CN101580800A - Separation method of lysine bacteria - Google Patents
Separation method of lysine bacteria Download PDFInfo
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- CN101580800A CN101580800A CNA2009100857184A CN200910085718A CN101580800A CN 101580800 A CN101580800 A CN 101580800A CN A2009100857184 A CNA2009100857184 A CN A2009100857184A CN 200910085718 A CN200910085718 A CN 200910085718A CN 101580800 A CN101580800 A CN 101580800A
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Abstract
The invention relates to a separation method of lysine bacteria, comprising the following steps: 1) adding assistant agents to fermentation liquor and mixing for 1 to 60 minutes; 2) pressing the fermentation liquor treated with the assistant agents into a plate and frame filter press for filtering. The used assistant agents comprise inorganic polymeric ferric and poly-aluminum assistant agents, and organic anionic assistant agents. Compared with the current common separation methods in the prior art, the invention has the advantages of simple and practical technique, low consumption of water, electricity and steam, low equipment investment, low maintenance cost, low moisture content and high yield of the obtained bacteria.
Description
Technical field
The present invention relates to the amino acid chemical field, relate to a kind of separation method of lysine bacteria specifically.
Background technology
Methionin is that human body one of can not self eight seed amino acid synthetic but that very need, because of the staple food of China: lack Methionin in the cereal, so be otherwise known as " first indispensable amino acid ".Methionin is added in the food such as drink, rice, flour, can, can improve proteinic utilization ratio, thus the nutrition of nutrient fortified food greatly, play promote to grow, appetite stimulator, minimizing disease, constitutional effect; And Methionin is a kind of good food fortifier, is used for the effect that can has deodorizing and fresh-keeping; Therefore Methionin is widely used in feed and foodstuffs industry.
Methionin is mainly prepared by fermentation method, the solid-liquid separation of its fermented liquid is the important step in the Methionin production process, if thalline promptly enters the later separation operation without solid-liquid separation, a large amount of high concentrated organic wastewaters will be produced, cause serious environmental pollution, and can cause the off quality of the finished product.At present, the solid-liquid separation of fermented liquid adopts solid-liquid separating equipments such as vacuum drum, whizzer, film mostly in the industry.
But aforesaid device itself is expensive, and in technological process, because thalline is little, needs to separate repeatedly, and the process energy consumption is bigger; Because the concentration of isolated thalline concentrated phase is lower, cause the yield of product to reduce on the other hand, and the energy consumption of the drying course of thalline is subsequently increased.
Summary of the invention
The purpose of this invention is to provide a kind of method that can effectively separate lysine bacteria, this method can overcome traditional technology energy consumption height, shortcoming that facility investment is big, reaches the purpose of effective separation lysine bacteria and lysine fermentation liquor clear liquid.
Method of the present invention comprises: 1) add flocculation agent in fermented liquid, mixed 1-60 minute; 2) fermented liquid after will flocculating is pressed in the plate-and-frame filter press, filters.
Method of the present invention also comprises sterilization before step 1): fermented liquid is warmed up to 65～70 ℃, insulation 1-3h.
Method of the present invention before described sterilization steps, also comprises lysine fermentation liquor is transferred PH to 3.0～6.0 with mineral acid.
Method of the present invention is in described step 2) afterwards, further comprising the steps of: as i) filter cake to be dried up; Or further comprise and ii) dry filter cake.
Clear liquid after the filtration directly enters subsequent processing.
Wherein, the concentration of the described fermented liquid of step 1) is 13-17%; The add-on of flocculation agent is 20-1000ppm;
The described interpolation flocculation agent of step 1) is to add inorganic flocculating agent earlier, mixes 1～30 minute; Add organic floculant again, mixed 1～30 minute.
The add-on of described inorganic flocculating agent is 100-500ppm, preferred 300ppm; The add-on of described organic floculant is 20-100ppm, preferred 60ppm.
Described inorganic flocculating agent is one or more in the flocculation agents such as poly-aluminium flocculating agent, poly-ferric flocculant, preferably poly-aluminium flocculating agent; Described organic floculant is that molecular weight is one or more in 500～1,500 ten thousand the anionic flocculant, preferred 5,000,000～1000 sub-very much weight polyacrylamide type flocculation agents.
Method of the present invention also is applicable to the separation of aminoglutaminic acid thalline in the fermented liquid.
The present invention is by flocculating to lysine bacteria, thereby makes lysine bacteria be easy to filtering separation, adopts plate-and-frame filter press separating thallus and clear liquid then, thereby effectively separates lysine bacteria, reduces the thalline separation costs; Mainly contain following advantage:
1) water, electricity, steam consumption are low.Adopt one ton of Methionin membrane filtration of the every production of membrane filtration lysine fermentation liquor operation need consume 3 tons of steam, electricity 200 degree, 1.5 tons in water; And adopt one ton of Methionin of the every production of flocculation process need consume 1 ton of steam, electricity 30 degree, 0.3 ton in water.
2) thalline moisture is low, the yield height.Owing to adopt membrane filtration or disk plate centrifuge all to require thalline to have flowability mutually, so isolated thalline moisture height reach more than 90%, and also contain part Methionin in the isolated water, so yield is lower; After adopting flocculation process, isolated thalline moisture can reach below 40%, when improving yield, has reduced the oven dry cost.
3) facility investment is low, and equipment is easy to safeguard that maintenance cost is low.Film or disk plate centrifuge price are comparatively expensive, and the facility investment height damages the maintenance cost height; Plate-and-frame filter press is a common equipment, and price is lower, and is simple to operate, and maintenance cost is low.
Description of drawings
The schema of Fig. 1 the inventive method.
Embodiment
Following examples are used to illustrate the present invention, but are not used for limiting the scope of the invention.Embodiment 1
1, material and equipment:
| Equipment and title material | Model | Quantity | Remarks |
| Impeller pump | Flow 100L | 1 | |
| Inorganic flocculating agent | Polyiron sulfate | 500g | |
| Organic floculant | Anionic | 500g | Molecular weight 1,000 ten thousand polyacrylamide resins |
| Lysine fermentation liquor | ----- | 250L | The workshop provides concentration 15% |
| The vitriol oil | Technical grade | 5kg | The workshop provides |
| Plate-and-frame filter press | --- | 1 | 0.25 square metre of filtration area |
2, concrete grammar and result:
2.1 the 250L fermented liquid is put in the retort, regulate pH value to 3.7 with the vitriol oil, heat sterilization, sterilising conditions are 70 ℃ and are incubated 1.5 hours;
2.2 it is 2% solution that the inorganic flocculating agent water is mixed with concentration;
2.3 the organic floculant water is mixed with 0.2% solution;
2.4 add inorganic flocculating agent earlier in fermented liquid, dosage is 50ppm, stirs 10 minutes; Add organic floculant then, dosage is 100ppm, stirs 10 minutes.
Squeeze in the plate-and-frame filter press 2.5 will add the fermented liquid of flocculation agent with impeller pump, flow is 60L/h, till fermented liquid has advanced.
2.6 the press filtration clear liquid is after the tripolite compound filter, clear liquid enters next process.
2.6 water inlet (5% fermentation liquid measure) flush cake is used air blow drying then.
Get final product 2.7 filter cake Tumblied Dry.
Note observing the filtrate quality in the filtration procedure, guarantee that the filtrate turbidity meets the requirements.Experimental result is: filter cake moisture 68%, wherein lysine content 8.2%, filtrate turbidity 4.8NTU.Every square of Plate Filtration volume is 1000L, and the filtrate quality meets the requirements.
Embodiment 2
1, material and equipment:
| Equipment and title material | Model | Quantity | Remarks |
| Impeller pump | Flow 100L | 1 | |
| Inorganic flocculating agent | Polymerize aluminum chloride | 500g | |
| Organic floculant | Anionic | 500g | Molecular weight 5,000,000 polyacrylamide resins |
| Lysine fermentation liquor | ----- | 250L | The workshop provides concentration 14.1% |
| The vitriol oil | Technical grade | 4kg | The workshop provides |
| Plate-and-frame filter press | --- | One | 0.25 square metre of filtration area |
2, concrete grammar and result:
2.1 the 250L fermented liquid is put in the retort, regulate pH value to 4.8 with the vitriol oil, heat sterilization, sterilising conditions are 65 ℃ and are incubated 2.5 hours;
2.2 it is 2% solution that the inorganic flocculating agent water is mixed with concentration;
2.3 the organic floculant water is mixed with 0.2% solution;
2.4 add inorganic flocculating agent earlier in fermented liquid, dosage is 400ppm, stirs 20 minutes; Add organic floculant then, dosage is 20ppm, stirs 30 minutes.
Squeeze in the plate-and-frame filter press 2.5 will add the fermented liquid of flocculation agent with impeller pump, flow is 60L/h, till fermented liquid has advanced.
2.6 the press filtration clear liquid is after the tripolite compound filter, clear liquid enters next process.
2.6 water inlet (5% fermentation liquid measure) flush cake is used air blow drying then.
Get final product 2.7 filter cake Tumblied Dry.
Note observing the filtrate quality in the filtration procedure, guarantee that the filtrate turbidity meets the requirements.Experimental result is: filter cake moisture 65%, wherein lysine content 8.0%, filtrate turbidity 3.2NTU.Every square of Plate Filtration volume is 1000L, and the filtrate quality meets the requirements.
Embodiment 3
1, material and equipment:
| Equipment and title material | Model | Quantity | Remarks |
| Impeller pump | Flow 100L | 1 | |
| Inorganic flocculating agent | Polymerize aluminum chloride | 500g | |
| Organic floculant | Anionic | 500g | Molecular weight 1,500 ten thousand polyacrylamide resins |
| Lysine fermentation liquor | ----- | 250L | The workshop provides concentration 13.5% |
| The vitriol oil | Technical grade | The workshop provides | |
| Plate-and-frame filter press | --- | 1 | 0.25 square metre of filtration area |
2, concrete grammar and result:
2.1 the 250L fermented liquid is put in the retort, regulate pH value to 5.6 with the vitriol oil, heat sterilization, sterilising conditions are 70 ℃ and are incubated 2 hours;
2.2 it is 2% solution that the inorganic flocculating agent water is mixed with concentration;
2.3 the organic floculant water is mixed with 0.2% solution;
2.4 add inorganic flocculating agent earlier in fermented liquid, dosage is 300ppm, stirs 30 minutes; Add organic floculant then, dosage is 60ppm, stirs 10 minutes.
Squeeze in the plate-and-frame filter press 2.5 will add the fermented liquid of flocculation agent with impeller pump, flow is 60L/h, till fermented liquid has advanced.
2.6 the press filtration clear liquid is after the tripolite compound filter, clear liquid enters next process.
2.6 water inlet (5% fermentation liquid measure) flush cake is used air blow drying then.
Get final product 2.7 filter cake Tumblied Dry.
Note observing the filtrate quality in the filtration procedure, guarantee that the filtrate turbidity meets the requirements.Experimental result is: filter cake moisture 61%, wherein lysine content 8.2%, filtrate turbidity 2.8NTU.Every square of Plate Filtration volume is 1000L, and the filtrate quality meets the requirements.
Claims (10)
1, a kind of separation method of lysine bacteria comprises: 1) add flocculation agent in fermented liquid, mixed 1-60 minute; 2) fermented liquid after will flocculating is pressed in the plate-and-frame filter press, filters.
2, separation method as claimed in claim 1 is characterized in that, also comprises sterilization before described step 1): fermented liquid is warmed up to 65～70 ℃, insulation 1-3h.
3, separation method as claimed in claim 2 is characterized in that, before described sterilization steps, also comprises lysine fermentation liquor is adjusted pH to 3.0～6.0 with mineral acid.
4, as the arbitrary described separation method of claim 1～3, it is characterized in that, in described step 2) afterwards, further comprising the steps of: as i) filter cake to be cleaned, dries up; Or further comprise and ii) dry filter cake.
5, separation method as claimed in claim 1 is characterized in that, the concentration of the described fermented liquid of step 1) is 13-17%; The add-on of flocculation agent is 20-1000ppm.
As claim 4 or 5 described separation methods, it is characterized in that 6, the described interpolation flocculation agent of step 1) is to add inorganic flocculating agent earlier, mixed 1～30 minute; Add organic floculant again, mixed 1～30 minute.
As claim 4 or 5 described separation methods, it is characterized in that 7, the add-on of described inorganic flocculating agent is 100-500ppm; The add-on of described organic floculant is 20-100ppm.
8, separation method as claimed in claim 7 is characterized in that, the add-on of described inorganic flocculating agent is 300ppm; The add-on of described organic floculant is 60ppm.
As claim 1～3,7 arbitrary described separation methods, it is characterized in that 9, described inorganic flocculating agent is one or more in the flocculation agents such as poly-aluminium flocculating agent, poly-ferric flocculant; Described organic floculant is that molecular weight is one or more in 500～1,500 ten thousand the anionic flocculant.
10, separation method as claimed in claim 9 is characterized in that, described inorganic flocculating agent is poly-aluminium flocculating agent; Described anionic flocculant is that molecular weight is 5,000,000～1,000 ten thousand superelocs.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2009100857184A CN101580800B (en) | 2009-05-27 | 2009-05-27 | Separation method of lysine bacteria |
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| CN2009100857184A CN101580800B (en) | 2009-05-27 | 2009-05-27 | Separation method of lysine bacteria |
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| CN101580800A true CN101580800A (en) | 2009-11-18 |
| CN101580800B CN101580800B (en) | 2011-03-09 |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103341191A (en) * | 2013-07-05 | 2013-10-09 | 梁山正大菱花生物科技有限公司 | Inactivated lysine strain and detection method |
| CN103725615A (en) * | 2013-12-30 | 2014-04-16 | 广东海纳川药业股份有限公司 | Bacteria recovery method and flocculation composition for bacteria recovery |
| CN114014770A (en) * | 2021-06-30 | 2022-02-08 | 安徽华恒生物科技股份有限公司 | Method for recycling concentrated phase of amino acid fermentation liquor |
-
2009
- 2009-05-27 CN CN2009100857184A patent/CN101580800B/en active Active
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103341191A (en) * | 2013-07-05 | 2013-10-09 | 梁山正大菱花生物科技有限公司 | Inactivated lysine strain and detection method |
| CN103725615A (en) * | 2013-12-30 | 2014-04-16 | 广东海纳川药业股份有限公司 | Bacteria recovery method and flocculation composition for bacteria recovery |
| CN103725615B (en) * | 2013-12-30 | 2016-06-15 | 广东海纳川生物科技股份有限公司 | A kind of thalline recovery method and the flocculating composition reclaimed for thalline |
| CN114014770A (en) * | 2021-06-30 | 2022-02-08 | 安徽华恒生物科技股份有限公司 | Method for recycling concentrated phase of amino acid fermentation liquor |
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| CN101580800B (en) | 2011-03-09 |
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