CN1086542A - Suspension bed continuous ferment reactor with flocculated yeast - Google Patents
Suspension bed continuous ferment reactor with flocculated yeast Download PDFInfo
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- CN1086542A CN1086542A CN92112100A CN92112100A CN1086542A CN 1086542 A CN1086542 A CN 1086542A CN 92112100 A CN92112100 A CN 92112100A CN 92112100 A CN92112100 A CN 92112100A CN 1086542 A CN1086542 A CN 1086542A
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- 240000004808 Saccharomyces cerevisiae Species 0.000 title claims abstract description 42
- 239000000725 suspension Substances 0.000 title claims abstract description 7
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 claims abstract description 22
- 239000002245 particle Substances 0.000 claims abstract description 17
- 230000003311 flocculating effect Effects 0.000 claims abstract description 14
- 238000005189 flocculation Methods 0.000 claims abstract description 9
- 230000016615 flocculation Effects 0.000 claims abstract description 9
- 238000000034 method Methods 0.000 claims abstract description 8
- 238000004062 sedimentation Methods 0.000 claims abstract description 7
- 239000007788 liquid Substances 0.000 claims description 35
- 239000007789 gas Substances 0.000 claims description 15
- 230000000694 effects Effects 0.000 claims description 7
- 238000001816 cooling Methods 0.000 claims description 6
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 6
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 5
- 239000001301 oxygen Substances 0.000 claims description 5
- 229910052760 oxygen Inorganic materials 0.000 claims description 5
- 238000006243 chemical reaction Methods 0.000 claims description 3
- 238000001914 filtration Methods 0.000 claims description 2
- 230000005484 gravity Effects 0.000 claims description 2
- 230000001954 sterilising effect Effects 0.000 claims description 2
- 238000004659 sterilization and disinfection Methods 0.000 claims description 2
- 238000007599 discharging Methods 0.000 claims 1
- 239000006185 dispersion Substances 0.000 claims 1
- 239000000203 mixture Substances 0.000 claims 1
- 230000003068 static effect Effects 0.000 claims 1
- 238000003466 welding Methods 0.000 claims 1
- 238000000855 fermentation Methods 0.000 abstract description 17
- 230000004151 fermentation Effects 0.000 abstract description 17
- 230000012010 growth Effects 0.000 abstract description 3
- 230000007774 longterm Effects 0.000 abstract 1
- 235000014680 Saccharomyces cerevisiae Nutrition 0.000 description 34
- 238000004519 manufacturing process Methods 0.000 description 10
- WQZGKKKJIJFFOK-GASJEMHNSA-N Glucose Natural products OC[C@H]1OC(O)[C@H](O)[C@@H](O)[C@@H]1O WQZGKKKJIJFFOK-GASJEMHNSA-N 0.000 description 7
- 238000011160 research Methods 0.000 description 3
- 230000001580 bacterial effect Effects 0.000 description 2
- 238000009395 breeding Methods 0.000 description 2
- 230000001488 breeding effect Effects 0.000 description 2
- 210000004027 cell Anatomy 0.000 description 2
- 238000013461 design Methods 0.000 description 2
- 239000003814 drug Substances 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 239000008103 glucose Substances 0.000 description 2
- 230000008676 import Effects 0.000 description 2
- 238000009423 ventilation Methods 0.000 description 2
- OWEGMIWEEQEYGQ-UHFFFAOYSA-N 100676-05-9 Natural products OC1C(O)C(O)C(CO)OC1OCC1C(O)C(O)C(O)C(OC2C(OC(O)C(O)C2O)CO)O1 OWEGMIWEEQEYGQ-UHFFFAOYSA-N 0.000 description 1
- 239000004375 Dextrin Substances 0.000 description 1
- 229920001353 Dextrin Polymers 0.000 description 1
- 102000004190 Enzymes Human genes 0.000 description 1
- 108090000790 Enzymes Proteins 0.000 description 1
- GUBGYTABKSRVRQ-PICCSMPSSA-N Maltose Natural products O[C@@H]1[C@@H](O)[C@H](O)[C@@H](CO)O[C@@H]1O[C@@H]1[C@@H](CO)OC(O)[C@H](O)[C@H]1O GUBGYTABKSRVRQ-PICCSMPSSA-N 0.000 description 1
- 241000235347 Schizosaccharomyces pombe Species 0.000 description 1
- CZMRCDWAGMRECN-UGDNZRGBSA-N Sucrose Chemical compound O[C@H]1[C@H](O)[C@@H](CO)O[C@@]1(CO)O[C@@H]1[C@H](O)[C@@H](O)[C@H](O)[C@@H](CO)O1 CZMRCDWAGMRECN-UGDNZRGBSA-N 0.000 description 1
- 229930006000 Sucrose Natural products 0.000 description 1
- 238000010521 absorption reaction Methods 0.000 description 1
- 230000001476 alcoholic effect Effects 0.000 description 1
- WQZGKKKJIJFFOK-VFUOTHLCSA-N beta-D-glucose Chemical compound OC[C@H]1O[C@@H](O)[C@H](O)[C@@H](O)[C@@H]1O WQZGKKKJIJFFOK-VFUOTHLCSA-N 0.000 description 1
- GUBGYTABKSRVRQ-QUYVBRFLSA-N beta-maltose Chemical compound OC[C@H]1O[C@H](O[C@H]2[C@H](O)[C@@H](O)[C@H](O)O[C@@H]2CO)[C@H](O)[C@@H](O)[C@@H]1O GUBGYTABKSRVRQ-QUYVBRFLSA-N 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 238000007664 blowing Methods 0.000 description 1
- 230000005587 bubbling Effects 0.000 description 1
- 230000025938 carbohydrate utilization Effects 0.000 description 1
- 239000002826 coolant Substances 0.000 description 1
- 239000000498 cooling water Substances 0.000 description 1
- 235000019425 dextrin Nutrition 0.000 description 1
- 239000006260 foam Substances 0.000 description 1
- 235000013305 food Nutrition 0.000 description 1
- 230000001788 irregular Effects 0.000 description 1
- 238000012856 packing Methods 0.000 description 1
- 230000002093 peripheral effect Effects 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 238000010008 shearing Methods 0.000 description 1
- 239000002893 slag Substances 0.000 description 1
- 238000003756 stirring Methods 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 239000005720 sucrose Substances 0.000 description 1
- 238000003786 synthesis reaction Methods 0.000 description 1
- 230000009897 systematic effect Effects 0.000 description 1
- 238000012360 testing method Methods 0.000 description 1
- 230000003245 working effect Effects 0.000 description 1
- 210000005253 yeast cell Anatomy 0.000 description 1
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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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- 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
- C12M21/00—Bioreactors or fermenters specially adapted for specific uses
- C12M21/12—Bioreactors or fermenters specially adapted for specific uses for producing fuels or solvents
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- 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
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- 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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- 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
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- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
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Abstract
The present invention is according to the grain wine flocculating yeast of seed selection voluntarily, and utilizes biological natures such as its growth, flocculation, fermentation, designed and developed suspension bed continuous ferment reactor with flocculated yeast for realizing that alcohol continuously ferments.This reactor adopts the method that feeds little air to make the flocculating yeast particle keep the slowly suspended state of motion, has both kept its particle shape, makes yeast increase vigor again, has improved fermentation capacity.In this reactor, be provided with gas diverter, make the CO of generation
2Separate with air, can get pure CO
2Product; Owing to designed the sedimentation guide, yeast particles is trapped in the medium-term and long-term use of reactor, realized continuously fermenting.
Description
The invention belongs to the biological fermentation engineering alcohol device that continuously ferments.
Alcohol is used every profession and trades such as chemical industry, medicine, food widely, and some country carries out systematic research with alcohol as " green energy resource ", and Chinese in recent years alcohol product is also increasing substantially.But in the Alcohol Production process, be batch fermentation, fermentation concentration is low always, general 7%(V) about, for up to 65～75 hours, plant factor was low, consume a large amount of distiller's yeasts, and yeast cell can not reclaim, so cost is higher.For this reason, adopt fixed yeast to continuously ferment to alcohol both at home and abroad and carried out a large amount of research, existing a lot of lab scale research papers of immobilization technologies such as carrier embedding or absorption that adopt are delivered, for example M.J.
And J.M.Lema is at Enzyme Microb., Technol 1987.vol 9, published article " Cell jmmobilization:Application to alcohol Production " on the NO vem ber magazine, analysis-by-synthesis these achievements.But because of its extensive technical sophistication of making fixed yeast, work-ing life is short, and cost is very high, thereby does not slowly realize suitability for industrialized production.
The present invention has adopted and above-mentioned diverse yeast immobilization technology.In order to realize the alcoholic fermentation process serialization, proposed to utilize some zymic flocculation feature to realize the new ideas of continuously fermenting, selected grain brewer yeast bacterial strain, made it self to flocculate into the particle of 0.5～1.5mm, as the immobilization means with strong self flocculation ability.And the biological nature of this bacterial strain studied, grasped flocculating conditions and flocculation particulate fermentation character.
Grain brewer yeast (SPombe) is a kind of fission yeast, can utilize glucose, maltose, sucrose and dextrin etc. to ferment, and stronger zymamsis ability is arranged.At 25～35 ℃, sugared concentration 2～25% is under the conditions such as pH value 3～5 after taming for this yeast, can flocculate into the particle of 0.5～1.5mm, certain firmness is arranged, and no longer include yeast in the breeding afterwards and dissociate away, this just provides possibility for continuously fermenting.The flocculation particle shape is irregular, is subjected to the influence of the hydromeehanics condition of environment and ferment strength very big.If flow velocity is too slow, may make the particle packing contact and further cohesion formation blob of slag shape bulk; If stir strongly, shearing stress is big, and particle promptly is broken.Flocculate particle proportion greater than fermented liquid, the energy natural subsidence, its speed is 0.45～0.72cm/s.In order to keep the particulate size, need allow them be suspended in motion lenitively in the fermented liquid, keep and the fermented liquid excellent contact.
Another feature of grain brewer yeast is that a small amount of oxygen can improve the active of it and to the tolerance of alcohol.When yeast concn is very high, need replenish a certain amount of oxygen especially.Yet traditional batch fermentation is an anaerobic, so will break the tradition of anaerobically fermenting, feeds little air during the fermentation, both can be used as the motivating force that keeps suspended state, and limited oxygen is provided again.
The method that the new yeast immobilization of the present invention's exploitation is continuously fermented can overcome the shortcoming that batch fermentation exists, and has invented suspension bed continuous ferment reactor with flocculated yeast for this reason.This method is simple to operate, without any need for carrier and medicament, can obtain the cell concentration more much higher than other fixing means (40～60kg(dry weight)/m
3), thereby can reach higher device fabrication intensity (8～12kg alcohol/m
3H), lay a good foundation for the realization suitability for industrialized production.For growth, flocculation and the fermenting process of realizing this flocculating yeast, need a kind of suitable reactor, the present invention promptly for this reason and the design a kind of " suspension bed continuous ferment reactor with flocculated yeast ".Test in 500 liter volumes, the result is very good, and carries out 10m
3Reactor design, output reach the commercial production scale in 2000 tons of alcohol/years.
The shell of this reactor is by bottom conical head (2), lower shell (3), and top expanding reach (8) and top elipse head (7) four parts are formed.Internals are by air-distributor (10), air-lift tube (4), and gas diverter (5) and sedimentation guide (6) four parts are formed.In addition, following cylinder is provided with water cooling chuck (9) outward.Whole reactor is a cylindrical vessel, operate continuously in confined conditions.(seeing accompanying drawing)
Suspend in order to satisfy the flocculating yeast particulate, growth and breeding and the needs of invigorating are wanted bubbling air in the reactor.So air intlet pipe (1) has been installed, devices such as air-distributor and air-lift tube in reactor.When pressurized air enters the air intlet pipe through behind the filtration sterilization, be dispersed into small bubbles at air-distributor, upwards enter in the air-lift tube.Air intlet pipe and air-lift tube are installed in the center of reactor, and air intlet pipe and bottom conical head weldering knot are together.Air-lift tube is the pipe of a both ends open.After air bubble enters air-lift tube, produced density difference inside and outside the pipe, fermented liquid moves upward with bubble in the air-lift tube, managing outer liquid flows into from the air-lift tube bottom downwards, form internal recycle, this just makes the fermented liquid in the whole reactor move lentamente, keeps the particle yeast to be the suspended motion state.Its speed can be controlled by the blowing air amount, and general ventilating ratio is 0.001～0.1m
3(gas)/m
3(liquid) divides, and in air-lift tube, yeast contacts with air, obtains needed oxygen.
Air bubble is from the air-lift tube gas diverter that comes out promptly to enter.Gas diverter is installed in the center of top expanding reach, is a pipe, and upper end weldering knot is at the top end socket, and the lower end is unsettled, and end opening is suitable for reading over against air-lift tube.Because fermentation alcohol generates CO simultaneously
2, purity is very high, is a kind of product.But after air feeds, as not with CO
2With air separation, CO then
2Concentration will descend greatly, becomes exhaust gas evacuation.The effect of gas diverter is exactly with air and CO
2Separately.After air bubble enters gas diverter, discharge by elipse head center, top air vent pipe.And CO
2Then outside gas diverter, rise from top elipse head sidepiece CO
2Gas outlet pipe is discharged.So just obtained pure CO
2As product.
When fermented liquid flows out from the air-lift tube upper end, promptly enter the top expanding reach.Because top expanding reach diameter is bigger 1.5～3 times than lower shell, the fermented liquid flow velocity slows down, and proceeds fermentation reaction, generates alcohol and CO
2Because flow velocity is slow, the CO of generation
2The bubble effusion that is easy to move upward.Simultaneously, leave than large space at the top expanding reach, (the fermented liquid liquid level is determined by the discharge port position), the bubble foam that fermenting process is produced is broken in this space, is unlikely with CO
2Or air runs out of reactor, causes feed liquid to overflow accident.
Fermented liquid is after expanding reach stays for some time, and flowing downward enters lower shell, moves downward to the bottom conical head with fast speed outside air-lift tube, and revolution upwards enters air-lift tube then, finishes a circulation.
The bottom conical head can not make flocculation particle yeast produce local the stop to pile up and stop up, so local dead angle can not be arranged.
In order to guarantee the particle yeast not to be discharged reactor, at the top expanding reach sedimentation guide has been installed, it is shaped as a cylinder, upper and lower opening, diameter is more smaller than top expanding reach.So formed an annular space shape space between guide and the expanding reach.At this space liquid almost is stationary state, so, particle yeast in the fermented liquid because of the gravity natural subsidence in the cylindrical shell of bottom, then form clarified broth in the annular space, this clear liquid is discharged reactor, the particle yeast just is trapped in the reactor fully, uses continuously, and keeps 30～60kg(dry weight)/m
3Concentration.
At reactor lower part the liquid glucose import is installed, can constantly imports liquid glucose and ferment.The fermented liquid that ferments can be discharged continuously, and its ethanol concn can reach 9%～12%(v), and device fabrication intensity can reach 8～12kg alcohol/m
3H improves 8～10 times than general batch fermentation.Thereby realized continuous industry production.
Fermentation is thermopositive reaction.In order to keep leavening temperature, the water cooling chuck is installed outside lower shell, feed cooling water temperature.
Reactor has the following characteristics:
1. the air intlet pipe is set in reactor, and air-distributor and air-lift tube so that can feed little air, make fermented liquid generation sluggish circulation motion in the reactor, and flocculating yeast is suspended in all the time and carries out zymamsis in the fermented liquid.Simultaneously, yeast directly contacts with air in air-lift tube, has improved yeast activity and alcohol tolerance, and yeast is slightly rised in value.
2. expanding reach enlarged diameter in reactor top makes flocculating yeast in this jogging of slowing down, and strengthens fermentation, makes CO
2Bubble is convenient to rise and is overflowed, and upper space can prevent that fermented liquid from overflowing with bubble breaking.
3. gas diverter is air and CO
2Separately, take their own roads, thereby obtain pure CO
2Product.
4. the sedimentation guide is trapped in flocculating yeast in the reactor fully, and life-time service need not add distiller's yeast fully again, does not also need to produce equipment, power and the raw material of distiller's yeast, can reduce cost about 10%.
5. the reactor peripheral hardware can feed water coolant in respect of the water cooling chuck, guarantees to be reflected under the optimal temperature conditions to carry out.
Embodiment:
Useful volume is the suspension bed continuous ferment reactor with flocculated yeast of 500 liters, its lower shell diameter 400mm, long 3200mm, air-lift tube internal diameter 125mm, high 3590mm, top expanding reach diameter is 800mm, high 950mm, settlement barrel diameter 700mm, high 650mm, gas diverter diameter are 250mm, high 700mm, the cooling jacket diameter is 500mm, high 2800mm.
The concentration that saccharification is good is 18～22% liquid glucose injecting reactor, presses the 0.1kg(dry weight)/m
3Liquid glucose inserts the flocculating yeast particle, and ventilation is cultivated.Do when flocculating yeast concentration reaches 30kg()/m
3The time, entering fermenting process, air flow is 0.016m
3(gas)/m
3(liquid) divides, and temperature is controlled at 28～35 ℃, and remaining sugar concentration is reduced to 3～4kg/m in fermented liquid
3The time, beginning constantly adds liquid glucose, and constantly discharges fermented liquid, enters the operate continuously process.
After operate continuously was stable, it was as follows to record every result:
Thinning ratio: D=0.05～0.2m
3(liquid glucose)/m
3(fermented liquid) h
Ventilation ratio: V=0.001～0.1m
3(air)/m
3(fermented liquid) divides
Saccharification liquid total reducing sugar: C=150～250kg/m
3
PH value: PH=5.0～6.0
In the fermented liquid:
Remaining sugar concentration: C=3～10kg/m
3
Total reducing sugar utilization ratio: γ=88.6～94.1%
Ethanol concn: C=9%～12%(v)
PH value: PH=3.0～5.0
Flocculating yeast concentration: C=18.3～41.0kg(does) m
3
Device fabrication intensity: 7.95～15.6kg(alcohol)/m
3H
CO
2Purity: 99.7%
By above result as can be seen, the result that this reactor continuously ferments is better than batch fermentation, and especially device fabrication intensity has improved 8～10 times, also is that volume of equipment and fermentation time have all dwindled 8～10 times than batch fermentation.
Claims (5)
1, a kind of cylindrical flocculating yeast suspension bed alcohol reactor that continuously ferments, its shell is made up of bottom conical head, lower shell, top expanding reach and top elipse head four parts, it is characterized in that the bottom conical head is equipped with air-distributor; Air-lift tube is housed in the lower shell, the water cooling chuck is arranged outward; Gas diverter and sedimentation guide are arranged in the expanding reach of top, and shell and all internals constitute the organic whole that is mutually related.
2, the reactor that continuously ferments according to claim 1, it is characterized in that conical head center, bottom is welded with air intlet pipe and orifice plate air-distributor, air dispersion behind the filtration sterilization can be become small bubbles, and enter the cylindric air-lift tube of the both ends open that is equipped with in the lower shell immediately, its effect is to form the inside and outside density difference of air-lift tube, promote fermented liquid and do the internal recycle motion, ventilating ratio is 0.001～0.1m
3(air)/m
3(fermented liquid) divides, and the flocculating yeast particle promptly evenly is suspended in the fermented liquid, unlikely caking in heaps; Yeast absorbs few oxygen in the air and raising vigor and alcohol tolerance, and leavening temperature is controlled by outer water cooling chuck.
3, according to the described reactor that continuously ferments of claim 1～2, it is characterized in that the top expanding reach, it is a cylinder, upward link to each other with top ellipsoidal head flange, following and lower shell welding, but its diameter is greater than lower shell, the diameter ratio is 1.5～3: 1, the effect of expanding reach is to slow down the mobile speed of fermented liquid, accelerates fermenting process, helps CO
2Bubble is overflowed, and bubble crushing is arranged, prevents the effect that fermented liquid overflows with bubble from the top vapor pipe.
4, according to the described reactor that continuously ferments of claim 1～3, it is characterized in that gas diverter is that the upper end is welded on ellipsoidal head, the lower end is suspended on the cylindrical drum in reaction expanding reach centre, top, and end opening is over against air-lift tube outlet suitable for reading, its effect is to make the air filled cavity of discharging in the air-lift tube through gas diverter, discharge from the elipse head pipe core, avoid and the CO that ferments and generate
2Mix, thereby obtain pure CO
2Product.
5, according to the described reactor that continuously ferments of claim 1～4, it is characterized in that also being equipped with in the expanding reach of reactor top a upper and lower opening, diameter is more smaller than top expanding reach, be sedimentation guide cylindraceous, be fixed on the expanding reach of top, its effect is, between sedimentation guide and top expanding reach, form an annular space, fermented liquid in the annular space remains static substantially, so make in the fermented liquid flocculation particle yeast because of the gravity natural subsidence to the bottom, annular space top forms and does not contain flocculation particulate clear liquor, discharge by the side vent pipe, flocculating yeast just is trapped within the reactor and recycles like this, realizes continuously fermenting.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN92112100A CN1086542A (en) | 1992-09-25 | 1992-09-25 | Suspension bed continuous ferment reactor with flocculated yeast |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN92112100A CN1086542A (en) | 1992-09-25 | 1992-09-25 | Suspension bed continuous ferment reactor with flocculated yeast |
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| Publication Number | Publication Date |
|---|---|
| CN1086542A true CN1086542A (en) | 1994-05-11 |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105372238A (en) * | 2015-12-10 | 2016-03-02 | 中国科学院西北高原生物研究所 | Automated discrete analyzer |
| CN109312291A (en) * | 2016-06-24 | 2019-02-05 | 隆萨有限公司 | Variable-diameter bioreactor |
| CN110057221A (en) * | 2019-05-16 | 2019-07-26 | 北京盛赢节能技术有限公司 | Fluid-bed heat exchanger lower resistance end socket |
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| CN105372238A (en) * | 2015-12-10 | 2016-03-02 | 中国科学院西北高原生物研究所 | Automated discrete analyzer |
| CN105372238B (en) * | 2015-12-10 | 2018-08-03 | 中国科学院西北高原生物研究所 | Full-automatic interruption chemical analyzer |
| CN109312291A (en) * | 2016-06-24 | 2019-02-05 | 隆萨有限公司 | Variable-diameter bioreactor |
| US11597900B2 (en) | 2016-06-24 | 2023-03-07 | Lonza Ltd. | Variable diameter bioreactors |
| TWI808057B (en) * | 2016-06-24 | 2023-07-11 | 瑞士商隆沙有限公司 | Variable diameter bioreactor vessel and system, method of producing a fermentation product using a reduced amount of reactors in a seed stage train and production reactor, and bioproduction facility |
| CN110057221A (en) * | 2019-05-16 | 2019-07-26 | 北京盛赢节能技术有限公司 | Fluid-bed heat exchanger lower resistance end socket |
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