JP5661673B2 - Multi-tank cell recycle fermentation method ethanol continuous production method - Google Patents

Description

  The present invention relates to a kind of ethanol production method, and more particularly, to a method for increasing ethanol production efficiency by continuous production of multi-tank cell recycle fermentation ethanol.

  Biomass alcohol is also called bioethanol, and is ethanol obtained by converting carbohydrates in biomass using microorganisms. Biomass is derived from living organisms, not a petrified organic substance, but is generally a carbon-containing compound generated by the photosynthetic action of plants.

  In recent years, oil prices have not fallen due to the steep rise in global oil demand and the unstable state of international politics. Taiwan's demand for energy sources is dependent on imports of large quantities of oil. Economically, manufacturing costs and consumer prices are greatly boosted, creating consumer instability. Affects national security. In the process of pursuing economic prosperity, countries around the world use a large amount of various resources and at the same time pollute the environment, and the global warming problem of the global climate is becoming increasingly severe. Each country is actively developing various clean energy technologies to reduce greenhouse gas emissions. For example, biomass energy, wind energy, solar energy, hydrogen energy, and fuel cells, IGCC (Coal Gasification Combined Cycle Power Generation) ) And the like. Under this circumstance, biomass energy source development has the combined effects of energy source independence, agricultural development, environmental protection and economic growth. More than 98% of Taiwan's energy sources rely on imports, and the international oil and gas market is becoming increasingly severe, and the development of energy sources that do not rely on imports is meaningful and provides new opportunities for agricultural development. . Energy source crops absorb greenhouse gases such as carbon dioxide during the growth process and help improve the environment. And once the biomass energy source industry reaches a certain scale, it will make a huge contribution to the effects of employment, income and production. For this reason, biomass energy is an item that is extremely worthy of promotion, regardless of the level of energy source, environment and economy.

  During the oil crisis in the 1970s, Brazil and the United States actively focused on the development of the biomass alcohol industry. In recent years, excessive carbon dioxide emissions, global warming, instability of international crude oil supply and sustained price increases Under the influence of such factors, more and more nations have come to put power. In 2006, 90% of the world's 40 million kiloliters of biomass alcohol production was produced in Brazil and the United States. Brazil uses sugar cane as a raw material, the United States mainly produces corn and biomass alcohol, and sugar cane and corn are sugar and starchy crops, respectively. The Ministry of Economic Affairs of Taiwan has already set up a biomass alcohol factory as a state-run business and has instructed to produce biomass alcohol from sugar cane and sugar corn.

  Biomass alcohol is a kind of Daejong chemical substance, and it is necessary to reduce the cost by mass production. Improvement of the fermentation process is a very important research subject. The fermentation method of biomass alcohol always uses batch fermentation, feed batch type and continuous type fermentation. Batch fermentation has a long fermentation time, a small output, or is relatively commonly used in solid state fermentation processes. However, fermentation under a high sugar concentration generates a substrate-inhibiting action, and the fermentation time becomes excessive, greatly reducing the ethanol production rate. Feedbatch fermentation can be employed to improve substrate (eg, glucose) suppression, but still has ethanol suppression problems, and the use of continuous fermentation reduces such suppression and increases production rates. Can do. Continuous fermentation can increase the production rate, but the dilution rate during fermentation should not be greater than the growth rate of the cells, otherwise cell overflow phenomenon may be formed.

  According to Patent Document 1, which is relatively early, the cells and the product in the Zymomonas mobilis fermentation broth are separated by a membrane filtration method, and the cells are returned to the fermenter for continuous fermentation, which is the cells in the fermenter. Although the concentration can be increased, the cost of recycling the bacterial cells by the membrane filtration method is relatively high and uneconomical.

In Patent Literature 2, ethanol is obtained by fermenting glucose by deploying a sedimentation type cell recycling apparatus in a single fermenter, and the Saccharomyces uvarum mutant strain (Saccharomyces uvarum 26602) is used for the agglutination yeast used. In this example, continuous fermentation was performed at a glucose feed concentration of 135 g / L and a dilution rate of 0.129 h ⁻¹ , and the ethanol productivity obtained was 6.7 g L ⁻¹ h ^−1. If the ethanol production rate is increased, the dilution rate needs to be further increased.

According to Patent Document 3 recently filed, a single cell fermenter is equipped with a sedimentation type cell recycling device to ferment high concentrations of glucose to obtain ethanol, and the aggregating yeast used is Saccharomyces cerevisae AM12. The feed concentration is 200 g / L, the dilution rate (D) is 0.2 ≤ D ≤ 0.3, and the ethanol production rate reaches 15 gL ^-1 h ^-1 or higher.

Due to the difference in raw materials for ethanol fermentation, the fermentable sugar is not limited to glucose, and the sugar concentration cannot always be controlled to a high level. If sugarcane juice is used as raw material to produce biomass ethanol, The sugar in sugarcane juice is mainly sucrose, and the concentration is about 80 g / L. If it is concentrated to a high concentration and further fermented, the cost performance will deteriorate. In recent years, there has been a paper on the use of flocculent yeast as a fermentation strain, and research on continuous cell recycling fermentation processes using a single fermenter has been conducted. According to this paper, As a nutrient substrate material, the dilution rate is 0.24 h ⁻¹ and the ethanol production rate is 9.14 gL ⁻¹ h ⁻¹ . For this reason, when the material is changed to sugarcane juice, the fermented ethanol production rate is significantly reduced compared to the fermentation method using glucose as the material.

  Therefore, if there is a fermentation method that is not restricted by fermentation raw materials, that is, cane sugar cane juice can be converted into ethanol, and conversion efficiency and production rate can be improved, from any aspect of energy source, environment and economy Even if it sees, there is a big merit.

U.S. Pat. No. 4,443,544 US Pat. No. 4,567,145 International Patent No. WO2008120644

  In order to solve the above-mentioned problems, an object of the present invention is to provide a method for producing a kind of ethanol, and in particular, a method for increasing the efficiency of continuous production of ethanol by a multi-tank cell recycle fermentation system.

The above-mentioned object is a multi-tank cell recycle fermentation method ethanol continuous production method provided by the present invention.
(A) providing a raw material, the raw material being a mixture composed of sugars, nitrogen sources, minerals, and vitamins, wherein the sugars are sucrose, glucose, fructose or any combination thereof; and Sugarcane juice can be used as a sugar source, and the sugarcane juice concentration is 60 g-100 g / L.
(B) A step of feeding the raw material to the first fermentation area at a high dilution rate, in which the first fermentation area is inoculated with a flocculating yeast in advance.
(C) fermenting the raw material to produce a fermentation broth, overflowing the fermentation broth and the aggregated yeast from the first fermentation area to the first cell sedimentation area, and Returning from the settling area to the first fermentation area.
(D) using the fermentation broth of step (c) as the raw material, utilizing at least one second fermentation area and at least one second cell sedimentation area, inoculating the aggregated yeast in the second fermentation area, Repeating step (b) and step (c) at least once and repeating until the ethanol production rate in the fermentation liquid exceeds 13 g / L per hour.
Including the above steps, of which the high dilution rate in step (b) is between 0.25 and 0.48 g / Lh.

The present invention also provides a kind of multi-tank cell recycle fermentation ethanol continuous production system,
A raw material tank for storing the raw material, wherein the raw material is a mixed liquid composed of sugar, nitrogen source, mineral and vitamin, and the sugar is sucrose, glucose, fructose or any combination thereof; and Sugar cane juice can be used as a saccharide source, and the sugar cane juice concentration is 60 g-100 g / L,
A first fermenter that communicates with the raw material tank and feeds the raw material to the second fermenter at a high dilution rate, produces a fermentation liquor, and inoculates the first fermenter with flocculant yeast And the first fermentor in which an oxygen-containing gas is introduced,
A first cell sedimentator, which is communicated with the first fermentor, wherein the fermented liquid overflowing from the first fermentor and the flocculated yeast flow in, and the flocculated yeast is the first cell sedimentator. The first cell sedimentator to be poured back into the first fermentor;
At least one second fermenter that communicates with the first cell sedimentator, the fermented liquid is sent from the first cell sedimentator to the second fermenter, and the flocculent yeast is fed to the second fermenter The at least one second fermentor inoculated with fungus and infused with oxygen-containing gas;
At least one second cell sedimentator, communicated with the second fermentor, wherein the first cell sedimentator and the second cell sedimentator are both upright containers, overflowing from the second fermentor The at least one second cell sedimentation wherein the fermented liquid and the aggregated yeast flow into the second cell sedimentator, and the aggregated yeast is flowed back from the second cell sedimentator to the second fermenter. And
Wherein the high dilution rate is between 0.25 and 0.48 g / Lh, and when the ethanol production rate in the fermentation broth exceeds 13 g / L per hour, the fermentation broth is ethanol Into the collecting unit.

  In a preferred embodiment of the multi-tank cell recycle fermentation ethanol continuous production system of the present invention, the system further includes a communication pipe connecting the first fermentation tank and the second fermentation tank, the communication pipe having a switch. It is.

The technical features used by the present invention have the advantage of a synergistic effect of cell recycle and multi-tank serial continuous operation. Therefore, the method of producing ethanol using the present invention is capable of fermentation at a high dilution rate. It has the advantages of being able to proceed, preventing the growth of various bacteria, and maintaining the stability of the system. In addition, the ethanol production method of the present invention is not limited by the raw material, and can be directly fermented with sugarcane juice as a saccharide raw material. Compared with Patent Document 3 (International Patent No. WO2000081644), the present invention It can be operated at a relatively high dilution rate and has an ethanol production rate of 18.0 gL ⁻¹ h ⁻¹ when the sucrose concentration is 80 g / L. On the other hand, in Patent Document 3, the ethanol production rate cannot be increased to 15 gL ⁻¹ h ⁻¹ or more unless a very high glucose concentration of 200 g / L is used. In addition, the present invention utilizes the characteristics of the agglutinating yeast to keep the cells in the fermenter, maintain the cell density in the fermenter, lower the ethanol production cost, and increase the production efficiency.

It is a fermentation system structure figure of the example of the present invention. It is a change figure with the time of the cell concentration of the 2nd fermenter exit of this invention, ethanol concentration, sucrose concentration, glucose concentration, and fructose concentration. In the figure, “biomass” refers to the weight of Saccharomyces diastaticus LORRE-316 yeast.

  In order to describe in detail the technical contents, structural features, and objects to be achieved of the present invention, examples will be described below in combination with the drawings.

The present invention provides a multi-tank cell recycle fermentation method ethanol continuous production method, and the multi-tank cell recycle fermentation method ethanol continuous production system used therefor includes two or more sets of bioreactors (fermenters) and cells. Includes settling circulation recycling equipment. Feed a certain concentration of sugar (sucrose, glucose, fructose or any combination thereof), with a cell recycling ratio (r) of 0.8-0.9 and 0.25-0.48 gL ^-1 h ^-1 When continuous fermentation is carried out with the dilution rate (D) set, the cell concentration in the fermenter reaches a stable value after the start-up, and at this time, the saccharide and product (ethanol) in the fermenter All concentrations are maintained and unchanged.

  The growth of yeast requires supply of sugars, nitrogen sources, vitamins, minerals, etc. Among them, vitamin B group is the most important among various vitamins, and this part is composed of yeast extract and peptone. More provided.

  The structure of the cell sedimentation circulation recycling apparatus is simple, any upright container can be a place for cell sedimentation, connected to the fermenter outlet, the aggregating yeast rapidly aggregates and settles by gravity, the bottom Cells are pumped to the fermentor and the upper supernatant is sent to the next fermentor or to the ethanol collection unit.

  An example of the present invention was deposited with the Saccharomyces diastaticus LORRE-316 yeast (which was already deposited on 19 January 2012 in China's CHINA CENTER FOR TYPE CULTURE COLLECTION (CCTCC)) and its deposit code Is CCTCC M 2012010), but is not limited to such an aggregating yeast in the practice of the present invention, and any ethanol-producing yeast having an aggregating property can be applied. Is possible.

  The fermentation method used in the examples of the present invention uses two sets of fermenters as an example, as shown in FIG. In the fermentation system 1 of FIG. 1, the raw material enters the first fermenter 121 from the raw material tank 14 through the first switch 181, and further enters the first cell sedimentator 131 from the second switch 182, thereby first cell sedimentation. In the vessel 131, the bacterial cells aggregate and settle by gravity, and the yeast cells are stored at the bottom of the first cell sedimentator 131, and then flowed back to the first fermenter 121 through the fourth switch 184. In addition, in the first cell sedimentator 131, the fermentation broth, which is the supernatant, flows into the second fermenter 122 from the fifth switch 185, and further enters the second cell sedimentator 132 from the sixth switch 186, In the second cell sedimentator 132, the bacterial cells aggregate and settle by gravity. The yeast cells are stored at the bottom of the second cell sedimentator 132 and then returned to the second fermenter 122 from the seventh switch 187. In addition, the fermentation broth, which is the supernatant in the second cell sedimentator 132, flows into the ethanol collection unit 15 from the eighth switch 188.

  Among them, the first fermenter 121 and the second fermenter 122 have a capacity of 5 L, and the first cell sedimentator 131 and the second cell sedimentator 132 are cylindrical glass tubes having a diameter of 4 cm and a height of 42.5 cm. The In addition, the 1st fermenter 121 and the 2nd fermenter 122 are each connected to the aeration apparatus, and this aeration apparatus contains the gas control apparatus 111 and the gas filtration apparatus 112, and the 1st fermentation tank 121 and the 2nd fermentation tank. Gas is passed through 122. The gas is an oxygen-containing gas and can be air or oxygen gas. And the computer 17 is connected to the 1st fermenter 121 and the 2nd fermenter 122, The pH value, temperature, and oxygen dissolution amount in the 1st fermenter 121 and the 2nd fermenter 122 are controlled by this computer 17, Among them, The pH value is 5 to 6, the normal fermentation temperature is 30 to 40 degrees Celsius, and the aeration rate is 1 vvm.

  In the present invention, the fermenter after the first fermenter 121 has a relatively high substrate concentration at the start, and so that the bacterial cell concentration in the fermenter increases relatively rapidly. Although the pipeline between the fermenters (the pipeline controlled by the third switch 183 in FIG. 1) is opened, this communication is closed in principle when a stable continuous operation period is entered. As a result, the fermenter concentration is rapidly stabilized and put into a continuous operation period operation. When feeding low concentrations of sugars such as 80 g / L sucrose solution, the effect is relatively unclear, but in another embodiment (not shown in the text), the inventor has a high concentration such as higher than 150 g / L. As a result, the time until the cell concentration in the fermenter reached the concentration in the continuous operation period was clearly reduced.

菌体リサイクル比ｒ＝０．８及び希釈率Ｄ＝０．４２h^-1で操作すると、８〜９時間で安定した連続発酵状態となり、且つ二槽の間の直接連通（すなわち図１中の第３スイッチ１８３）は遮断される。この時、第２発酵槽１２２内の細胞濃度は２５．８g/Lで、出口エタノール濃度は３７g/Lであり、残留蔗糖濃度は０．８g/Lであり、ブドウ糖及び果糖の残留はなく、エタノール生産率は１５．５gL^-1h^-1であった。エタノール生産率の定義は、エタノール生産率＝希釈率（Ｄ）×出口エタノール濃度である。開始期より安定した連続発酵にいたるまでの、第２発酵槽１２２出口の細胞濃度、エタノール濃度、蔗糖濃度、ブドウ糖濃度、及び果糖濃度は時間の変化と共に、図２のようである。 [Example 1-1]
-Fermentation test which isolate | separated two fermenters The fermentation system of the two tank continuous-type microbial cell recycling module of the Example of this invention is as FIG. 1 shows. An 80 g / L sucrose solution was fed as a substrate, and the composition of the fermentation broth is as shown in the following table. The temperature is 35 degrees Celsius, the pH value is 5, the flow rate of air passing through the gas control device 111 and the gas filtration device 112 is 1 vvm, the rotation speed of the stirrer 16 is set to 100 rpm, and fermentation of continuous bacterial cell recycling is performed. .

When operated at a cell recycle ratio r = 0.8 and dilution rate D = 0.42 h ⁻¹ , a stable continuous fermentation state was achieved in 8 to 9 hours, and direct communication between the two tanks (that is, the first in FIG. 1) 3 switch 183) is cut off. At this time, the cell concentration in the second fermenter 122 is 25.8 g / L, the outlet ethanol concentration is 37 g / L, the residual sucrose concentration is 0.8 g / L, and there is no residual glucose and fructose. The ethanol production rate was 15.5 gL ⁻¹ h ⁻¹ . The definition of the ethanol production rate is ethanol production rate = dilution rate (D) × exit ethanol concentration. The cell concentration, ethanol concentration, sucrose concentration, glucose concentration, and fructose concentration at the outlet of the second fermentor 122 from the start to the stable continuous fermentation are as shown in FIG.

[Example 1-2]
Fermentation test in which two fermenters were separated and the dilution rate was increased. Two sets of 5 L fermenters and two sets of cell sedimentators were connected in series for cell recycle fermentation. Same as 1.
When operated at a cell recycle ratio r = 0.8 and dilution rate D = 0.48 h ⁻¹ , a stable continuous fermentation state was obtained in 10 hours, and direct communication between the two tanks (ie, the third switch in FIG. 1). 183) is blocked. At this time, the cell concentration in the second fermentor 122 is maintained at 25-26 g / L, the outlet ethanol concentration is 37.5 g / L, the residual sucrose concentration is 2.6 g / L, and glucose and fructose remain. The ethanol production rate was 18.0 gL ⁻¹ h ⁻¹ .

[Example 1-3]
-Control test in which the two fermenters of Example 1-2 were communicated. Two sets of 5L fermenters and two sets of cell sedimentators were connected in series to ferment cell recycle. Same as -1.
When operated at a cell recycle ratio r = 0.8 and dilution rate D = 0.48 h ⁻¹ , a stable continuous fermentation state was obtained in 10 hours, and direct communication between the two tanks (ie, the third switch in FIG. 1). 183) is opened. At this time, the cell concentration in the second fermenter 122 is 30 g / L, the outlet ethanol concentration is 37 g / L, the residual sucrose concentration is 6.7 g / L, there is no residual glucose and fructose, and ethanol production The rate was 17.8 gL ⁻¹ h ⁻¹ .

[Example 2-1]
・ Fermentation test in which two fermenters were in communication Two sets of 5L fermenters and two sets of cell sedimentators were connected in series for cell recycle fermentation, and the composition of the fermentation liquor and fermentation conditions were the same as in Example 1-1. .
The first fermenter 121 and the second fermenter so that the fermenter after the first fermenter has a relatively high substrate concentration at the start, and the bacterial cell concentration in the fermenter increases relatively rapidly. The third switch 183 that directly connects between the 122 is opened, but this communication is closed in principle when a stable continuous operation period is entered.
When operated at a cell recycle ratio r = 0.8 and dilution rate D = 0.36 h ⁻¹ , a stable continuous fermentation state is achieved in 10 hours. At this time, the cell concentration in the second fermenter 122 is 30 g / L, the outlet ethanol concentration is 36 g / L, the residual sucrose concentration is 1.3 g / L, there is no glucose and fructose residue, and ethanol production The rate was 13.3 gL ⁻¹ h ⁻¹ .

[Example 2-2]
・ Fermentation test in which two fermenters were connected and the cell recycling ratio was increased. Two sets of 5L fermenters and two sets of cell sedimentators were connected in series for cell recycle fermentation. Same as 1-1.
When operated at a cell recycling ratio r = 0.9 and dilution rate D = 0.36 h ⁻¹ , a stable continuous fermentation state is obtained in 10 hours, but direct communication between the two fermenters (third switch 183) Is open. At this time, the cell concentration in the second fermenter 122 is 32.3 g / L, the outlet ethanol concentration is 38.3 g / L, the residual sucrose concentration is 0.62 g / L, and glucose and fructose remain. rather, ethanol production rate was 13.8gL ^-1 h ^-1.

[Example 3]
-Fermentation test with increased sucrose concentration Two sets of 5L fermenters and two sets of cell sedimentators were connected in series for cell recycle fermentation, and the composition of fermentation broth and fermentation conditions were the same as in Example 1-1, except that The sucrose concentration in the fermentation broth composition is 160 g / L.
When operated at a cell recycling ratio r = 0.9 and dilution rate D = 0.2 h ⁻¹ , a stable continuous fermentation state is achieved in 15 hours, but direct communication between the two fermenters (third switch 183) Is open. At this time, the cell concentration in the second fermenter 122 is 40 g / L, the outlet ethanol concentration is 72 g / L, the residual sucrose concentration is 0.92 g / L, there is no residual glucose and fructose, and ethanol production The rate was 14.4 gL ⁻¹ h ⁻¹ .

  As can be seen from the above examples, the multi-tank cell recycle fermentation ethanol continuous production system of the present invention can reduce the inhibitory action of the substrate and product, and the previous fermenter product (ethanol) concentration is low. For this reason, the product inhibitory action is small, the subsequent fermenter substrate (saccharide) concentration is low, and the substrate inhibitory action is small. In addition, the method of the present invention is not limited by the sugar raw material, and can be obtained by directly fermenting sugarcane juice (concentration of about 80 g / L) to obtain ethanol, as well as increasing the ethanol production rate and obtaining a relatively high ethanol production rate. Therefore, it is not necessary to concentrate the saccharide raw material in advance.

  In addition, the method of the present invention has the advantages that it can be operated at a high dilution rate, prevents the growth of bacteria by the high dilution rate, and maintains the stability of the system. Factors affecting the production efficiency of ethanol in continuous fermentation production are not only the sugar concentration but also the dilution rate, but when continuous fermentation reaches a stable state, the dilution rate is the growth rate of the cells in the fermenter. Equal to the speed, and therefore a relatively low dilution ratio is achieved relatively easily, the fed sugars are completely digested and no residual sugar is present.

  Taken together, the present invention fully utilizes the synergistic effect of cell recycling and continuous operation in a multi-tank series, provides an ethanol fermentation process different from the conventional one, and the method of the present invention is limited by saccharide raw materials. In addition, it can be operated at a high dilution rate, saves manufacturing costs, prevents the growth of germs, and stabilizes the system.

DESCRIPTION OF SYMBOLS 1 Fermentation system 111 Gas control apparatus 112 Gas filtration apparatus 121 1st fermentation tank 122 2nd fermentation tank 131 1st cell sedimentator 132 2nd cell sedimentator 14 Raw material tank 15 Ethanol collection unit 16 Stirrer 17 Computer 181 1st switch 182 2nd switch 183 3rd switch 184 4th switch 185 5th switch 186 6th switch 187 7th switch 188 8th switch

Claims (11)

In the multi-tank cell recycle fermentation method ethanol continuous production method,
(A) providing a raw material which is a mixed liquid composed of sugars, nitrogen source, mineral substance, and vitamin;
(B) a step of feeding the raw material at a high dilution rate to the first fermentation area that has been previously inoculated with the flocculating yeast;
(C) fermenting the raw material to produce a fermentation broth, overflowing the fermentation broth and the aggregated yeast from the first fermentation area to the first cell sedimentation area, and Returning from the sedimentation area to the first fermentation area;
(D) Using the fermentation broth of step (c) as the raw material, using at least one second fermentation area and at least one second cell sedimentation area, inoculating the second fermentation area with the aggregated yeast. Repeating the steps (b) and (c) at least once, until the ethanol production rate in the fermentation liquid exceeds 13 g / L per hour,
Including the above,
Among them, the high dilution ratio in step (b) is 0.25 to 0.48 h ⁻¹ , the residual sugar concentration is 1 g / L or less, and the flocculating yeast is Saccharomyces diastaticus LORRE-316, and its deposit code Is a CCTCC M2012010 , wherein the first fermentation area and the second fermentation area are in a state of communication until a stable fermentation state is reached. .   The multi-tank cell recycle fermentation ethanol method according to claim 1, wherein the saccharide is sucrose, glucose, fructose or any combination thereof. Continuous production method.   3. The multi-tank cell recycle fermentation method ethanol continuous production method according to claim 1 or 2, wherein sugarcane juice is used as a saccharide source, and the concentration of the sugarcane juice is 60 g-100 g / L. A multi-tank cell recycle fermentation method ethanol continuous production method.   The multi-tank cell recycle fermentation ethanol continuous production method according to claim 1, wherein an oxygen-containing gas is introduced into the first fermentation area and the second fermentation area, and the temperature in these fermentation areas is 30-40 degrees Celsius. The multi-tank cell recycle fermentation method ethanol continuous production method, wherein the pH value is 5-6. In the multi-tank cell recycle fermentation method ethanol continuous production system,
A raw material tank for storing the raw material, the raw material storing a raw material which is a mixed liquid composed of sugars, nitrogen source, mineral and vitamin;
A first fermentor that communicates with the raw material tank and that feeds the raw material at a high dilution rate, produces a fermentation liquor, is inoculated with flocculated yeast, and is fed with an oxygen-containing gas;
A first cell sedimentator that communicates with the first fermenter, the fermented liquid overflowing from the first fermentor and the flocculating yeast, and flows the flocculated yeast back into the first fermentor; ,
At least one second fermentor that communicates with the first cell sedimentator, into which the fermentation broth flows from the first cell sedimentator, inoculated with the flocculent yeast, and into which oxygen-containing gas is introduced;
At least one second cell sedimentation that communicates with the second fermenter, the fermented liquid overflowing from the second fermenter and the flocculating yeast flow in, and flows the flocculated yeast back into the second fermenter. And
A communication pipe connecting the first fermentor and the second fermentor;
The high dilution ratio is 0.25 to 0.48 h ⁻¹ , the residual sugar concentration is 1 g / L or less, and the flocculating yeast is Saccharomyces diastaticus LORRE-316, and the deposit code is CCTCC When the ethanol production rate of the second cell sedimentator in the fermentation broth exceeds 13 g / L per hour, the fermentation broth in the second cell sedimentator is collected in the ethanol collection unit. A multi-tank cell recycle fermentation system ethanol continuous production system.   The multi-tank cell recycle fermentation system according to claim 5, wherein the saccharide is sucrose, glucose, fructose or any combination thereof. Ethanol continuous production system.   The multi-tank cell recycle fermentation ethanol continuous production system according to claim 5 or 6, wherein sugarcane juice is used as a saccharide source, and the concentration of sugarcane juice is 60 g-100 g / L. A multi-tank cell recycle fermentation system ethanol continuous production system.   The multi-tank cell recycle fermentation method ethanol continuous production system according to claim 5, wherein both the first cell sedimentator and the second cell sedimentator are upright containers. Bacteria recycle fermentation ethanol continuous production system.   The multi-tank cell recycle fermentation fermentation ethanol continuous production system according to claim 5, wherein the communication pipe includes a switch.   The multi-tank cell microbial cell recycle fermentation method ethanol continuous production system according to claim 5, comprising a venting device connected to the first fermenter and the second fermenter. Recycle fermentation ethanol continuous production system.   The multi-tank cell recycle fermentation ethanol continuous production system according to claim 10, wherein the aeration apparatus passes an oxygen-containing gas into the first fermentation tank and the second fermentation tank, and the temperature in the fermentation tank. Is a multi-tank cell recycle fermentation fermentation ethanol continuous production system, characterized in that the temperature is 30-40 degrees Celsius and the pH value is 5-6.

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