TW201317344A - A method for continuously producing ethanol with a cell recycling multi-tank system - Google Patents

Abstract

The present invention provides a method for continuously producing ethanol with a cell recycling multi-tank system, which is mainly composed of multiple fermenters, each individually equipped with a settler. The method uses the property of flocculent yeast to retreat the yeast back to the fermenter within the settler, and passes the supernatant liquid to the next fermenter of the multi-tank system. The disclosed method can be operated at a high dilution rate, prohibiting the growth of bacteria, making the system more stabilized. In addition, the present invention without constraints on raw material, even sugarcane juice can be directly converted into ethanol.

Description

Method for continuously producing ethanol by multi-tank cell reflux

This invention relates to a process for the production of ethanol, and more particularly to a process for increasing the efficiency of continuous production of ethanol by multi-tank cell reflux.

Biomass alcohol, also known as bioethanol, is the use of microbial fermentation to convert the sugar in the biomass (biomass) to ethanol. Biomass is derived from organisms rather than petrochemicals and generally refers to carbonaceous compounds produced by plants through photosynthesis.

In recent years, due to the sharp increase in global oil demand and the instability of international politics, oil prices have remained high. In view of China's energy demand, it is heavily dependent on oil imports, which has led to a sharp rise in the manufacturing costs and consumer prices of the industry, resulting in instability in people's livelihood. This phenomenon has indirectly affected the security of the country. In the process of pursuing economic prosperity, countries around the world have used a lot of resources and polluted the environment, causing the global climate warming problem to become increasingly serious. In order to reduce greenhouse gas emissions, all countries are actively developing various clean energy technologies, such as biomass energy, wind energy, solar energy, hydrogen energy and fuel cells, and integrated gasification cycle power plants (IGCC). In this situation, the market kinetic energy of biomass energy has risen sharply, and there is a tendency to compete with oil. Biomass energy development has the synergy of energy independence, agricultural development, environmental protection and economic growth. More than 98% of China's energy is dependent on imports. In the case of increasingly tight supply in the international oil and gas market, the development of its own energy is of special significance and can provide new opportunities for agricultural development. Energy crops can absorb greenhouse gases such as carbon dioxide during their growth, which is helpful for environmental improvement. And once the biomass energy industry reaches the scale economy, it will make a great contribution to the effects of employment, income and output. Therefore, regardless of energy, environment and economic considerations in China, biomass energy is a project worthy of vigorous promotion.

As early as the oil crisis of the 1970s, Brazil and the United States actively invested in the development of the bio-alcohol industry. In recent years, under the influence of factors such as excessive CO ₂ emissions, global warming, unstable supply and demand of international crude oil, and rising prices, More and more countries are investing. In 2006, the global production of raw alcohol was about 40 million metric tons, and 90% was produced in Brazil and the United States. Brazil uses sugar cane as a raw material, while the United States produces corn with predominantly corn. Sugar cane and corn are sugar and starchy crops, respectively. The Ministry of Economic Affairs of the country has instructed the state-owned enterprises to take the lead in setting up a biomass alcohol factory to produce quality alcohol from sugar cane and sweet sorghum.

Biomass alcohol is a large-scale chemical that must be mass-produced to meet cost, so the improvement of the fermentation process is an extremely important research topic. The fermentation method of raw alcohol often uses batch fermentation, feed batch and continuous fermentation. Batch fermentation is more commonly used in long fermentation times, low yields or applied to solid fermentation procedures. However, fermentation under high sugar concentration produces matrix inhibition, which causes the fermentation time to be too long and greatly reduces the rate of ethanol production. In order to improve the inhibition of matrix (such as glucose), feed batch fermentation can be used, but there is still a problem of ethanol inhibition, and continuous fermentation can reduce these inhibitions and increase the yield. Continuous fermentation can increase the yield, but the dilution rate during fermentation cannot be greater than the growth rate of the cells, otherwise it will cause the overflow of the cells to appear.

Earlier patents (US Pat. No. 4,443,544) used membrane filtration to separate the bacteria and products from the Zymomonas mobilis broth and return to the fermentation tank for continuous fermentation, which increased the concentration of the cells in the tank. However, it is not economical to use a membrane filtration method to recover the reflux of the cells.

U.S. Patent No. 4,567,145, which uses a single cell fermentation tank equipped with a sedimentation cell reflux device to ferment glucose to obtain ethanol, and the coagulating yeast used is a Saccharomyces uvarum mutant of respiratory metabolic defects (from Saccharomyces uvarum 26602), examples display / L, a dilution rate of 0.129 h ^-1 under Po continuous fermentation, ethanol yield (ethanol productivity) was obtained 6.7 g L ^-1 h ^-1, to increase ethanol yield, diluted in 135 g glucose feed concentration The rate needs to rise again.

The recently proposed Japanese patent (WO 2008120644) also uses a single fermentation tank equipped with a sedimentation type cell reflux device to ferment a high concentration of glucose to obtain ethanol. The coagulating yeast used is Saccharomyces cerevisae AM12 , and the feed glucose concentration is 200 g. /L, the dilution rate (D) is operated between 0.2 ≦D ≦ 0.3, and the ethanol yield can reach 15 g L ^-1 h ^-1 or more.

Because ethanol fermentation is different depending on the source of raw materials, the sugar can not be glucose, and the concentration of sugar can not be controlled at a high concentration. If sugar cane is used as raw material to produce raw ethanol, the sugar in sugar cane juice is mainly sucrose. About 80 g/L, it is not economical to concentrate to a high concentration and then ferment. Recently, although there have been papers on the use of flocculent yeast as a fermentation strain, a single fermentation tank continuous cell reflux fermentation process was studied. This paper uses simulated virgin cane juice as a nutrient substrate feed, diluted. The rate was 0.24 h ^-1 and the yield of ethanol was 9.14 g L ^-1 h ^-1 . It is indicated that after the feed is changed into the cane juice, the yield of the fermented ethanol using the cane juice is greatly reduced as compared with the aforementioned fermentation method using the glucose feed.

Therefore, if we can develop a fermentation method that is not restricted by the fermentation material, we can also convert the cane juice into ethanol and improve the conversion efficiency and yield of the fermentation method, regardless of energy, environment and economy. For a big benefit.

In order to solve the aforementioned problems, it is an object of the present invention to provide a method for producing ethanol, and more particularly to a method for improving the efficiency of continuous production of ethanol by multi-tank cell reflux.

In order to achieve the foregoing object, the present invention provides a method for continuously producing ethanol by multi-tank cell recirculation, the steps comprising:

(a) providing a raw material consisting of a mixture of sugars, nitrogen sources, minerals and vitamins, which are sucrose, glucose, fructose or any combination thereof, and can be used as a sugar source, cane juice The concentration is between 60g-100g/L;

(b) feeding the material to a first fermentation zone at a high dilution rate, wherein the first fermentation zone is previously inoculated with a cohesive yeast;

(c) fermenting the material to produce a fermentation broth, overflowing the lysate and the coagulating yeast from the first fermentation zone to a first cell sedimentation zone, and causing the cohesive yeast to Returning the first cell sedimentation zone to the first fermentation zone;

(d) using the fermentation broth of step (c) as the raw material, using at least a second fermentation zone and at least a second cell sedimentation zone, wherein the second fermentation tank inoculates the coagulating yeast, and repeating the steps (b) and step (c) at least once, until the ethanol yield in the fermentation broth exceeds 13 g/L per hour,

The high dilution rate of step (b) is between 0.25 and 0.48 g/Lh.

The invention further provides a multi-tank cell reflux continuous production system for ethanol, comprising a raw material tank for storing a raw material, the raw material is a mixture of a sugar, a nitrogen source, a mineral and a vitamin, and the sugar can be In addition to sucrose, glucose, fructose or any combination thereof, a cane juice can also be used as a source of sugar, and the concentration of the cane juice is between 60g and 100g/L; a first fermentation tank is connected to the raw material tank, and the raw material is Feeding to the first fermentation tank at a high dilution rate, and producing a fermentation broth, wherein the first fermentation tank is inoculated with a coagulating yeast and is provided with an oxygen-containing gas; a first cell settler is connected to the first a fermentation tank overflowing the broth and the coagulating yeast from the first fermentation tank to the first cell settler, and returning the cohesive yeast from the first cell settler to the a first fermentation tank; at least a second fermentation tank connected to the first cell settler, and feeding the fermentation broth from the first cell settler to the second fermentation tank, wherein the second fermentation tank The fermentation tank inoculates the coagulating yeast and has an oxygen-containing gas; a second cell settler is connected to the second fermentation tank, wherein the first and second cell settlers are all vertical containers, and the fermentation broth overflows from the second fermentation tank and the cohesiveness The yeast flows to the second cell settler, and the cohesive yeast is returned from the second cell settler to the second fermentation tank; wherein the high dilution rate is between 0.25 and 0.48 g/Lh Between the time when the ethanol yield in the broth of the second cell settler exceeds 13 g/L per hour, the mash is flowed to an ethanol collection unit.

In a preferred embodiment of the system for continuously producing ethanol by multi-tank cell reflow according to the present invention, the system further comprises a communication tube connected to the first fermentation zone and the second fermentation zone, wherein the communication tube has a switch.

The technical feature used in the present invention is to make full use of the advantages of both the reflux of the cells and the continuous operation of the multi-tank series. Therefore, the method for producing ethanol by the present invention can be fermented at a high dilution rate to avoid the growth of bacteria. Maintain the stability of the system and other advantages. Moreover, the method for producing ethanol of the present invention is not limited by raw materials, and can be directly fermented by using cane juice as a saccharide raw material. Compared with Japanese Patent (WO 2008120644), the present invention can be operated at a higher dilution rate, and the sucrose concentration is 80. At g/L, there is an ethanol yield of 18.0 g L ^-1 h ^-1 . On the contrary, the Japanese patent must use a very high glucose concentration, that is, 200 g/L, and the ethanol yield can reach 15 g L ^-1 h ^-1 or more. Further, in the present invention, the cells are left in the fermentation tank by utilizing the characteristics of the cohesive yeast, the cell density in the fermentation tank is maintained, the ethanol production cost is lowered, and the production efficiency is improved.

The embodiments of the present invention are further described in the following description, and the embodiments of the present invention are set forth to illustrate the present invention, and are not intended to limit the scope of the present invention. In the scope of the invention, the scope of protection of the invention is defined by the scope of the appended claims.

The invention continuously produces ethanol by a multi-tank reflux fermentation method, and the fermentation comprises two or more sets of bioreactors (fermentation tanks) and a bacterial sedimentation circulation reflux device. Under a certain concentration of sugar (sucrose, glucose, fructose or any combination of the three), set the bacterial reflux ratio (r) of 0.8 to 0.9 and the dilution rate of 0.25 to 0.48 gL ^-1 h ^-1 ( D) Continuous fermentation, after a period of start-up, the concentration of the bacteria in the fermentation tank reaches a stable value, and the concentration of the sugar and the product (ethanol) in the tank remain unchanged.

Yeast growth requires the feeding of sugars, nitrogen sources, vitamins and minerals. Among the various vitamins, vitamin B group is especially needed, which can be provided from yeast extract and peptone.

The cell sedimentation circulation reflux device mentioned here has a simple structure, and any container that is standing upright can be used as a place for cell sedimentation, and is connected with the outlet of the fermentation tank, and the coagulating yeast rapidly aggregates and sinks due to gravity, and the cells at the bottom The pump is sent back to the fermentation tank, and the supernatant clarified broth is removed to the next fermentation tank or sent to the ethanol collection unit.

The present invention is exemplified by Saccharomyces diastaticus LORRE-316 yeast (provided by Purdue University LORRE Laboratory, registration number BCRC 920074), but the present invention is not limited to the implementation of such cohesive yeast, and any condensation Sexual ethanol production yeast can be applied to this.

The fermentation method used in the examples of the present invention is exemplified by two sets of fermentation tanks, as shown in the first figure. In the fermentation system 1 of the first figure, the raw material enters the first fermentation tank 121 from the raw material tank 14 via the first switch 181, and then enters the first cell settler 131 by the second switch 182, in the first cell settler 131. In the middle, the cells will agglomerate and sink by gravity, so that the bottom of the first cell settler 131 is rich in yeast cells, and then is returned to the first fermentation tank 121 by the fourth switch 184, and the upper layer of the first cell settler 131 is clarified. The broth is flowed into the second fermentation tank 122 via the fifth switch 185, and then enters the second cell settler 132 by the sixth switch 186. In the second cell settler 132, the bacteria will aggregate and sink by gravity, so that The bottom of the second cell settler 132 is rich in yeast cells, and is returned to the second fermentation tank 122 by the seventh switch 187, and the supernatant clarified fermentation liquid in the second cell settler 132 flows into the ethanol collection via the eighth switch 188. Unit 15.

The first fermentation tank 121 and the second fermentation tank 122 have a capacity of 5 L. The first cell settler 131 and the second cell settler 132 are cylindrical glass tubes having a diameter of 4 cm and a height of 42.5 cm. In addition, the first fermentation tank 121 and the second fermentation tank 122 are each connected with a ventilation device, and the ventilation device includes a gas control device 111 and a gas filtering device 112 for the first fermentation tank 121 and the second fermentation tank 122. A gas is introduced therein, which is an oxygen-containing gas, which may be air or oxygen. The first fermentation tank 121 and the second fermentation tank 122 are connected to a personal computer 17 to control the pH, temperature and dissolved oxygen in the first fermentation tank 121 and the second fermentation tank 122, wherein the pH value is 5~ 6, commonly used fermentation temperature is 30 ~ 40 ° C, ventilation is 1 vvm.

In order to allow the fermentation tank after the first fermentation tank 121 to have a relatively high substrate concentration at the initial stage, the concentration of the bacteria in the tank is relatively fast, and the present invention suggests that the fermentation tank and the fermentation tank should be in the early stage of fermentation. The inter-line (the line controlled by the third switch 181 in the first figure) is turned on, but reaches a stable continuous operation period, which is in principle closed. This makes the concentration of the fermentation tank reach the continuous operation period, and the effect is less obvious when the low concentration of sugar, such as 80g/L sucrose solution is fed, but the inventor is in another embodiment (not shown). In the case of high concentration of sugars, such as more than 150g / L of feed, the concentration of bacteria in the fermentation tank can be significantly shortened for a continuous operation period.

Example 1-1 Fermentation test separated by two fermentation tanks

The fermentation system of the double-slot continuous bacterial cell reflux module of the embodiment of the present invention is as shown in the first figure. A sucrose solution of 80 g/L was used as a substrate feed, and the composition of the mash was shown in the following table. The temperature was set to 35 ° C, the pH was set to 5, and the flow rate of the air ventilated by the gas control device 111 and the gas filtering device 112 was 1 vvm, and the rotation speed of the agitator 16 was set to 100 rpm to carry out continuous cell reflux fermentation.

Operating at a reflux ratio of r=0.8 and a dilution rate of D=0.42 h ^-1 , a stable continuous fermentation state can be achieved after 8 to 9 hours, and direct communication between the two tanks (ie, in the first figure) The third switch 183) is closed. At this time, since the second slot 122 Po fermentation cell concentration 25.8 g / L, the ethanol concentration of the outlet 37 g / L, the residual sucrose concentration 0.8 g / L, no residual glucose and fructose, ethanol yield was 15.5 gL ^-1 h ^{- 1} . The ethanol yield is defined as: ethanol yield = dilution rate (D) x outlet ethanol concentration. From the initial period to the stable continuous fermentation, the cell concentration, ethanol concentration, sucrose concentration, glucose concentration, and fructose concentration at the outlet of the second fermentation tank 122 are as shown in the second graph.

Example 1-2 Fermentation test with two fermentation tanks separating and increasing the dilution rate

The cells of the two groups of 5L fermentation tanks and the two sets of cell settlers were refluxed, and the fermentation broth composition and fermentation conditions were the same as those in Example 1-1.

Operating at a reflux ratio of r=0.8 and a dilution rate of D=0.48 h ^-1 , a stable continuous fermentation state can be achieved after 10 hours, and the direct communication between the two tanks (the third switch 183) is closed. . At this time, the cell concentration in the second fermentation tank 122 was maintained at 25-26 g/L, the outlet ethanol concentration was 37.5 g/L, and the residual sucrose concentration was 2.6 g/L. There was no glucose or fructose residue, and the ethanol yield was 18.0 gL. ^-1 h ^-1 .

Examples 1-3 Example 1-2 bis fermentation tank connection control test

The cells of the two groups of 5L fermentation tanks and the two sets of cell settlers were refluxed, and the fermentation broth composition and fermentation conditions were the same as those in Example 1-1. After the cell reflux ratio r = 0.8 and the dilution rate D = 0.48 h ^-1 , a stable continuous fermentation state was obtained after 10 hours, but the direct communication between the two slots (the third switch 183) was turned on. At this time, the cell concentration in the second fermentation tank 122 was 30 g/L, the outlet ethanol concentration was 37 g/L, and the residual sucrose concentration was 6.7 g/L. There was no residual glucose and fructose, and the ethanol yield was as high as 17.8 g L ^-1 h. ^-1 .

Example 2-1 Fermentation test of the two fermentation tanks

The cells of the two groups of 5L fermentation tanks and the two sets of cell settlers were refluxed, and the fermentation broth composition and fermentation conditions were the same as those in Example 1-1.

In order to allow the fermentation tank after the first tank to have a relatively high substrate concentration at the initial stage, the concentration of the bacteria in the tank is relatively fast, and the direct flow between the first fermentation tank 121 and the second fermentation tank 122 is The third switch 183 is open, but reaches a steady continuous operation period, which is in principle closed.

The cell reflux ratio is r=0.8 and the dilution rate is D=0.36 h ^-1 , and a stable continuous fermentation state can be obtained after 10 hours. At this time, the cell concentration in the second fermentation tank 122 was 30 g/L, the outlet ethanol concentration was 36 g/L, and the residual sucrose concentration was 1.3 g/L. There was no residual glucose and fructose, and the ethanol yield was 13.3 gL ^-1 h ^{- 1} .

Example 2-2 The fermentation test of connecting the two fermenters and increasing the reflux ratio of the cells

The cells of the two groups of 5L fermentation tanks and the two sets of cell settlers were refluxed, and the fermentation broth composition and fermentation conditions were the same as those in Example 1-1.

When the cell reflux ratio r = 0.9 and the dilution rate D = 0.36 h ^{-1 were} operated, a stable continuous fermentation state was obtained after 10 hours, but the direct communication between the two grooves (the third switch 183) was turned on. At this time, the cell concentration in the second fermentation tank 122 was 32.3 g/L, the outlet ethanol concentration was 38.3 g/L, and the residual sucrose concentration was 0.62 g/L. There was no residual glucose and fructose, and the ethanol yield was 13.8 gL ^-1 h ^{- 1} .

Example 3 Fermentation test for increasing sucrose concentration

The cells of the two groups of 5L fermentation tanks and the two sets of cell settlers were refluxed, and the fermentation broth composition and fermentation conditions were the same as those in Example 1-1. However, the sucrose concentration in the composition of the mash was changed to 160 g/L.

When the cell reflux ratio is r=0.9 and the dilution rate is D=0.2 h ^-1 , a stable continuous fermentation state can be obtained after 15 hours, but the third switch 183 which is directly connected between the two tanks is turned on. At this time, the cell concentration in the second fermentation tank 122 was 40 g/L, the outlet ethanol concentration was 72 g/L, and the residual sucrose concentration was 0.92 g/L. There was no residual glucose and fructose, and the ethanol yield was 14.4 gL ^-1 h ^{- 1} .

According to the above embodiment, the multi-tank fermentation system of the present invention can reduce the inhibition of the matrix and the product, and the concentration of the previous fermentation tank product (ethanol) is low, so that the product inhibition effect is small, and the subsequent fermentation tank base (sugar) The concentration is low and the matrix inhibition is small. Moreover, the method of the present invention is not limited by the saccharide raw material, and can directly ferment the cane juice (concentration of about 80 g/L) to obtain ethanol, and has a high ethanol yield without obtaining a high ethanol yield. The saccharide raw material is further concentrated in advance.

In addition, the method of the present invention can be operated at a high dilution rate, and the high dilution rate has the advantages of avoiding the growth of bacteria, maintaining the stability of the system, and the like. In addition to the feed sugar concentration, the dilution rate is the main operational cause, and the dilution rate is equal to the bacteria in the fermentation tank. The growth rate, so the lower dilution rate is easier to achieve, the feed sugar can be completely digested without residual sugar.

In summary, the present invention fully utilizes the additive effect of both cell reflux and multi-tank serial continuous operation, and proposes a different ethanol fermentation procedure than in the past, so that the method of the present invention is not limited by the sugar raw material, and can also be high. Operating at a dilution rate to achieve cost savings, avoiding the growth of bacteria and system stability.

1. . . Fermentation system

111. . . Gas control device

112. . . Gas filter

121. . . First fermentation tank

122. . . Second fermentation tank

131. . . First cell settler

132. . . Second cell settler

14. . . Raw material tank

15. . . Ethanol collection unit

16. . . Blender

17. . . personal computer

181. . . First switch

182. . . Second switch

183. . . Third switch

184. . . Fourth switch

185. . . Fifth switch

186. . . Sixth switch

187. . . Seventh switch

188. . . Eighth switch

The first figure is a diagram of the fermentation system architecture of the embodiment of the present invention.

The second graph is a graph showing changes in cell concentration, ethanol concentration, sucrose concentration, glucose concentration, and fructose concentration at the second trough outlet of the fermentation tank over time. In the figure, "biomass" means the weight of Saccharomyces diastaticus LORRE-316 yeast.

1. . . Fermentation system

111. . . Gas control device

112. . . Gas filter

121. . . First fermentation tank

122. . . Second fermentation tank

131. . . First cell settler

132. . . Second cell settler

14. . . Raw material tank

15. . . Ethanol collection unit

16. . . Blender

17. . . personal computer

181. . . First switch

182. . . Second switch

183. . . Third switch

184. . . Fourth switch

185. . . Fifth switch

186. . . Sixth switch

187. . . Seventh switch

188. . . Eighth switch

Claims (14)

A multi-tank cell reflux method for continuously producing ethanol comprises the steps of: (a) providing a raw material which is a mixture of a sugar, a nitrogen source, a mineral and a vitamin; (b) a raw material Feeding to a first fermentation zone at a high dilution rate, wherein the first fermentation zone is pre-inoculated with a cohesive yeast; (c) fermenting the material to produce a fermentation broth, the fermentation broth and the cohesiveness The yeast overflows from the first fermentation zone to a first cell sedimentation zone, and returns the cohesive yeast from the first cell sedimentation zone to the first fermentation zone; and (d) the step (c) As the raw material, the mashing solution utilizes at least a second fermentation zone and at least a second cell sedimentation zone, wherein the second fermentation tank inoculates the cohesive yeast, and repeats steps (b) and (c) At least once, until the ethanol yield in the fermentation broth exceeds 13 g/L per hour, wherein the high dilution rate in step (b) is between 0.25 and 0.48 g/Lh. The method of claim 1, wherein the saccharide is sucrose, glucose, fructose or any combination thereof. The method of claim 1 or 2, wherein a cane juice is used as a source of sugar, and the concentration of the cane juice is between 60 g and 100 g/L. The method of claim 1, wherein the coagulating yeast is Saccharomyces diastaticus LORRE-316, and the accession number is BCRC 920074. The method of claim 1, wherein the first fermentation zone and the second fermentation zone are provided with an oxygen-containing gas, and the temperature in the fermentation zone is 30-40 ° C, and the pH is 5 -6. The method of claim 1, wherein the first fermentation zone and the second fermentation zone are in a connected state before stable fermentation. A multi-tank cell reflux continuous production system for ethanol comprises: a raw material tank for storing a raw material, the raw material is a mixed liquid composed of a sugar, a nitrogen source, a mineral and a vitamin; a first fermentation tank, which is connected a raw material tank, and the raw material is fed to the first fermentation tank at a high dilution rate, and a mashing solution is produced, wherein the first fermentation tank is inoculated with a cohesive yeast and has an oxygen-containing gas; a cell settler communicating with the first fermentation tank, overflowing the lysate and the coagulating yeast from the first fermentation tank to the first cell settler, and causing the cohesive yeast to The first cell settler is refluxed to the first fermentation tank; at least a second fermentation tank is connected to the first cell settler, and the fermentation broth is fed from the first cell settler to the second a fermentation tank, wherein the second fermentation tank inoculates the coagulating yeast and is provided with an oxygen-containing gas; and at least a second cell settler is connected to the second fermentation tank to overflow the second fermentation tank The broth and the coagulating yeast flow to the second cell settler and cause the coagulation The yeast is returned from the second cell settler to the second fermentation tank; wherein the high dilution rate is between 0.25 and 0.48 g/Lh, and the mash of the second cell settler When the medium ethanol yield exceeds 13 g/L per hour, the fermentation broth flows to an ethanol collection unit. The system of claim 7, wherein the saccharide is sucrose, glucose, fructose or any combination thereof. The system of claim 7 or 8, wherein a cane juice is used as a source of sugar, and the concentration of the cane juice is between 60 g and 100 g/L. The system of claim 7, wherein the cohesive yeast is Saccharomyces diastaticus LORRE-316 and the accession number is BCRC 920074. The system of claim 7, wherein the first and second cell settlers are all upright containers. The system of claim 1, further comprising a communication tube connected to the first fermentation zone and the second fermentation zone, wherein the communication tube has a switch. The system of claim 7, further comprising a venting device coupled to the first fermentation tank and the second fermentation tank. The system of claim 13, wherein the venting device is configured to pass an oxygen-containing gas to the first fermentation tank and the second fermentation tank, and the temperature in the fermentation tank is 30-40 ° C , pH is 5-6.