EP1618202A1 - Polylactic acid production from sugar molasses - Google Patents

Polylactic acid production from sugar molasses


Publication number
EP1618202A1 EP20030777502 EP03777502A EP1618202A1 EP 1618202 A1 EP1618202 A1 EP 1618202A1 EP 20030777502 EP20030777502 EP 20030777502 EP 03777502 A EP03777502 A EP 03777502A EP 1618202 A1 EP1618202 A1 EP 1618202A1
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Prior art keywords
lactic acid
industrial process
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German (de)
French (fr)
Tiago Botelho
Nadia Teixeira
Filipe Aguiar
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Aguiar Filipe
Botelho Tiago
Teixeira Nadia
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Tiago Botelho
Nadia Teixeira
Filipe Aguiar
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    • C12P7/00Preparation of oxygen-containing organic compounds
    • C12P7/40Preparation of oxygen-containing organic compounds containing a carboxyl group including Peroxycarboxylic acids
    • C12P7/56Lactic acid
    • C12M47/00Means for after-treatment of the produced biomass or of the fermentation or metabolic products, e.g. storage of biomass
    • C12M47/10Separation or concentration of fermentation products


The present invention describes the industrial process for polyl actic acid (PLA) production through sterification and polymerization of purified lactic acid, being the referred acid obtained through a fermentative process.




Polylactic acid Production from Sugar Molasses


This invention describes the production process of polylactic acid (PLA) obtained by sterification and polymerisation of purified lactic acid, produced through a fermentative process.


The PLA is a natural polymer composed by lactic acid chains. This polymer is a completely biodegradable aliphatic polyester when placed in a biologically rich environment, such as a composting plant. Despite its characteristics, the use of this polymer as a substitute for the common polymers obtained through petroleum is still quite small. This situation is a consequence of the fact that the industrial processes used nowadays to produce this polymer are not able to provide enough good quality product at competitive prices.

This polymer is obtained by sterification and polymerisation of lactic acid dimmers. This acid has an asymmetrical carbon that can exist under the form of two enantiomers, L (+) - lactic acid and a D (-) - lactic acid. Thus, the obtain dimmer has two asymmetrical carbons and, consequently, can exist under the form of three enantiomers: dimmer L (two asymmetrical carbons have configuration L), the D dimmer (two asymmetrical carbons in configuration D) and the meso dimmer (an asymmetric carbon with configuration D and the other configuration L). The properties of the obtained polymer are subject to the stereochemistry of the lactic acid and its dimmer. Polylactic acid is synthesized mainly through isomer L.

The lactic acid is obtained, mainly, in a biological way, through fermentative processes using lactic bacteria, in rich environments containing fermentable sugars.

The lactic acid can be obtained by a great variety of bacteria of the Lactobacillus type, but according to the culture used in fermentation we can obtain any of the two isomers and their matching racemic mixtures.

Nowadays, the industrial processes to produce lactic acid use substrates obtained through com seeds. However, it is often necessary to pre-treat these substrates by adding enzymes that will decompose the substrate sugars into simpler ones susceptible of being used by the bacterial species. Besides that, and due to the fact that these substrates do not have all the mineral and protein content necessary for culture growth, these nutrients also have to be added.

The lactic acid isolation and purification use techniques such as filtration, extraction, electrodialysis, reversed osmosis and chromatography, or, in some cases, the combination of two or more techniques at the same time. Some of these techniques are very expensive and difficult to put into practise or use organic solvents harmful to the environment.

The lactic acid sterification and polymerisation into PLA, is often carried out using chemical methods involving organic solvents, which originates effluents that are difficult to treat and to eliminate.

We will mention, as example, the following patents:

1. The European patent nr. 230,021 describes a process through which glucose is continuously fermented into lactic acid and in which this acid is continuously removed by direct electrodialysis of the fermentation broth. Yeast extracts and inorganic salts are used in this process as supplements. We can point out two big disadvantages in this process: On the one hand, the bacteria quickly clog up the ED membranes reducing their effectiveness, with a resulting increase in the energetic costs; on the other, the use of yeast extract makes the process too much expensive.

2. Boyaval et al. (Biotechnology Letters, Vol. 9, N° 3, 207-212, 1987) describe a lactic acid fermentation process in three steps (production of biomass and lactic acid, separation and concentration of the cellules by ultra filtration (UF) and, in the last step, the concentration and purification of the lactic acid by ED.

The main disadvantage of this system is that it is a discontinuous process.

3. The U.S. patent nr. 5,002,881 describes a lactic acid purification method in solutions, in which the lactic acid is produced as ammonia lactate, through a medium with glucose. The removal of the ammonia lactate is carried out using UF and in which the retained returns to the fermenter, reducing the energetic consumption. The fermentation is carried out by Bacillus coagulans. The permeable concentration is made by reverse osmosis (RO) and the lactic acid recovery is made by ED.

The main disadvantage of this process is in the use of a bacterial strain that requires the addition of amino acids as a nutrient, which increases the costs of the process. 4. The US patent 6,319,382 B1 describes the use of enzymes directly in the fermenter in order to hydrolyse the lactic proteins supplied as a nutritional supplement for the fermentation of the lactic acid. Commercial proteases are also used according to the fermentation pH to hydrolyse the existing proteins in the environment. A combination of ion-exchange resin ED is used in the recovery of lactic acid.

The disadvantages of this process are due to the fact that the use of hydrolytic enzymes is necessary for the uptake of the complex nutrients used.

5. The US patent 5,892,109 B1 describes a process for the production of lactic acid and its separation and recuperation, using, to this effect, an extraction with water-soluble trialquilamine in the presence of carbon dioxide. The lactic acid is recovered in the resulting organic phase. The main disadvantage of this process is precisely the use of organic solvents to purify the lactic acid.

6. The US patent 6,187,951 describes a very similar process to the one in the previous patent. It describes the lactic acid production through the fermentation of a sugar solution carried out by Lactobacillus. The lactic acid produced is precipitated by the addition of ammonia carbonate and then recovered using long chain trialquilamine.

The most obvious disadvantage is the same described in the previous patent.


According to the present invention, a sugar rich growth medium is used, specifically, sugar-beet molasses. The beet is a root, where high amounts of sucrose are stored, and it is becoming more and more a source of common sugar. Only half of the available sugars are extracted from beet, because the other 50 % would imply a highly expensive process to extract. Three main products are obtained from the sugar extraction from beet: the refined sugar, the pulp and the molasses. The sugar-beet molasses contain a high organic content, which can become an environmental problem when released in the environment without prior treatment.

The existing sugars in sugar-beet molasses are all fermentable. Molasses are comprised of monosaccharides like fructose, disaccharides like sucrose and other polysaccharides. Besides sugars, this growth medium contains mineral and protein supplements, which, therefore do not need to be added in large amounts. The composition of common sugar molasses can be observed in the following table. Sugar-beet Sugar-cane

Composition Molasses Molasses

Dry weight (%) 78-85 77-84

Sucrose 48.5 33.4

Rafinose 1.0 -

Frutose 1.0 21.2

Other Organic materials 20.7 19.6


N 0.2-2.8 0.4-1.5

P205 0.02 - 0.07 0.6-2.0

CaO 0.15-0.7 0.1-1.1

MgO 0.01 -0.1 0.03-0.1

K20 2.2-4.5 2.6 - 5.0

Si02 0.1-0.5 -

AI2O3 0.005 - 0.06 -

Fe03 0.001 - 0.02 -

Ashes 4-8 7-11

Vitamins (mg/100g dry weight)

Tiamin 130 830

Riboflavin 41 250

Piridoxin 540 650

Niacinamin 5100 2100

Pantotenic Acid 130 2140

Folic Acid 21 3.8

Biotin 5.3 120

The composition of each lot may vary slightly, even if the lots originate from the same source. In order to increase the fermentation yield, the sugar-beet molasses must be submitted to a pre- treatment. This way, the undesired impurities and toxic substances, which sometimes exist in sugar molasses, are separated and/or inactivated. The pre-treatment consists firstly, of a dilution to 35° Brix, followed by an acidification with H2SO42 M to a pH of 4.0, boiled for 5 min and finally centrifuged and filtered. After this treatment the growth medium is now pasteurised. This growth medium is then conducted to a fermenter where it will be fermented by a pure culture of lactic bacteria, from a strain known as Lactobacillus delbrueckii. These bacteria exist in many food products and can be also found in the normal flora of the mouth and intestines of many animal species, including humans and are rarely pathogenic. The bacteria cells have an average diameter of about 0.7 micrometers.

The microorganism chosen for this fermentation process is an unicellular bacteria. The cells have a rod like shape and do not possess mobility. They are Gram Positive bacteria, due to the peptidoglycan that exists on the cell wall, are microaerophile and have a strictly sarcolastic metabolism. The strain is homofermentative, which means that sugars fermentation into lactic acid occurs exclusively by the Embden-Meyerhof way, or glicolisys, and therefore there are no other products resulting from the fermentation.

This strain produces only the L form of lactic acid and the bacteria do not consume this product. It has an optimal growth temperature between 30 and 50 °C and an optimal pH between 6 and


The strain used in this invention has complex nutritional needs. Therefore, the growth medium must contain between 12 and 13 % of glucose, 0.25% of ammonia and phosphate, and B complex Vitamins. In order to satisfy these needs, after the dilution of the molasses, a solution of (NH4)2HPO4 has to be added, to suppress the growth medium lack of these two components.

The growth medium contains a wide variety of remaining cells and spores from its constituting elements. These must be eliminated prior to inoculation, in order to maximize the fermentation yield.

The sterilization occurs continuously and takes place in heat exchangers, with the shape of concentric tubes, where steam or overheated water at 140 °C passes trough the external tube and the growth medium passes trough the internal tube. The hold-up is between 30 and 120 seconds depending on work rate. The medium must then pass trough a cooler, in order to reduce its temperature to match the fermentation temperature.

To reduce energy costs with heating and cooling the medium, un-sterilized medium (cold) is crossed with sterilized medium so that the last one can be cooled to the fermentation temperature.

This type of sterilization has the advantage of reducing the sterilization cycle time, easy control and productivity increase, without the destruction of the existing nutrients in the solution. During the sterilization process it is common to observe the formation of foam. Adding a tensioactive compound such as Tween 80 in a concentration of 0.001 % can minimize this effect.

The sterilization of the reactor and of the filtration systems is made by direct steam injection; this is possible because the filtration membranes are thermoresistant.

In order to increase even further the process productivity, the fermentation takes place in a continuously agitated reactor, like a chimostat, with a high cell concentration. This system avoids, simultaneously, substrate inhibition - since the substrate is continuously supplied into the fermenter - and product inhibition - since the lactic acid is continuously removed from the fermenter.

The high cell concentration is obtained trough cell immobilization. The immobilization is achieved by restraining the cells to a confined space using a physical barrier. The physical barrier used in this invention is cell recycling trough ultrafiltration membranes. This method has several advantages, mainly in product productivity increase, and in high fermentation yield. It also presents low energy costs and advantages in operation safety and stability of the production system.

Furthermore, this system prevents many of the mass transfer problems, caused by diffusional problems, from occurring and also prevents contamination of the fermentation broth, where the final product can be found, as well as contamination of the fermenter, where the fermentation is occurring.

At the same time, this system allows operating at high dilution rates, without system collapsing, phenomenon known has wash-out. The high dilution rates at which the system operates is another very important factor that contributes to the productivity of the system. All of these factors combined make this a viable and profitable system.

For the fermentation process to be initiated, a pre-inocule must be prepared, with 10 % of the reactor's work volume. This can be prepared in smaller reactors. Moreover, the fermentation process must begin with a discontinuous phase of about 8 hours in order to obtain biomass.

After this discontinuous period, the bioreactor is ready for full functioning. A general diagram of the fermentation and purification process can be observed in the process description diagram. Probes control the fermentation conditions continuously. The information is analysed so that the conditions are stable, especially regarding temperature, pH and cell concentration. The pH is controlled by addition of concentrated NaOH (recovered from following process steps).

The purification of the Lactic acid, that exits the fermenter in the form of Sodium Lactate, due to the added NaOH, is initiated in the ultrafiltration membrane system used to maintain the high cell concentration. These ceramic membranes retain bacterial cells and other macromolecules, which are then reintroduced in the reactor. The fermentation broth containing the lactic acid is conducted to further purification.

The next purification step takes place in a nanofiltration system. This system contains nanofiltration membranes with an exclusion limit between 0.5 and 5 nanometers. This way all of the contaminants that are bigger than the lactic acid are eliminated.

The separation of the sodium lactates in lactic acid and NaOH, and the consequent concentration of the lactic acid is achieved through bipolar electrodialysis. The resulting NaOH is reused for pH control.

Electrodialysis is an electrochemical process that allows the separation, purification and concentration of ionic substances, by applying an electrical potential difference. \Ve is the use of the bipolar membrane that allows the purification and concentration to occur simultaneously. By using bipolar electrodialysis the entire separation and purification process is simplified, eliminating by-products and avoiding the use of organic solvents.

From the electrodialysis process result two fractions, one containing lactic acid and residual sodium lactate, and the other fraction, containing NaOH. The residual sodium lactate fraction can be reduced by increasing the number of bipolar membranes used.

The lactic acid purified in this process in intended for the production of polylactic acid (PLA). PLA is obtained by polymerisation (ring opening), of a cyclic dimmer of lactic acid (intermediate) without the use of organic solvents.

The lactic acid, produced, purified and concentrated in the previous steps is transported to a CSTR (continuously stirred tank reactor), where it will be dehydrated and pre-condensed. The reactor is equipped with a stirrer, a condenser and temperature control devices, important to assure that the reaction occurs for 2 hours at temperatures between 160 and 200 °C, at atmospheric pressure. The effluent water contains only residual lactic acid, meaning that it is not considered as a dangerous effluent and therefore does not require any treatment.

From the first polymerisation process lactic acid dimmers and oligomers are obtained, which are then separated, purified and concentrated by distillation in a distillation column. The effluent resulting from this process is recirculated and reintroduced in the first polymerisation reactor (CSTR 1).

The concentrated dimmers and oligomers are then transported to a second reactor (CSTR 2) where the polycondensation reactions will occur. The reaction time for these reactions is 20 hours at temperatures between 160 and 200 °C, and at reduced pressure around 0,2 - 20 mmHg, in the presence of a catalyst, iron lactate, used in a concentration of 0.005-0.5% (p/p), regarding the initial lactic acid. The polycondensation reactions should take place, maintaining the initial conditions, until the desired molecular weight is achieved, around 25000 - 30000 kDa. The condensation step can be performed in several steps, lowering the pressure gradually.

The yield of the polycondensation reaction is around 80% (p/p), and the yield in dimmers and oligomers around 20%. The polylactic acid is collected and the resulting dimmers and oligomers are transported to a fractional distillation column, where these dimmers and oligomers are purified at temperatures between 144-170 °C and a pressure between 0.5-0.8 mmHg. From this fractional distillation, purified dimmers are obtained which can be recycled and reintroduced in the polycondensation reactor (CSTR 2), and pure lactic acid residues and water, which are recycled and reintroduced in the first polymerisation reactor (CSTR 1). Since the non- condensate fractions are recycled, the overall yield is close to 100 %.


The production of organic acids and aminoacids with low production costs is a long pursued objective in several industrial applications: food industry, animal feed and biodegradable plastics, in the case of lactates.

This polymer has several advantages comparing to common petroleum derived plastics:

• Biodegradable, which means that microorganisms are able to alter the plastic properties and modify its chemical structure.

• Biocompatible, which means that these plastics are, in normal conditions, not rejected by biological cells or tissues? • Produced from a renewable resource (an industrial residue), and not from petroleum- derived products.

• 100% recyclable: Trough hydrolysis the lactic acid can be obtained and reused for a different application or it can be merged to produce another object

• No organic or toxic solvents are used in the production of these biopolymers.

• They can be incinerated emitting only CO2 (previously removed from the atmosphere) and H O.

PLA can be produced with a wide variety of properties and characteristics, because the lactic acid molecule is a chiral molecule with two asymmetry centers and therefore three possible enantiomers derived from this dimmer. This way controlling the stechiometry of the lactic acid dimmer formation, it is possible to obtain different mixtures of lactic acid containing the L and D or meso-lactate forms.

These different mixtures result in different properties such as strength, stiffness and others. PLA is often compared to PET (Polyethylene thereftalate), due to the enormous similarity between the properties of the two compounds.

These polymers are resistant to fats and are an effective barrier against odours and flavours. They have a better resistance to heat variations then the common polyolefins.

PLA can be used for the same purposes as normal polyesters. The main applications are:

• Product wrapping, for instance candy or caramels

• Natural textile fibber

• Wide array of medical applications, such has bone implants, biodegradable stitches or biodegradable capsules or vectors for pharmaceutical and chemical compounds.

• Besides the applications referred above PLA has many other different applications in the form of fibber, resin or thermoplastic. Future perspectives are very positive for PLA. The decrease in the price of production is increasing the range of applications and the level of substitution of petroleum-based plastics for biodegradable plastics such as PLA will increase significantly in the forecoming years.

The technological developments in recent years can drop the production price of PLA production to levels close to the price of common plastics, making PLA more and more competitive. Moreover, Governmental pressure, mainly in Countries in the European Union and Japan, is forcing package producers to find solutions for the environmental problem caused by the enormous accumulation of urban solid residues. All of these arguments support the use of PLA as a viable alternative to common plastics.


The diagram represents the continuous process for the production of polylactic acid from sugar molasses.

The entrance flow (1) (constituted by fresh broth previously prepared), passes through a sterilizer and then through a cooler (2) (where it is sterilized and cooled to the fermentation temperature). It then enters in the fermentation tank (3) in witch sugars are fermented to lactic acid.

The temperature inside the tank is held constant with circulating water. Into the fermentator enters a sodium hydroxide flow (4) from the electrodialysis system (5).

The exit flow (6) feeds an ultrafiltration system (7) in witch cells are separated from the fermentation broth. Cells can or not (in case of purge), re-enter the fermentator through flow (8). The fermentation broth, containing the sodium lactate flows (9) to a nanofiltration system to separate macromolecules. The permeate flow (11), containing the sodium lactate and other solutes smaller than the cut-off of the filtering membranes, enters the electrodialysis system (5) to concentration and purification of the lactic acid; The held can or not, be recirculated to dilute the entrance flow (1), through flow (10).

From the electrodialysis system (5) result three different flows: one containing NaOH (4), another the impurities (12) and the last one, lactic acid (13).

Flows (13) and (14) enter the CSTR (16) - flow 14 comes from the fractionated distillation (15). From reactor (16) exits, by evaporation, a flow (17) containing water and traces of lactic acid, and another one (18) containing the dimmer and other oligomers that are directed to a distiller (19).

From this distiller come out two flows (20 and 21) that mix with flow (14) and the polycondensation reactor (22), respectively. From this reactor (22) come out a flow (23) containing the final product (polylactic acid), and another one (24) containing dimmers and all lactic acid oligomers that can be separated by fractionated distillation (15).

Dimmers can be directly polymerised in the casting box (25) by adding a catalytic octanoate (between 180 and 195°C) and impurities are recirculated to flow (14) to a new polycondensation.


Example 1

Lactic acid fermentation is held in a 50L fermentator coupled to an ultrafiltration system with a size exclusion of 5 kDa and a total membrane area of 3.75 m2, with internal and external pressures of 4.4 e 2.9 bar, respectively.

45 L of aqueous broth (composed of whey, milk protein concentrate and additional nutrients such as inorganic salts and cystein), were heated at 70°C for 45 minutes and then cooled to 45°C. To this, 9 g of Lactobacillus helveticus and 26.5 g of Flavourzyme® were added. Fermentation in batch mode was taken for 9 hours, after witch continuous mode was started. Added fresh broth contained only whey, lactose and Flavourzyme®. pH was made constant at 5.75 by addition of ammonia gas.

Biomass density was held constant between 7 and 8% by a continuous purge. Permeate flow was continuous during all fermentation at 1 Uminute.

Dilution rate varied between 0.15 and 0.3 h"1. This rate did not alter the yield that was constant during the 34 days of fermentation. The concentration of lactate in the flow-through was about 4% and productivity, at a dilution rate of 0.3 h-1 was 12 g/l.h.

The lactic acid in the permeate was isolated using a combination of ion-exchange resins with quelating agents, followed by two consecutive electrodialysis steps. The recovery rate was about 85-90% depending on the starting sugar amount. Example 2

The aqueous lactic acid solution from purification processes is led to a 25 dm3 CSTR. This solution contains 85% in weight of L-lactic acid (17.6 kg). The reactor is equipped with a condenser, heating shirt and temperature control. Reaction lasts for 2 hours at 160-200 °C and at room pressure in order to obtain 4.38 kg of distillate.

From this first step we obtain lactic acid dimmers and oligomers, which are subsequently, separated in a distillation column, from witch exits a much more concentrated solution. This concentrated solution goes into a second reactor, in witch take place the polycondensation reaction. These reactions occur at 160-220 °C and a pressure of 0.2-20 mmHg for 20 hours, in the presence of a catalyst, iron lactate (II), in a concentration of 0.005-0.5% (w/w) relative to initial lactic acid.

Polycondensation reactions should occur, in the previously described conditions, until the polymer has the desired molecular weight (25000-30000). Condensation step can be taken in several steps, with a progressive diminution of pressure.

Polylactic acid is redraw and dimmers are redirected to a fractionated distillation column, in witch they are purified at temperatures between 144 - 170 °C, and a pressure between 0.5 - 0.8 mmHg. The purified dimmers are recirculated to the second CSTR and the water and monomers are recirculated to the first one.

17th December 2003


1. An industrial process characterised by the use of an industrial residue as a substrate, which is fermented by a pure culture of Lactobacillus delbrueckii, to obtain polylactic acid (PLA) with high levels of purity, high molecular weight and with a high transformation yield.
2. An industrial process, according to claim 1 , characterised by the use of sugar molasses as industrial residue.
3. An industrial process, according to claim 1 , characterised by the fermentation to be carried out observing the following criteria:
• With a fermentation temperature between 30.0 and 50.0°C.
• With a constant pH, with values between 6.0 and 7.0, adding recovered NaOH from a purification step of the system.
4. An industrial process, according to the previous claim, characterised by the fermentation to be carried out in conditions of cellular immobilization, through cellular retention with modules of filtration membranes, promoting a high cellular concentration and, consequently, a high production of lactic acid.
5. An industrial process, according to claim 1, characterised by the purification and concentration of the lactic acid resulting from the fermentation step, through the modules of the ultrafiltration, nanofiltration and electrodialysis membranes, of the highest technology, containing:
• An ultrafiltration module, to remove biomass and purify the solution containing lactic acid, in which the membrane cut-off lies between 1.0 and 100.0 nm.
• A nanofiltration step for the purification of the lactic acid, in which the membrane cut-off lies between 0.5 and 5.0 nm.
• An electrodialysis module with bipolar membranes to purify and concentrate the lactic acid.
6. An industrial process, according to the previous claim, characterised by obtaining high purity lactic acid (-99%).
7. An industrial process, according to claim 1 , characterised by using supplements recovered from each one of the system purification steps to complement the substrate used in fermentation.
8. An industrial process, according to claim 1, characterised by the fact that the lactic acid sterification and polymerisation to polylactic acid are carried out by a thermal treatment and distillation, which includes the following sequential steps:
• The sterification process occurs for 2 hours between 160 and 200°C and subject to atmospheric pressure.
• The separation of the lactic acid dimmers and oligomers resulting from sterification is obtained through simple distillation.
• The polymerisation process occurs for 20 hours, between 160 and 220°C and subject to a pressure between 0.2 and 20.0 mmHg, in the presence of Iron Lactate (II), with a concentration between 0.005 and 0.5% (p/p).
• The separation of the polylactic acid and of the dimmers resulting from the polymerisation, through fractional distillation, is carried out between 144 and 170°C and subjected to a pressure between 0.5 and 0.8 mmHg.
9. An industrial process, according to claim 8, characterised by not using organic solvents to obtain polylactic acid.
10. An industrial process, according to the previous claim, characterised by the high yield obtained in the transformation of lactic acid into polylactic acid (between 95 and 100%).
11. An industrial process, according to the previous claims, characterised by obtaining a high molecular weight polylactic acid (between 25000 and 3000 kDa).
12. An industrial process, according to the previous claims, characterised by preventing the loss of intermediate products during the sterification and transformation processes.
13. An industrial process, according to claim 1, characterised by obtaining a final product that is 100% biodegradable, bioreabsorbable and obtained in a biological way.
EP20030777502 2002-12-23 2003-12-19 Polylactic acid production from sugar molasses Withdrawn EP1618202A1 (en)

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US7332119B2 (en) 2003-06-13 2008-02-19 Poet Research Biopolymer structures and components
US7507561B2 (en) * 2004-05-20 2009-03-24 Reliance Life Sciences Pvt. Ltd. Process for the production of polylactic acid (PLA) from renewable feedstocks
US8702819B2 (en) 2008-09-10 2014-04-22 Poet Research, Inc. Oil composition and method of recovering the same
US9061987B2 (en) 2008-09-10 2015-06-23 Poet Research, Inc. Oil composition and method for producing the same
CN101392273B (en) 2008-11-10 2013-02-06 南京工业大学 Clean production process of lactic acid
RU2650802C1 (en) * 2008-12-26 2018-04-17 Торэй Индастриз, Инк. Lactic acid composition and its application
EP3272799A1 (en) 2016-07-19 2018-01-24 Omya International AG Use of mono-substituted succinic anhydride in polylactic acid composite filled with calcium carbonate

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JPH07173264A (en) * 1993-12-20 1995-07-11 Mitsui Toatsu Chem Inc Production of polyhydroxycarboxylic acid
JP3024907B2 (en) * 1994-07-15 2000-03-27 株式会社日本製鋼所 Method for producing a poly (lactic acid)
JP2001506504A (en) * 1996-12-23 2001-05-22 ラクタスキャン・アンパルトセルスカブ Fermentative production and isolation of lactic acid
CA2423727C (en) * 2001-01-31 2007-06-05 Toyota Jidosha Kabushiki Kaisha Process for producing lactide and process for producing polylactic acid from fermented lactic acid employed as starting material

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