cooled to room temperature by but water；A concentrate for being cooled to room temperature is pumped into plate and frame filter press to be filtered, is removed
The resulting solid of filtrate is leucine crude product I.This step needs to detect thermal concentration liquid Baume degrees >=24 °, and notes down.
II preparatory phase of step 3 leucine crude product includes a decolorization and secondary N-process.Step 3 it is primary
Decolorization is to put into leucine crude product I in bleacher, and the mass content according to leucine crude product is that water is added in 35% ratio
Afterwards, salt acid for adjusting pH value is added to 0.5-1.0, the hydrochloric acid molar concentration should be 0.6mol-1.0mol；Make leucine crude product I
It is completely dissolved, and measures material liquid volume, open steam valve and be heated to 60 DEG C -65 DEG C, the activated carbon after purification is added is described
The additional amount for refining active carbon is every 1000L solution 30kg-80kg, and after heat preservation 30 minutes, filtering, filtrate is shallow dark brown；Once
Decolourize liquid yield control range >=96%.Calculation method are as follows: (material liquid volume after material liquid volume/acid adding after filtering) × 100%.
The secondary N-process of step 3 is that the filtrate after primary decoloration is put into secondary neutralizing tank, and concentration is passed through into tank
For the ammonium hydroxide of 8mol-12mol, temperature control is 42 DEG C -47 DEG C, adjusts pH value to 4.5-4.8, and the time of the secondary neutralization is
It -4 hours 3 hours, after being then cooled to room temperature secondary neutralizer, is pumped into plate and frame filter press and is filtered, after removing filtrate
Solid bagging and weighing after being centrifuged and doing is leucine crude product II.Leucine crude product II yield control range after secondary neutralization
10%-15%.Calculation method are as follows: (crude product II weight/crude product I weight) × 100%.
Leucine finished product preparatory phase described in step 4 includes secondary decolourization process, fine work concentration process and post-processed
Journey；The secondary decolourization process is that leucine crude product II and water are added into bleacher, described according to leucine crude product II
Additional amount with water is that the mass concentration of control leucine crude product II is 6.0%；Open steam valve heating, stirring, temperature control
System is at 40 DEG C -45 DEG C, after leucine crude product II is completely dissolved, liquid sodium hydroxide is added into tank and adjusts pH to 6.0-7.0,
The liquid sodium hydroxide mass concentration is 30%-42%, and measures material liquid volume, and refined using active carbon is then added, described
Refine active carbon additional amount be every 1000L solution 4kg-30kg, when be back to liquid it is limpid when, sampling analysis solution light transmission
Filtrate is put to high-order material-storage jar when light transmittance reaches 100%, crosses anion-exchange column, remove impurity by rate；Secondary decolourization
Afterwards, the SO42- in sampling analysis solution needs theoretical barium chloride dosage, as just a kind of detection method.
Fine work concentration process is to control feed liquid height for being put into reacting tank body by the feed liquid of anion-exchange column processing
For reacting tank body 2/3；Steam valve is opened, control vapour pressure is not more than 0.2Mpa, is warming up to 80 DEG C -85 DEG C and is concentrated, when
When the intracorporal material liquid volume of tank is concentrated into original volume 1/10, steam is closed, closes cooling water, closes vacuum, opens exhaust-valve, fine work is dense
Contracting product is transferred in crystallization cylinder；It is primary at interval of feed supplement in 6 hours in step 4 fine work concentration process, guarantee the intracorporal feed liquid of tank
Height is reacting tank body 2/3；
The last handling process of step 4 is to cover after fine work enriched product is transferred to completely in crystallization cylinder, open cooling
Water crystallisation by cooling, when crystallizing the feed liquid temperature in cylinder and being down to 45 DEG C -50 DEG C, by the transferred product after crystallization to centrifuge, from
600-900 revs/min of scheming revolving speed, centrifugation time are -20 minutes 10 minutes, after centrifugation is dry, deionized water such as are added to wash repeatedly；It will
Finished product after washing is qualified moves into double-cone vacuum drier, and holding vacuum degree is -0.06--0.08Mpa, opens steam valve, pressure
Power control should be not more than 0.1Mpa, and heating, keeping temperature is 60 DEG C -65 DEG C, after -2.5 hours 2 hours dry, discharging；To product
After being cooled to room temperature, 12-15 mesh is crossed, obtains leucine finished product according to product requirement weighing packaging.Step 4 post-processed
In the crystallization process of journey, need to wash crystallized product the water to centrifugation without nitric acid silver reaction.In practical operation, in crystallization
It was stirred in the process every 15 minutes with poly- third sticking plaster primary.
It in practical application, is packed generally according to every bag of 25kg/ with vinyon inner membrance, moves into intermediate station and place, wait take out
After sample analysis is qualified, after loading onto outer packaging barrel packaging, lot number is stamped, is put in storage.Product yield control range 55%-60% is calculated
Method are as follows: (II weight of crude product is thrown in total weight/decoloration after dry) × 100%.
It is carried out in step 1 solution preocess plus vapour is handled, be 10-15 points first 4 hours of hydrolysis plus vapour frequency
Clock adds straight-through vapour primary, is every time 5-10 seconds；Afterwards 4 hours every 15-20 minutes it is straight-through plus vapour is primary, be every time 6-8 seconds, hydrolyzate
Face keeps slightly boiled and stirs state.In the present invention plus vapour is that air is added in hydrolytic decomposition pot using air compressor machine, in order to
The hydrolysis material in tank is stirred using compressed air, is allowed to uniformly hydrolyze thoroughly, is improved yield.
The present invention utilizes corn protein powder as a raw material for production using the method that corn protein powder extracts leucine, and price is more
Add cheap, substantially reduces production cost.Product purity made from method of the invention simultaneously is very high, and the process conditions of production are more
Simply, it is more suitable for use of large-scale production.
Above in conjunction with specific embodiment, an exemplary description of the invention, it is clear that realization of the invention is not by upper
The limitation of mode is stated, as long as using the various improvement that the inventive concept and technical scheme of the present invention carry out, or not improved general
Conception and technical scheme of the invention directly apply to other occasions, are within the scope of the invention.
Claims (5)
1. a kind of method for extracting leucine using corn protein powder, it is characterised in that the following steps are included:
Step 1: the hydrolysis stage of corn protein powder；The hydrolysis stage of corn protein powder described in step 1 is elder generation Xiang Fanying appearance
Hydrochloric acid is added in device, adds corn protein powder, opens steam valve heating, vapour pressure is not more than 0.2Mpa, and keeping temperature is 105
DEG C -115 DEG C, start to calculate hydrolysis time after corn protein powder is completely dissolved, carry out heat preservation hydrolysis, hydrolysis when
Between be -10 hours 6 hours, after hydrolysis, starting vacuum pump carries out catching up with acid, and catching up with the sour time is -3 hours 1 hour, catches up with acid
After carry out cooling treatment, after hydrolyzate is cooled to 40 DEG C or less, turn off coolant valve, by hydrolyzate squeeze into plate and frame filter press into
Row filtering after having filtered, rinses filter residue with the tap water of 300L-500L, flushing water merges hydrolyzate and is pumped into tone pitch tank；
Step 2: I preparatory phase of leucine crude product；I preparatory phase of leucine crude product described in step 2 is a N-process,
N-process is to add ammonium hydroxide tune after the flushing water of the hydrolyzate filtrate of step 1 and flushing filter residue is put into tone pitch tank
PH value is saved to 2.8-3.0, controlled at 40 DEG C -50 DEG C；Then the hydrolyzate after tone pitch is sucked into concentration tank, opens steam
Valve, heating, Steam pressure control 0.15Mpa-0.2Mpa, the stopping to be concentrated to after there is mass crystallization are concentrated, will once be concentrated
Liquid squeezes into cooling tank, and starting stirring opens cooling water, a concentrate is cooled to room temperature；The primary concentration of room temperature will be cooled to
Liquid pump enters plate and frame filter press and is filtered, and removing the resulting solid of filtrate is leucine crude product I；
Step 3: II preparatory phase of leucine crude product；II preparatory phase of leucine crude product described in step 3 includes once decolourizing
Journey and secondary N-process；Decolorization of the step 3 is to put into leucine crude product I in bleacher, according to bright ammonia
The mass content of acid crude is that salt acid for adjusting pH value is added to 0.5-1.0, the hydrochloric acid molar concentration after water is added in 35% ratio
It should be 0.6mol-1.0mol；It is completely dissolved leucine crude product I, and measures material liquid volume, steam valve is opened and is heated to 60
DEG C -65 DEG C, the activated carbon after purification is added, the additional amount of the purification active carbon is every 1000L solution 30kg-80kg, heat preservation
After 30 minutes, filtering, filtrate is shallow dark brown；
The secondary N-process of the step 3 is that the filtrate after primary decoloration is put into secondary neutralizing tank, and concentration is passed through into tank
For the ammonium hydroxide of 8mol-12mol, temperature control is 42 DEG C -47 DEG C, adjusts pH value to 4.5-4.8, and the time of the secondary neutralization is
It -4 hours 3 hours, after being then cooled to room temperature secondary neutralizer, is pumped into plate and frame filter press and is filtered, after removing filtrate
Solid bagging and weighing after centrifugal drying is leucine crude product II；
Step 4: leucine finished product preparatory phase；Leucine finished product preparatory phase described in step 4 include secondary decolourization process,
Fine work concentration process and last handling process；
The secondary decolourization process is that leucine crude product II and water are added into bleacher, described according to leucine crude product II
Additional amount with water is that the mass concentration of control leucine crude product II is 6.0%；Open steam valve heating, stirring, temperature control
System is at 40 DEG C -45 DEG C, after leucine crude product II is completely dissolved, liquid sodium hydroxide is added into tank and adjusts pH to 6.0-7.0,
The liquid sodium hydroxide mass concentration is 30%-42%, and measures material liquid volume, and refined using active carbon is then added, described
Refine active carbon additional amount be every 1000L solution 4kg-30kg, when be back to liquid it is limpid when, sampling analysis solution light transmission
Filtrate is put to high-order material-storage jar when light transmittance reaches 100%, crosses anion-exchange column, remove impurity by rate；
The fine work concentration process is that will be put into reacting tank body by the feed liquid of anion-exchange column processing, and control feed liquid is high
Degree is reacting tank body 2/3；Steam valve is opened, control vapour pressure is not more than 0.2Mpa, is warming up to 80 DEG C -85 DEG C and is concentrated,
When the intracorporal material liquid volume of tank is concentrated into original volume 1/10, steam is closed, closes cooling water, closes vacuum, exhaust-valve is opened, by fine work
Enriched product is transferred in crystallization cylinder；
The last handling process is to cover after fine work enriched product is transferred to completely in crystallization cylinder, it is cooling to open cooling water
Crystallization, when crystallizing the feed liquid temperature in cylinder and being down to 45 DEG C -50 DEG C, by the transferred product after crystallization to centrifuge, it is described from
600-900 revs/min of scheming revolving speed, centrifugation time are -20 minutes 10 minutes, after centrifugal drying, deionized water are added to wash repeatedly；It will
Finished product after washing is qualified moves into double-cone vacuum drier, and keeping vacuum degree is -0.06 to -0.08Mpa, opens steam valve,
Pressure control should be not more than 0.1Mpa, and heating, keeping temperature is 60 DEG C -65 DEG C, after -2.5 hours 2 hours dry, discharging；Wait produce
After product are cooled to room temperature, 12-15 mesh is crossed, obtains leucine finished product according to product requirement weighing packaging.
2. the method according to claim 1 for extracting leucine using corn protein powder, it is characterised in that:
It is carried out in hydrolytic process described in step 1 plus vapour is handled, be 10- first 4 hours of hydrolysis plus vapour frequency
Add within 15 minutes straight-through vapour primary, is every time 5-10 seconds；Afterwards 4 hours every 15-20 minutes it is straight-through plus vapour is primary, be every time 6-8 seconds, water
Solution liquid level keeps slightly boiled and stirs state.
3. the method according to claim 1 for extracting leucine using corn protein powder, it is characterised in that:
Corn protein powder described in step 1 and hydrochloric acid are according to 1 ton of corn protein powder: the ratio of the hydrochloric acid of 1.5 cubic meter volumes into
Row feeds intake.
4. the method according to claim 1 for extracting leucine using corn protein powder, it is characterised in that:
It for adjusting pH value to obtain the concentration of ammonium hydroxide be mass concentration is 15%-22% ammonium hydroxide described in step 2.
5. the method according to claim 1 for extracting leucine using corn protein powder, it is characterised in that:
It is primary at interval of feed supplement in 6 hours in fine work concentration process described in step 4, guarantee that the intracorporal feed liquid height of tank is reaction
Tank body 2/3；
In the crystallization process of last handling process described in step 4, need to wash crystallized product the water to centrifugation without silver nitrate
Reaction.
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| CN201710737885.7A CN109422661A (en) | 2017-08-24 | 2017-08-24 | A method of leucine is extracted using corn protein powder |
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| CN113501765A (en) * | 2021-08-30 | 2021-10-15 | 连云港华昌生物工程有限公司 | System and method for extracting amino acid required by human body |
Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103922951A (en) * | 2014-05-06 | 2014-07-16 | 鲁成宪 | Method for extracting leucine by utilizing corn protein powder |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103922951A (en) * | 2014-05-06 | 2014-07-16 | 鲁成宪 | Method for extracting leucine by utilizing corn protein powder |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN113501765A (en) * | 2021-08-30 | 2021-10-15 | 连云港华昌生物工程有限公司 | System and method for extracting amino acid required by human body |
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