WO1993002075A1 - Depolymerisation de films minces en esters cycliques dimeres - Google Patents

Depolymerisation de films minces en esters cycliques dimeres Download PDF

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Publication number
WO1993002075A1
WO1993002075A1 PCT/US1992/006003 US9206003W WO9302075A1 WO 1993002075 A1 WO1993002075 A1 WO 1993002075A1 US 9206003 W US9206003 W US 9206003W WO 9302075 A1 WO9302075 A1 WO 9302075A1
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WO
WIPO (PCT)
Prior art keywords
oligomer
evaporator
cyclic ester
film
lactic acid
Prior art date
Application number
PCT/US1992/006003
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English (en)
Inventor
Kamlesh Kumar Bhatia
Kang Lin
Robert Stephen Nash
Thomas Walter Stambaugh
Original Assignee
E.I. Du Pont De Nemours And Company
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by E.I. Du Pont De Nemours And Company filed Critical E.I. Du Pont De Nemours And Company
Priority to EP92915974A priority Critical patent/EP0641336A1/fr
Publication of WO1993002075A1 publication Critical patent/WO1993002075A1/fr

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    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07D—HETEROCYCLIC COMPOUNDS
    • C07D319/00—Heterocyclic compounds containing six-membered rings having two oxygen atoms as the only ring hetero atoms
    • C07D319/10—1,4-Dioxanes; Hydrogenated 1,4-dioxanes
    • C07D319/12—1,4-Dioxanes; Hydrogenated 1,4-dioxanes not condensed with other rings
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D1/00—Evaporating
    • B01D1/22—Evaporating by bringing a thin layer of the liquid into contact with a heated surface
    • B01D1/222—In rotating vessels; vessels with movable parts
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J19/18—Stationary reactors having moving elements inside
    • B01J19/1887—Stationary reactors having moving elements inside forming a thin film
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J6/00—Heat treatments such as Calcining; Fusing ; Pyrolysis

Definitions

  • This invention relates to a reduced pressure reactive distillation process for the preparation of dimeric cyclic esters.
  • the process of the invention comprises depolymerizing thin films of an oligomer of a hydroxycarboxylic acid to form a dimeric cyclic ester and recovering the cyclic ester.
  • the thin film process of the invention affords rapid and substantially complete conversion to a dimeric cyclic ester, low hold-up times, little or no decomposition to undesirable by-products, and high quality product in high yields.
  • Dimeric cyclic esters of hydroxycarboxylic acids such as glycolide (l,4-dioxane-2,5-dione) and lactide (l,4-dioxane-3,5-dimethyl-2,5-dione), are intermediates to high molecular weight polyhydroxycarboxylic acids which may be useful in biomedical and other applications because of their ability to be degraded biologically and hydrolytically to form physiologically and environmentally acceptable by-products.
  • a process for producing dimeric cyclic esters may be found in Aigner et al, European Patent Application Publication No.264926.
  • Aigner et al. discloses conducting a thermolysis depolymerization reaction continuously in a forced feed flow tube reactor (double screw extruder) under reduced pressure, while maintaining an increasing temperature gradient along its length.
  • the dimeric cyclic ester product distills from the reaction mass through vapor ports located at the downstream end of the reactor, while the higher-boiling residue is extruded under the force-feed extrusion conditions. It is an object of this invention to provide an improved process for converting low molecular weight oligomers or polymers of alpha- hydroxycarboxylic compositions to cyclic esters in short residence times and at high production rates.
  • This invention is based on the discovery that conversion of an oligomer of an alpha-hydroxycarboxylic acid moiety (e.g., an oligomer of lactic acid), to a cyclic ester (e.g., lactide), proceeds more rapidly than heretofore 0 believed when the reaction mass comprising the oligomer is spread as a thin liquid or molten film onto a surface which has been heated to depolymerization temperatures.
  • a cyclic ester e.g., lactide
  • Disposing the oligomer on the heated surface as a thin film preferably one having a relatively large surface area to film thickness ratio, enables (1) heat to be transferred rapidly from the heating surface to the 5 oligomer composition and, (2) reaction products (e.g., lactide) to be transferred rapidly through the oligomer film and vaporized rapidly from the oligomer surface (i.e., the reaction products are more volatile than the oligomer).
  • reaction products e.g., lactide
  • the invention is directed to an improved process for depolymerizing (the ⁇ nolyzing) a depolymerizable oligomer of an alpha- hydroxycarboxylic acid composition to a dimeric cyclic ester under thin film distillation conditions by heating to effective depolymerization and distillation 5 temperatures, whereby conversion of the oligomer to a vaporized cyclic ester is effected at short residence times.
  • the invention relates to a process for converting an oligomer of an alpha-hydroxycarboxylic acid, an alkyl ester or salt thereof, comprising (1) disposing a thin liquid film of a preformed oligomer on a heated surface in a o reaction zone, (2) maintaining the surface at a temperature sufficient to heat the film to a depolymerization temperature and convert the oligomer to dimeric cyclic ester while maintaining the reaction zone at a reduced pressure sufficiently low to form a vapor product stream containing the dimeric cyclic ester, and (3) recovering the product stream.
  • the process of the invention is particularly applicable to preparing lactide, including L-lactide, in high yield and at a high conversion rate from an oligomer of lactic acid or an ester or a nitrogen base salt thereof.
  • the vapor product stream is cooled, condensed and collected as a liquid.
  • the oligomer film is formed and depolymerized continuously, and the vaporized product is collected continuously.
  • the feed rate of the oligomer to the heated surface, the thickness of the oligomer film, the temperature and the pressure are coordinated and controlled such that the depolymerization proceeds substantially completely to form a vaporized product.
  • Minor quantities, if any, of a residue e.g., so-called heel
  • the residue can be removed periodically and recycled or hydrolyzed as hereinafter described.
  • thin film depolymerization is conducted, according to the invention, within a wiped-film evaporator.
  • the invention is a reactive distillation process comprising a series of steps which include thermolysis/depolymerization of an open-chain poly
  • Fig. 1 is a sectional view of a wiped film evaporator with an internal condenser.
  • Fig. 2 is a sectional view of the wiped film evaporator of Fig. 1 which is coupled with an external condenser.
  • Fig. 3 is a schematic block diagram of the invention.
  • the invention is directed to a process for preparing a cyclic ester having the formula:
  • an oligomer of an alpha-hydroxycarboxylic acid, an ester or a nitrogen base salt thereof is introduced as a thin molten film into a reaction surface in a reaction zone which is maintained at a reduced pressure and an elevated temperature.
  • the pressure and temperature within the reaction zone are maintained such that the oligomer is depolymerized and a thermolysis product, or products, are vaporized to form a product stream containing the cyclic ester.
  • the product stream may be recovered by any suitable method which does not adversely affect the cyclic ester.
  • the product stream may be condensed which may be followed by one or more of redistillation, extraction and/or crystallization from a solvent to recover the desired cyclic ester product.
  • the oligomeric feed material may comprise an oligomer of an oligomerizable alpha-hydroxycarboxylic acid, ester and/or a nitrogen base salt thereof, which has the formula:
  • n is an integer of 2 to 50:
  • X is independently H, R3 or a cationic group HA:
  • Ri, R2, and R3 are independently H or a C -C hydrocarbyl radical: and "A" is a nitrogen base.
  • R-j_, R2 and R3, when other than H in the above formula, is an alkyl group.
  • the cationic group HA is preferably derived from a nitrogen base, such as ammonia or an alkyl amine, and preferably is ammonia or a tertiary amine, such as
  • the degree of acceptable polymerization (i.e., the value of (n)) and the resultant molecular weight can vary widely so long as the oligomer may be rendered molten and depolymerized at the operating temperature.
  • the value of n is in the range of from about 5 to about 30 (e.g., not more than about 25) and normally between about 10 and 15.
  • the value of n tends to increase during the course of the depolymerization reaction so that any heel (i.e., polymeric residue) remaining upon completion of the reaction usually has a greater degree of polymerization than the starting oligomer.
  • the heel may be recycled to the reactor in accordance with the invention so long as the oligomer may be rendered molten and is depolymerizable.
  • the heel can be hydrolyzed to lower molecular weight alpha-hydroxy carboxylic acids, including the monomeric acid, which can be re-polymerized to oligomers of the desired degree of polymerization for reuse in the process.
  • the oligomer should generally be free of dissolved gases, solvents or other low boiling components to avoid or minimize the possibility of film deterioration resulting from bubbling and flashing of the film when subjected to a reduced operating pressure. Also, the oligomer is preferably preheated at or close to the operating temperature before it is fed to the reaction zone of the evaporator.
  • the depolymerization process is advantageously carried out in a continuous manner using a thin film evaporator.
  • the thin film evaporator may comprise a heated cylindrical or tapered tubular reactor which includes means for distributing the oligomer over the heated inner surface of the reactor.
  • the tubular reactor includes a series of ratable wiper elements that maintain a close clearance from the wall or ride upon a film of liquid on the wall.
  • the oligomer is continuously fed to and disposed onto the heated surface of the reactor wall as a thin liquid film.
  • the thin film is disposed onto the heated surface in a manner sufficient to provide a relatively large surface area and a uniform thickness.
  • the film thickness should be as thin as can be practicably attained, and may range from about 0.05 to at least about 1.0mm, and normally about 0.2 through 0.5mm thick. For best results, the thickness of the thin film will range from about 0.3 to 1mm. Apparatuses which are acceptable for creating continuous depolymerization conditions are exemplified by:
  • SUBSTITUTE SHEET A A falling film evaporator, wherein the molten/liquified oligomer flows downward along heated walls of the evaporator.
  • the quality of the film that forms depends primarily on the force of gravity, the viscosity of the oligomer and its flow rate along the heated surface.
  • a falling film evaporator of the wiped film type is employed and equipped with means for spreading the incoming oligomer horizontally and vertically on the heat surface so as to create a thin film having a substantially uniform thickness and a relatively large surface area.
  • the ratio of surface area to film thickness is not critical.
  • a greater ratio should increase the heat transfer from the heating means to a greater quantity of the liquid oligomer film, enhance the mass transfer of the depolymerization products through and out of the film thereby into the reduced pressure space above the film as vapor, and result in a greater quantity of product being formed in a given time period.
  • a desirable wiped-film evaporator for carrying out the process of the invention is equipped with rotating wiper elements that can be operated at various speeds of rotation and adjusted to provide different spacings between the heated evaporator wall and the wiper blades.
  • the wiper blade spacing determines film thickness, while wiper rotation rate and oligomer feed rate determine the rate of film formation.
  • Suitable wiper spacing e.g., for appropriate film thickness
  • speed of rotation are readily determined by trial for any particular oligomer composition, oligomer viscosity and other process conditions (e.g., temperature, pressure, etc.)
  • the vapor product stream produced on depolymerizing the oligomer to volatile products in the evaporator is preferably contacted with a condensing surface, maintained at a temperature such that the product stream condenses as a liquid, which is allowed to drain into a receiver.
  • the condensing surface may comprise an internal or an external condenser or a combination of the two which is discussed below in more detail in connection with Figs. 1 and 2.
  • the wiped film evaporator may include a heated surface which surrounds and is spaced apart from an internal condenser.
  • the wiped-film evaporator may also be connected to an external condenser which functions as a substitute for or as a supplement to the internal condenser.
  • the surface area of the condensing surface may be modified to control the manner in which the product stream is condensed.
  • the surface area of a coiled tube condenser may be increased by decreasing the diameter of the tube and increasing the number of coils.
  • the vapor product stream normally may comprise the dimeric cyclic ester and other volatiles, including open-chain hydroxycarboxylic acids (e.g., lactic acid, lactoyllactic acid, etc).
  • the condensed vapor product is readily separated into its constituents using methods such as distillation, extraction, crystallization, etc.
  • the process of this invention is generally conducted in the presence of a catalyst, which may be included in the oligomeric reactant before it is fed to the evaporator.
  • the catalyst can be any catalyst which is suitable for promoting the thermolysis of the oligomers to cyclic esters.
  • Suitable catalysts are generally metals or compounds of metals of groups IV, V and VIII of the Periodic Table. Preferred are metals of groups IV, notably Sn as the metal (powdered), oxide, halogenide or carboxylate, or V, notably Sb, usually as the oxide Sb203.
  • Sn (II) carboxylates especially those that are soluble in the molten oligomer and exemplified by stannous bis(2- ethylhexanoate), commonly referred to as stannous octoate.
  • the catalyst will be employed in catalytically-effective amounts, which can vary widely depending upon the particular feed material employed and the reaction conditions.
  • the optimum catalytically-effective amounts for any particular system can readily be determined through trial runs.
  • the quantity of catalyst will generally be such that the reaction mass contains from about 0.01 to about 5% by weight, usually from about 0.3 to 3% and for best results, at least about 1%.
  • Higher catalyst loadings are more desirable because oligomer residence time decreases with increases in the initial catalyst concentration, thereby improving the dimeric cyclic ester production rate.
  • a solvent of the cyclic ester with the oligomer before the oligomer is introduced into the evaporator.
  • a suitable solvent must be substantially inert under the depolymerization process conditions and be generally equal to and/or less volatile than the cyclic ester.
  • a solvent can improve the fluidity of the oligomer and maintain the cleanliness of the heating wall within the wiped-film evaporator.
  • a suitable solvent having a volatility generally equivalent to the cyclic ester may also serve to maintain the cleanliness of the condenser by washing cyclic ester from the condenser surface.
  • Suitably effective temperatures in the evaporator can vary widely provided the temperature is below the decomposition temperature of the dimeric cyclic ester being formed. Normally, the temperature is in the range of from about
  • the optimum temperature range for any particular oligomer- to-cyclic ester conversion will vary with the composition of the oligomer.
  • the temperature is usually in the range from about 250°C through about 270°C and, for glycolide from about 260°C through 280°C .
  • the surface of the evaporator's heating zone can be heated by any expedient means.
  • the heating zone is advantageously constructed of a thermally conductive material so that heat can be supplied from an outside source through the wall of the heating zone to its internal evaporation surface and thus heat the oligomer film to depolymerization temperatures.
  • Heat may be supplied, for example, electrically by wrapping the outside of the heating zone with heating tape or by jacketing the zone with an electrically-heated mantle.
  • the heating zone may be jacketed such that hot oil may be circulated through it and in this way bring the internal heating surface to the desired temperature.
  • thermocouples can be placed at the external surface of the evaporator's heating zone to monitor and record the depolymerization temperature.
  • the depolymerization process is carried out under subatmospheric pressures which are consistent with the vapor pressure of the cyclic ester being recovered at the operating (depolymerizing) temperature.
  • the pressure can vary from below about 1mm of Hg upwards and is normally below about 20mm of Hg. Generally, the pressure is the range of about 1 to 5mm of Hg.
  • An important aspect of the invention is that one or more of the following process conditions, such as the oligomer composition, oligomer viscosity, oligomer feed rate, speed of film formation (e.g., rotation rate of the wiper blades), film thickness, temperature, pressure and oligomer catalyst loading, can be coordinated such that substantially all the oligomer being fed is converted to a vapor product stream rapidly and substantially completely with little or no heel formation. Control of these process conditions makes feasible a short residence time continuous process affording high conversion of oligomer and high yields of the desired dimeric cyclic ester with little or no occurrence of racemization, decomposition or other undesirable side reactions, such as charring.
  • process conditions such as the oligomer composition, oligomer viscosity, oligomer feed rate, speed of film formation (e.g., rotation rate of the wiper blades), film thickness, temperature, pressure and oligomer catalyst loading
  • Residence times can be extremely short, i.e., generally are a matter of minutes, often between about 1 and 10 minutes. While it may be desirable to achieve as high a conversion/ production rate as possible by eliminating heel formation, it is generally advisable to maintain the depolymerization conditions such that a small quantity of oligomer heel can be removed from the evaporator as the reaction proceeds since the heel retains the catalyst, which might
  • SUBSTITUTE SHEET otherwise leave deposits on the evaporator walls.
  • the heel may be recycled directly to the evaporator or it may first be hydrolyzed to lower molecular weight alpha-hydroxy carboxylic acids which may be recycled along with the catalyst to form additional oligomer which is then used for producing the cyclic ester.
  • the characteristics of the heel which is formed determines the degree to which it may be recycled.
  • the practicality of recycling the heel typically is related to the degree to which it is polymerized. For example, heels which have a relatively high degree of polymerization (as shown by a high molecular weight) are more difficult to recycle due in part to the reduced quantity of hydroxyl groups on the end of the polymer chain.
  • Any heel which may be produced in the process will have had a short residence time in the wiped-film evaporator and, therefore, possess relatively low molecular weights which typically permits these heels to be directly recycled or readily transformed into a recyclable form.
  • the flow of oligomer to the heated wall of the wiped-film evaporator can vary widely depending on the oligomer, its viscosity and its temperature (viscosity decreasing with increasing temperature); also on the depolymerization temperature and configuration of the evaporator itself.
  • the flow of oligomer into the wiped film evaporator should be sufficient for the oligomer to form a film under gravitational flow onto the surface of the heated wall, but it should not be so fast as to flood the evaporator.
  • the oligomer flow rate should be coordinated with the depolymerization temperature so that a thin film is established and maintained throughout the run and depolymerization proceeds such that most, if not substantially all the oligomer, is depolymerized to the desired cyclic ester product. Further, the flow rate of the oligomer should also be coordinated with the rotation rate of the wiper blades (i.e., the wiper blades cause the oligomer to form a film along the heated surface of the wiped- film evaporator). For example, a relatively high oligomer flow rate should be accompanied with a rapid wiper blade rotation rate to ensure effective depolymerization of the oligomer without excessive charring or heel formation.
  • FIG. 1 The apparatus of Fig. 1 consists essentially of a jacketed cylindrical evaporator 1 evacuatable to reduced pressures through line 7 by a vacuum pump not shown.
  • Evaporator 1 contains internal condenser .8 spaced apart from inside wall 2 of evaporator! and a rotatable cylindrically shaped wiper blade mechanism 5 disposed between wall 2 and condenser .8.
  • Wiper blade mechanism 5 has a plurality of wiper blades 6 adapted to spread liquid oligomer evenly and uniformly over wall 2; the wiper blade mechanism 5 also has a plurality of openings 6A between the blades and along the circumference of the cylindrical shape formed by the blades, whereby wall 2 communicates with condenser .8 through the combined 6A openings.
  • the spacing between wall 2 and blades 6 can be fixed or adjusted to provide a variety of wall-to-wiper blade spacings.
  • Wiper blade mechanism 5 is rotatable at various controlled speeds by a motor drive not shown at 5 A.
  • Evaporator wall 2 is heated from an external surface to operating temperatures by circulating appropriately hot oil through the jacket, the oil entering at 3 and exiting at 4.
  • Thermocouples placed at the jacket of _1 provides a measure of the temperature at wall 2.
  • the depolymerization temperature developed at wall 2 is a function of the temperature of the heating fluid, which temperature is readily determined by trial for any particular oligomer.
  • the temperature of condenser 8 is controllable by circulating coolant through it via entering and leaving lines 9 and 10.
  • Evaporator! is adapted to receive molten oligomer from jacketed feed vessel JL6.
  • the oligomer, fed to 16 through line 15, is maintained molten by circulating sufficiently hot oil through the jacket, the oil entering at 17 and exiting at 17A.
  • the temperature of the molten oligomer should be below but reasonably close to the depolymerization temperature.
  • Valve 18A controls the feed rate of the molten oligomer to evaporator 1. Normally, valve 18A is adjusted such that about 500cc of oligomer will pass into the jacketed cylinderical evaporator in from about 45 minutes through about 2 hours.
  • Deflector plate .19 is positioned to direct molten oligomer fed via line 18 to wall 2 of the evaporator so that it can flow under gravity down the wall and can be spread by wiper blades 6 vertically and horizontally to a substantially uniform thickness over the entire inside wall of the evaporator.
  • Depolymerization products vaporized from the oligomer heated to depolymerization temperatures at wall 2 pass through openings 6A, condense at least in part on condenser 8 and are collected as condensate H, via line 12, in receiver 12A.
  • Molten material not converted to vapor collects as heel 13, via line 14, in receiver 14A.
  • Condensate 11 can be further processed by any means known to the art for recovering and further refining the cyclic ester product, if desired. Similarly, the recovered “heel” may be recycled to the reactor for conversion to additional quantities of cyclic ester. If its degree of polymerization is higher than desired, it may be further processed to convert it to an oligomer having a more optimum degree of polymerization.
  • Fig.2 incorporates the features of Fig. 1 and includes as well external condenser 20 communicating with evaporator 1 through insulated line 7 (insulation not shown).
  • Condenser 20 is cooled by a coolant (e.g., ethylene glycol, water, mixtures thereof, etc.) circulating through it via lines 21 and 22, and is so sized and placed as to condense substantially all vaporized product not condensed by condenser 8, condensate 23 passing through line 24 to receiver 24A.
  • Uncondensed product vapor, if any, leaving condenser 20 through line 7A passes through cold trap 26 maintained at a low temperature, for example that provided by a solid CO2 - alcohol mixture 27.
  • Sensor 28 measures the reduced pressure established by the vacuum pump.
  • the distance between the wall at which the oligomer is depolymerized and the condensing surface can vary widely.
  • the distance between heating surface and condensing surface is not critical provided the pressure is sufficiently low and the depolymerization temperature is sufficiently high to ensure an adequate cyclic ester production rate.
  • Fig. 3 is a schematic block diagram of the operation for producing the cyclic ester, concentrated aqueous lactic acid, preferably containing about 80-90% by weight lactic acid (e.g., 88% acid as is available commercially), is fed through line 31 to converter 32 where it is further
  • SUBSTITUTE SHEET concentrated by distillation and polymerized to polylactic acid (PLA) with further removal of water-of-reaction by heating gradually to about 160°C, then to 175°C usually under reduced pressure or with a N2 sweep.
  • the aqueous distillate removed during this concentration and polymerization stage is passed through 33 to concentrator 34, where it is dehydrated to concentrated lactic acid for recycle.
  • Polylactic acid produced in 32 is sent through .36 to a thin film evaporator 37, such as illustrated in Figs. 2 and 3, where it is converted to the corresponding dimeric cyclic ester(e.g., lactide), as described above.
  • the condensed product produced in evaporator 37 containing lactide, minor proportions of lactic acid and still minor proportions of volatilized water-soluble oligomers generally having 2 to 3 lactic acid units, can be further processed/purified by solvent treatments.
  • the condensed product exits the thin film evaporator through 38 and enters an extractor 3_9, where it is extracted with a suitable solvent, for example acetone, to form a solution of lactide and its lactic acid value impurities.
  • a suitable solvent for example acetone
  • the solution is concentrated to start precipitation of lactide, and diluted with water, preferably water cooled to 0-5°C, in an amount sufficient to precipitate the lactide substantially completely, leaving the lactic acid values in the aqueous solution.
  • Lactide, substantially free of its impurities is separated, as by filtration or centrifugation, removed through line 41 and purified further if desired, by washing, drying and recrystallization from non-reactive solvents (e.g., toluene).
  • non-reactive solvents e.g., toluene
  • the organic solution produced in .39 is thoroughly extracted with water in an amount sufficient to remove substantially all the lactic acid values from the solution, and the resulting aqueous phase separated from the organic.
  • the lactide-containing organic phase is removed via line 40 and lactide recovered from the solution by any means known to the art (e.g., solvent evaporation), crystallization and recrystallization, as necessary or desired.
  • the aqueous solution containing substantially all the lactic acid values and residual organic solvent is sent through line 41 to concentrator ⁇ where any organic solvent present is stripped therefrom, and the aqueous solution concentrated for recycle (e.g., to 88% lactic acid), the organic solvent and excess water being removed via line 43, the recycle stream through 47.
  • the polylactic acid residue remaining in the thin-film evaporator 37 is removed through 44. If necessary or desired, the residue (or heel) can be hydrolyzed back to monomeric (e.g., lactic acid), by passing it to hydrolyzer 45 where it is heated
  • the hydrolysate is filtered and concentrated, if necessary, to, for example, 88% lactic acid for recycle.
  • the proportion of water employed for hydrolysis will be sufficient to provide an hydrolysate having the desired lactic acid concentration.
  • dilute aqueous lactic acid for hydrolysis Lactic acid hydrolysate for recycle leaves hydrolyzer 45 through 47, is combined with the lactic acid recycle stream 48 (from 43) and .35 (from 34) to form combined stream 49, which is recycled to line 31, then to converter 2 along with make up concentrated lactic acid.
  • the overall operation representing a single illustrative recycle stage, can be repeated to achieve a lined-out recycle process wherein the amount of recycle material will equal the amount of lactic acid material generated in each pass.
  • Recycle of recovered lactic acid enables the quantity of fresh lactic acid feed to the converter to be reduced and the overall yield of lactide thereby increased.
  • Model KDL-4 wiped film evaporator was used in each of the following examples.
  • the evaporator included a vertically arranged cylindrical housing which possessed about 0.043 square meters of evaporator surface.
  • the evaporator was modified to include an external condenser downstream from its internal condenser which is illustrated in Figure 2.
  • the evaporator was jacketed for heating its evaporator surface with circulating hot oil and was also equipped with (a) a jacketed feed funnel, also heatable with circulating hot oil, (b) a feed means for metering molten oligomer into the evaporator at controlled rates, the feed being provided at the top and allowed to flow down the interior cylindrical wall of the evaporator, (c) glass- reinforced Teflon® polytetra-fluoroethylene rollers serving as rotating wiper blades for mechanically spreading the oligomer as a thin film both horizontally and vertically over the heated wall.
  • the wiper blades were rotated by a Janke- Kunkel model no. RW20 drive mechanism which had a setting of 2.5.
  • the wiper blade spacing was set to provide a film thickness of about 0.5mm.
  • SUBSTITUTE SHEET included means for evacuating and maintaining the evaporator under reduced pressure.
  • EXAMPLE 1 A An oligomer of lactic acid was prepared by gradually heating a mixture of about 1650 grams 88% L-lactic acid containing less than about 1% D- lactic acid and about 18.5 grams stannous octoate up to a temperature of about 180°C while a stream of N2 gas was passed through the mass to facilitate removal of water. The process was continued until the oligomeric produced show an average chain length of 10, determined by titration in methanol with methanolic sodium methoxide using phenolphthalein as the indicator. The resultant oligomer contained about 0.69% by weight of the stannous octoate catalyst.
  • the wiper roller of the wiped film evaporator was set at agitation setting of about 2.5; about 260°C oil was circulated through the evaporator jacket and about 150°C oil through the feed funnel jacket. Hot water was circulated through the condensers to a temperature of about 90°C and the evaporator was evacuated and maintained at about 1 mm of Hg pressure.
  • Preheated (150°C) molten oligomer was fed to the evaporator at a rate of about 273 grams/hour. Distillate from the evaporator surface was collected as drainage from the condensers at the rate of abut 234.5 grams/hour. A heel was drained from the heated evaporator wall, was collected at the rate of about 35.5 grams/hour. The wiped-film evaporator was operated for about 85 minutes. The residence time in the reactor was about 6.0 minutes.
  • the ratio of the distillate collection rate to the oligomer feed rate was about 85.9% [(234.5/273) X 100].
  • the ratio of the sum of the distillate and heel collection rates to the feed rate was 98.9% [(270/273) X 100] which indicated substantially complete recovery of the thermolysis products (distillate).
  • the distillate contained about 69.5% L-lactide, 6.5% meso-lactide and 0.04%, D-lactide, which was determined by high pressure liquid chromatography.
  • the remainder of the distillate consisted essentially of lactic acid and volatilized water-soluble lactic acid oligomers amounting to about 1130 milliequivalents of acidity per kilogram of distillate.
  • the above lactide content on a 100% basis corresponds to about 91.2% L-lactide, 8.3% meso-lactide and 0.5% D-lactide.
  • Example 1 The procedure of Example 1 was repeated except that (a) the lactic acid was oligomerized to an average chain length of 18 and the oligomer contained about 0.59% by weight of the stannous octoate, (b) the oligomer feed rate was about 255 g/hr, (c) the distillate recovery rate was about 244 g/hr and (d) the heel recovery rate was nil. Thus, the ratio of distillate rate to feed rate was about 95.7%.
  • the distillate contained abut 77.6% L-lactide, 6.1% meso-lactide and 0.2% D-lactide.
  • the remaining 16.1% of distillate consisted of lactic acid and volatilized lactic acid oligomers corresponding to abut 650 milliequivalents of acidity /kg of distillate.
  • the lactide content correspond to about 92.5% L-, 7.3% meso and 0.24% D-lactide.
  • Example 1 was repeated except that (a) the oligomer contained 2.9% by weight of stannous octoate, (b) 170°C oil was circulated through the feed funnel jacket and 270°C oil through the evaporator jacket, (c) the feed rate of oligomer to the evaporator was 941 grams/hour.
  • Distillate was collected at the rate of 731 grams/hour, and unconverted material (heel) at 197 grams/hour.
  • the duration of the run was 0.6 hours.
  • the residence time in the reactor was about 4 minutes.
  • the ratio of the distillate collection rate to the oligomer feed rate was 77.7% [731/941 X 100]; the ratio of the sum of the distillate and heel collection rates to the feed rate was 98.6% [928/941 X 100],
  • the distillate was found to contain 64.4% L-lactide, 5.92% mesolactide and 0.62% D-lactide, by HPLC, and 1334 me/kg of acidity.
  • the lactide content on a 100% basis corresponded to 90.8% L-, 8.3% meso- and 0.8% D-lactide.
  • SUBSTITUTE SHEET evaporator section equipped with a variable speed drive film wiper mechanism and coupled to an external condenser.
  • a lactic acid oligomer was prepared by gradually heating 2000 grams of 88% L-lactic acid and 20 grams of stannous octoate to 180°C and holding at that temperature for 1 hour. The pressure was reduced and heating at 180°C was continued to remove water until the resulting oligomer showed an average chain length of 11.8.
  • the evaporator was evacuated and heated by circulating 245°C oil through its jacket. 1344 grams of the oligomer was fed to the evaporator at the rate of about 1209 grams/hour over a period of about 50 minutes. During this time, the pressure in the evaporator ranged between 2.5 and 10mm of Hg. 197 grams of distillate was condensed by the external condenser; 1156 grams of heel remained in the still.
  • the distillate contained 52.1% L-lactide, 3.64% meso- lactide, 0.93% D-lactide and 2700 me/kg of acidity. On a 100% basis, the lactide portion contained 91.9% L-, 6.4% meso- and 1.64% D-lactide.

Abstract

Procédé et dispositif servant à dépolymériser un film mince, de façon à constituer un ester cyclique dimère. Le procédé et le dispositif permettent d'obtenir une conversion rapide et pratiquement complète en un ester cyclique dimère, une quantité peu importante ou une absence de sous-produits de décomposition, ainsi que des rendements élevés d'un produit de qualité.
PCT/US1992/006003 1991-07-24 1992-07-23 Depolymerisation de films minces en esters cycliques dimeres WO1993002075A1 (fr)

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EP92915974A EP0641336A1 (fr) 1991-07-24 1992-07-23 Depolymerisation de films minces en esters cycliques dimeres

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US73497791A 1991-07-24 1991-07-24
US734,977 1991-07-24

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JP (1) JP3255413B2 (fr)
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CA (1) CA2113799A1 (fr)
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WO (1) WO1993002075A1 (fr)

Cited By (16)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US5359026A (en) * 1993-07-30 1994-10-25 Cargill, Incorporated Poly(lactide) copolymer and process for manufacture thereof
WO1995009879A1 (fr) * 1993-10-07 1995-04-13 Cargill, Incorporated Procede pour la production continue de lactide et de polymeres de lactide
US5475080A (en) * 1992-10-02 1995-12-12 Cargill, Incorporated Paper having a melt-stable lactide polymer coating and process for manufacture thereof
BE1008099A3 (fr) * 1994-03-04 1996-01-16 Brussels Biotech Sa Production semi-continue de polylactides par ouverture de cycle lactides obtenus a partir de derives d'acide lactique.
EP0789023A2 (fr) * 1996-02-09 1997-08-13 Kureha Kagaku Kogyo Kabushiki Kaisha Procédé pour la préparation et la purification d'esters cycliques dimeriques d'acides alpha-hydroxycarboxyliques
US5665474A (en) * 1992-10-02 1997-09-09 Cargill, Incorporated Paper having a melt-stable lactide polymer coating and process for manufacture thereof
US5686630A (en) * 1993-09-29 1997-11-11 Chronopol, Inc. Purifying cyclic esters by aqueous solvent extraction
US6005068A (en) * 1992-10-02 1999-12-21 Cargill Incorporated Melt-stable amorphous lactide polymer film and process for manufacture thereof
US6277951B1 (en) 1992-01-24 2001-08-21 Cargill, Incorporated Continuous process for manufacture of lactide polymers with controlled optical purity
US6313319B1 (en) 1998-09-25 2001-11-06 Shimadzu Corporation Method for purifying lactide and lactide for food additives
WO2005009985A1 (fr) * 2003-07-24 2005-02-03 Shell Internationale Research Maatschappij B.V. Production de carbonate de trimethylene a partir de carbonate de poly(trimethylene) par l'evaporation reactive par essuyage de films
WO2005030358A1 (fr) * 2003-10-02 2005-04-07 Vtu-Engineering Planungs- Und Beratungsgesellschaft M.B.H. Vaporisateur a couche mince
EP1873185A1 (fr) * 2006-06-30 2008-01-02 Hitachi Plant Technologies, Ltd. Procédé et appareil pour produire de l'acide polyhydroxy carboxylique
CN105536653A (zh) * 2015-12-22 2016-05-04 江苏瑞安特重型机械有限公司 一种处理高粘物料的熔融混合器
CN111013520A (zh) * 2019-12-23 2020-04-17 高立文 一种固体乳酸的制备工艺
EP2559725B1 (fr) * 2011-08-19 2024-05-08 Uhde Inventa-Fischer GmbH Procédé et dispositif de récupération de lactide à partir de polylactide ou de polylactile

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JP4696824B2 (ja) * 2005-10-07 2011-06-08 株式会社日立プラントテクノロジー ポリエステルの製造方法及びポリエステルの製造装置
AU2007327594B2 (en) * 2006-11-28 2013-08-22 Purac Biochem Bv Stable lactide particles
JP4650427B2 (ja) * 2007-01-04 2011-03-16 株式会社日立プラントテクノロジー 遠心薄膜蒸発装置及びその運転方法
JP5229268B2 (ja) * 2010-05-10 2013-07-03 株式会社日立プラントテクノロジー ポリ乳酸の合成装置及び方法

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US5023349A (en) * 1990-05-08 1991-06-11 E. I. Du Pont De Nemours And Company Continuous process for rapid conversion of oligomers to cyclic esters

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US5023349A (en) * 1990-05-08 1991-06-11 E. I. Du Pont De Nemours And Company Continuous process for rapid conversion of oligomers to cyclic esters

Cited By (37)

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Publication number Priority date Publication date Assignee Title
US6326458B1 (en) 1992-01-24 2001-12-04 Cargill, Inc. Continuous process for the manufacture of lactide and lactide polymers
US6277951B1 (en) 1992-01-24 2001-08-21 Cargill, Incorporated Continuous process for manufacture of lactide polymers with controlled optical purity
US5856523A (en) * 1992-03-19 1999-01-05 Chronopol, Inc. Purifying cyclic esters by aqueous solvent extraction and further purification
US6005068A (en) * 1992-10-02 1999-12-21 Cargill Incorporated Melt-stable amorphous lactide polymer film and process for manufacture thereof
US5475080A (en) * 1992-10-02 1995-12-12 Cargill, Incorporated Paper having a melt-stable lactide polymer coating and process for manufacture thereof
US5536807A (en) * 1992-10-02 1996-07-16 Cargill, Incorporated Melt-stable semi-crystalline lactide polymer film and process for manufacture thereof
US5585191A (en) * 1992-10-02 1996-12-17 Cargill, Incorporated Melt-stable amorphous lactide polymer film and process for manufacture thereof
US6207792B1 (en) 1992-10-02 2001-03-27 Cargill, Incorporated Melt-stable amorphous lactide polymer film and process for manufacture thereof
US5852166A (en) * 1992-10-02 1998-12-22 Cargill, Incorporated Paper having a melt-stable lactide polymer coating and process for manufacture thereof
US5665474A (en) * 1992-10-02 1997-09-09 Cargill, Incorporated Paper having a melt-stable lactide polymer coating and process for manufacture thereof
US5484881A (en) * 1992-10-02 1996-01-16 Cargill, Inc. Melt-stable amorphous lactide polymer film and process for manufacturing thereof
US5798436A (en) * 1992-10-02 1998-08-25 Cargill, Incorporated Melt-stable amorphous lactide polymer film and process for manufacture thereof
US6291597B1 (en) 1993-07-30 2001-09-18 Cargill, Incorporated Viscosity-modified lactide polymer composition and process for manufacture thereof
US5359026A (en) * 1993-07-30 1994-10-25 Cargill, Incorporated Poly(lactide) copolymer and process for manufacture thereof
US5798435A (en) * 1993-07-30 1998-08-25 Cargill, Incorporated Viscosity-modified lactide polymer composition and process for manufacture thereof
US5594095A (en) * 1993-07-30 1997-01-14 Cargill, Incorporated Viscosity-modified lactide polymer composition and process for manufacture thereof
US5998552A (en) * 1993-07-30 1999-12-07 Cargill, Incorporated Viscosity-modified lactide polymer composition and process for manufacture thereof
US5686630A (en) * 1993-09-29 1997-11-11 Chronopol, Inc. Purifying cyclic esters by aqueous solvent extraction
EP1247808A3 (fr) * 1993-10-07 2003-03-19 Cargill, Incorporated Procédé continu pour la préparation de lactide et polylactide
EP1247808A2 (fr) * 1993-10-07 2002-10-09 Cargill, Incorporated Procédé continu pour la préparation de lactide et polylactide
WO1995009879A1 (fr) * 1993-10-07 1995-04-13 Cargill, Incorporated Procede pour la production continue de lactide et de polymeres de lactide
BE1008099A3 (fr) * 1994-03-04 1996-01-16 Brussels Biotech Sa Production semi-continue de polylactides par ouverture de cycle lactides obtenus a partir de derives d'acide lactique.
EP0789023A3 (fr) * 1996-02-09 1997-09-10 Kureha Chemical Ind Co Ltd
US5830991A (en) * 1996-02-09 1998-11-03 Kureha Kagaku Kagyo Kk Preparation process and purification process of dimeric cyclic ester of hydroxycarboxylic acid
EP0789023A2 (fr) * 1996-02-09 1997-08-13 Kureha Kagaku Kogyo Kabushiki Kaisha Procédé pour la préparation et la purification d'esters cycliques dimeriques d'acides alpha-hydroxycarboxyliques
US6313319B1 (en) 1998-09-25 2001-11-06 Shimadzu Corporation Method for purifying lactide and lactide for food additives
WO2005009985A1 (fr) * 2003-07-24 2005-02-03 Shell Internationale Research Maatschappij B.V. Production de carbonate de trimethylene a partir de carbonate de poly(trimethylene) par l'evaporation reactive par essuyage de films
US7591930B2 (en) 2003-10-02 2009-09-22 Vtu Holding Gmbh Thin-film evaporator
WO2005030358A1 (fr) * 2003-10-02 2005-04-07 Vtu-Engineering Planungs- Und Beratungsgesellschaft M.B.H. Vaporisateur a couche mince
AU2004275429B2 (en) * 2003-10-02 2009-12-24 Wolfgang Glasl Thin-film evaporator
EP2147708A1 (fr) * 2003-10-02 2010-01-27 VTU Holding GmbH Evaporateur à couche mince
EP1873185A1 (fr) * 2006-06-30 2008-01-02 Hitachi Plant Technologies, Ltd. Procédé et appareil pour produire de l'acide polyhydroxy carboxylique
US7723540B2 (en) 2006-06-30 2010-05-25 Hitachi Plant Technologies, Ltd. Method and apparatus for producing polyhydroxy carboxylic acid
EP2559725B1 (fr) * 2011-08-19 2024-05-08 Uhde Inventa-Fischer GmbH Procédé et dispositif de récupération de lactide à partir de polylactide ou de polylactile
CN105536653A (zh) * 2015-12-22 2016-05-04 江苏瑞安特重型机械有限公司 一种处理高粘物料的熔融混合器
CN111013520A (zh) * 2019-12-23 2020-04-17 高立文 一种固体乳酸的制备工艺
CN111013520B (zh) * 2019-12-23 2022-04-05 重庆市天友乳业股份有限公司 一种固体乳酸的制备工艺

Also Published As

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JP3255413B2 (ja) 2002-02-12
CA2113799A1 (fr) 1993-02-04
JPH07500091A (ja) 1995-01-05
AU2374092A (en) 1993-02-23
EP0641336A1 (fr) 1995-03-08
TW211577B (fr) 1993-08-21

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