CN202924999U - Fermentation linkage device - Google Patents
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- CN202924999U CN202924999U CN 201220588863 CN201220588863U CN202924999U CN 202924999 U CN202924999 U CN 202924999U CN 201220588863 CN201220588863 CN 201220588863 CN 201220588863 U CN201220588863 U CN 201220588863U CN 202924999 U CN202924999 U CN 202924999U
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Abstract
The utility model discloses a fermentation linkage device which comprises a fermentation primary tank, a fermentation secondary tank, a monitoring system and an analysis system, wherein the fermentation primary tank is connected with the fermentation secondary tank through a pipeline; the fermentation primary tank and the fermentation secondary tank are connected with the monitoring system respectively; and the analysis system performs concentration analysis on the data measured by the monitoring system. By optimizing the fermentation process by the fermentation linkage device disclosed by the utility model, the development period is shortened, and the optimization cost is lowered.
Description
Technical field
The utility model relates to technical field of biological fermentation, particularly a kind of fermentation linkage system.
Background technology
Biological fermentation process is to have the cell of vitality to be the theme, give the process that specific culture environment condition is produced valuable purpose product, the optimization of technological condition for fermentation research effectively carries out for what instruct production process the very important effect that plays smoothly, existing fermentation technology optimization research is mainly to investigate by batch fermentation or the test of continuously fermenting in specific fermentor tank, or utilize several fermentor tanks to carry out simultaneously batch experiment and investigate, what have has also equipped multi-parameter collecting system to fermentor tank, carries out the optimization research of fermenting process.Due to the complicacy of microbial physiology metabolic characteristic in fermenting process and variation uncertainty affected by environment, make when carrying out optimization of fermentation condition the comparability between lot data relatively poor, therefore the optimization conclusion of process has been brought larger deviation or obtained opposite conclusion, simultaneously for long antibiotic fermentation process optimization of cycle, required cycle of global optimization is longer, is unfavorable for the propelling of production schedule and the quick raising of productivity effect.
for this reason, existing method is to have formed various or general device technique system and methods for using them take the different fermentations product as object, as Chinese patent " method and apparatus of a kind of optimizing fermentation and the amplification " (patent No.: 200810042759.0), its emphasis is exactly the apparatus system that is designed for research, the data and the computer packages data processing that obtain by the various sensors of fermenting process, bioprocess complicated in bio-reactor is decomposed into the characteristic research of different scale, relation between the event of understanding different scale, each yardstick has different subject principle and Changing Pattern, study their quantitative change to qualitative change, and the impact overall on complex system that forms thus, so just might solve part that optimizing fermentation faces and whole relation, formed thus a cover based on the optimisation technique of the fermenting process Issues On Multi-scales research of parameter correlation analysis and the amplifying technique that the fermenting process multiparameter is adjusted.In a word, the bioinformation of each aspect of acquisition fermenting process as much as possible, then with the multi-scale parameters relative theory, real time data processing by computer software, find the process optimization key parameter that is characterized as foundation with dependence on parameter in mass data, be sensitive parameter, and then be used for instructing the zymotechnique operation, greatly promoted thus the progress of optimizing fermentation and amplifying technique.
But above apparatus and method just find the crucial sensitive parameter of process optimization foundation from mass data, it is the research work with directivity, really accomplishing also needs to do great many of experiments work for actual production, that is to say and to carry out Study on thinning on acquired research direction, could further obtain process conditions or the equipment amplification design of optimization.
The greatest difficulty that these refinement cut-and-try works run into is the comparability between every batch of test, requires initial cell physiological status consistence, reactor growth environment comparability, data collection and analysis credibility relatively during test.Due to vital process and with the high complexity relation of external environment Relations Among, as long as a small variation just may cause the difference of process, this small variation might be from the difference of the nuance of the difference of the acquisition of bacterial classification and seed culture, different substratum starting material source, disinfecting action, operational condition, different fermentations device characteristics, employee's operating habit etc. even, and the Bearing performance that these slight changes cause is in diversity, time variation, correlative coupling and the uncertainty of the Fermentation Process of Parameter trend curve that obtains.Therefore, under so complicated multifactoral study changes, be again to reach the fermentation operation experiment of tens to up to a hundred hours, the data comparability between every batch just becomes large problem, and for this reason, the whole Study on thinning cycle reaches several months or several years sometimes.Even so, also always there are various doubt in the result of acquisition, has affected the decision-making of relevant production or problems of engineering design.
In sum, fermentation unit of the prior art can not guarantee the consistence of initial cell physiological status, the consistence of reactor growth environment, so the data collection and analysis credibility is inadequate.In addition, the existing fermentation optimization cycle is long, and cost is high.
The utility model content
Fermenting process is the Living system of a complexity, and its process feature is correlative coupling between the parameter diversity that comprises bioinformation, parameter time varying, parameter and the uncertainty of process parameter change.for adapting to the process study of These characteristics, reach the purpose of process optimization and amplification, the parallel fermentation culture device of design interlock, when the process control condition of sending out certain stage of yeast tank fermenting process is optimized, with this aseptic being transferred in the sub-tank of parallel fermentation of fermentation culture constantly, TT﹠C system by sub-tank the initial physiological status furnishing of microorganism in the sub-tank of fermentation with after a yeast tank is consistent, the sub-tank that ferments is carried out the control of different investigation factors or different levels, and Real-time Collection is carried out in the variation of its physiological metabolism parameter, investigate the metabotic change of fermenting process in certain hour, the optimization that obtains this stage is controlled technique, thereby instruct the production test research of sending out yeast tank.
Optimize more quickly and accurately the technological condition for fermentation of different steps in order to promote the fermenting process experimental study, urgent need is optimized the adjustment test to the culturing process of different steps, to guarantee that simultaneously microbial physiology state initial when the factors influencing in this stage has consistence, and except treating the investigation factor, other environmental factorss guarantee consistence as far as possible, but the comparative of guarantee the data obtained like this.
The purpose of this utility model is in order to solve the problems of the prior art, a kind of fermentation linkage system is provided, the fermented liquid of sending out in yeast tank is optimized in the sub-tank of a plurality of fermentations, to realize the consistence of its initial cell physiological status, and except treating the investigation factor, other environmental factorss guarantee consistence as far as possible, has comparability with the data that realize gained, the parameter of respectively controlling of each yeast tank, the sub-tank of fermentation is concentrated collection analysis simultaneously, thereby has guaranteed that the relevant thalline physiology or the operational parameter data that obtain have reliability.
The technical solution of the utility model is:
A kind of fermentation linkage system, it is characterized in that, comprise and send out yeast tank, ferment sub-tank, supervisory system and analytical system, described yeast tank is connected with the sub-tank of described fermentation by pipeline, described yeast tank is connected with described supervisory system respectively with the sub-tank of fermentation, the data analysis that described analytical system records described supervisory system.
Further, described yeast tank is 1 to 2, and the sub-tank of described fermentation is 2 to 8, and preferred 4 to 8, the described sub-tank of respectively fermenting is in parallel and be connected to by pipeline and send out on yeast tank.
Further, the volume of the sub-tank of described fermentation is 0.25L to 50L, and the volume of described yeast tank is 50L to 500L.
Further, the cubic capacity of described yeast tank is 2.5 to 50 times of cubic capacity of the sub-tank of fermentation.
Further, the volume of the sub-tank of described fermentation is 5L to 50L, and the capacity of described yeast tank is 500L to 120000L.
Further, the cubic capacity of described yeast tank is 2.5 to 480 times of cubic capacity of the sub-tank of fermentation.
Further, geometrical shape, the volume of the sub-tank of described each fermentation are identical with relevant accessory.
Further, each sub-tank of fermentation and a yeast tank all are furnished with motor, agitator, sensing unit, mounting bracket, process pipe system and electrical control cabinet, and described electrical control cabinet is controlled the sub-tank of described fermentation and a yeast tank by the computer chip in it and electric components.
Further, described sensing unit comprises temperature sensor, pH sensor, dissolved oxygen sensor, full tank weighing sensor, exhaust analyzer, tachogenerator, pressure transmitter, froth breaking sensor and feed supplement LOAD CELLS, also comprises one or more in the micro-online visualizer of cell, viable bacteria quantity sensor, redox potential ORP sensor, the dense OD sensor of bacterium and air flow sensor.
Further, described supervisory system is the three-level computer Controlling System, and wherein first step computer control system is carried out Detection ﹠ Controling to the loop of each parameter of described yeast tank and the sub-tank formation of fermentation; Second stage computer control system is carried out data gathering, set(ting)value control and control loop to the parameter of the single tank body in described yeast tank and the sub-tank of fermentation and is adjusted; Third stage computer control system is carried out the parametric synthesis analysis and outputs to terminal the parameter of front two-stage system.
when can be used for fermenting process, fermentation linkage system of the present utility model becomes operational condition research (temperature, rpm, ventilation, pH, DO, ), fermention medium proportioning and adjustment research, the best feeding-system of fermenting process and work study, mycelia form and anti-shearing research, trace element impact and adjusting, plant age, cultivate progression and seed quality research, the fermentation equipment characteristic research, perseveranceization characteristic and multistage cultured continuously research, the research of thalline physiological property, genetically engineered is than growth rate and inducible factor research, genetic modification and biological characteristics, bioprocess is transcribed, express, control technique and information biology research, systems biology or synthetic biology chassis cell physiological characteristic research, etc..
The beneficial effects of the utility model are:
By a plurality of parallel sub-tank of fermentation that is connected with a yeast tank, the initial physiological status consistence of sub-tank can guarantee respectively to ferment;
By in each sub-tank except treating the investigation factor, other environmental factorss guarantee consistence as far as possible, but the comparative of guarantee the data obtained like this, thereby guaranteed the credibility of the data that optimizing process obtains;
The sub-tank of a plurality of fermentations can carry out high believable optimization research to a plurality of factors that affect sensitive parameter simultaneously, thereby shortens the R﹠D cycle, reduces the cost of optimizing;
The sub-tank of each fermentation adopts centralized Control and data centralization collection and unified analysis-by-synthesis with sending out yeast tank, has brought error thereby reduced the artificial or software analysis that the independent analysis of every tank may cause, thereby has had data collection and analysis credibility relatively.
In sum, fermentation linkage system of the present utility model has overcome the complicated multifactoral study variation of fermenting process and tens and has arrived the caused data reliability problem of batch fermentation operation experiments of up to a hundred hours, greatly increase experiment credible, shortened the process optimization research cycle that reaches several months or several years.
Description of drawings
Accompanying drawing 1 is fermentation linkage system schematic diagram;
Accompanying drawing 2 is the schema of fermentation interlock implementation method;
Accompanying drawing 3 is fermentation interlock block diagram.
Mark in accompanying drawing is respectively:
1. send out yeast tank; 2. sub-tank ferments;
3. agitator; 4. the fermented liquid after inoculating;
201-207. block diagram step.
Embodiment
Elaborate below in conjunction with the embodiment of accompanying drawing to the utility model fermentation linkage system.
referring to accompanying drawing 1, sending out yeast tank 1 is connected by pipeline with the sub-tank 2 of a plurality of fermentations, after being connected in parallel, the sub-tank of a plurality of fermentations is connected with a yeast tank 1, form the fermentation linkage system, the sub-tank 2 of each fermentation with send out the pipe fittings such as valve is set between yeast tank 1 and come being communicated with between the sub-tank 2 of controlled fermentation and a yeast tank 1, and the process that can be delivered to nutrient solution the tank 2 of fermentation from sending out yeast tank 1 is controlled, postvaccinal fermented liquid 4 in the sub-tank 2 of assurance fermentation is identical with the fermented liquid in sending out yeast tank 1, and the amount of each sub-tank indirect fermentation liquid is identical, namely guaranteed the consistence of the initial physiological status of the thalline in the sub-tank of each fermentation.The fermentation linkage system also comprises supervisory system and analytical system, sends out yeast tank 1 and is connected with supervisory system respectively with the sub-tank 2 of fermentation, the data analysis that analytical system records supervisory system.The quantity of the sub-tank 2 of a plurality of fermentations is 4 to 8, sends out yeast tank and is generally one, also can arrange two and link together.The volume of the sub-tank 2 of each fermentation is 2L to 50L, and each volume of sending out yeast tank is 50L to 500L, and the cubic capacity of preferably sending out yeast tank 1 is 1 to 4 times of sub-tank 2 cubic capacitys of fermentation.In order to guarantee the environmental parameter consistence to be investigated of removing of the sub-tank 2 of each fermentation, geometrical shape, volume and the relevant accessory (only showing agitator 3 in figure) of the sub-tank 2 of each fermentation are identical.Send out yeast tank 1 and the sub-tank 2 of fermentation and all be furnished with related accessory and comprise motor, agitator 3, sensing unit, mounting bracket, process pipe system and electrical control cabinet, electrical control cabinet by the computer chip in it and electric components to fermenting sub-tank and send out a yeast tank and control.Wherein sensing unit comprises temperature sensor, pH sensor, dissolved oxygen sensor, full tank weighing sensor, exhaust analyzer interface, tachogenerator, pressure transmitter, froth breaking sensor, feed supplement LOAD CELLS, the micro-online visualizer of cell, viable bacteria quantity sensor, redox potential ORP sensor, the dense OD sensor of bacterium, air flow sensor.Electronic monitoring and control system comprises the three-level computer Controlling System, wherein first step system to single loop parameter such as temperature, rotating speed, air flow, pH, DO, feed supplement weigh, tank body is weighed etc. carries out Detection ﹠ Controling; Second stage system is to each single tank parameter such as temperature, mixing speed, ventilation flow rate, tank pressure, froth breaking, pH, dissolved oxygen concentration, fermented liquid weight, feed supplement amount set(ting)value are controlled, and comprise that implementation data demonstration, electrode automatic Calibration, the loop parameter such as adjust carries out Detection ﹠ Controling; Third stage system concentrates the state parameter of each tank and shows and control.Data analysis system is visual comprehensive data analysis and process study software package (Shanghai DGY-2007-0798), can show in the multiple terminals, and can show different pictures at different terminals according to the research needs.
Referring to accompanying drawing 2, the implementation method of fermentation through transport comprises that step is as follows: the first step: add substratum, sterilization, inoculation and cultivation (the 201st step in figure) in described yeast tank;
Second step: the fermenting process multi-scale parameters that supervisory system is obtained from send out yeast tank by described analytical system carries out correlation analysis (the 202nd step in figure);
The 3rd step: the crucial sensitive parameter (the 203rd step in figure) of determining to affect fermenting process according to the analytical results of analytical system;
The 4th step: will send out yeast tank and cultivate predefined phase (the 204th step in figure);
The 5th step: the nutrient solution that will send out in yeast tank is transported to (the 205th step in figure) in the sub-tank of a plurality of fermentations with volume;
The 6th step: according to the crucial sensitive parameter that affects fermenting process of sending out yeast tank and determining, determine that each sub-tank controls parameter accordingly, regulates and controls by supervisory system the sub-tank that respectively ferments, and each sub-tank that ferments is carried out multi-parameters sampling (in figure, the 206th goes on foot);
The 7th step: by analytical system, the multiparameter that collects in the sub-tank that ferments is carried out correlation analysis, instruct and send out yeast tank production test (the 207th step in figure).
Fermenting process multi-scale parameters in second step comprises direct parameter and indirect parameter;
Wherein said direct parameter comprises direct-on-line detect parameters and off-line manual inspection parameter;
Described direct-on-line detect parameters is temperature, mixing speed, ventilation flow rate, tank pressure, froth breaking, pH, dissolved oxygen concentration, fermented liquid weight, feed supplement amount, tail gas oxygen concn, tail gas carbon dioxide concentration;
Described off-line manual inspection parameter is bacterium amount, remaining sugar concentration, specific growth rate and NH
2-N content;
Described indirect parameter is consumption rate, carbon dioxide evolution rate, respiratory quotient and volume oxygen transfer rate.
referring to accompanying drawing 3, the axes experimental process is, after sending out yeast tank and carrying out sterilising treatment, inoculation after preparation substratum and sterilization in sending out yeast tank, premenstruum fermentation obtains affect after the crucial sensitive parameter of fermenting process culture transferring extremely in the sub-tank of sterile a plurality of fermentation, thereby the consistence of initial thalline physiological status in the sub-tank that guaranteed to ferment, regulate the operating parameters of the sub-tank that respectively ferments, the sub-tank that ferments is carried out except treating the investigation factor, other environmental factorss guarantee conforming cultivation as far as possible, according to the different condition of the crucial sensitive parameter that affects fermenting process, the sub-tank of each fermentation is optimized culture studies, obtain macroscopical metabolic chart of thalline after cultivating, be used for instructing the research of the female tank production test of fermentation.
Embodiment 1:
4 sub-tanks of parallel 5L fermentation, also comprise that 1 50L sends out yeast tank and electronic monitoring Controlling System and data analysis system, sending out yeast tank is connected by pipeline each tank with the sub-tank of fermentation, in female tank, fermented liquid is transported to each sub-tank in order to realization, each fermentor tank of the sub-tank of fermentation and the fermentor tank of a yeast tank can both be realized pH in fermenting process, DO, volume, tail carbon concentration, tail oxygen concentration, oxygen uptake rate (OUR), release of carbonate dioxide speed (CER), respiratory quotient (RQ), the isoparametric online acquisition of viable cell concentrations and comparative analysis.
Utilize the utility model to the red Zymomonas mobilis of pod membrane (
Rhodopseudomonas capsulatus) pilot scale research of Coenzyme Q10 99.0 production process;
Bacterial classification: the red Zymomonas mobilis of pod membrane (select Zhejiang newly with the bacterial classification that becomes biomedical company).
Concrete steps are:
(1) bacterial classification goes down to posterity: substratum is 2% yeast extract medium, and the substratum temperature is 30 ℃, and incubation time is 72 hours, to growing the mazarine bacterium colony;
(2) strain expanded culture: the sterilized seeding tank of bacterial classification access with step (1), carry out two-stage and cultivate, under the condition of unglazed photograph, controlling temperature is 28～30 ℃, stirs 100～300rpm, pressure is 0.02～0.05Mpa, cultivates 20～24 hours;
(3) feeding medium during fermentation is cultivated: under aseptic condition, the seed liquor that step (2) is turned out accesses fermentor tank, under the condition of unglazed photograph, 28～32 ℃ of controlled fermentation temperature, stir 100～300rpm, pressure 0.02～0.05Mpa, incubation time 100～120 hours, fermenting process carry out glucose solution (containing 0.15% potassium dihydrogen phosphate) add continuously keep sugared concentration 0.7%, pH is controlled at 6.7 with ammoniacal liquor, fermentation culture 108h;
The culture medium prescription of seeding tank in step (2) wherein, be by mass percentage: ammonium sulfate 0.10～0.50%, sal epsom 0.10～0.50%, potassium primary phosphate 0.02～0.10%, glucose 0.30～1.00%, corn starch 0.02～0.10%, calcium carbonate 0.35～0.90%, VITMAIN B1 0.001～0.01%, surplus is water, pH value 6.8, the medium sterilization temperature is 118～121 ℃, and the time is 30 minutes;
The culture medium prescription of fermentor tank in step (3) wherein, count in mass ratio: glucose 2.50～4.50%, corn starch 0.80～1.30%, ammonium sulfate 0.10～0.50%, potassium primary phosphate 0.05～0.30%, sal epsom 0.50～2.00%, surplus is water, pH value 6.8, the medium sterilization temperature is 118～121 ℃, and the time is 30 minutes.
Send out yeast tank by 50L and carry out fermenting experiment, the sensitive parameter of finding to affect fermenting process by relation analysis of parameter is the oxygen consumption rate (OUR) of process, and the oxygen restriction is the key that affects fermenting process product anabolism and thalli growth metabolism.and oxygen consumption rate is subject to the control of oxygen transfer rate, the nutrient solution that therefore will be in synthesis phase carries out different oxygen transfer rates control the effects on 4 sub-tanks of parallel fermentation, when culture cycle is 38h, fermentation culture is transferred in 4 sub-tank culture systems of 5L fermentation that link parallel (the sub-tank of 2.5L/) by aseptic pipeline, the rotating speed that the sub-tank adjustment of fermenting is consistent and total air flow, by adjusting the ratio of sub-tank Air and pure oxygen, 4 sub-tanks of fermentation are controlled at different OUR level (75mmol/L/h, 65mmol/L/h, 55mmol/L/h, 45mmol/L/h), cultivate after 10 hours and to investigate the red Zymomonas mobilis of pod membrane to turn to synthesis phase from vegetative period be that best oxygen consumption rate is controlled.
Experimental result shows, the sub-tank that ferments can be good at carrying out collection and the control of oxygen consumption rate OUR etc., the control error of OUR is less than 4.5%, the simultaneous test test result shows, the level that in this stage, OUR is controlled at 55mmol/L/h is synthetic the most favourable to promoting thalli growth and product, and transformation efficiency is apparently higher than other control levels, and its result is as shown in the table:
Net result is used further to instruct 50L to send out the production of yeast tank, in the fermenting process of Coenzyme Q10 99.0, when cell concentration (online viable cell) when changing stationary phase over to, by stirring, OUR is controlled at 55 ± 2mmol/L/h, put tank point 104 hours, production concentration reaches 2780 ± 45mg/ml, and (2463 ± 59mg/ml) have improved 12.9% to its yield increased.
Adopt technical solutions of the utility model, fully shortened and investigated the required time of a plurality of OUR control level in batches, but guaranteed simultaneously the initial physiological status consistence of thalline of investigation and the comparative of experimental result, improved conventional efficient.
Embodiment 2:
Adopt 8 sub-tanks of parallel 5L fermentation, 1 500L to send out the experimental installation that yeast tank forms, utilize this combination can investigate the variation of specified phase shear-stress and key factor envrionment temperature in fermenting process to the impact of fermentating metabolism.
The optimization research of the present embodiment to the rifomycin fermenting process, the production bacterial strain is: Nocardia intermedien (
Nocardia mediterranei), its experimental procedure is as follows:
(1) slant medium (%): sucrose 3.0, peptone 0.5, KCl 0.05, FeSO
40.001, KH
2PO
40.1, MgSO
47H
2O 0.05, agar 1.8, and pH7.0, surplus is water.In the flat board that slant medium is housed, 28 ℃, incubation time is 48 hours, relative humidity 30--60%, culture cycle 12～15d with the seed streak inoculation.
(2) seed culture medium (%): glucose 2.0, soybean cake powder 1.0, peptone 1.0, KH
2PO
40.01, KNO
30.05 surplus is water.28 ℃ of culture temperature, incubation time 48h.
The sterilized seeding tank of bacterial classification access with step (2) carries out two-stage and cultivates, and controlling temperature is 28～30 ℃, stirs 250～400rpm, and pressure is 0.02～0.05Mpa, cultivates 20～24 hours;
(3) fermention medium (%): glucose 11.0, fish meal 0.5, soybean cake powder 1.0, KNO
30.8, KH
2PO
40.02, CaCO
30.5, cobalt chloride 3 μ g/ml, surplus is water.Feeding medium during fermentation is cultivated: under aseptic condition, yeast tank is sent out in the seed liquor access that step (2) is turned out, under the condition of unglazed photograph, 28～32 ℃ of controlled fermentation temperature, pressure 0.02～0.05Mpa, incubation time 100～120 hours, fermenting process carry out glucose solution (containing 0.15% potassium dihydrogen phosphate) add continuously keep sugared concentration 0.7%, pH is controlled at 6.7 with ammoniacal liquor, fermentation culture 108h;
(4) the parallel experimental assembly of interlock, begin timing after packing, after cultivating the time of some cycles, puts the analysis that tank carries out process parameter.
Carry out multi-parameters sampling by the sub-tank that ferments, can realize better optimizing from the angle of process dynamics the modulation process of key factor simultaneously.
Each sub-tank that ferments is in the situation that different shearing force (rotating speed 400,500,600,700rpm), increase along with shearing force, the diameter that bacterium ball in the mycobacterium fermented liquid is intended in Mediterranean Sea diminishes rapidly, when rotating speed during higher than 600rpm, the mesh-like mycelia that thalline becomes to be scattered exists, although dissolved oxygen concentration is all in critical dissolved oxygen concentration more than 35%, the synthesis rate of product significantly descends, and the thalli morphology product synthesis rate under the shearing force of 500rpm is the fastest.
Simultaneous temperature is also the influence factor of a key in the rifomycin fermenting process, temperature directly affects outstanding thalline born of the same parents intracellular metabolite vigor and to the uptake rate of oxygen, each sub-tank that ferments is controlled respectively 26,27,28,29 ℃, can find out that the rising oxygen consumption rate along with culture temperature also increases when temperature is controlled at 28 ℃, the wear rate of oxygen is at 14.5mmol/L/h, and the synthesis rate of product is 125mg/L/h the soonest.As seen utilize 8 parallel fermenter systems to carry out the optimization of gained Key Influential Factors optimum control level in fermenting process, play very important effect for shortening research and development time and scientific effort efficient.
Embodiment 3:
The sub-tanks of 4 2L fermentation, 1 50L send out the experimental installation that yeast tank forms, and utilize this combination can investigate the pH value control strategy optimization of little oxygen consumption such as lactic acid, ethanol, caproic acid and anaerobic fermentation process different steps.50L or larger production tank are cultivated aseptic being transferred in the aseptic sub-tank of 2L fermentation of nutrient solution of specified phase, by adjusting the ratio of air inlet Air and nitrogen, and in conjunction with each the sub-tank of fermentation that collects and the Fermentation Process of Parameter information of a yeast tank, the thalline state of controlling in the sub-tank of each fermentation is consistent with a yeast tank, then change pH control levels different in sub-tank, after cultivating for some time, carry out the multiparameter correlation analysis, obtain the control strategy at the pH of this stage optimum, be used for instructing the production of the female tank of fermentation.
Embodiment 4:
Adopt 5 sub-tanks of 50L fermentation, 1 120 tons (volume is 120000L) to send out the parallel fermentation test of yeast tank interlock, carry out the research of gluconic acid industrial fermentation process optimization, utilize this combination to investigate and keep different sugar concentration in fermenting process to the impact research of the transmission of process oxygen and fermentating metabolism.
Culture condition: aspergillus niger (the Shanghai Industrial aspergillus niger M276 of institute of microbiology).
Substratum:
(1) slant medium, by every liter of calculating, glucose 8g, yeast extract paste 2g, peptone 2g, MgSO
40.2 g, NaH
2PO
40.19g, KH
2PO
4O.1g, MnSO
4O.01g, agar 1.5g, surplus is water.Bacterial classification in preservation pipe is inoculated on slant medium, cultivates in incubator, 28 ℃, cultivated 3 days.
(2) seed culture medium, by every liter of calculating, glucose 609g, MgSO
40.029g, NaH
2P0
40.19g, KH
2P0
40.1g, MnS0
40.01g surplus is water.
Scrape hypothallus with transfering loop and be inoculated in the 15L shaking flask on aseptic operating platform, cultivate 24h, rotating speed 420rpm, 30 ℃.Adopt the two-stage fermentation process control.
(3) basic fermented liquid, by every liter of calculating, glucose 100g, MgSO
40.03g, KH
2PO
40.2g, (NH
4)
2HPO
40.9g, MnSO
40.06g, CaCO
3(2.69g sterilization separately), surplus is water.
Seed liquor in step (2) is produced in tanks to 85 tons of fermention mediums are housed by 10% inoculum size, 32 ℃, control OUR in 158 level, cultivated 32 hours.
120 tons yeast tanks are cultivated 8 hours, and (thalli growth enters stationary phase, product begins fast synthetic) fermented liquid respectively aseptic switching 30 be raised in 50 liters of aseptic sub-tanks of fermentation, by with the contrast of sending out yeast tank physiological metabolism curve, adjust the control condition in the sub-tank of 50L fermentation, make the metabolism state that reaches consistent with sending out yeast tank, then by changing the speed of adding of feed supplement liquid glucose, make the sugared concentration in the sub-tank of fermentation be controlled at different concentration levels, be respectively 1 ± 0.4%, 3 ± 0.6%, 7 ± 0.6%, 9 ± 0.8%, 14 ± 0.9% and control each the fermentation sub-tank have identical temperature, rotating speed, the condition such as air flow and whipped form, observe concentration of substrate to the impact of oxygen transmission and bacterial metabolism.
Result shows, the fermented liquid of initial physiological metabolism state consistency, under identical control condition, the variation of substrate glucose concn affects highly significant to the fermenting process oxygen transfer rate, when glucose concn drops to 6% when following, can obviously promote the effect that in nutrient solution, oxygen transmits, dissolved oxygen is ascendant trend slightly along with glucose concn reduces, thereby brings the oxygen consumption rate OUR of thalline significantly to rise.OUR is obviously higher when glucose concn is controlled at 1 ± 0.4%, sugar consumption speed is very fast, the synthesis rate of glucose saccharic acid has reached 22.4g/L/h, synthesis rate when glucose concn is controlled at 3 ± 0.6%, 7 ± 0.6%, 9 ± 0.8% and 14 ± 0.9% is respectively 15.4 g/L/h, 12.2 g/L/h, 9.6 g/L/h and 9.4 g/L/h, as seen obviously relatively poor when glucose concn oxygen transmission effect higher than 9% time, and no longer change with the change in concentration of glucose.Therefore in the fermentative production of glucose saccharic acid, control suitable glucose fed strategy very crucial to improving productive rate and energy saving aspect.
Embodiment 5
Adopt 4 sub-tanks of 250mL fermentation, 1 50L to send out the parallel fermentation test of yeast tank interlock, carry out the research of vitamin B12 optimizing fermentation, utilize this combination to investigate and keep Oxygen supplied level in fermenting process to the impact research of fermentating metabolism.
(1) produce bacterium: Pseuomonas denitrifican (the Shijiazhuang AL-0125 of Huarong company of pharmacy group).
(2) seed culture medium (g/L): sucrose 40, corn steep liquor 20, trimethyl-glycine 5, (NH
4)
2SO
41, (NH
4)
2 HPO
42, MnSO
4H
2O 0.8, CoCl6H
2O 0.02, and MgO 0.3, and DMBI 0.01, ZnSO
47H
2O 0.01, pH 7.2-7.4;
(3) fermention medium (g/L): sucrose 80, corn steep liquor 45, trimethyl-glycine 14, (NH
4)
2SO
41, KH
2PO
40.75, CoCl6H
2O 0.075, and MgO 0.5, and DMBI 0.05, ZnSO
47H
2O 0.08, CaCO
31, pH 7.2-7.4;
Supplemented medium 1 (g/L): glucose 500, DMBI 0.15, CoCl6H
2O 0.15, the pH nature;
Supplemented medium 2 (g/L): trimethyl-glycine 30, DMBI 0.4, CoCl6H
2O 0.3, pH6.2-6.5.
(4) collecting cells: with the cultured inclined-plane of sterilized water washing, making bacterium dense is 10
8The bacteria suspension that individual cell is every milliliter.
(5) female bottle seed culture: with the bacterial suspension inoculation 2ml that makes in female bottle substratum, loading amount 100ml/500ml, 32 ℃, rotating speed 260rpm cultivated 20-22 hour.
(6) 50L sends out yeast tank and cultivates: will cultivate good after the aseptic female bottle seed liquor 1250ml of microscopy and bottle in aseptic 2L triangular flask; the flame protection is inoculated into the 50L that the 25L substratum is housed and sends out in yeast tank; culture condition is the secondary stirring arm; 32 ℃; air flow 20L/min begins to add continuously glucose and trimethyl-glycine feed liquid substratum according to the thalli growth situation in fermenting process.
with 50L send out fermented liquid that yeast tank cultivates 110 hours (thalline be in product quick synthesis phase) respectively aseptic switching 150ml in the aseptic sub-tank of 250mL fermentation, contrast by the online acquisition parameter, pass through speed adjustment, control four sub-tanks of parallel fermentation and be in different OUR levels (because Pseuomonas denitrifican is to the high-affinity of oxygen, cultivate the middle and later periods, oxyty is 0 minimum level always, therefore the height of OUR has just reflected the height of different keeping levels), and the OUR level that makes No. 2 sub-tanks that ferment wherein and 50L to send out yeast tank consistent, be controlled at 33 ± 0.8mmol/L/h, other three are controlled at respectively 15 ± 0.7mmol/L/h, 24 ± 0.9mmol/L/h and 41 ± 1.1mmol/L/h, and control each the fermentation sub-tank have identical temperature, the condition such as air flow and whipped form, observe different Oxygen supplied levels to the impact of bacterial metabolism.
Result shows, the fermented liquid of initial physiological metabolism state consistency, different Oxygen supplied levels is to fermentating metabolism variable effect highly significant, in the 50L that keeps the oxygen consumption rate level and be controlled at 33 ± 0.8mmol/L/h sent out the interlock fermentor tank that the sub-tank of fermentation of yeast tank and 4 250mL forms, the wear rate of substrate glucose, the synthesis rate of product, product were all very consistent to the transformation efficiency of glucose.Investigation result in the sub-tank of fermentation of 4 parallel 4 250ml that control different Oxygen supplied levels shows, when Oxygen supplied level is regulated to keep the OUR level and is 24 ± 0.9mmol/L/h, the synthesis rate of vitamin B12, transformation efficiency are for the highest, be that in 15 ± 0.7mmol/L/h situation, sugar consumption speed obviously reduces and keep the OUR level, the product synthesis rate is low by 29% during than 24 ± 0.9mmol/L/h.Along with the continuation increase of Oxygen supplied level, the wear rate of sugar significantly increases, but the synthesis rate of vitamin B12 and transformation efficiency present obvious downward trend.
The impact of different Oxygen supplied levels on Fermentation Process of Parameter
* μ, the specific growth rate of logarithmic phase; P, synthesis rate mg/L/h; Y
x/s, the yield coefficients of biomass to substrate; Y
P/s, the yield coefficients of product to substrate glucose; RQ breathes entropy.
Therefore in the fermentation process for vitamin production process of Pseuomonas denitrifican, controls suitable Oxygen supplied level regulation and control to improving productive rate and to fall cost very crucial.The enforcement of this interlock fermenting experiment has guaranteed the consistence of initial thalline state between the accuracy of the sub-reactor investigated and the interlock of female reactor and sub-reactor and the comparability of final test-results.
The above embodiment only is used for explanation the utility model and is not used in restriction scope of the present utility model; should be understood that; for those skilled in the art; under the prerequisite that does not break away from the utility model principle; can also make some improvements and modifications, these improvements and modifications also should be considered as protection domain of the present utility model.
Claims (11)
1.
A kind of fermentation linkage system, it is characterized in that: comprise and send out yeast tank, ferment sub-tank, supervisory system and analytical system, described yeast tank is connected with the sub-tank of described fermentation by pipeline, described yeast tank is connected with described supervisory system respectively with the sub-tank of fermentation, and described analytical system is carried out centralized Analysis to the data that described supervisory system records.
2.
Fermentation linkage system according to claim 1 is characterized in that: described yeast tank is 1 to 2, and the sub-tank of described fermentation is 4 to 8, and the sub-tank of described fermentation is parallel-connected to by pipeline and sends out on yeast tank.
3.
Fermentation linkage system according to claim 2 is characterized in that: the volume of the sub-tank of described fermentation is 0.25L to 5L, and the volume of described yeast tank is 50L to 500L.
4.
Fermentation linkage system according to claim 3 is characterized in that: the cubic capacity of described yeast tank is 2.5 to 50 times of cubic capacity of the sub-tank of fermentation.
5.
Fermentation linkage system according to claim 2 is characterized in that: the volume of the sub-tank of described fermentation is 5L to 50L, and the capacity of described yeast tank is 500L to 120000L.
6.
Fermentation linkage system according to claim 5 is characterized in that: the cubic capacity of described yeast tank is 2.5 to 480 times of cubic capacity of the sub-tank of fermentation.
7.
Fermentation linkage system according to claim 2 is characterized in that: geometrical shape, the volume of the sub-tank of described each fermentation are identical with relevant accessory.
8.
Fermentation linkage system according to claim 2, it is characterized in that: each sub-tank of fermentation and a yeast tank all are furnished with motor, agitator, sensing unit, mounting bracket, process pipe system and electrical control cabinet, and described electrical control cabinet is controlled the sub-tank of described fermentation and a yeast tank by the computer chip in it and electric components.
9.
Fermentation linkage system according to claim 8 is characterized in that: described sensing unit comprises temperature sensor, pH sensor, dissolved oxygen sensor, full tank weighing sensor, exhaust analyzer, tachogenerator, pressure transmitter, froth breaking sensor and feed supplement LOAD CELLS.
10.
Fermentation linkage system claimed in claim 9 is characterized in that: described sensing unit also comprises one or more in the micro-online visualizer of cell, viable bacteria quantity sensor, redox potential sensor, the dense sensor of bacterium and air flow sensor.
11.
The described fermentation linkage system of any one according to claim 1 to 10, it is characterized in that: described supervisory system is the three-level computer Controlling System, and wherein first step computer control system is carried out Detection ﹠ Controling to the loop of each parameter of described yeast tank and the sub-tank formation of fermentation; Second stage computer control system is carried out data gathering, set(ting)value control and control loop to the parameter of the single tank body in described yeast tank and the sub-tank of fermentation and is adjusted; Third stage computer control system is carried out the parametric synthesis analysis and outputs to terminal the parameter of front two-stage system.
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN114561281A (en) * | 2022-02-21 | 2022-05-31 | 广州市博之越精细化工有限公司 | Synthesis process and synthesis device of micromolecular ellagic acid |
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| CN114561281A (en) * | 2022-02-21 | 2022-05-31 | 广州市博之越精细化工有限公司 | Synthesis process and synthesis device of micromolecular ellagic acid |
| CN114561281B (en) * | 2022-02-21 | 2022-10-25 | 广州市博之越精细化工有限公司 | Synthesis process and synthesis device of micromolecular ellagic acid |
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