CN2078322U - Air-lift biological reactor for high-visco sity fermentation - Google Patents
Air-lift biological reactor for high-visco sity fermentation Download PDFInfo
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- CN2078322U CN2078322U CN 90225805 CN90225805U CN2078322U CN 2078322 U CN2078322 U CN 2078322U CN 90225805 CN90225805 CN 90225805 CN 90225805 U CN90225805 U CN 90225805U CN 2078322 U CN2078322 U CN 2078322U
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Abstract
The utility model relates to an inner circular flowing type air-lift biological reactor for high viscosity fermentation, which is mainly characterized in that segments of hoisting pipes are arranged in a tank of a reactor. Compared with a stirring fermentation tank of a traditional mechanism, the reactor has the advantages of low investment, easy manufacture, energy consumption saving (saving 30%), convenient maintenance, stable operation, difficult bacterium infection, favorable liquid mixing, high intensity of the transfer of gas-liquid mass, low shearing force and wide application range. The suitable condition for the mycelial growth is provided. The utility model is suitable for the high viscosity microbial polysaccharide fermentation, the fermentation of other microorganisms, and the cultivation of the cells of the animals and plants, etc.
Description
The present invention relates to a kind of microorganism fermentation reactor, circulation type bio-reactor in particularly a kind of high viscosity fermentation air lift type.
Existing microbial fermentation mostly is mechanical agitation type with bio-reactor, is commonly referred to as the standard fermentor tank, in adorn the horizontal garden of six leaves disc type turbine oar, tank skin is installed 4 vertical baffles, the stdn of the size of tank body and stirring blade.Though at present multiple improved pattern is arranged, its basic structure is still constant, its principal feature is the mechanical agitation type ventilation fermentation tank.Though the existing machinery stirred-tank fermenter has secular use experience and reliable and stable, advantages such as adaptability is big, but its outstanding shortcoming is the energy consumption height, and because the effect of the high shear force of impeller easily damages (M.B.Moo-Young to mycelium, Comprehensive Biotechnology.Vo1.2, Pergamon Press, N.Y., 1985).Particularly under the situation of high viscosity fermentation, the performance of mechanical agitator tank significantly descends, and energy consumption increases, and fluid mixes deterioration, and mass-transfer efficiency reduces, can not normal growth to cause certain micro-organisms.In addition, mechanical agitating fermentation tank also has investment big, processed complex, and shortcomings such as maintenance difficult, and owing to stir shaft sealing place is easily leaked gas, so easy microbiological contamination.
Also has a kind of airlift bioreactor (being also referred to as gas lift formula fermentor tank) that is applicable to the low viscosity fermentation at present.Its principal feature is that external loop type reaches two kinds of interior circulation types (Rehm, H.J.and G.Reed, Biotechnology, Vo1.2, VCH, 1985), and the structure of external loop type mainly is made up of vertical type gas-lift tube and downtake.Top, the end of two pipes, connect with adapting pipe, after gas feeds from gas-lift tube, entrained liquids rises, enter expanding reach to the top, overflowed by the top of expanding reach after most of gas delivery, small part enters downtake with liquid through pipe connecting and descends, enter the bottom of gas-lift tube again through the bottom adapting pipe to the bottom, form that liquid is well-regulated to circulate, carry out that fluidic mixes and gas-liquid between the transmission of oxygen, to guarantee the needs of fermentation.The structure of interior circulation type mainly is made of vertical cylindrical shell and concentric garden inner core.Inner core is a gas-lift tube, and the annular space of inner core and urceolus is as downtake, and its fluidic characteristics of motion is identical with external loop type, and function is also substantially the same.
Existing gas lift formula fermentor tank is when being used for high viscosity fermentation, because fermentation media viscosity up to hundreds of extremely centipoises up to ten thousand, still have the oxygen supply deficiency and mix bad shortcoming, thereby efficient is not high.
In order to overcome the above-mentioned shortcoming that mechanical agitating fermentation tank and existing gas lift formula fermentor tank exist, the spy has invented a kind of vertical type high viscosity fermentation airlift bioreactor.
The present invention's " high viscosity fermentation airlift bioreactor " (high viscosity gas lift formula fermentor tank), mainly comprise fermentation tank body, riser tube, expanding reach, air chamber, reinforced inoculation mouth, discharge gate etc., it is characterized in that fermenting the interior pipe of 3～10 sections concentric garden tubulars is housed in the tank body, interior pipe can be as riser tube, and the interannular of interior pipe and tank body is as downtake.Also can use conversely, promptly in pipe and the interannular of tank body as riser tube, and interior pipe as downtake.The bottom of riser tube is provided with gas distributor, and sparger can be single or multiple gas jets, or endless tube shape, grizzly bar shape gas distributor, is connected by union lever between interior each section of pipe, and is fixed on tank base by fulcrum.
High viscosity fermentation airlift bioreactor of the present invention also is interior circulation type.When the interior pipe of reactor during as riser tube, the riser tube top can be provided with the retaining cap, when the interannular of interior pipe and tank body during as riser tube, can be provided with ring baffle in the riser tube top expanded section.Can prevent splash like this, reduce the deflated entrainment, make operation more stable, and form the foam layer of certain altitude, can increase gas-liquid mass transfer.The riser tube bottom is provided with single or multiple gas jets, or annular, grizzly bar shape gas distributor, makes gas distribution even, forms big lift simultaneously, liquid is formed circulate, and can make gas dispersion become small bubbles, increase gas-to-liquid contact area.Riser tube is divided into multistage, can guarantee part and overall circulation and better mixing and oxygen supply condition that liquid is good, makes oxygen supply condition up and down more even, and particularly the supply of oxygen is also relatively more abundant in downtake.Because the sectional result, partial circulating district of inside and outside formation of each of riser tube section.Also form overall systemic circulation simultaneously.So can guarantee good mixing and oxygen supply condition.
The aspect ratio of the whole fermentation tank body of this reactor is 6～20, and tank body is 1.3～2 with the diameter of inner pipe ratio, jar height with every section in the aspect ratio of pipe be 3～10, interior pipeline section spacing is 1/10～1/100 of a tank body height.
The reactor of this invention is that to adopt gas be power, utilizes the gas expansion merit that energy is provided, and drives liquid and circulates, and even air is dispersed in carry out excellent contact in the liquid phase, to promote gas-liquid mass transfer.Owing to save mechanical stirring, so its total power consumption can save 20～30%.Simultaneously can obtain good mixing of materials, higher gas-liquid mass transfer intensity, low shearing speed and suitable microorganism growth condition can significantly improve the utilization of carbon source rate, shorten fermentation period, increase productive rate.Owing to there is not mechanical driving part, simple in structure, processing charges is low, and easy to operate, and maintenance easily realizes automatization easily.The fermentation reactor of invention, since its unique internal structure, wide accommodation, and the viscosity of fermentation media can be by the number centipoise to centipoises up to ten thousand.Be successfully used to high viscosity fermentation, as fermentation of microbial polysaccharide etc.To the fermentation of other types, also will be efficient, energy-conservation equipment as cell culture of animals.Reactor of the present invention also can be used for the fermentation of conventional viscosity, as the fermentation of bacterium, mould, budding fungus.
Below in conjunction with accompanying drawing, embodiment specifically describes the present invention.
Fig. 1 is the present invention's's a kind of " high viscosity fermentation airlift bioreactor " synoptic diagram.
Fig. 2 is an endless tube shape gas distributor synoptic diagram, and Fig. 3 is a grizzly bar shape gas distributor synoptic diagram.
This reactor is by tank body (1), interior pipe (2), union lever (3), heat exchange jacket (4), liquidometer (5), retaining cap (6), expanding reach (7), reinforced inoculation mouthful (8), venting port (9), tensimeter (10), stream adds a mouthful froth breaker mouth (11), hand (people) hole (12), probe hole, thief hole (13), water outlet (14), holder ear (15), flange (16), discharge gate (17), inlet mouth (18), air chamber (19), gas distributor (nozzle) (20), and water-in compositions such as (21).Weld with 3-4 root union lever (3) between the pipe (2) in two sections.In next root effective 3-4 ask ear (15) to be supported on tank base.
As shown in Figure 1, when interior pipe was done riser tube, pressurized air entered air chamber (19) by inlet mouth (18), entered fermentor tank by nozzle (gas distributor) (20), rise piecemeal by interior pipe (2) entrained liquids, to expanding reach (7) and liquid separation, discharge by venting port (9).Liquid is then descended by the outer interannular of interior pipe (2), and pipe constitutes circulation in being entered by the bottom again, is discharged by discharge gate (17) until the fermentation termination.Interior pipe (2) bottom as Fig. 1 is straight tubular, also can make toroidal, is beneficial to air-flow and concentrates on rising in the pipe.Gas distributor (20) also can be made the grizzly bar shape sparger as the endless tube shape of Fig. 2 or Fig. 3, has aperture up on the pipe, and when interior pipe was riser tube, the diameter of endless tube should be slightly less than diameter of inner pipe.Reactor of the present invention can be used for intermittently batch job, also can be used for continuous or semicontinuous (stream adds) operation.
Embodiment:
1. high viscosity fermentation airlift bioreactor as shown in Figure 1,200 liters of volumes, the high 5010mm of tank body, tank diameter 250mm, riser diameter 160mm, riser tube divide three sections, every section 1300mm, every intersegmental distance is 100mm, 180 liters of reactor useful volumes.The gas distributor single-nozzle.Each parts is all made with stainless steel.
Adopting 5% sucrose solution is substratum, with addition of following nutrition (%): KH
2PO
40.2 NaCl 0.1, MgSO
47H
2O 0.2, urea 0.02, yeast extract paste 0.2.Use Aureobasidium pullulans (Aureobasidium Pullulans) to be bacterial classification, after cultivating in 24 hours, inoculum size inoculation with 5%, fermentation condition is: 28 ± 2 ℃ of temperature, ventilation is 1vvm, the carbon source transformation efficiency of substratum can reach 50% after 96 hours, generates short stalk mould polysaccharide (Pullulan) fermentation broth viscosity near 1000 centipoises, and polysaccharide molecular weight can reach 4～5 * 10
4Stable operation, product performance are good.Compare with the traditional standard stirred pot, can save energy 30%, the carbon source transformation efficiency improves 5%, and fermentation period shortens 12 hours.
2. 3000 rising viscosity fermentations airlift bioreactor as shown in Figure 1, the high 10800mm of tank body, tank diameter 600mm, riser diameter is 400mm, and air-lift tube is 7 sections, and every section is 1000mm, spacing is 200mm, the reactor useful volume is 2500 liters, and gas distributor is 4 nozzles or adopts grizzly bar shape gas distributor as Fig. 3 that reactor is made by stainless material.
Adopt the fermenting process identical with embodiment 1, ventilation is 0.75vvm, other conditions are identical, obtain with embodiment 1 in identical carbon source transformation efficiency and identical quality product, compare with traditional standard stirred pot, can save energy 30%, the carbon source transformation efficiency can improve 5%, and fermentation period shortens more than 12 hours.
3. rising viscosity fermentation airlift bioreactor, adopt endless tube shape gas distributor as Fig. 2, make gas be evenly distributed on the interannular of managing in the tubular of garden with reacting tank body, (this moment, interannular became riser tube) makes gas drive liquid and rises at interannular, and liquid descends from interior pipe then, at this moment, interior pipe becomes downtake to be used, and gas is overflowed (the former retaining cap cancellation that is positioned at above the pipe) from the top through annular plate washer, and other structures are same as shown in Figure 1.The high 5010mm of the tank body of reactor, diameter are 250mm, and inner tube diameter 150mm is divided into three sections, every section 1000mm, and spacing is 100mm.
In above-mentioned reactor, adopt the identical technological condition for fermentation of embodiment 1, also obtain identical experimental result with embodiment 1.
Claims (4)
1, a kind of fermentation airlift bioreactor, mainly comprise fermentation tank body, riser tube, expanding reach, air chamber, reinforced inoculation mouth, discharge gate etc., it is characterized in that fermenting the interior pipe of 3～10 sections concentric garden tubulars is housed in the tank body, interior pipe can be as riser tube as the interannular of riser tube or interior pipe and tank body, the bottom of riser tube is provided with gas distributor, sparger can be single or multiple gas jets, or endless tube shape, grizzly bar shape gas distributor, connect by union lever between interior each section of pipe, and be fixed on tank base by fulcrum.
2, bio-reactor according to claim 1, the interior pipe that it is characterized in that reactor is during as riser tube, can be provided with the retaining cap at the top of riser tube,, can establish ring baffle at the interannular outside the interior pipe of expanding reach part when the interannular of interior pipe and tank body during as riser tube.
3, bio-reactor according to claim 1 and 2, the tank body aspect ratio that it is characterized in that reactor is 6～20, tank body is 1.3～2 with the diameter ratio of interior pipe, and the aspect ratio of pipe is 3～10 in tank body height and every section, and distance is 1/10～1/100 of a tank body height between interior pipeline section.
4, bio-reactor according to claim 1 and 2, the interior pipe that it is characterized in that reactor are during as riser tube, and interior pipe bottom can be straight tubular, also can be toroidal.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 90225805 CN2078322U (en) | 1990-12-13 | 1990-12-13 | Air-lift biological reactor for high-visco sity fermentation |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 90225805 CN2078322U (en) | 1990-12-13 | 1990-12-13 | Air-lift biological reactor for high-visco sity fermentation |
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| Publication Number | Publication Date |
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| CN2078322U true CN2078322U (en) | 1991-06-05 |
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| Application Number | Title | Priority Date | Filing Date |
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| CN 90225805 Withdrawn CN2078322U (en) | 1990-12-13 | 1990-12-13 | Air-lift biological reactor for high-visco sity fermentation |
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Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1049008C (en) * | 1996-08-29 | 2000-02-02 | 中国科学院化工冶金研究所 | Air lift internal cross-current type bio-reactor |
| CN1078247C (en) * | 1998-01-22 | 2002-01-23 | 中国科学院生态环境研究中心 | Bioreactor with baffling element |
| CN1329500C (en) * | 2005-10-21 | 2007-08-01 | 上海理工大学 | Multi-tubular airlift reactor and its inner eddy flow field organizing method |
| CN101671626B (en) * | 2009-08-18 | 2011-11-30 | 王相刚 | Method for fermenting fungi liquid and ferment tank |
| CN104130929A (en) * | 2013-05-02 | 2014-11-05 | 台美生物资源股份有限公司 | Multi-module circulating-type microalgae breeding system having energy-saving function |
| CN104774750A (en) * | 2015-04-24 | 2015-07-15 | 亿利资源集团有限公司 | Photoreactor for culturing microalgae |
| CN117187030A (en) * | 2023-11-06 | 2023-12-08 | 万华化学集团股份有限公司 | Fermentation reaction kettle, corresponding fermentation system and application thereof |
-
1990
- 1990-12-13 CN CN 90225805 patent/CN2078322U/en not_active Withdrawn
Cited By (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1049008C (en) * | 1996-08-29 | 2000-02-02 | 中国科学院化工冶金研究所 | Air lift internal cross-current type bio-reactor |
| CN1078247C (en) * | 1998-01-22 | 2002-01-23 | 中国科学院生态环境研究中心 | Bioreactor with baffling element |
| CN1329500C (en) * | 2005-10-21 | 2007-08-01 | 上海理工大学 | Multi-tubular airlift reactor and its inner eddy flow field organizing method |
| CN101671626B (en) * | 2009-08-18 | 2011-11-30 | 王相刚 | Method for fermenting fungi liquid and ferment tank |
| CN104130929A (en) * | 2013-05-02 | 2014-11-05 | 台美生物资源股份有限公司 | Multi-module circulating-type microalgae breeding system having energy-saving function |
| CN104130929B (en) * | 2013-05-02 | 2018-12-25 | 台建生技股份有限公司 | Has the circulating both culturing microalgae system of multimode group of energy-saving effect |
| CN104774750A (en) * | 2015-04-24 | 2015-07-15 | 亿利资源集团有限公司 | Photoreactor for culturing microalgae |
| CN117187030A (en) * | 2023-11-06 | 2023-12-08 | 万华化学集团股份有限公司 | Fermentation reaction kettle, corresponding fermentation system and application thereof |
| CN117187030B (en) * | 2023-11-06 | 2024-02-27 | 万华化学集团股份有限公司 | Fermentation reaction kettle, corresponding fermentation system and application thereof |
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| C06 | Publication | ||
| PB01 | Publication | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| C15 | Extension of patent right duration from 15 to 20 years for appl. with date before 31.12.1992 and still valid on 11.12.2001 (patent law change 1993) | ||
| RN01 | Renewal of patent term | ||
| C19 | Lapse of patent right due to non-payment of the annual fee | ||
| CF01 | Termination of patent right due to non-payment of annual fee |