CN112851629A - Micro-interface reaction system and method for preparing lactide from lactic acid - Google Patents
Micro-interface reaction system and method for preparing lactide from lactic acid Download PDFInfo
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Abstract
A micro-interfacial reaction system for lactic acid to lactide, comprising: the device comprises a lactic acid raw material tank, an oligomerization rectification reactor and a lactide rectification reactor, wherein the lactic acid raw material tank is connected with the oligomerization rectification reactor; a first reboiler is arranged at the bottom of the oligomerization rectification reactor, and an external micro-interface unit is arranged in the oligomerization rectification reactor; a second reboiler is arranged at the bottom of the lactide rectification reactor, and the second reboiler gasifies materials discharged from the bottom of the lactide rectification reactor and then introduces the gasified materials into a first micro-interface generator inside the lactide rectification reactor; and a second micro-interface generator is also arranged below the first micro-interface generator. The reaction system of the invention can reduce the temperature during the reaction and improve the reaction efficiency.
Description
Technical Field
The invention relates to the field of lactide preparation, in particular to a micro-interface reaction system and a micro-interface reaction method for preparing lactide from lactic acid.
Background
The production and exploitation of lactide has gained increasing attention in recent years, mainly because the ring-opening polymerization of lactide is an efficient method for preparing high molecular weight polylactic acid. Polylactic acid is a biodegradable material with a great development prospect, and is an excellent medical high polymer material because the final products decomposed in the natural environment are carbon dioxide and water, so that the polylactic acid is nontoxic and harmless to the environment, and has the advantages of good biocompatibility and biodegradability, excellent mechanical property, easiness in processing and forming and the like. The ring-opening polymerization reaction of lactide is an effective method for preparing high-molecular-weight polylactic acid, and the molecular weight of the polylactic acid of a polymerization product can reach millions.
The existing lactide generation process comprises the following steps:
(1) oligomerization reaction: the lactic acid is subjected to multistage esterification reaction under certain temperature and pressure conditions, and is dehydrated and polycondensed into oligomer;
(2) and (3) synthesis reaction: under certain temperature and pressure conditions, the oligomer is thermally decomposed and broken to form lactide.
Wherein, the oligomerization reaction process of the first step is lactic acid intermolecular dehydration, and because the oligomerization reaction is a reversible reaction, the existence of water can dilute reaction materials and influence the reaction rate, thereby influencing the normal operation of the reaction process. The lactide synthesis reaction separation system in the second step has low efficiency, and the generated lactide can not be taken out in time to enable the esterification reaction to reach a balanced state due to large system viscosity and small separation interface, so that oligomer is carried out towards the polymerization reaction direction, and the yield of the lactide product is reduced. The retention time in the reaction process is long, so that more byproducts are generated, and the quality of the product is indirectly influenced. The reaction temperature is higher, and the production cost is increased.
In view of the above, the present invention is particularly proposed.
Disclosure of Invention
The first purpose of the present invention is to provide a micro-interface reaction system for preparing lactide from lactic acid, which is based on a micro-interface reaction enhancement technology, wherein the micro-interface is used to break vaporized materials and inert gas into micron-sized bubbles, and the micron-sized bubbles are dispersed in a solution to form a micro-interface system, such that a reaction temperature can be reduced, and a reaction efficiency can be improved.
The second purpose of the invention is to provide a reaction method for preparing lactide by lactic acid by adopting the reaction system, the lactide product obtained by the reaction has good quality and high yield, and the conversion rate of raw materials is also improved to a certain extent.
In order to achieve the above purpose of the present invention, the following technical solutions are adopted:
the invention provides a micro-interface reaction system for preparing lactide from lactic acid, which is characterized by comprising the following components in parts by weight: the device comprises a lactic acid raw material tank, an oligomerization rectification reactor and a lactide rectification reactor, wherein the lactic acid raw material tank is connected with the oligomerization rectification reactor;
a first reboiler is arranged at the bottom of the oligomerization rectification reactor, one part of the material discharged from the bottom of the oligomerization rectification reactor is sent to the first reboiler for gasification and return, the other part of the material is sent to the lactide rectification reactor, an external micro-interface unit is arranged in the oligomerization rectification reactor, the external micro-interface unit is connected with the first reboiler, and the material gasified by the first reboiler is crushed and dispersed;
a second reboiler is arranged at the bottom of the lactide rectification reactor, the second reboiler gasifies materials coming out of the bottom of the lactide rectification reactor and then leads the gasified materials into a first micro-interface generator in the lactide rectification reactor, and the gasified materials of the second reboiler are subjected to splitting and dispersion; and a second micro-interface generator is also arranged below the first micro-interface generator, the second micro-interface generator is connected with an inert gas inlet pipeline for dispersing and crushing the incoming inert gas, and the second micro-interface generator is connected with a gas ejector.
In the prior art, the efficiency of a lactide synthesis reaction separation system is low, and due to the fact that the system viscosity is large and the separation interface is small, the generated lactide cannot be taken out in time to enable the esterification reaction to reach a balanced state, so that oligomers are carried out towards the polymerization reaction direction, and the yield of lactide products is reduced. The retention time in the reaction process is long, so that more byproducts are generated, and the quality of the product is indirectly influenced. The reaction temperature is higher, and the production cost is increased.
In order to solve the technical problems, the bottom of the oligomerization rectification reactor is provided with a reboiler, a first gas-liquid separator is connected behind the reboiler and is used for carrying out gas-liquid separation on materials discharged from the reboiler, and the vaporized materials are sent to an external micro-interface unit, so that the vaporized materials are dispersed and crushed in advance before entering the oligomerization rectification reactor and are mixed with lactic acid in the oligomerization rectification reactor, the fusion degree of a gas phase and a liquid phase is improved, and the conversion rate of raw materials is correspondingly improved.
The first micro-interface generator and the second micro-interface generator are arranged in the lactide rectification reactor, the vaporized materials are broken and dispersed by the first micro-interface generator, and the fusion degree of a gas phase and a liquid phase is improved. The second micro-interface generator disperses and crushes the inert gas entering from the inert gas pipeline, micro-bubbles of the crushed and dispersed inert gas are mixed in the lactide rectification reactor, the phase interface area between gas and liquid is increased, the viscosity of oligomer in the lactide rectification reactor is reduced, the temperature during reaction is reduced, the lactide gas at the top is brought into the first rectification tower, the retention time of the lactide in the lactide rectification reactor is reduced, and therefore the generated lactide can be taken out in time to enable the esterification reaction to reach a balanced state, and the product quality is improved.
Preferably, the external micro-interface unit is composed of a plurality of external micro-interface generators. The middle of the external micro-interface generator is provided with a communicating pipeline, the vaporized material is broken into micro-bubbles in the external micro-interface generator, the micro-bubbles of the vaporized material are mixed with the lactic acid solution in the oligomerization rectification reactor, the degree of fusion of gas phase and liquid phase is improved, and the conversion rate of the raw materials is correspondingly improved.
Preferably, the first reboiler is connected with a first gas-liquid separator for performing gas-liquid separation on the material coming out of the first reboiler, and the gas-phase material coming out of the top of the first gas-liquid separator is introduced into an external micro-interface generator at the bottom of the external micro-interface unit. The first gas-liquid separator is arranged behind the first reboiler, because the external micro-interface unit is mainly used for dispersing and crushing gas, the first gas-liquid separator separates vaporized materials from liquid materials, the vaporized materials enter the external micro-interface unit, the vaporized materials are dispersed and crushed into micro-bubbles, and the micro-bubbles return to the oligomerization rectification reactor along with the solution.
Preferably, the second reboiler is connected with a second gas-liquid separator for performing gas-liquid separation on the material discharged from the second reboiler, the gas-phase material discharged from the top of the second gas-liquid separator is introduced into the first micro-interface generator for dispersion and crushing, and the liquid-phase material discharged from the bottom of the second gas-liquid separator is directly discharged.
Preferably, the second micro-interface generator is arranged at the bottom of the lactide rectification reactor, and the injection direction of the gas injector faces the bottom of the lactide rectification reactor and is used for dispersing the incompletely reacted oligomers at the bottom of the lactide rectification reactor by injecting the broken inert gas. Because the density of the inert gas is small, the second micro-interface generator is arranged at the bottom of the lactide rectification reactor, the inert gas rises upwards from the bottom and is mixed into the solution in the rising process, the phase boundary mass transfer area is increased, the product quality is improved, and the reaction temperature is reduced; the injection direction of the gas injector faces the bottom of the lactide rectification reactor, so that lactic acid which is not completely reacted but is deposited at the bottom of the lactide rectification reactor can be impacted, oligomers which are completely reacted are flushed to the middle of the lactide rectification reactor again to continue the reaction, and the problem caused by the accumulation of impurities in the lactide rectification reactor can be prevented.
It will be appreciated by those skilled in the art that the micro-interface generator used in the present invention is described in the prior patents of the present inventor, such as the patents of application numbers CN201610641119.6, CN201610641251.7, CN201710766435.0, CN106187660, CN105903425A, CN109437390A, CN205833127U and CN 207581700U. The detailed structure and operation principle of the micro bubble generator (i.e. micro interface generator) is described in detail in the prior patent CN201610641119.6, which describes that "the micro bubble generator comprises a body and a secondary crushing member, wherein the body is provided with a cavity, the body is provided with an inlet communicated with the cavity, the opposite first end and second end of the cavity are both open, and the cross-sectional area of the cavity decreases from the middle of the cavity to the first end and second end of the cavity; the secondary crushing member is disposed at least one of the first end and the second end of the cavity, a portion of the secondary crushing member is disposed within the cavity, and an annular passage is formed between the secondary crushing member and the through holes open at both ends of the cavity. The micron bubble generator also comprises an air inlet pipe and a liquid inlet pipe. "the specific working principle of the structure disclosed in the application document is as follows: liquid enters the micro-bubble generator tangentially through the liquid inlet pipe, and gas is rotated at a super high speed and cut to break gas bubbles into micro-bubbles at a micron level, so that the mass transfer area between a liquid phase and a gas phase is increased, and the micro-bubble generator in the patent belongs to a pneumatic micro-interface generator.
In addition, the first patent 201610641251.7 describes that the primary bubble breaker has a circulation liquid inlet, a circulation gas inlet and a gas-liquid mixture outlet, and the secondary bubble breaker communicates the feed inlet with the gas-liquid mixture outlet, which indicates that the bubble breakers all need to be mixed with gas and liquid, and in addition, as can be seen from the following drawings, the primary bubble breaker mainly uses the circulation liquid as power, so that the primary bubble breaker belongs to a hydraulic micro-interface generator, and the secondary bubble breaker simultaneously introduces the gas-liquid mixture into an elliptical rotating ball for rotation, thereby realizing bubble breaking in the rotating process, so that the secondary bubble breaker actually belongs to a gas-liquid linkage micro-interface generator. In fact, the micro-interface generator is a specific form of the micro-interface generator, whether it is a hydraulic micro-interface generator or a gas-liquid linkage micro-interface generator, however, the micro-interface generator adopted in the present invention is not limited to the above forms, and the specific structure of the bubble breaker described in the prior patent is only one of the forms that the micro-interface generator of the present invention can adopt.
Furthermore, the prior patent 201710766435.0 states that the principle of the bubble breaker is that high-speed jet flows are used to achieve mutual collision of gases, and also states that the bubble breaker can be used in a micro-interface strengthening reactor to verify the correlation between the bubble breaker and the micro-interface generator; moreover, in the prior patent CN106187660, there is a related description on the specific structure of the bubble breaker, see paragraphs [0031] to [0041] in the specification, and the accompanying drawings, which illustrate the specific working principle of the bubble breaker S-2 in detail, the top of the bubble breaker is a liquid phase inlet, and the side of the bubble breaker is a gas phase inlet, and the liquid phase coming from the top provides the entrainment power, so as to achieve the effect of breaking into ultra-fine bubbles, and in the accompanying drawings, the bubble breaker is also seen to be of a tapered structure, and the diameter of the upper part is larger than that of the lower part, and also for better providing the entrainment power for the liquid phase.
Since the micro-interface generator was just developed in the early stage of the prior patent application, the micro-interface generator was named as a micro-bubble generator (CN201610641119.6), a bubble breaker (201710766435.0) and the like in the early stage, and is named as a micro-interface generator in the later stage along with the continuous technical improvement, and the micro-interface generator in the present invention is equivalent to the micro-bubble generator, the bubble breaker and the like in the prior art, and has different names. In summary, the micro-interface generator of the present invention belongs to the prior art.
Preferably, the gas injector comprises a nozzle and a mixing chamber, the inert gas enters the mixing chamber to extrude the reaction material in the mixing chamber, and the reaction material is sprayed out from the nozzle.
Preferably, a first condenser is arranged at the top of the oligomerization rectification reactor, a part of vaporized water is condensed by the first condenser and returned to the oligomerization rectification reactor, the other part of the vaporized water is discharged, a second condenser is arranged at the top of the lactide rectification reactor, and the vaporized water, the lactic acid and the lactide are condensed by the second condenser and returned to the lactide rectification reactor.
Preferably, the lactide rectification reactor is connected with a first rectification tower for primarily rectifying lactide, the first rectification tower is connected with a second rectification tower for further rectifying lactide, and the second rectification tower is connected with a lactide storage tank.
In addition, the invention also provides a reaction method for preparing lactide by lactic acid, which comprises the following steps:
carrying out oligomerization reaction on lactic acid, continuously gasifying, dispersing and crushing products in the reaction process, and rectifying;
and carrying out condensation reaction on the oligomerization reaction product under the protection of inert gas after micro-interface crushing and dispersion to obtain lactide, and rectifying to obtain purified lactide.
Preferably, the average temperature of the oligomerization reaction is 120-160 ℃, the average temperature of the condensation reaction is 160-190 ℃, and the rectification temperature in the process of rectifying to obtain the purified lactide is 130-170 ℃.
Specifically, the method comprises the steps of smashing gas-phase materials into micro-bubbles with a micron scale through a first micro-interface generator, conveying the micro-bubbles to a rectifying section at the top of an oligomerization rectifying reactor, increasing the mass transfer area of a phase boundary between a lactic acid solution and the gas materials, reducing the viscosity of the lactic acid solution, and improving the yield of lactide products as oligomers are carried out in the oligomerization reaction direction. The method breaks and disperses the inert gas into micro bubbles through the second micro interface generator, and the micro bubbles are dispersed into the lactide rectification reactor, so that the phase boundary mass transfer area between the micro bubbles and the oligomer is increased, the phase boundary mass transfer area is increased, the product quality is improved, and the reaction temperature is reduced.
The reaction method for preparing lactide by adopting lactic acid has good product quality and high yield. Greatly reduces the temperature and the dosage of the catalyst during the reaction.
Compared with the prior art, the invention has the beneficial effects that:
(1) the external micro-interface unit is arranged outside the oligomerization rectification reactor, gas-phase materials are dispersed and crushed into micro-bubbles and are conveyed to a reaction section of the oligomerization rectification reactor, and inert gas is mixed into the lactide rectification reactor after being crushed and dispersed, so that the phase boundary mass transfer area between the inert gas and oligomers is increased, the reaction temperature and the catalyst use amount are reduced, and the reaction efficiency is improved.
(2) Compared with the traditional lactide preparation reaction by lactic acid, the whole reaction of the invention has greatly reduced temperature and improved product quality.
Drawings
Various other advantages and benefits will become apparent to those of ordinary skill in the art upon reading the following detailed description of the preferred embodiments. The drawings are only for purposes of illustrating the preferred embodiments and are not to be construed as limiting the invention. Also, like reference numerals are used to refer to like parts throughout the drawings. In the drawings:
fig. 1 is a schematic structural diagram of a micro-interfacial reaction system for preparing lactide from lactic acid according to an embodiment of the present invention;
wherein:
a 10-lactic acid feed tank; 20-oligomerization rectification reactor;
21-a first condenser; 22-a rectification section;
23-external micro interface unit; 231-external micro-interface generator;
24-a first reboiler; 25-a first gas-liquid separator;
a 30-lactide rectification reactor; 31-a second condenser;
32-a first micro-interface generator; 33-a second micro-interface generator;
34-a gas injector; 341 mixing Chamber
342-a nozzle; 35-an inert gas inlet duct;
36-a gas heater; 37-a second reboiler;
38-a second gas-liquid separator; 40-a first rectification column;
50-a second rectification column; 60-lactide storage tank.
Detailed Description
The technical solutions of the present invention will be clearly and completely described below with reference to the accompanying drawings and the detailed description, but those skilled in the art will understand that the following described embodiments are some, not all, of the embodiments of the present invention, and are only used for illustrating the present invention, and should not be construed as limiting the scope of the present invention. All other embodiments, which can be derived by a person skilled in the art from the embodiments given herein without making any creative effort, shall fall within the protection scope of the present invention. The examples, in which specific conditions are not specified, were conducted under conventional conditions or conditions recommended by the manufacturer. The reagents or instruments used are not indicated by the manufacturer, and are all conventional products available commercially.
In the description of the present invention, it should be noted that the terms "center", "upper", "lower", "left", "right", "vertical", "horizontal", "inner", "outer", etc., indicate orientations or positional relationships based on the orientations or positional relationships shown in the drawings, and are only for convenience of description and simplicity of description, but do not indicate or imply that the device or element being referred to must have a particular orientation, be constructed and operated in a particular orientation, and thus, should not be construed as limiting the present invention. Furthermore, the terms "first," "second," and "third" are used for descriptive purposes only and are not to be construed as indicating or implying relative importance.
In the description of the present invention, it should be noted that, unless otherwise explicitly specified or limited, the terms "mounted," "connected," and "connected" are to be construed broadly, e.g., as meaning either a fixed connection, a removable connection, or an integral connection; can be mechanically or electrically connected; they may be connected directly or indirectly through intervening media, or they may be interconnected between two elements. The specific meanings of the above terms in the present invention can be understood in specific cases to those skilled in the art.
In order to more clearly illustrate the technical solution of the present invention, the following description is made in the form of specific embodiments.
Examples
Referring to fig. 1, a schematic structural diagram of a micro-interfacial reaction system for preparing lactide from lactic acid according to an embodiment of the present invention mainly includes a lactic acid raw material tank 10, an oligomerization rectification reactor 20, a lactide rectification reactor 30, a first rectification column 40, a second rectification column 50, and a lactide storage tank 60. The lactic acid solution in the lactic acid material tank 10 enters an oligomerization rectification reactor 20 for oligomerization. Wherein the lactic acid solution comprises the following components in percentage by mass: 88-92% lactic acid, the remainder consisting of water.
The upper half part of the oligomeric rectification reactor 20 is a rectification section 22 of the oligomeric rectification reactor 20, and the lower half part of the oligomeric rectification reactor 20 is a reaction section of the oligomeric rectification reactor 20. The rectifying section 22 is mainly used for gathering gas-phase materials, then sending the vaporized materials into the first condenser 21 to be condensed into liquid solution, controlling the liquid solution returned to the oligomerization rectifying reactor 20 through a regulating valve, and taking the rest liquid solution which is not sent to the oligomerization rectifying reactor 20 as wastewater to be extracted and treated by a water treatment unit. The liquid solution returning to the oligomerization rectification reactor 20 is dropped to the reaction section of the oligomerization rectification reactor 20, and the reaction is continued.
The feed inlet of the lactic acid solution is also arranged at the reaction section of the oligomerization rectification reactor 20, and the lactic acid solution can be directly introduced into the reaction section of the oligomerization rectification reactor 20. The oligomerization rectification reactor 20 is provided with a material outlet, a shunt tube is arranged below the material outlet, one of the tubes is connected with a first reboiler 24, and the other tube is connected with the lactide rectification reaction zone.
The water generated in the reaction section of the oligomerization rectification reactor 20 is continuously vaporized and enters a first condenser 21 at the top of the tower, the unreacted materials enter the bottom of the oligomerization rectification reactor 20, and the liquid materials at the bottom are forcibly circulated and fed into a first reboiler 24 beside the bottom of the oligomerization rectification reactor 20 by a tower bottom pump for heating and vaporization. A portion of the liquid material passing through the first reboiler 24 is vaporized and a portion remains in a liquid state. The vaporized material and the unvaporized material are conveyed to a first gas-liquid separator 25, the first gas-liquid separator 25 separates gas-phase material from liquid-phase material, the gas-phase material is discharged from a gas outlet at the top of the first gas-liquid separator 25 and then is introduced into an external micro-interface unit 23, specifically, an external micro-interface generator 231 at the bottom of the external micro-interface unit 23. The external micro-interface unit 23 is composed of two external micro-interface generators 231, and the two external micro-interface generators 231 are connected through a communication pipeline. The external micro-interface unit 23 breaks and disperses the gas-phase material into micro-bubbles and conveys the micro-bubbles to the reaction section of the oligomerization rectification reactor 20 through a pipeline for continuous reaction. Lactic acid and water in the reaction section material of the oligomerization rectification reactor 20 are further removed to obtain oligomer, and the oligomer enters the lactide rectification reactor 30 through a pipeline.
An oligomer feeding hole is formed in the side wall of the lactide rectification reactor 30, oligomers enter the lactide rectification reactor 30 through the oligomer feeding hole, a second condenser 31 is arranged at the top of the lactide rectification reactor 30, water, lactic acid and lactide generated in the reaction enter the second condenser 31 at the top of the lactide rectification reactor 30 after being vaporized, and liquid phase materials after condensation are controlled to return to the lactide rectification reactor 30 by controlling the outlet temperature of the second condenser 31. The condensed liquid phase material descends to the reaction section of the lactide rectification reactor 30 to continue to react, and the generated vomit acid, water and lactide are continuously vaporized and enter a second condenser 31 at the top of the lactide rectification reactor 30.
The bottom of the lactide rectification reactor 30 is provided with a second reboiler 37, and the liquid material at the bottom of the lactide rectification reactor 30 is forcibly sent to the second reboiler 37 beside the bottom of the lactide rectification reactor 30 by a tower bottom pump to be heated and vaporized. A portion of the liquid material passing through the second reboiler 37 is vaporized and a portion remains in a liquid state. The vaporized material and the unvaporized material are input into the second gas-liquid separator 38 together, the second gas-liquid separator 38 separates the gas phase material from the liquid phase material, the gas phase material is discharged from the gas outlet at the top of the second gas-liquid separator 38 and then is introduced into the first micro-interface generator 32, the gas phase material is broken and dispersed into micro-bubbles by the first micro-interface generator 32, and the micro-bubbles are mixed into the reaction material, so that the mass transfer area of the gas-liquid phase interface is enlarged, and the reaction efficiency is improved.
The lactide rectification reactor 30 is also internally provided with a second micro-interface generator 33, the second micro-interface generator 33 is connected with an inert gas inlet pipeline 35, a valve of the inert gas inlet pipeline 35 is opened, the inert gas enters the second micro-interface generator 33 through the pipeline, and the second micro-interface generator 33 breaks and disperses the inert gas into micro-bubbles. The inert gas in the inert gas inlet line 35 enters the second micro-interface generator through the gas heater 36. The gas injector 34 is further disposed below the second micro-interface generator 33, the gas injector 34 includes a mixing chamber 341 and a nozzle 342, the micro bubbles of the inert gas reach the mixing chamber 341 to mix with the liquid material inside, when more inert gas enters the mixing chamber 341, the pressure inside the mixing chamber 341 increases, so that the inert gas and the liquid material are discharged together to enter the lactide rectification reactor 30. The inert gas from the gas injector 34 flushes the incompletely reacted materials accumulated at the bottom of the lactide rectification reactor 30, and returns the incompletely reacted materials to the reaction section of the lactide rectification reactor 30 again to continue the reaction. The microbubbles of inert gas do not participate in the reaction and continue to rise towards the top of the lactide rectification reactor 30 due to the low density. After reaching the top of the lactide rectification reactor 30, the vacuum space at the top of the lactide rectification reactor 30 is squeezed, and the produced crude lactide is transferred to the first rectification column 40 together.
The oligomers form crude lactide in the lactide rectification reactor 30, which is transported to the first rectification column 40 through the feed inlet of the first rectification column 40 by means of a take-off pump and the impetus of an inert gas. The crude lactide contains water, lactic acid and a small amount of lactide, the water, the lactic acid and the small amount of lactide are vaporized in the first rectifying tower 40 and then pass through a condenser at the top of the first rectifying tower 40, one part of liquid material from the condenser returns to the first rectifying tower 40, and the other part of liquid material is directly discharged. The liquid material returned from the condenser descends to the tower kettle, the material liquid in the tower kettle is pumped into a reboiler beside the tower kettle by a tower bottom pump to be heated and vaporized, one part of the material returns to the first rectifying tower 40 to continue the reaction, and the other part of the material is conveyed to the second rectifying tower 50.
The crude lactide from the first rectification column 40, which now contains a small amount of water, lactic acid and a large amount of lactide, enters the second rectification column 50 through the feed inlet of the second rectification column 50. A small amount of water, lactic acid and a large amount of lactide continue to be vaporized in the second rectifying tower 50, and are sent to a condenser at the top of the second rectifying tower 50 after being vaporized, one part of liquid material returns to the second rectifying tower 50, and the other part is directly discharged. The liquid material after returning descends to the tower kettle to continue the reaction, the feed liquid in the tower kettle is sent to a reboiler by a tower bottom pump to be heated and vaporized, one part of the feed liquid returns to the second rectifying tower 50, and the other part of the feed liquid is directly discharged. The discharge port of the second rectifying tower 50 is connected with a lactide storage tank 60, and the lactide discharged from the second rectifying tower 50 passes through a lactide flaking machine and then is sent to the lactide storage tank 60 for storage.
During the reaction, the internal temperature of the oligomerization rectification reactor 20 is 130 ℃, the temperature of the top of the specific oligomerization rectification reactor 20 is 51 ℃, the error is within plus or minus 5%, the temperature of the bottom of the oligomerization rectification reactor is 144 ℃, the error is within plus or minus 5%, the lactic acid feeding temperature is 120 ℃, the temperature error is within plus or minus 20%, the pressure is 14KPa, and the error is within plus or minus 10%.
The internal temperature of the lactide rectification reactor 30 is 170 ℃, the temperature of the top of the lactide rectification reactor 30 is 116 ℃, the error is +/-5%, the temperature of the bottom of the lactide rectification reactor is 196 ℃, the error is +/-5%, the oligomer feeding temperature is 190 ℃, the temperature error is +/-20%, the pressure is 2KPa, and the error is +/-10%.
The internal temperature of the first rectifying tower 40 is 150 ℃, the temperature of the top of the first rectifying tower 40 is 118 ℃, the error is +/-5%, the temperature of the bottom of the first rectifying tower is 162 ℃, the error is +/-5%, the feeding temperature is 150 ℃, the temperature error is +/-20%, the pressure is 2KPa, and the error is +/-10%.
The internal temperature of the second rectifying tower 50 is 170 ℃, the temperature of the top of the second rectifying tower 50 is 141 ℃, the error is +/-5%, the temperature of the bottom of the second rectifying tower is 198 ℃, the error is +/-5%, the feeding temperature is 150 ℃, the temperature error is +/-20%, the pressure is 2KPa, and the error is +/-10%.
The indexes of the lactide product obtained by the reaction are as follows:
the product needs L-lactide, so that the lactide produced by the method has high purity and contains less water and meso-lactide as can be seen from the figure.
Therefore, compared with the prior art, the reaction system for preparing the lactide has the advantages of low energy consumption, low cost, high purity of the obtained lactide and high conversion rate of raw materials, and is worthy of wide popularization and application.
Finally, it should be noted that: the above embodiments are only used to illustrate the technical solution of the present invention, and not to limit the same; while the invention has been described in detail and with reference to the foregoing embodiments, it will be understood by those skilled in the art that: the technical solutions described in the foregoing embodiments may still be modified, or some or all of the technical features may be equivalently replaced; and the modifications or the substitutions do not make the essence of the corresponding technical solutions depart from the scope of the technical solutions of the embodiments of the present invention.
Claims (10)
1. A micro-interfacial reaction system for preparing lactide from lactic acid, comprising: the device comprises a lactic acid raw material tank, an oligomerization rectification reactor and a lactide rectification reactor, wherein the lactic acid raw material tank is connected with the oligomerization rectification reactor;
a first reboiler is arranged at the bottom of the oligomerization rectification reactor, one part of the material discharged from the bottom of the oligomerization rectification reactor is sent to the first reboiler for gasification and return, the other part of the material is sent to the lactide rectification reactor, an external micro-interface unit is arranged in the oligomerization rectification reactor, the external micro-interface unit is connected with the first reboiler, and the material gasified by the first reboiler is crushed and dispersed;
a second reboiler is arranged at the bottom of the lactide rectification reactor, the second reboiler gasifies materials coming out of the bottom of the lactide rectification reactor and then leads the gasified materials into a first micro-interface generator in the lactide rectification reactor, and the gasified materials of the second reboiler are subjected to splitting and dispersion; and a second micro-interface generator is also arranged below the first micro-interface generator, the second micro-interface generator is connected with an inert gas inlet pipeline for dispersing and crushing the incoming inert gas, and the second micro-interface generator is connected with a gas ejector.
2. The reaction system of claim 1 wherein the external micro-interface unit comprises a plurality of external micro-interface generators.
3. The reaction system as claimed in claim 1, wherein the first reboiler is connected with a first gas-liquid separator for gas-liquid separation of the material from the first reboiler, and the gas phase material from the top of the first gas-liquid separator is passed into an external micro-interface generator at the bottom of the external micro-interface unit.
4. The reaction system of claim 1, wherein the second reboiler is connected with a second gas-liquid separator for gas-liquid separation of the material from the second reboiler, the gas-phase material from the top of the second gas-liquid separator is passed into the first micro-interface generator for dispersion and fragmentation, and the liquid-phase material from the bottom of the second gas-liquid separator is directly discharged.
5. The reaction system of claim 1, wherein the second micro-interface generator is disposed at the bottom of the lactide rectification reactor, and the injection direction of the gas injector is toward the bottom of the lactide rectification reactor to disperse the broken inert gas injection to disperse the incompletely reacted oligomers at the bottom of the lactide rectification reactor.
6. The reaction system of claim 5 wherein the gas injector comprises a nozzle and a mixing chamber, the entry of inert gas into the mixing chamber pressing the reaction mass for ejection from the nozzle.
7. The reaction system of claim 1, wherein a first condenser is arranged at the top of the oligomerization rectification reactor, a part of vaporized water is condensed by the first condenser and returned to the oligomerization rectification reactor, and the other part of vaporized water is discharged, and a second condenser is arranged at the top of the lactide rectification reactor and condensed by the second condenser and returned to the lactide rectification reactor.
8. The reaction system according to claim 1, wherein the lactide rectification reactor is connected with a first rectification column for primary rectification of lactide, the first rectification column is connected with a second rectification column for further rectification of lactide, and the second rectification column is connected with a lactide storage tank.
9. The reaction method of the micro-interfacial reaction system for the preparation of lactide using lactic acid according to any one of claims 1 to 8, comprising the steps of:
carrying out oligomerization reaction on lactic acid, continuously gasifying, dispersing and crushing products in the reaction process, and rectifying;
and carrying out condensation reaction on the oligomerization reaction product under the protection of inert gas after micro-interface crushing and dispersion to obtain lactide, and rectifying to obtain purified lactide.
10. The reaction method as claimed in claim 9, wherein the oligomerization reaction temperature is 160 ℃ and the condensation reaction temperature is 190 ℃ and the rectification reaction temperature in the process of rectifying to obtain purified lactide is 130 ℃ and 170 ℃.
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202110122705.0A CN112851629A (en) | 2021-01-29 | 2021-01-29 | Micro-interface reaction system and method for preparing lactide from lactic acid |
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| Application Number | Priority Date | Filing Date | Title |
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| CN202110122705.0A CN112851629A (en) | 2021-01-29 | 2021-01-29 | Micro-interface reaction system and method for preparing lactide from lactic acid |
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| CN202110122705.0A Withdrawn CN112851629A (en) | 2021-01-29 | 2021-01-29 | Micro-interface reaction system and method for preparing lactide from lactic acid |
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