CN202951402U - Lysine production device with fermentation liquor treatment - Google Patents
Lysine production device with fermentation liquor treatment Download PDFInfo
- Publication number
- CN202951402U CN202951402U CN2012207178232U CN201220717823U CN202951402U CN 202951402 U CN202951402 U CN 202951402U CN 2012207178232 U CN2012207178232 U CN 2012207178232U CN 201220717823 U CN201220717823 U CN 201220717823U CN 202951402 U CN202951402 U CN 202951402U
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- CN
- China
- Prior art keywords
- storage tank
- ion exchange
- hydrochloric acid
- district
- fermentation liquor
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- 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.)
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
Abstract
The utility model discloses a lysine production device with fermentation liquor treatment. The lysine production device a fermentation liquor storage tank and a membrane filtration system which are connected via a pipeline, wherein a fermentation liquor concentrated-phase reception and storage tank, and a clear liquor storage tank are respectively communicated on the membrane filtration system via pipelines; a membrane drainage pipeline and a return pipeline are used for separation; and 65% lysine is produced by fermentation liquor filtered by the membrane filtration system and then is drained in the fermentation liquor concentrated-phase reception and storage tank. According to the lysine production device disclosed by the utility model, dialysis filtration steps are reduced, the dialysis time is shortened, a hydrochloric acid regeneration step is added in an ion exchange step, the consumption of raw materials such as sulphuric acid and ammonia is saved, the energy consumption of water, electricity and steam is saved, and the yield and the output of lysine are improved compared with the prior.
Description
Technical field
The utility model relates to the process units that a kind of lysine fermentation liquor is processed, and specifically, relates to the process units that a kind of lysine fermentation liquor is processed.
Background technology
In traditional lysine is produced, zymotic fluid is first used the sulfuric acid acid adjustment, and then heating is by after film, and clear liquid enters ion exchange system in the clear liquid storage tank, concentrated phase is back in the zymotic fluid storage tank, with the material prolongation of running time, the material in the zymotic fluid storage tank is more and more denseer, when being concentrated to 7-8 times, start to add the water dialysis, until in concentrated phase lysine content lower than 1.2g/dl after, this concentrated phase material is mainly mycoprotein, produces animal feeding-stuff containing somatic protein after dry; And add the clear liquid that filters out in the water dialysis procedure also in the clear liquid storage tank, cause in the clear liquid storage tank lysine content on the low side; The ceramic membrane method of operation different (filtering fermentating liquid, for a moment filter dislysate) a little while, cause the fluctuation of clear liquid lysine content larger.Simultaneously, the lysine clear liquid is through ammonia type resin adsorption, and the adsorption capacity of ammonia type resin is lower, causes the ion exchange system disposal ability low.This technique is low in ceramic membrane workshop section utilization rate of equipment and installations, and water consumption is large, and the production time is long, causes ion exchange system charging content lower; Simultaneously, ion exchange system ammonia type production of resins ability is low, collects the liquid lysine content after ion-exchange low, and the ion exchange system quantity of wastewater effluent is larger, and energy consumption is high.
The utility model content
Technical problem to be solved in the utility model is to provide a kind of lysine fermentation liquor clear liquid separates with concentrated phase, and the process units that the lysine fermentation liquor of production different cultivars lysine product, ion exchange system change method of operation raising output is processed.
For addressing the above problem, the utility model by the following technical solutions:
The process units that a kind of lysine fermentation liquor is processed, comprise the zymotic fluid storage tank, the membrane filtration system that connect by pipeline, be communicated with respectively the zymotic fluid concentrated phase by pipeline on membrane filtration system and receive storage tank and clear liquid storage tank, the film discharge pipe is separated with the feed back pipeline, and the zymotic fluid concentrated phase that is discharged to after membrane filtration system filters receives production 65% lysine in storage tank.
Below further improvement of these options:
The clear liquid storage tank is communicated with ion exchange system, and clear liquid enters absorption in ion exchange system, purifies, and produces 98.5% FE-5.
Further improve: the zymotic fluid storage tank comprises the first zymotic fluid storage tank and the second zymotic fluid storage tank.
Further improve: ion exchange system comprises that several hydrochloric acid turn Hydrogen ion exchange resin tank, several hydrochloric acid turn Hydrogen ion exchange resin tank be separated into respectively independently from hand over absorption wash district, from handing over feed zone, secondary feeds district, salt acid washing water district, regeneration of hydrochloric acid district, free Qu Heding and wash district.
Further improve: from handing over absorption to wash hydrochloric acid in district, turn Hydrogen ion exchange resin tank and turn on the connecting pipeline between Hydrogen ion exchange resin tank the secondary feeds storage tank is installed with hydrochloric acid in the friendship feed zone; The secondary feeds storage tank simultaneously turns Hydrogen ion exchange resin tank with hydrochloric acid in the secondary feeds district and is communicated with, and the clear liquid storage tank turns Hydrogen ion exchange resin tank with hydrochloric acid in the friendship feed zone and is communicated with.
Further improve: the hydrochloric acid in the secondary feeds district turns on Hydrogen ion exchange resin tank and is communicated with the hc effluent storage tank.
Further improve: the hydrochloric acid in salt acid washing water district turns on Hydrogen ion exchange resin tank and is communicated with the deionization water pot.
Further improve: the hydrochloric acid in the regeneration of hydrochloric acid district turns on Hydrogen ion exchange resin tank and is communicated with the watery hydrochloric acid tank.
Further improve: free hydrochloric acid in district and turn on Hydrogen ion exchange resin tank and be communicated with the weak aqua ammonia tank.
The utility model is compared with original technology, there is following characteristics: not acid adjustment of zymotic fluid, zymotic fluid concentrated phase after membrane filtration system is back to the zymotic fluid concentrated phase and receives in storage tank, clear liquid, in the clear liquid storage tank, is produced respectively the lysine product of different content, like this, zymotic fluid realize the film continuous separate from purpose, material is without dialysis, and the clear liquid lysine content is high, and the ion exchange system inlet amount is large; Ion exchange system increases by a step regeneration of hydrochloric acid technique, ammonia type resin is changed into to h type resin, improved the adsorption capacity of resin, increased after ion-exchange and collected the liquid lysine content, reduce follow-up workshop section processing pressure, further improved lysine production ability.Material is in continuous flow procedure, adopt this combined unit, reduced diafiltration step and dialysis time, ion-exchange step has increased the regeneration of hydrochloric acid step, has saved the consumption of raw materialss such as sulfuric acid, ammonia, save water, electricity, vapour energy consumption, improved lysine yield, output.
Below in conjunction with accompanying drawing and embodiment, to this experiment is novel, be described further
The accompanying drawing explanation
The structural representation that accompanying drawing 1 is the utility model embodiment.
In figure: 1-the first zymotic fluid storage tank; 2-the second zymotic fluid storage tank; The 3-membrane filtration system; 4-clear liquid storage tank; 5-secondary feeds storage tank; 6-hc effluent storage tank; 7-deionization water pot; 8-watery hydrochloric acid tank; 9-weak aqua ammonia tank; 10-zymotic fluid concentrated phase receives storage tank; 12-is from handing over absorption to wash district; 13-is from handing over feed zone; 14-secondary feeds district; 16-frees district; The 17-Ding Xi district; 18-salt acid washing water district; 19-regeneration of hydrochloric acid district; The 20-ion exchange system.
The specific embodiment
Embodiment, as shown in Figure 1,The process units that a kind of lysine fermentation liquor is processed, comprise the zymotic fluid storage tank, the membrane filtration system 3 that connect by pipeline, be communicated with respectively the zymotic fluid concentrated phase by pipeline on membrane filtration system 3 and receive storage tank 10 and clear liquid storage tank 4, after membrane filtration, the concentrated phase discharge pipe is separated with the feed back pipeline, concentrated phase is discharged to the zymotic fluid concentrated phase and receives production 65% lysine in storage tank 10;
Filtering fermentating liquid in membrane filtration system 3 is back to the zymotic fluid concentrated phase and receives in storage tank 10, mounted valve on reflux line, and material not only can postback the ferment liquid storage tank but also can return zymotic fluid concentrated phase reception storage tank 10, and membrane filtration system 3 can be realized continuous production.
Clear liquid storage tank 4 is communicated with ion exchange system 20, and clear liquid enters absorption in ion exchange system 20, purifies, and produces 98.5% FE-5.
The zymotic fluid storage tank comprises the first zymotic fluid storage tank 1 and the second zymotic fluid storage tank 2.
Ion exchange system 20 comprises that several hydrochloric acid turn Hydrogen ion exchange resin tank, several hydrochloric acid turn Hydrogen ion exchange resin tank be separated into respectively independently from hand over absorption wash district 12, from handing over feed zone 13, secondary feeds district 14, salt acid washing water district 18, regeneration of hydrochloric acid district 19, freeing 16 He Dingxi districts 17, district;
The setting in salt acid washing water district 18 and regeneration of hydrochloric acid district 19, be mainly used in ion exchange resin conversion, because h type resin is higher than the adsorption capacity of ammonia type resin, can improve equipment capacity.
Salt acid washing water district 18 and regeneration of hydrochloric acid district 19 are at charging absorption lysine, because ammonia type resin is higher than the adsorption capacity of h type resin, so after changing technique, ion exchange system is processed can and be increased, and collects the liquid lysine content and improves.
Turn Hydrogen ion exchange resin tank and from handing over the interior hydrochloric acid of feed zone 13 to turn on the connecting pipeline between Hydrogen ion exchange resin tank, secondary feeds storage tank 5 is installed from the hydrochloric acid of handing over absorption to wash in district 12; Secondary feeds storage tank 5 turns Hydrogen ion exchange resin tank with hydrochloric acid in secondary feeds district 14 simultaneously and is communicated with, and clear liquid storage tank 4 turns Hydrogen ion exchange resin tank with the hydrochloric acid interior from friendship feed zone 13 and is communicated with.
Hydrochloric acid in secondary feeds district 14 turn on Hydrogen ion exchange resin tank and are communicated with hc effluent storage tank 6;
Hydrochloric acid in salt acid washing water district 18 turn on Hydrogen ion exchange resin tank and are communicated with deionization water pot 7;
Hydrochloric acid in regeneration of hydrochloric acid district 19 turn on Hydrogen ion exchange resin tank and are communicated with watery hydrochloric acid tank 8, for ion exchange resin conversion.
Freeing hydrochloric acid in district 16 turns on Hydrogen ion exchange resin tank and is communicated with weak aqua ammonia tank 9;
Material is in continuous flow procedure, adopt this combined unit, reduced diafiltration step and dialysis time, ion-exchange step has increased the regeneration of hydrochloric acid step, has saved the consumption of raw materialss such as sulfuric acid, ammonia, save water, electricity, vapour energy consumption, improved lysine yield, output.
Claims (9)
1. the process units that lysine fermentation liquor is processed, comprise the zymotic fluid storage tank, the membrane filtration system (3) that connect by pipeline, it is characterized in that:
Membrane filtration system (3) is upper is communicated with respectively zymotic fluid concentrated phase reception storage tank (10) and clear liquid storage tank (4) by pipeline, the film discharge pipe is separated with the feed back pipeline, and the zymotic fluid concentrated phase that is discharged to after membrane filtration system (3) filters receives production 65% lysine in storage tank (10).
2. the process units that a kind of lysine fermentation liquor according to claim 1 is processed is characterized in that:
Clear liquid storage tank (4) is communicated with ion exchange system (20), and clear liquid enters absorption in ion exchange system (20), purifies, and produces 98.5% FE-5.
3. the process units that a kind of lysine fermentation liquor according to claim 1 is processed is characterized in that:
The zymotic fluid storage tank comprises the first zymotic fluid storage tank (1) and the second zymotic fluid storage tank (2).
4. the process units of processing according to the described a kind of lysine fermentation liquor of claim 2 or 3 is characterized in that:
Ion exchange system (20) comprises that several hydrochloric acid turn Hydrogen ion exchange resin tank, several hydrochloric acid turn Hydrogen ion exchange resin tank be separated into respectively independently from hand over absorption wash district (12), from handing over feed zone (13), secondary feeds district (14), salt acid washing water district (18), regeneration of hydrochloric acid district (19), freeing district (16) He Dingxi district (17).
5. the process units that a kind of lysine fermentation liquor according to claim 4 is processed is characterized in that:
Turn Hydrogen ion exchange resin tank and from handing over the interior hydrochloric acid of feed zone (13) to turn on the connecting pipeline between Hydrogen ion exchange resin tank, secondary feeds storage tank (5) is installed from the hydrochloric acid of handing over absorption to wash in district (12); Secondary feeds storage tank (5) simultaneously turns Hydrogen ion exchange resin tank with hydrochloric acid in secondary feeds district (14) and is communicated with, and clear liquid storage tank (4) turns Hydrogen ion exchange resin tank with the hydrochloric acid interior from friendship feed zone (13) and is communicated with.
6. the process units that a kind of lysine fermentation liquor according to claim 4 is processed is characterized in that:
Hydrochloric acid in secondary feeds district (14) turns on Hydrogen ion exchange resin tank and is communicated with hc effluent storage tank (6).
7. the process units that a kind of lysine fermentation liquor according to claim 4 is processed is characterized in that:
Hydrochloric acid in salt acid washing water district (18) turns on Hydrogen ion exchange resin tank and is communicated with deionization water pot (7).
8. the process units that a kind of lysine fermentation liquor according to claim 4 is processed is characterized in that:
Hydrochloric acid in regeneration of hydrochloric acid district (19) turns on Hydrogen ion exchange resin tank and is communicated with watery hydrochloric acid tank (8).
9. the process units that a kind of lysine fermentation liquor according to claim 4 is processed is characterized in that: free hydrochloric acid in district (16) and turn on Hydrogen ion exchange resin tank and be communicated with weak aqua ammonia tank (9).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2012207178232U CN202951402U (en) | 2012-12-24 | 2012-12-24 | Lysine production device with fermentation liquor treatment |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2012207178232U CN202951402U (en) | 2012-12-24 | 2012-12-24 | Lysine production device with fermentation liquor treatment |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN202951402U true CN202951402U (en) | 2013-05-29 |
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN2012207178232U Expired - Lifetime CN202951402U (en) | 2012-12-24 | 2012-12-24 | Lysine production device with fermentation liquor treatment |
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| Country | Link |
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| CN (1) | CN202951402U (en) |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103992964A (en) * | 2014-03-21 | 2014-08-20 | 山东寿光巨能金玉米开发有限公司 | High pH value tolerant bacterial strain and novel fermentation method for producing lysine |
| CN113122443A (en) * | 2021-04-23 | 2021-07-16 | 徐州生物工程职业技术学院 | Energy-saving fermentation device for producing polypeptide drugs |
| CN113201438A (en) * | 2021-05-14 | 2021-08-03 | 泰山恒信有限公司 | Intelligent capsule type multi-region continuous fermentation system and fermentation method |
-
2012
- 2012-12-24 CN CN2012207178232U patent/CN202951402U/en not_active Expired - Lifetime
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103992964A (en) * | 2014-03-21 | 2014-08-20 | 山东寿光巨能金玉米开发有限公司 | High pH value tolerant bacterial strain and novel fermentation method for producing lysine |
| CN103992964B (en) * | 2014-03-21 | 2016-10-12 | 山东寿光巨能金玉米开发有限公司 | A kind of resistant to high pH value strain and fermentative Production lysine method |
| CN113122443A (en) * | 2021-04-23 | 2021-07-16 | 徐州生物工程职业技术学院 | Energy-saving fermentation device for producing polypeptide drugs |
| CN113122443B (en) * | 2021-04-23 | 2021-09-10 | 徐州生物工程职业技术学院 | Energy-saving fermentation device for producing polypeptide drugs |
| CN113201438A (en) * | 2021-05-14 | 2021-08-03 | 泰山恒信有限公司 | Intelligent capsule type multi-region continuous fermentation system and fermentation method |
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| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| CX01 | Expiry of patent term | ||
| CX01 | Expiry of patent term |
Granted publication date: 20130529 |