CN101955881A - Airlift bioreactor - Google Patents
Airlift bioreactor Download PDFInfo
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- CN101955881A CN101955881A CN2009101579256A CN200910157925A CN101955881A CN 101955881 A CN101955881 A CN 101955881A CN 2009101579256 A CN2009101579256 A CN 2009101579256A CN 200910157925 A CN200910157925 A CN 200910157925A CN 101955881 A CN101955881 A CN 101955881A
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- C—CHEMISTRY; METALLURGY
- C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
- C12M—APPARATUS FOR ENZYMOLOGY OR MICROBIOLOGY; APPARATUS FOR CULTURING MICROORGANISMS FOR PRODUCING BIOMASS, FOR GROWING CELLS OR FOR OBTAINING FERMENTATION OR METABOLIC PRODUCTS, i.e. BIOREACTORS OR FERMENTERS
- C12M23/00—Constructional details, e.g. recesses, hinges
- C12M23/38—Caps; Covers; Plugs; Pouring means
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- C—CHEMISTRY; METALLURGY
- C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
- C12M—APPARATUS FOR ENZYMOLOGY OR MICROBIOLOGY; APPARATUS FOR CULTURING MICROORGANISMS FOR PRODUCING BIOMASS, FOR GROWING CELLS OR FOR OBTAINING FERMENTATION OR METABOLIC PRODUCTS, i.e. BIOREACTORS OR FERMENTERS
- C12M29/00—Means for introduction, extraction or recirculation of materials, e.g. pumps
- C12M29/06—Nozzles; Sprayers; Spargers; Diffusers
- C12M29/08—Air lift
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- C—CHEMISTRY; METALLURGY
- C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
- C12M—APPARATUS FOR ENZYMOLOGY OR MICROBIOLOGY; APPARATUS FOR CULTURING MICROORGANISMS FOR PRODUCING BIOMASS, FOR GROWING CELLS OR FOR OBTAINING FERMENTATION OR METABOLIC PRODUCTS, i.e. BIOREACTORS OR FERMENTERS
- C12M41/00—Means for regulation, monitoring, measurement or control, e.g. flow regulation
- C12M41/12—Means for regulation, monitoring, measurement or control, e.g. flow regulation of temperature
- C12M41/18—Heat exchange systems, e.g. heat jackets or outer envelopes
- C12M41/22—Heat exchange systems, e.g. heat jackets or outer envelopes in contact with the bioreactor walls
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Abstract
The invention discloses an airlift bioreactor which comprises a tank cover (5), a jacket (6), a tank body (7), a discharging pipe (8) and an air distributing pipe (9), wherein the jacket (6) is arranged outside the tank body (7). The lower part of the tank body (7) is provided with a tower flow-guiding ring (12), the flow-guiding ring (12) comprises an upper flow-guiding ring (1), a middle flow-guiding ring (2) and a lower flow-guiding ring (3), which respectively have the diameters of D1, D2 and D3 and the heights of h1, h2 and h3; the discharging pipe (8) is arranged below the side wall of the tank body (7), the bottom of the tank body (7) is provided with the air distributing pipe (9), a feeding connecting port (10) and a constant pressure connecting port (11) are arranged above the tank body (7); and a multi-layer ring spacing member (4) with a tapering top-down structure is arranged in the tank body (7). The airlift bioreactor is beneficial to the growth of a cell hypha flocculant and is suitable for the liquid culture of various mushroom myceliums.
Description
Technical field
Technical solutions according to the invention belong to the microbiology field, concretely, are to belong to microbiology device field, according to International Patent Classification, belong to C12M3/00 culture plant cell device.
Background technology
Bio-reactor for bacterium, fungi, vegetable cell and zooblast etc. provide aseptic, temperature suitable, mn, oxygen supply fully, the device of growing environment.Existing antibiotic production is to use mechanical stir-reactor, or air lift type, self-priming, jet-type, bubbling style bio-reactor.But these mechanically stirred reactors, energy consumption is big, complex structure.And the mixed performance of airlift reactor, bubbling style reactor and heat transfer property are better, gas-liquid mass transfer excellent property when vapour-liquid ratio is big, movement-less part, it is more convenient to make maintenance, be amplified to thousands of even tens thousand of cubic meters easily, this is that stirring reactor is beyond one's reach.But also there is deficiency in they for the mycelial cultivation of gill fungus bacterium, can not satisfy gill fungus mycetocyte liquid culture needs well, and the present invention makes adequate solution to this.
The gill fungus bacterium is the large-scale filamentous fungus microorganism of a class, and its sporophore is commonly referred to mushroom, comprises edible mushroom, medical mushroom, malicious mushroom.The production of gill fungus mycetocyte and meta-bolites thereof has obvious social and considerable economic.Pharmacology of both at home and abroad medicinal large-scale filamentous fungal cells and product thereof being carried out and clinical study result have shown that technical scale develops the necessity of the medicinal gill fungus bacterium of this class in recent years.As Cordyceps sinensis, the artificial culture sporophore does not reach a standard, and must adopt the mushroom liquid deep layer culture process, and a large amount of mycelium products that just can obtain having practical value lack the predicament of resource with solution, allow the mankind that valuable medicine therapy is arranged, and keep fit.The present invention is exactly the bio-reactor in the gill fungus mycetocyte liquid culture technology, comprises kind of a liquid cultivation reactor and a liquid fermenting reactor.Concerning the gill fungus bacterium, its many cells mycelia is more fine long than other microorganism mycelia.Mechanical stirring can produce physical abuse to the long mycelia of fibre, makes the mycelia fracture dead, influences the formation speed of secondary metabolite; Mechanical stirring also produces fluid whirl air pocket, high speed bubble and equally also can make the damaged death of very thin mycelia and the influence growth simultaneously.These results of study show that the present invention can perform well in gill fungus mycetocyte liquid culture.
Existing technology, as China's patent No. be: 99121894.9, in please day be: on October 22nd, 1999, denomination of invention is: " a kind of new bio-reactor that is used for the microbial liquid cultivation ", it is for solving filamentous fungus mycelia cracky during liquid culture in traditional mechanically stirred reactor, the difficult problem that cenobium knot wall and being unfavorable for is grown, growth characteristic at filamentous fungus has designed different with existing gas lift reactor, the gas lift reactor that has low recirculating zone and relate to other special parameters such as lifting recycle ratio comprises kind of liquid mycelium culture reactor and liquid fermenting reactor.Its weak point: because fermenting process can not add materials, therefore, fermentation unit can not artificially be controlled.
Summary of the invention
The objective of the invention is to propose a kind ofly have multilayer turriform guide ring and detachable pressure-balance type stream adds device, be fit to the airlift bioreactor of gill fungus mycetocyte liquid culture.
The object of the present invention is achieved like this: a kind of airlift bioreactor comprises: cover, chuck, tank body, discharge nozzle and air distribution pipe.Chuck is equipped with in the outside of tank body, the turriform guide ring is equipped with in the bottom of tank body, guide ring is made up of last guide ring, middle guide ring and three rings of following guide ring, its diameter is respectively D1, D2, D3, the sidewall below of tank body is provided with discharge nozzle, the bottom is provided with the air distribution pipe, and reinforced Link Port and weighing apparatus press Link Port to be contained in the top of tank body.Be provided with up-thin-low-thick multilayer interannular spacing body in the tank body, its interfloor height is k, and its diameter ratio is D1: D2: D3=0.85: 0.90: 1.00; From top to bottom the height of three guide rings is respectively h1, h2, h3, and the ratio of its height is h1: h2: h3=1: 2: 3; The ratio of upper strata guide ring diameter D1 and reactor tank body diameter D is D1: D=0.65: 1.00; The ratio h1 of the height of interlayer: h2: h3: k=1: 2: 3: 0.1.Be connected to stream on reinforced Link Port and the weighing apparatus pressure Link Port and add device, stream adds device and is made up of cylindrical shell, glass visor, balance tube, filling tube and cylindrical shell end socket, the glass visor is housed on the cylindrical shell, balance tube is equipped with on its top, filling tube is equipped with in the bottom, top is the cylindrical shell end socket, and it is made up of turning gland, cylindrical shell top cover ring flange, closure stud button, top cover trip shaft and top cover plug.When using stream to add device, it is placed on the top of bio-reactor, balance tube is linked the weighing apparatus of bio-reactor and pressed Link Port, again filling tube is connected with the reinforced Link Port of bio-reactor.
This bio-reactor has following characteristics:
1. according to the characteristics of gill fungus mycetocyte growth, 1～3 layer turriform guide ring is set in the reactor, applies soft drawing force to mycelium, and supply with competent oxygen; Help the growth of cell mycelia floc sedimentation;
2. the big gapping interval structure between the multilayer guide ring makes fermenting process can adopt the supplying technics of substratum and stirs;
3. stream removable jew, that weighing apparatus is pressed adds device, and it is unobstructed and aseptic to guarantee to flow the add operation process, can control fermenting process better;
4. at the different process requirement of kind of liquid and fermentation, design has the fermentation reactor of different structure, can make this airlift bioreactor be applicable to that multiple gill fungus bacterium mycelium liquid is cultivated or the different process process of liquid fermenting.
Description of drawings
Fig. 1 airlift bioreactor structural representation.
Fig. 2 removable jew weighing apparatus baric flow adds the device structural representation.
Component part numbers: go up guide ring 1 diameter D1 height h1, middle guide ring 2 diameter D2 height h2, following guide ring 3 diameter D3 height h3, interannular spacing body 4 height k, cover 5, chuck 6, tank body 7 diameter D, height H v, discharge nozzle 8, air distribution pipe 9, reinforced Link Port 10, weighing apparatus press Link Port 11, guide ring 12 height H t, cylindrical shell 13, glass visor 14, turning gland 15, cylindrical shell top cover ring flange 16, closure stud button 17, top cover trip shaft 18, balance tube 19, filling tube 20, top cover plug 21, stream to add device 22, cylindrical shell end socket 23.
Embodiment
Below in conjunction with drawings and Examples the present invention is further described.
Fig. 1 is the airlift bioreactor structural representation.As can be seen from Figure 1: this bio-reactor is by cover 5, chuck 6, tank body 7, discharge nozzle 8, air distribution pipe 9, reinforced Link Port 10, weighing apparatus is pressed compositions such as Link Port 11 and guide ring 12, chuck 6 is enclosed within the outside of tank body 7, guide ring 12 is in the bottom of tank body 7, it is by last guide ring 1,3 three rings of middle guide ring 2 and following guide ring are formed, its diameter is respectively D1, D2, D3, highly be respectively h1, h2, h3, cover 5 is the end socket of tank body 7, be contained in the top of tank body 7, the sidewall below of tank body 7 is provided with discharge nozzle 8, the bottom is provided with air distribution pipe 9, reinforced Link Port 10 and weighing apparatus press Link Port 11 to be contained in the top of tank body 7, and reinforced Link Port 10 and weighing apparatus press Link Port 11 to add the Link Port of device 22 for stream.Be provided with up-thin-low-thick multilayer interannular spacing body 4 in the tank body 7, its interlayer has big space, highly (void size) is k, guide ring 12 structures of this turriform, can guarantee that culture system has uniform flow stream velocity from top to bottom in guide ring 12, and form tangible several integral body and partial big or small circulation, thereby promote the formation and the growth of thread fungus wadding by the big space of guide ring 12 interlayers.Large-scale filamentous fungus growth morphology result of study shows that thread fungus wadding form is the mushroom performance of cell in the liquid culture system.The interior guide ring of this bio-reactor from top to bottom can be formed by 1～3 layer, and from top to bottom the internal diameter of 3 guide rings is ascending, is followed successively by D1: D2: D3=0.85: 0.90: 1.00; From top to bottom height h1, h2, the h3 of 3 guide rings are ascending simultaneously, and its structure proportion is followed successively by h1: h2: h3=1: 2: 3.The ratio of upper strata guide ring diameter D1 and reactor tank body 7 diameter D is D1: D=0.65: 1.00; The interfloor height of interannular spacing body 4 is k, its texture ratio h3: h2: h1: k=3: 2: 1: 0.1.
The guide ring 12 of this bio-reactor can be designed to 1 layer according to the above ratio, it is single independently guide ring 12, or 2 layers, such structure can reduce amount and the formation speed that culturing process bacterium wadding forms, correspondingly can increase amount and formation speed that the bacterium ball forms, both of these case can be selected to different Objects of Development and meta-bolites.
The guide ring 12 of this bio-reactor has the structure in the big space of multilayer, and it has provides the possibility of implementing supplying technics.With regard to microorganism culturing and zymotechnique control thereof, thereby improve cell and meta-bolites concentration thereof for fear of substratum substrate retarding effect, usually adopt the supplying technics of fermenting process, to change from small to big be the feature of supplying technics to volume of culture in the feed supplement process.Common gas lift type common loop reactor can not be implemented supplying technics.Among the present invention, guide ring 12 is divided into 1,2,3 layer, and interlayer has enough big space can both produce space circulation at nutrient solution original volume and feed supplement initial stage, guarantees the mixing of feed liquid and the growth of bacterium wadding.
Fig. 2 adds the device synoptic diagram for self-mountable ﹠ dismountuble weighing apparatus baric flow.It is the auxiliary facility of bio-reactor, can load onto during use, not the time spent detachable down, its effect is to be used for replenishing material or bacterial classification to operating bio-reactor, to guarantee equipressure, aseptic.Stream adds device 22 and is made up of cylindrical shell 13, glass visor 14, balance tube 19, filling tube 20 and cylindrical shell end socket 23 etc., glass visor 14 is housed on the cylindrical shell 13, balance tube 19 is equipped with on its top, filling tube 20 is equipped with in the bottom, its top is cylindrical shell end socket 23, and cylindrical shell end socket 23 is made up of turning gland 15, cylindrical shell top cover ring flange 16, closure stud button 17, top cover trip shaft 18 and top cover plug 21.When using stream to add device 22, it is placed on the top of bio-reactor, the weighing apparatus that balance tube 19 is connected to bio-reactor is pressed Link Port 11, and it is identical to make bio-reactor and stream add the cylinder pressure of device 22.Then filling tube 20 is connected with the reinforced Link Port 10 of bio-reactor, at this moment stream adds in the device 22 and keeps weighing apparatus to press in the bio-reactor, open the clip that stream adds device bottom feed pipe 20, alkali lye or foam killer or kind liquid just can flow under action of gravity in the tank body 7 reposefully, are convenient to dominant discharge like this and can keep sterile state again.Can carry out feed supplement or inject bacterial classification bio-reactor.
That this bio-reactor also can be designed to is mutually different ' plant liquid and cultivate reactor ' and ' liquid fermenting reactor '.Its difference is: ' plant liquid and cultivate reactor ' interior guide ring 12 is divided into three layers (comprising the space), and it highly is Ht; Tank body 7, promptly the reactor volume virtual height is Hv, its ratio is Ht: Hv=0.45: 1.00, and the ratio of ' liquid fermenting reactor ' is Ht: Hv=0.65: 1.00.Reason is in large-scale filamentous fungus kind liquid is cultivated, and the criterion of acceptability of planting liquid is that cell is in the growth animated period, and this just requires to contain in kind of the liquid thread fungus wadding or the bacterium floc sedimentation rather than the mycelium pellet of more amount.Experimental result shows that lower inner draft tube height can further promote the formation of thread fungus wadding.
Embodiment 1:
The guide ring 12 of this bio-reactor has only one deck, and the ratio of its height H t and tank body height H v is Ht: Hv=0.65: 1.Present embodiment is used for the liquid fermenting process and do not add control processs such as nutrient solution, and this moment, designs simplification but can satisfy service requirements fully.
Embodiment 2:
The guide ring 12 of this bio-reactor has two layers, be upper strata and middle level, its height overall Ht and tank body height H v ratio are Ht: Hv=0.65: 1, the ratio of upper strata diameter D1, middle level diameter D2 and jar diameter D is D1: D2: D=0.60: 0.65: 1, the ratio of two lamellar spacing k and floor height h1, h2 was h1: h2: k=1: 2: 0.1.Present embodiment can fluid infusion once surpass the nutrient solution height overall and get final product above the guide ring of middle level in culturing process.
The guide ring 12 of this bio-reactor has three layers, be the upper, middle and lower, the ratio of its height overall Ht and tank body height H v is Ht: Hv=0.65: 1, the ratio of upper strata diameter D1, middle level diameter D2, the diameter D3 of lower floor and jar diameter D is D1: D2: D3D=0.55: 0.60: 0.65: 1, the ratio of three lamellar spacing k and last floor height h1, middle floor height h2, following floor height h3 was h1: h2: h3: k=1: 2: 3: 0.1.But present embodiment is the fluid infusion secondary in culturing process, and the nutrient solution total amount there was not the middle level guide shell for the first time, and the nutrient solution total amount there was not the upper strata guide shell to get final product for the second time.
Embodiment 4:
Present embodiment is the spawn culture reactor, and its guide ring 12 is three layers, and the ratio of its height overall Ht and tank body 7 height H v is Ht: Hv=0.45: 1.00.But feed supplement is 2 times in the culturing process.
Embodiment 5:
Present embodiment is the spawn culture reactor, and its guide ring 12 is two layers, and the ratio of its height overall Ht and tank body 7 height H v is Ht: Hv=0.45: 1.00.But feed supplement once in the culturing process.
Embodiment 6:
Present embodiment is the spawn culture reactor, and its guide ring 12 has only one deck, and the ratio of its height H t and tank body 7 height H v is Ht: Hv=0.45: 1.00.Can not feed supplement in the culturing process.
Claims (8)
1. airlift bioreactor, comprise: cover (5), chuck (6), tank body (7), discharge nozzle (8) and air distribution pipe (9), chuck (6) is equipped with in the outside of tank body (7), it is characterized in that: turriform guide ring (12) is equipped with in the bottom of tank body (7), guide ring (12) is by last guide ring (1), middle guide ring (2) and following guide ring (3) are formed, its diameter is respectively D1, D2, D3, highly be respectively h1, h2, h3, the sidewall below of tank body (7) is provided with discharge nozzle (8), the bottom is provided with air distribution pipe (9), and reinforced Link Port (10) and weighing apparatus press Link Port (11) to be contained in the top of tank body (7); Be provided with up-thin-low-thick multilayer interannular spacing body (4) in the tank body (7), its interfloor height is k, and its diameter ratio is D1: D2: D3=0.85: 0.90: 1.00; From top to bottom the height of three guide rings (12) is respectively h1, h2, h3, and the ratio of its height is h1: h2: h3=1: 2: 3; Guide ring diameter D1 of lower floor and reactor tank body (7) diameter D ratio be D1: D=0.65: 1.00; The ratio h1 of the height of interlayer: h2: h3: k=1: 2: 3: 0.1.
2. according to the described airlift bioreactor of claim 1, it is characterized in that: be connected to stream on described reinforced Link Port (10) and the weighing apparatus pressure Link Port (11) and add device (22), stream adds device (22) by cylindrical shell (13), glass visor (14), balance tube (19), filling tube (20) and cylindrical shell end socket (23) are formed, glass visor (14) is housed on the cylindrical shell (13), balance tube (19) is equipped with on its top, filling tube (20) is equipped with in the bottom, top is cylindrical shell end socket (23), and it is by turning gland (15), cylindrical shell top cover ring flange (16), closure stud button (17), top cover trip shaft (18) and top cover plug (21) are formed; When using stream to add device (22), it is placed on the top of bio-reactor, balance tube (19) is linked the weighing apparatus of bio-reactor and pressed Link Port (11), again filling tube (20) is connected with the reinforced Link Port (10) of bio-reactor.
3. according to the described airlift bioreactor of claim 1, it is characterized in that: described guide ring (12) is one deck, and the ratio of its height H t and tank body height H v is Ht: Hv=0.65: 1.
4. according to the described airlift bioreactor of claim 1, it is characterized in that: described guide ring (12) is for two-layer, promptly go up guide ring (1) and middle guide ring (2), the ratio of its height overall Ht and tank body height H v is Ht: Hv=0.65: 1, its diameter D1, D2 are D1: D2: D=0.60 with the ratio of jar diameter D: 0.65: 1, two lamellar spacing k were h1: h2: k=1 with the ratio of floor height h1, h2: 2: 0.1.
5. according to the described airlift bioreactor of claim 1, it is characterized in that: described guide ring (12) is three layers, promptly go up guide ring (1), middle guide ring (2) and following guide ring (3), the ratio of its height overall Ht and tank body height H v is Ht: Hv=0.65: 1, the ratio of its diameter D1, D2, D3 and jar diameter D is D1: D2: D3: D=0.55: 0.60: 0.65: 1, and three lamellar spacing k and h
1, h
2, h
3Example be h
1: h
2: h
3: k=1: 2: 3: 0.1.
6. according to the described airlift bioreactor of claim 1, it is characterized in that: described guide ring (12) is three layers, and the ratio of its height overall Ht and tank body height H v is Ht: Hv=0.45: 1.00.
7. according to the described airlift bioreactor of claim 1, it is characterized in that: described guide ring (12) is for two-layer, and the ratio of its height overall Ht and tank body height H v is Ht: Hv=0.45: 1.00.
8. according to the described airlift bioreactor of claim 1, it is characterized in that: described guide ring (12) is one deck, and the ratio of its height H t and tank body height H v is Ht: Hv=0.45: 1.00.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2009101579256A CN101955881A (en) | 2009-07-17 | 2009-07-17 | Airlift bioreactor |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2009101579256A CN101955881A (en) | 2009-07-17 | 2009-07-17 | Airlift bioreactor |
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| Publication Number | Publication Date |
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| CN101955881A true CN101955881A (en) | 2011-01-26 |
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| CN2009101579256A Pending CN101955881A (en) | 2009-07-17 | 2009-07-17 | Airlift bioreactor |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| ITUB20153722A1 (en) * | 2015-09-18 | 2017-03-18 | Eni Spa | Reaction device with internal Air-Lift type circulation and fermentation process using said device |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1071455A (en) * | 1991-10-12 | 1993-04-28 | 中国科学院化工冶金研究所 | A kind of gas-lift fermentation reactor |
| CN1302862A (en) * | 1999-10-22 | 2001-07-11 | 中国科学院微生物研究所 | Bioreactor for liquid culture of microbes |
| CN201250224Y (en) * | 2008-09-02 | 2009-06-03 | 天津大学 | Air-lift reactor for cultivating aerobic microbe inocula |
-
2009
- 2009-07-17 CN CN2009101579256A patent/CN101955881A/en active Pending
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1071455A (en) * | 1991-10-12 | 1993-04-28 | 中国科学院化工冶金研究所 | A kind of gas-lift fermentation reactor |
| CN1302862A (en) * | 1999-10-22 | 2001-07-11 | 中国科学院微生物研究所 | Bioreactor for liquid culture of microbes |
| CN201250224Y (en) * | 2008-09-02 | 2009-06-03 | 天津大学 | Air-lift reactor for cultivating aerobic microbe inocula |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| ITUB20153722A1 (en) * | 2015-09-18 | 2017-03-18 | Eni Spa | Reaction device with internal Air-Lift type circulation and fermentation process using said device |
| WO2017046720A1 (en) * | 2015-09-18 | 2017-03-23 | Eni S.P.A. | Reaction device with air-lift type internal circulation and fermentation process using said device |
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Application publication date: 20110126 |