CN103933862A - Membrane method extraction system and membrane method extraction process for alanine production - Google Patents
Membrane method extraction system and membrane method extraction process for alanine production Download PDFInfo
- Publication number
- CN103933862A CN103933862A CN201410168842.8A CN201410168842A CN103933862A CN 103933862 A CN103933862 A CN 103933862A CN 201410168842 A CN201410168842 A CN 201410168842A CN 103933862 A CN103933862 A CN 103933862A
- Authority
- CN
- China
- Prior art keywords
- organic
- alanine
- filter
- production
- membrane
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Pending
Links
Landscapes
- Separation Using Semi-Permeable Membranes (AREA)
- Preparation Of Compounds By Using Micro-Organisms (AREA)
Abstract
The invention discloses a membrane method extraction process for alanine production. A membrane method extraction system for the alanine production comprises a circulating tank, an organic ultrafiltration membrane system, an organic decolorizing membrane system, a filter, a cleaning tank, a material feeding pump, a circulating pump, a booster pump and a pipeline valve system. A pressure gauge, a thermometer, a level gauge and a flow meter are arranged in the overall extraction system, so that the safe and stable operation of the system is monitored and protected constantly; organic ultrafiltration membrane and organic decolorizing membrane combination process production equipment is applied to subsequent sterilization and cleaning processes of alanine fermentation broth so as to monitor and protect the safe and stable operation of the system constantly. The membrane method extraction process is a combination membrane production process which can be used safely and effectively for a long time and is convenient to maintain; the alanine fermentation broth completely meets market requirements after being processed by the membrane method combination production process; meanwhile, the using cost of activated carbon is greatly reduced; the production cost is reduced; direct and obvious economic benefits are brought to enterprises.
Description
Technical field
Alanine extraction process of the present invention, relates in particular to alanine production embrane method extraction system and extraction process thereof.
Background technology
At present amino acids production technique has two kinds of enzymatic conversion method and fermentation methods, and wherein to produce amino acid cost higher for enzymatic conversion method, and fermentation method is produced amino acid, and cost is lower.Along with development, the maturation of fermentation technique, on amino acids production, more and more favored, praise highly by manufacturer.The production of alanine at present adopts enzyme transforming process to produce substantially, and fermentation method is produced when alanine, in its zymotic fluid, contain a large amount of thalline, albumen, pigment and different kinds of ions, salt grades, seriously restrict the quality of producing alanine finished product, if adopt original plate-frame filtering and active carbon to carry out the method for adsorption bleaching, cost is higher, product yield is low, and processing adsorption effect is not very desirable.
Therefore, be necessary to invent a kind of production technology and solve the difficult problem that alanine is produced, thereby improve alanine product yield, yield, quality, and reduce production costs.
Summary of the invention
The object of this invention is to provide alanine production embrane method extraction process, for shortcoming in the technology of background, use organic milipore filter and organic decolouring film group technology production equipment to be applied to follow-up degerming, removal of impurities, decolouring, the desalination process of alanine zymotic fluid, improve alanine product yield, yield, quality, and reduce production costs.
In order to solve the existing problem of background technology, the present invention is by the following technical solutions: alanine production embrane method extraction system, it includes circulating tank, and circulating tank exit is provided with charging pump, and charging pump one end be provided with successively filter,, organic milipore filter, organic decolouring film.
On described organic milipore filter and organic decolouring film one end, be respectively equipped with booster pump, pipe valve, Pressure gauge, thermometer, tank gage, flowmeter.
Described filter is cloth envelop collector, and filtering filter cloth is PE or nylon material, and filtering accuracy 100 order-300 orders.
Described organic milipore filter is modification PVDF material, and organic decolouring film is PPTE and aromatic polyamides polymer composite.
Alanine production embrane method process for extracting, concrete operations flow process is as follows:
1) the alanine zymotic fluid that is 8%-12% by content is pumped into filter by charging pump and carries out pre-filtering, filters out the impurity of larger particles;
2) pretreated alanine zymotic fluid is passed in organic ultrafiltration membrane system, operating pressure is in 2-5bar, running temperature is in 50 DEG C, after filter pretreatment, alanine zymotic fluid enters in organic ultrafiltration membrane system, through circulating pump circulating filtration, by Impurity removals such as thalline, bacterium colony, mycelium, soluble type albumen and soluble large molecule albumen, wherein zymotic fluid is after organic ultrafiltration membrance filter, residue filter residue liquid is the 3-10% of total filtered fluid total amount, and dialysis is the 3%-10% of every batch fermentation liquid total amount by pure water amount;
3) the alanine solution after organic ultrafiltration membrance filter is delivered in organic decolouring film system by booster pump, in running temperature in 45 DEG C, operating pressure filters, separates in 15-25bar, make solubility small molecular protein, ion salinity, pigment, wherein remaining condensed slag liquid is the 5-10% that always filters liquid measure, and wherein dialysing by pure water amount is the 3%-10% of every batch of organic decolouring membrane filtration liquid total amount.
4) after organic decolouring film is processed, then through follow-up crystallization, the alanine crystal that stoving process final production goes out.
Operation principle of the present invention is as follows: by pending alanine zymotic fluid by charging pump suction, after filter pretreatment, enter organic ultrafiltration membrane system, utilize circulating pump to carry out circulating filtration, by thalline, bacterium colony, the Impurity removals such as mycelium and soluble type albumen reach more than 99%, then pass through closing pipe line tube system, after being filtered by decolouring film charging pump input filter, again by being delivered to after supercharging in organic decolouring film system, filter, separate, solubility small molecular protein, ion salinity, the removal of impurity such as pigment reach 40-90%, final alanine liquid light transmittance reaches 80-90%, pass through so follow-up crystallization, the alanine crystal quality that after stoving process, final production goes out.
The cecum that the cross-flow filtration of organic ultrafiltration membrane system of utilizing substitutes traditional sheet frame filters, and greatly improved filter effect and speed, and organic milipore filter adopts online CIP cleaning and regeneration, and simple to operate, easy cleaning is recovered, and can steady in a long-term move; And the filtration time of plate-frame filtering is limited, its filter cloth that plays main filtration belongs to consumptive material, and needs disassembly, cleaning at every turn, and labour intensity is larger, and operating environment is severe compared with ultrafiltration membrane system;
Utilize organic decolouring film system to substitute traditional charcoal absorption decolouring, can filter at normal temperatures decolouring, desalination, just can carry out adsorption bleaching without need be warming up to 80 DEG C as traditional charcoal absorption operation, operate more energy-saving and environmental protection, reduce activated carbon dosage cost, also improved the yield of product simultaneously;
Organic milipore filter running temperature is in 50 DEG C, and operating pressure is in 5bar, and organic decolouring film running temperature is in 45 DEG C, and operating pressure is in 30bar, and can produce continuously 20 hours every day, long service life, the production cost of minimizing enterprise.
The invention of this technique is a kind of energy long-term safety, the high-effect combined films production technology that uses and maintain easily, and makes alanine zymotic fluid after embrane method combined production process is processed, and the alanine crystal quality that final production goes out accords with the demands of the market completely; Both substituted plate-frame filtering, greatly saved the consumption cost of active carbon simultaneously, having reduced production cost is that enterprise brings directly, obvious economic benefit.
Brief description of the drawings
Fig. 1 is structural principle schematic diagram of the present invention.
1, circulating tank; 2, filter; 3, charging pump; 4, organic milipore filter; 5, organic decolouring film; 6, booster pump; 7, pipe valve; 8, Pressure gauge; 9, thermometer; 10, tank gage; 11, flowmeter.
Detailed description of the invention
Embodiment 1
1) the alanine zymotic fluid of the 3000kg that is 10% by content is pumped into filter by charging pump and carries out pre-filtering, filters out the impurity of larger particles;
2) the alanine zymotic fluid of pretreated 2982kg is passed in organic ultrafiltration membrane system, operating pressure is in 5bar, running temperature is in 50 DEG C, after filter pretreatment, alanine zymotic fluid enters in organic ultrafiltration membrane system, in dialysis procedure, add 245kg pure water to continue through circulating pump circulation dialysis, by Impurity removals such as thalline, bacterium colony, mycelium, soluble type albumen and soluble large molecule albumen, obtain organic ultrafiltration liquid 2837kg;
3) organic ultrafiltration membrance filter liquid of 2837kg is delivered in organic decolouring film system by booster pump, in running temperature in 45 DEG C, operating pressure filters in 25bar, add the pure water of 280kg to separate in decolorization, make solubility small molecular protein, ion salinity, pigment, finally obtaining remaining condensed slag liquid is 2890kg;
4) after organic decolouring film is processed, then through follow-up crystallization, the alanine crystal 279kg that stoving process final production goes out.
Embodiment 2
1) the alanine zymotic fluid of the 2500kg that is 9% by content is pumped into filter by charging pump and carries out pre-filtering, filters out the impurity of larger particles;
2) the alanine zymotic fluid of pretreated 2450kg is passed in organic ultrafiltration membrane system, operating pressure is in 3bar, running temperature is in 50 DEG C, after filter pretreatment, alanine zymotic fluid enters in organic ultrafiltration membrane system, in dialysis procedure, add 200kg pure water to continue through circulating pump circulation dialysis, by Impurity removals such as thalline, bacterium colony, mycelium, soluble type albumen and soluble large molecule albumen, obtain organic ultrafiltration liquid 2528kg;
3) organic ultrafiltration membrance filter liquid of 2528kg is delivered in organic decolouring film system by booster pump, in running temperature in 45 DEG C, operating pressure filters in 20bar, add the pure water of 180kg to separate in decolorization, make solubility small molecular protein, ion salinity, pigment, finally obtaining remaining condensed slag liquid is 2508kg;
4) after organic decolouring film is processed, then through follow-up crystallization, the alanine crystal 238kg that stoving process final production goes out.
Claims (5)
1. alanine production embrane method extraction system, it is characterized in that: it includes circulating tank (1), circulating tank (1) exit is provided with charging pump (3), and charging pump one end is provided with filter (2), organic milipore filter (4), organic decolouring film (5) successively.
2. alanine production embrane method extraction system according to claim 1, is characterized in that: on described organic milipore filter (4) and organic decolouring film (5) one end, be respectively equipped with booster pump (6), pipe valve (7), Pressure gauge (8), thermometer (9), tank gage (10), flowmeter (11).
3. alanine production embrane method extraction system according to claim 1, is characterized in that: described filter (2) is cloth envelop collector, and filtering filter cloth is PE or nylon material, and filtering accuracy 100 order-300 orders.
4. alanine production embrane method extraction system according to claim 1, is characterized in that: described organic milipore filter (4) is modification PVDF material, and organic decolouring film (5) is PPTE and aromatic polyamides polymer composite.
5. alanine production embrane method process for extracting: it is characterized in that:
Concrete operations flow process is as follows:
1) the alanine zymotic fluid that is 8%-12% by content is pumped into filter by charging pump and carries out pre-filtering, filters out the impurity of larger particles;
2) pretreated alanine zymotic fluid is passed in organic ultrafiltration membrane system, operating pressure is in 2-5bar, running temperature is in 50 DEG C, after filter pretreatment, alanine zymotic fluid enters in organic ultrafiltration membrane system, through circulating filtration, by Impurity removals such as thalline, bacterium colony, mycelium, soluble type albumen and soluble large molecule albumen, wherein zymotic fluid is after organic ultrafiltration membrance filter, residue filter residue liquid is the 3-10% of total filtered fluid total amount, and dialysis is the 3%-10% of every batch fermentation liquid total amount by pure water amount;
3) the alanine solution after organic ultrafiltration membrance filter is delivered in organic decolouring film system by booster pump, in running temperature in 45 DEG C, operating pressure filters, separates in 15-25bar, make solubility small molecular protein, ion salinity, pigment, wherein remaining condensed slag liquid is the 5-10% that always filters liquid measure, and wherein dialysing by pure water amount is the 3%-10% of every batch of organic decolouring membrane filtration liquid total amount.
4) after organic decolouring film is processed, then through follow-up crystallization, the alanine crystal that stoving process final production goes out.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201410168842.8A CN103933862A (en) | 2014-04-24 | 2014-04-24 | Membrane method extraction system and membrane method extraction process for alanine production |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201410168842.8A CN103933862A (en) | 2014-04-24 | 2014-04-24 | Membrane method extraction system and membrane method extraction process for alanine production |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN103933862A true CN103933862A (en) | 2014-07-23 |
Family
ID=51181895
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201410168842.8A Pending CN103933862A (en) | 2014-04-24 | 2014-04-24 | Membrane method extraction system and membrane method extraction process for alanine production |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN103933862A (en) |
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106509330A (en) * | 2016-09-24 | 2017-03-22 | 合肥信达膜科技有限公司 | Extraction technology of monellin |
| CN106543053A (en) * | 2016-09-23 | 2017-03-29 | 合肥信达膜科技有限公司 | A kind of methionine extraction system |
| CN107115705A (en) * | 2017-05-23 | 2017-09-01 | 天地壹号饮料股份有限公司 | A kind of beverage filter device |
| CN107200693A (en) * | 2017-07-18 | 2017-09-26 | 精晶药业股份有限公司 | A kind of method for crystallising of beta Alanine |
| CN107382800A (en) * | 2017-08-20 | 2017-11-24 | 合肥信达膜科技有限公司 | A kind of methionine preparation system |
| CN113755540A (en) * | 2021-08-06 | 2021-12-07 | 合肥信达膜科技有限公司 | Alanine production method based on membrane separation process |
Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5814498A (en) * | 1996-04-29 | 1998-09-29 | Archer Daniels Midland Company | Process for the recovery of organic acids and ammonia from their salts |
| JP4487045B2 (en) * | 2004-08-04 | 2010-06-23 | 独立行政法人産業技術総合研究所 | Membrane separation and purification system for fermented ethanol |
| CN202297430U (en) * | 2011-09-30 | 2012-07-04 | 合肥信达膜科技有限公司 | Plasma protein ultrafiltration membrane device |
| CN102659612A (en) * | 2012-05-10 | 2012-09-12 | 杭州蓝然环境技术有限公司 | Process for purifying L-phenylalanine |
| CN202497826U (en) * | 2012-03-15 | 2012-10-24 | 合肥创想能源环境科技有限公司 | Membrane treatment device system |
| CN102757355A (en) * | 2012-07-26 | 2012-10-31 | 无锡晶海氨基酸有限公司 | Method for extracting and separating L-isoleucine from fermentation liquid by membrane separation and electrodialysis combined technology |
| CN202803121U (en) * | 2012-09-20 | 2013-03-20 | 石药银湖制药有限公司 | Membrane separation system for purification and concentration of Chinese medicinal injection |
-
2014
- 2014-04-24 CN CN201410168842.8A patent/CN103933862A/en active Pending
Patent Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5814498A (en) * | 1996-04-29 | 1998-09-29 | Archer Daniels Midland Company | Process for the recovery of organic acids and ammonia from their salts |
| JP4487045B2 (en) * | 2004-08-04 | 2010-06-23 | 独立行政法人産業技術総合研究所 | Membrane separation and purification system for fermented ethanol |
| CN202297430U (en) * | 2011-09-30 | 2012-07-04 | 合肥信达膜科技有限公司 | Plasma protein ultrafiltration membrane device |
| CN202497826U (en) * | 2012-03-15 | 2012-10-24 | 合肥创想能源环境科技有限公司 | Membrane treatment device system |
| CN102659612A (en) * | 2012-05-10 | 2012-09-12 | 杭州蓝然环境技术有限公司 | Process for purifying L-phenylalanine |
| CN102757355A (en) * | 2012-07-26 | 2012-10-31 | 无锡晶海氨基酸有限公司 | Method for extracting and separating L-isoleucine from fermentation liquid by membrane separation and electrodialysis combined technology |
| CN202803121U (en) * | 2012-09-20 | 2013-03-20 | 石药银湖制药有限公司 | Membrane separation system for purification and concentration of Chinese medicinal injection |
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106543053A (en) * | 2016-09-23 | 2017-03-29 | 合肥信达膜科技有限公司 | A kind of methionine extraction system |
| CN106509330A (en) * | 2016-09-24 | 2017-03-22 | 合肥信达膜科技有限公司 | Extraction technology of monellin |
| CN107115705A (en) * | 2017-05-23 | 2017-09-01 | 天地壹号饮料股份有限公司 | A kind of beverage filter device |
| CN107200693A (en) * | 2017-07-18 | 2017-09-26 | 精晶药业股份有限公司 | A kind of method for crystallising of beta Alanine |
| CN107382800A (en) * | 2017-08-20 | 2017-11-24 | 合肥信达膜科技有限公司 | A kind of methionine preparation system |
| CN113755540A (en) * | 2021-08-06 | 2021-12-07 | 合肥信达膜科技有限公司 | Alanine production method based on membrane separation process |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN103933862A (en) | Membrane method extraction system and membrane method extraction process for alanine production | |
| Weng et al. | Separation of furans and carboxylic acids from sugars in dilute acid rice straw hydrolyzates by nanofiltration | |
| KR101938604B1 (en) | Method for producing sugar solution | |
| Murthy et al. | Concentration of xylose reaction liquor by nanofiltration for the production of xylitol sugar alcohol | |
| CN102329018B (en) | Device for desalting sea water by low-pressure membrane method | |
| CN204174012U (en) | Pure water processor | |
| CN101434553B (en) | Method for all-film extraction of valine | |
| CN102863096A (en) | Method for recovering waste water generated in production of starch sugar | |
| CN102603478B (en) | Method for separating and purifying erythritol from mother liquid obtained after repeated crystallization of erythritol | |
| CN103130664A (en) | Process method of extracting gamma-aminobutyric acid through membrane separation technique | |
| CN101870639A (en) | Method for producing kelp mannitol with low energy consumption | |
| CN102838624B (en) | Method for purifying clavulanic acid from fermentation liquor | |
| Tomczak et al. | The application of ultrafiltration for separation of glycerol solution fermented by bacteria | |
| CN105219889A (en) | A kind of method of membrane separation purification starch saccharificating liquid | |
| Hang et al. | Enzyme membrane reactor coupled with nanofiltration membrane process for difructose anhydride III from inulin conversion | |
| CN109970226B (en) | Method for treating sodium phenylacetate deesterification liquid generated by cracking penicillin G sylvite crystallization mother liquor | |
| CN106518700A (en) | Glutamicacid membrane method production process | |
| CN103539688B (en) | A kind of method of separation and Extraction Serine from Corynebacterium glutamicum fermented liquid | |
| CN202080970U (en) | Reverse osmosis treatment system with high recovery rate | |
| CN215162258U (en) | Device for extracting succinic acid from fermentation liquor | |
| CN104084047A (en) | Glycyrrhiza extracting solution clarification and concentration membrane system | |
| CN210560185U (en) | Device for purifying and recovering protein peptide by membrane method | |
| CN107324992A (en) | A kind of novel lactic extraction system | |
| JP2010095450A (en) | Method for producing monocarboxylic acid | |
| CN205035121U (en) | Reverse osmosis membrane water processing system |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| RJ01 | Rejection of invention patent application after publication |
Application publication date: 20140723 |
|
| RJ01 | Rejection of invention patent application after publication |