CN103922951B - Method for extracting leucine by utilizing corn protein powder - Google Patents
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- CN103922951B CN103922951B CN201410186726.9A CN201410186726A CN103922951B CN 103922951 B CN103922951 B CN 103922951B CN 201410186726 A CN201410186726 A CN 201410186726A CN 103922951 B CN103922951 B CN 103922951B
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Abstract
The invention relates to a method for extracting leucine by utilizing corn protein powder. The method is characterized by comprising the steps of 1, hydrolysis stage of the corn protein powder; 2, preparation stage of leucine crude product I; 3, preparation stage of leucine crude product II; 4 preparation stage of leucine finished product. The method for extracting the leucine by the utilizing corn protein powder takes the corn protein powder as a production raw material, and the corn protein powder is lower in price, so that the production cost is greatly lowered. Furthermore, the product prepared by the method is high in purity, and the production technological conditions are simple, so that the method is more suitable for large-scale production and use.
Description
Technical field
The invention belongs to chemical technology field, particularly relate to one and utilize Zein powder to extract leucic method.
Background technology
Leucine is a kind of main biochemical products, is widely used in fields such as medicine, food.Leucine is generally used for bread, dough product; Preparation amino acid transfusion and comprehensive amino acid preparation, Hypoylycemic agents, plant growth promoter; Can be used as spices, can flavour of food products be improved.In pharmaceutical industries, L-Leu is the indispensable raw material of aminoacids complex intravenous fluid of Clinical Selection, and for the nutritional need maintaining urgent patient, the life rescuing patient plays a part positive; Leucine also plays an important role in adjustment amino acid and protein metabolism.Research finds, leucine is the amino acid of unique adjustable Protein Turnover in skeletal muscle and cardiac muscle.In addition, also there are some researches show, leucine can promote the synthesis of skeletal muscle protein.Leucic meta-bolites one ketoisocaproic acid also has the effect of Function protein matter metabolism, and leucic market outlook are boundless.
At present, for extracting leucic manufacturing condition all more complicated, long reaction time, production cost is high, and the utilization ratio for raw material is low.Have not been reported about utilizing Zein powder to extract leucic technique simultaneously.
Summary of the invention
The present invention devises one and utilizes Zein powder to extract leucic method; its object is to provide a kind of reactant of this relative low price of Zein powder that utilizes as raw material; simultaneously; reaction conditions requires simple; production cost is low; product purity is high, is suitable for the leucic extracting method of large-scale promotion.
To achieve these goals, present invention employs following scheme:
One utilizes Zein powder to extract leucic method, it is characterized in that comprising the following steps:
Step one: the hydrolysis stage of Zein powder;
Step 2: leucine crude product I preparatory phase;
Step 3: leucine crude product II preparatory phase;
Step 4: leucine finished product preparatory phase.
The hydrolysis stage of the Zein powder described in step one for first adding hydrochloric acid in reaction vessel, add Zein powder again, open steam valve heating, vapour pressure is not more than 0.2Mpa, temperature is kept to be 105 DEG C-115 DEG C, start to calculate hydrolysis time after Zein powder dissolves completely, carry out insulation hydrolysis reaction, the time of hydrolysis reaction is 6 hours-10 hours, after hydrolysis reaction terminates, start vacuum pump to carry out catching up with acid, the acid time is caught up with to be 1 hour-3 hours, cooling process is carried out after catching up with acid, when hydrolyzed solution is cooled to after below 40 DEG C, turn off coolant valve, hydrolyzed solution is squeezed into plate-and-frame filter press filter, after having filtered, first filter residue is rushed with the tap water of 300L-500L, wash-down water merges hydrolyzed solution and pumps into tone pitch tank.
Leucine crude product I preparatory phase described in step 2 is a N-process, a described N-process is add ammoniacal liquor adjust ph to 2.8-3.0 after the hydrolyzed solution filtrate of step one and the wash-down water rinsing filter residue are put into tone pitch tank, and control temperature is 40 DEG C-50 DEG C; Then the hydrolyzed solution after tone pitch is sucked concentration tank, open steam valve, heating, Steam pressure control 0.15 Mpa-0.2Mpa, to be concentrated concentrated to occurring stopping after mass crystallization, once concentration liquid is squeezed into cooling tank, start and stir, open water coolant, once concentration liquid is cooled to room temperature; The once concentration liquid pump being chilled to room temperature is entered plate-and-frame filter press filter, the solid of removing filtrate gained is leucine crude product I.
Described in step 3, leucine crude product II preparatory phase comprises a decolorization and Two-step neutralization process.
A decolorization of described step 3 is dropped in bleacher by leucine crude product I, and be after 35% ratio adds water according to the mass content of leucine crude product, add salt acid for adjusting pH value to 0.5-1.0, described hydrochloric acid volumetric molar concentration should be 0.6mol-1.0mol; Leucine crude product I is dissolved completely, and measures material liquid volume, open steam valve and be heated to 60 DEG C-65 DEG C, add the activated carbon after refining, the add-on of described refining gac is every 1000L solution 30kg-80kg, is incubated after 30 minutes, filter, filtrate is shallow dark brown;
The Two-step neutralization process of described step 3 is that the filtrate after once decolouring is put into Two-step neutralization tank, the ammoniacal liquor that concentration is 8mol-12mol is passed in tank, it is 42 DEG C-47 DEG C that temperature controls, adjust ph is to 4.5-4.8, the time of described Two-step neutralization is 3 hours-4 hours, then after Two-step neutralization liquid being cooled to room temperature, pumping into plate-and-frame filter press and filter, the bagging and weighing after centrifugal doing of the solid after removing filtrate is leucine crude product II.
Leucine finished product preparatory phase described in step 4 comprises secondary decolourization process, fine work concentration process and last handling process; Described secondary decolourization process for add leucine crude product II and water in bleacher, and the described add-on according to leucine crude product II and water is the mass concentration controlling leucine crude product II is 6.0%; Open steam valve to heat up, stir, temperature controls at 40 DEG C-45 DEG C, after leucine crude product II dissolves completely, in tank, add liquid sodium hydroxide regulate pH to 6.0-7.0, described liquid sodium hydroxide mass concentration is 30%-42%, and measure material liquid volume, then add refined using active carbon, the add-on of described refining gac is every 1000L solution 4kg-30kg, when being back to liquid and being limpid, sampling analysis solution transmittance, when transmittance reaches 100%, puts filtrate to high-order material-storage jar, cross anion-exchange column, remove impurity;
Described fine work concentration process is that the feed liquid through anion-exchange column process is put into reacting tank body, and controlling feed liquid height is reacting tank body 2/3; Open steam valve, control vapour pressure and be not more than 0.2Mpa, be warming up to 80 DEG C-85 DEG C and concentrate, when the material liquid volume in tank body is concentrated into original volume 1/10, close steam, close water coolant, close vacuum, open exhaust-valve, fine work enriched product is transferred in crystallization cylinder;
Described last handling process is for being transferred to completely after in crystallization cylinder until fine work enriched product, build, open water quench crystallization, when the feed temperature in crystallization cylinder is down to 45 DEG C-50 DEG C, by the transferred product after crystallization to whizzer, described centrifuge speed 600-900 rev/min, centrifugation time is 10 minutes-20 minutes, centrifugal dry after, add as deionized water repetitive scrubbing; Finished product after qualified for washing is moved into double-cone vacuum drier, and maintenance vacuum tightness is-0.06--0.08Mpa, opens steam valve, and pressure-controlling should be not more than 0.1Mpa, and heating keeps temperature to be 60 DEG C-65 DEG C, after dry 2 hours-2.5 hours, and discharging; Be cooled to after room temperature until product, cross 12-15 mesh sieve, namely weigh to pack according to product requirement obtains leucine finished product.
Needing in hydrolytic process described in step one to carry out adding vapour process, is add straight-through vapour once in 10-15 minutes in the vapour frequency that adds for first 4 hours of hydrolysis reaction, is 5-10 second at every turn; Within latter 4 hours every 15-20 minute, lead directly to and add vapour once, is 6-8 second at every turn, and hydrolysis liquid level keeps micro-boiling to stir state.
Zein powder described in step one and hydrochloric acid are according to 1 ton of Zein powder: the ratio of the hydrochloric acid of 1.5 cubic meter volume feeds intake.
The concentration obtaining ammoniacal liquor for adjust ph described in step 2 is mass concentration is 15%-22% ammoniacal liquor.
In fine work concentration process described in step 4 at interval of feed supplement in 6 hours once, ensure that the feed liquid height in tank body is reacting tank body 2/3;
In the crystallisation process of the last handling process described in step 4, need crystallized product washing to react to the water after centrifugal without Silver Nitrate.
This utilizes Zein powder to extract leucic method to have following beneficial effect:
The present invention utilizes Zein powder to extract leucic method to utilize Zein powder as raw materials for production, and price is cheaper, greatly reduces production cost.The product purity that method of the present invention is obtained is simultaneously very high, and the processing condition of production are comparatively simple, are more suitable for use of large-scale production.
Needing in hydrolytic process described in step one to carry out adding vapour process, is add straight-through vapour once in 10-15 minutes in the vapour frequency that adds for first 4 hours of hydrolysis reaction, is 5-10 second at every turn; Within latter 4 hours every 15-20 minute, lead directly to and add vapour once, is 6-8 second at every turn, and hydrolysis liquid level keeps micro-boiling to stir state.The vapour that adds in the present invention utilizes air compressor machine to join in hydrolytic decomposition pot by air, and object is to utilize pressurized air to stir the hydrolysis material in tank, makes it evenly hydrolysis thoroughly, improve yield.
Embodiment
Below in conjunction with specific embodiment, the present invention will be further described.
Embodiment
The invention discloses one utilizes Zein powder to extract leucic method, it is characterized in that comprising the following steps: step one: the hydrolysis stage of Zein powder; Step 2: leucine crude product I preparatory phase; Step 3: leucine crude product II preparatory phase; Step 4: leucine finished product preparatory phase.
The hydrolysis stage of the Zein powder of step one for first adding hydrochloric acid in reaction vessel, then adds Zein powder, and the Zein powder described in step one and hydrochloric acid are according to 1 ton of Zein powder: the ratio of the hydrochloric acid of 1.5 cubic meter volume feeds intake.Open steam valve heating, vapour pressure is not more than 0.2Mpa, keeps temperature to be 105 DEG C-115 DEG C, start to calculate hydrolysis time after Zein powder dissolves completely, carry out insulation hydrolysis reaction, the time of hydrolysis reaction is 6 hours-10 hours, after hydrolysis reaction terminates, start vacuum pump to carry out catching up with acid, catch up with the acid time to be 1 hour-3 hours, after catching up with acid, carry out cooling process, when hydrolyzed solution is cooled to after below 40 DEG C, turn off coolant valve, hydrolyzed solution is squeezed into plate-and-frame filter press and filters, filtrate is continued to employ.After feed liquid has been filtered, rush first filter residue with about 400L tap water, wash-down water merges hydrolyzed solution and pumps into tone pitch tank.
Leucine crude product I preparatory phase described in step 2 is a N-process, a described N-process is by the hydrolyzed solution filtrate of step one and rinses after the wash-down water of filter residue puts into tone pitch tank and add ammoniacal liquor adjust ph to 2.8-3.0, and the concentration obtaining ammoniacal liquor for adjust ph described in step 2 is mass concentration is 15%-22% ammoniacal liquor.Control temperature is 40 DEG C-50 DEG C; Then the hydrolyzed solution after tone pitch is sucked concentration tank, open steam valve, heating, Steam pressure control 0.15 Mpa-0.2Mpa, to be concentrated concentrated to occurring stopping after mass crystallization, once concentration liquid is squeezed into cooling tank, start and stir, open water coolant, once concentration liquid is cooled to room temperature; The once concentration liquid pump being chilled to room temperature is entered plate-and-frame filter press filter, the solid of removing filtrate gained is leucine crude product I.This step needs to detect hot concentrated solution degree Beaume >=24 °, and notes down.
Step 3 leucine crude product II preparatory phase comprises a decolorization and Two-step neutralization process.A decolorization of step 3 is dropped in bleacher by leucine crude product I, and be after 35% ratio adds water according to the mass content of leucine crude product, add salt acid for adjusting pH value to 0.5-1.0, described hydrochloric acid volumetric molar concentration should be 0.6mol-1.0mol; Leucine crude product I is dissolved completely, and measures material liquid volume, open steam valve and be heated to 60 DEG C-65 DEG C, add the activated carbon after refining, the add-on of described refining gac is every 1000L solution 30kg-80kg, is incubated after 30 minutes, filter, filtrate is shallow dark brown; Destainer yield span of control >=96%.Method of calculation are: (after the rear material liquid volume/acid adding of filtration material liquid volume) × 100%.
The Two-step neutralization process of step 3 is that the filtrate after once decolouring is put into Two-step neutralization tank, the ammoniacal liquor that concentration is 8mol-12mol is passed in tank, it is 42 DEG C-47 DEG C that temperature controls, adjust ph is to 4.5-4.8, the time of described Two-step neutralization is 3 hours-4 hours, then after Two-step neutralization liquid being cooled to room temperature, pumping into plate-and-frame filter press and filter, the bagging and weighing after centrifugal doing of the solid after removing filtrate is leucine crude product II.Leucine crude product II yield span of control 10%-15% after Two-step neutralization.Method of calculation are: (crude product II weight/crude product I weight) × 100%.
Leucine finished product preparatory phase described in step 4 comprises secondary decolourization process, fine work concentration process and last handling process; Described secondary decolourization process for add leucine crude product II and water in bleacher, and the described add-on according to leucine crude product II and water is the mass concentration controlling leucine crude product II is 6.0%; Open steam valve to heat up, stir, temperature controls at 40 DEG C-45 DEG C, after leucine crude product II dissolves completely, in tank, add liquid sodium hydroxide regulate pH to 6.0-7.0, described liquid sodium hydroxide mass concentration is 30%-42%, and measure material liquid volume, then add refined using active carbon, the add-on of described refining gac is every 1000L solution 4kg-30kg, when being back to liquid and being limpid, sampling analysis solution transmittance, when transmittance reaches 100%, puts filtrate to high-order material-storage jar, cross anion-exchange column, remove impurity; After secondary decolourization, the SO in sampling analysis solution
4 2-need theoretical bariumchloride consumption, as just a kind of detection method.
Fine work concentration process is that the feed liquid through anion-exchange column process is put into reacting tank body, and controlling feed liquid height is reacting tank body 2/3; Open steam valve, control vapour pressure and be not more than 0.2Mpa, be warming up to 80 DEG C-85 DEG C and concentrate, when the material liquid volume in tank body is concentrated into original volume 1/10, close steam, close water coolant, close vacuum, open exhaust-valve, fine work enriched product is transferred in crystallization cylinder; In step 4 fine work concentration process at interval of feed supplement in 6 hours once, ensure that the feed liquid height in tank body is reacting tank body 2/3;
The last handling process of step 4 is for being transferred to completely after in crystallization cylinder until fine work enriched product, build, open water quench crystallization, when the feed temperature in crystallization cylinder is down to 45 DEG C-50 DEG C, by the transferred product after crystallization to whizzer, centrifuge speed 600-900 rev/min, centrifugation time is 10 minutes-20 minutes, centrifugal dry after, add as deionized water repetitive scrubbing; Finished product after qualified for washing is moved into double-cone vacuum drier, and maintenance vacuum tightness is-0.06--0.08Mpa, opens steam valve, and pressure-controlling should be not more than 0.1Mpa, and heating keeps temperature to be 60 DEG C-65 DEG C, after dry 2 hours-2.5 hours, and discharging; Be cooled to after room temperature until product, cross 12-15 mesh sieve, namely weigh to pack according to product requirement obtains leucine finished product.In the crystallisation process of step 4 last handling process, need crystallized product washing to react to the water after centrifugal without Silver Nitrate.In actually operating, stirred once with poly-third sticking plaster every 15 minutes in the process of crystallization.
In practical application, generally pack according to 25kg/ every bag vinyon inner membrance, move into through-station and place, after sampling analysis is qualified, after loading onto outer packaging barrel packaging, stamp lot number, warehouse-in.Product yield span of control 55%-60%, method of calculation are: (after dry, crude product II weight is thrown in gross weight/decolouring) × 100%.
Needing to carry out adding vapour process in step one solution preocess, is add straight-through vapour once in 10-15 minutes in the vapour frequency that adds for first 4 hours of hydrolysis reaction, is 5-10 second at every turn; Within latter 4 hours every 15-20 minute, lead directly to and add vapour once, is 6-8 second at every turn, and hydrolysis liquid level keeps micro-boiling to stir state.The vapour that adds in the present invention utilizes air compressor machine to join in hydrolytic decomposition pot by air, and object is to utilize pressurized air to stir the hydrolysis material in tank, makes it evenly hydrolysis thoroughly, improve yield.
The present invention utilizes Zein powder to extract leucic method to utilize Zein powder as raw materials for production, and price is cheaper, greatly reduces production cost.The product purity that method of the present invention is obtained is simultaneously very high, and the processing condition of production are comparatively simple, are more suitable for use of large-scale production.
Above in conjunction with specific embodiments to invention has been exemplary description; obvious realization of the present invention is not subject to the restrictions described above; as long as have employed the various improvement that method of the present invention is conceived and technical scheme is carried out; or design of the present invention and technical scheme directly applied to other occasion, all in protection scope of the present invention without to improve.
Claims (5)
1. utilize Zein powder to extract a leucic method, it is characterized in that comprising the following steps:
Step one: the hydrolysis stage of Zein powder, the hydrolysis stage of the Zein powder described in step one for first adding hydrochloric acid in reaction vessel, add Zein powder again, open steam valve heating, vapour pressure is not more than 0.2Mpa, temperature is kept to be 105 DEG C-115 DEG C, start to calculate hydrolysis time after Zein powder dissolves completely, carry out insulation hydrolysis reaction, the time of hydrolysis reaction is 6 hours-10 hours, after hydrolysis reaction terminates, start vacuum pump to carry out catching up with acid, the acid time is caught up with to be 1 hour-3 hours, cooling process is carried out after catching up with acid, when hydrolyzed solution is cooled to after below 40 DEG C, turn off coolant valve, hydrolyzed solution is squeezed into plate-and-frame filter press filter, after having filtered, with the tap water filter residue of 300L-500L, wash-down water merges hydrolyzed solution and pumps into tone pitch tank,
Step 2: leucine crude product I preparatory phase; Leucine crude product I preparatory phase described in step 2 is a N-process, a described N-process is add ammoniacal liquor adjust ph to 2.8-3.0 after the hydrolyzed solution filtrate of step one and the wash-down water rinsing filter residue are put into tone pitch tank, and control temperature is 40 DEG C-50 DEG C; Then the hydrolyzed solution after tone pitch is sucked concentration tank, open steam valve, heating, Steam pressure control 0.15 Mpa-0.2Mpa, to be concentrated concentrated to occurring stopping after mass crystallization, once concentration liquid is squeezed into cooling tank, start and stir, open water coolant, once concentration liquid is cooled to room temperature; The once concentration liquid pump being chilled to room temperature is entered plate-and-frame filter press filter, the solid of removing filtrate gained is leucine crude product I;
Step 3: leucine crude product II preparatory phase; Described in step 3, leucine crude product II preparatory phase comprises a decolorization and Two-step neutralization process; A decolorization of described step 3 is dropped in bleacher by leucine crude product I, and be after 35% ratio adds water according to the mass content of leucine crude product, add salt acid for adjusting pH value to 0.5-1.0, described hydrochloric acid volumetric molar concentration should be 0.6mol-1.0mol; Leucine crude product I is dissolved completely, and measures material liquid volume, open steam valve and be heated to 60 DEG C-65 DEG C, add the activated carbon after refining, the add-on of described refining gac is every 1000L solution 30kg-80kg, is incubated after 30 minutes, filter, filtrate is shallow dark brown;
The Two-step neutralization process of described step 3 is that the filtrate after once decolouring is put into Two-step neutralization tank, the ammoniacal liquor that concentration is 8mol-12mol is passed in tank, it is 42 DEG C-47 DEG C that temperature controls, adjust ph is to 4.5-4.8, the time of described Two-step neutralization is 3 hours-4 hours, then after Two-step neutralization liquid being cooled to room temperature, pumping into plate-and-frame filter press and filter, the solid bagging and weighing after centrifugal drying after removing filtrate is leucine crude product II;
Step 4: leucine finished product preparatory phase; Leucine finished product preparatory phase described in step 4 comprises secondary decolourization process, fine work concentration process and last handling process;
Described secondary decolourization process for add leucine crude product II and water in bleacher, and the described add-on according to leucine crude product II and water is the mass concentration controlling leucine crude product II is 6.0%; Open steam valve to heat up, stir, temperature controls at 40 DEG C-45 DEG C, after leucine crude product II dissolves completely, in tank, add liquid sodium hydroxide regulate pH to 6.0-7.0, described liquid sodium hydroxide mass concentration is 30%-42%, and measure material liquid volume, then add refined using active carbon, the add-on of described refining gac is every 1000L solution 4kg-30kg, when being back to liquid and being limpid, sampling analysis solution transmittance, when transmittance reaches 100%, puts filtrate to high-order material-storage jar, cross anion-exchange column, remove impurity;
Described fine work concentration process is that the feed liquid through anion-exchange column process is put into reacting tank body, and controlling feed liquid height is reacting tank body 2/3; Open steam valve, control vapour pressure and be not more than 0.2Mpa, be warming up to 80 DEG C-85 DEG C and concentrate, when the material liquid volume in tank body is concentrated into original volume 1/10, close steam, close water coolant, close vacuum, open exhaust-valve, fine work enriched product is transferred in crystallization cylinder;
Described last handling process is for being transferred to completely after in crystallization cylinder until fine work enriched product, build, open water quench crystallization, when the feed temperature in crystallization cylinder is down to 45 DEG C-50 DEG C, by the transferred product after crystallization to whizzer, described centrifuge speed 600-900 rev/min, centrifugation time is 10 minutes-20 minutes, after centrifugal drying, add deionized water repetitive scrubbing; Finished product after qualified for washing is moved into double-cone vacuum drier, and keep vacuum tightness to be-0.06 to-0.08Mpa, open steam valve, pressure-controlling should be not more than 0.1Mpa, and heating keeps temperature to be 60 DEG C-65 DEG C, after dry 2 hours-2.5 hours, and discharging; Be cooled to after room temperature until product, cross 12-15 mesh sieve, namely weigh to pack according to product requirement obtains leucine finished product.
2. the Zein powder that utilizes according to claim 1 extracts leucic method, it is characterized in that:
Needing in hydrolytic process described in step one to carry out adding vapour process, is add straight-through vapour once in 10-15 minutes in the vapour frequency that adds for first 4 hours of hydrolysis reaction, is 5-10 second at every turn; Within latter 4 hours every 15-20 minute, lead directly to and add vapour once, is 6-8 second at every turn, and hydrolysis liquid level keeps micro-boiling to stir state.
3. the Zein powder that utilizes according to claim 1 extracts leucic method, it is characterized in that:
Zein powder described in step one and hydrochloric acid are according to 1 ton of Zein powder: the ratio of the hydrochloric acid of 1.5 cubic meter volume feeds intake.
4. the Zein powder that utilizes according to claim 1 extracts leucic method, it is characterized in that:
The concentration obtaining ammoniacal liquor for adjust ph described in step 2 is mass concentration is 15%-22% ammoniacal liquor.
5. the Zein powder that utilizes according to claim 1 extracts leucic method, it is characterized in that:
In fine work concentration process described in step 4 at interval of feed supplement in 6 hours once, ensure that the feed liquid height in tank body is reacting tank body 2/3;
In the crystallisation process of the last handling process described in step 4, need crystallized product washing to react to the water after centrifugal without Silver Nitrate.
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106349096A (en) * | 2016-08-29 | 2017-01-25 | 成都科源生物技术有限公司 | Method for preparing L-leucine from plant cells |
Families Citing this family (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104926670B (en) * | 2015-06-02 | 2017-03-29 | 江苏三宝药业有限公司 | It is a kind of to extract the leucic methods of L from vegetable protein |
| CN109422661A (en) * | 2017-08-24 | 2019-03-05 | 张坤 | A method of leucine is extracted using corn protein powder |
| CN108047070A (en) * | 2017-12-29 | 2018-05-18 | 韩久新 | A kind of method using niblet extraction amino acid |
| 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 (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1775744A (en) * | 2005-12-08 | 2006-05-24 | 华侨大学 | Leucine extracting method |
| CN103396331A (en) * | 2013-07-26 | 2013-11-20 | 临汾市万国全生物科技有限公司 | Technology for extracting leucine and cystine by adopting two-step method |
-
2014
- 2014-05-06 CN CN201410186726.9A patent/CN103922951B/en not_active Expired - Fee Related
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1775744A (en) * | 2005-12-08 | 2006-05-24 | 华侨大学 | Leucine extracting method |
| CN103396331A (en) * | 2013-07-26 | 2013-11-20 | 临汾市万国全生物科技有限公司 | Technology for extracting leucine and cystine by adopting two-step method |
Non-Patent Citations (2)
| Title |
|---|
| L-亮氨酸提取的研究;来彩霞 等;《沈阳药学院学报》;19911031;第8卷(第4期);第285、308页 * |
| 从玉米麸质中提取L-亮氨酸;黄艳刚 等;《湖北化工》;20021231(第6期);第28-29页 * |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106349096A (en) * | 2016-08-29 | 2017-01-25 | 成都科源生物技术有限公司 | Method for preparing L-leucine from plant cells |
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