CN111187164A - 6-carbonyl-8-chloro ethyl caprylate synthesis device and method for synthesizing 6-carbonyl-8-chloro ethyl caprylate by using same - Google Patents
6-carbonyl-8-chloro ethyl caprylate synthesis device and method for synthesizing 6-carbonyl-8-chloro ethyl caprylate by using same Download PDFInfo
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Abstract
A6-carbonyl-8-chlorine ethyl caprylate synthesis device and a method for synthesizing 6-carbonyl-8-chlorine ethyl caprylate by the device comprise the following steps: introducing 6-chloro-6-oxoethyl hexanoate, dichloroethane and anhydrous aluminum trichloride which are reaction raw materials into a complexing liquid preparation kettle to obtain a complexing liquid; conveying ethylene to an inlet of an ethylene compressor, conveying the ethylene to an ethylene buffer tank from an opening of the ethylene buffer tank through an outlet pipeline of the ethylene compressor, and conveying the ethylene to a premixer of a reaction mechanism through an outlet pipeline of the ethylene buffer tank to obtain a reaction material to be synthesized; and leading the reaction material to be synthesized in the premixer into the static mixer from the inlet end of the static mixer, leading the reaction material to be synthesized into the heat exchanger from the inlet end of the heat exchanger through the outlet end pipeline of the static mixer, leading the reaction material to be synthesized into the hydrolysis kettle through the outlet end pipeline of the heat exchanger, and obtaining a finished product through layering and distillation. The preparation efficiency is improved, the consistency and stability of the product quality under the continuous flow reaction are ensured, the yield is improved, and the preparation method is energy-saving, environment-friendly and safe.
Description
Technical Field
The invention belongs to the technical field of lipoic acid intermediate synthesis devices, and particularly relates to a 6-carbonyl-8-ethyl chlorooctoate synthesis device, and a method for synthesizing 6-carbonyl-8-ethyl chlorooctoate by using the device.
Background
The above-mentioned apparatus for synthesizing ethyl 6-carbonyl-8-chlorooctanoate is substantially a continuous flow synthesis apparatus for ethyl 6-carbonyl-8-chlorooctanoate (the same applies hereinafter), and accordingly, the above-mentioned method for synthesizing ethyl 6-carbonyl-8-chlorooctanoate is substantially a continuous flow synthesis method for ethyl 6-carbonyl-8-chlorooctanoate (the same applies hereinafter).
The english name of ethyl 6-carbonyl-8-chlorooctanoate is: ethyl 8-chloro-6-oxoctanoate, molecular formula: c10H17O3Cl; the molecular weight is: 220.69, is a chemical reaction intermediate used for synthesizing 6, 8-dichloro octanoic acid ethyl ester, and the 6, 8-dichloro octanoic acid ethyl ester is an indispensable important intermediate for synthesizing lipoic acid.
The lipoic acid is a substance which can eliminate aging and pathogenic diseases and is similar to vitamins, can remove free radicals of a matrix, promote the matrix to synthesize vitamin C by using glucose, can effectively remove melanin, can assist coenzyme to carry out physiological metabolism favorable for the immunity of the organism, is a universal antioxidant medicine, and is widely applied to preventing and treating heart diseases, diabetes and senile dementia.
In recent years, with the increasing attention of people to resources, environment and the like, the demand for sustainable development, green chemistry, environmental friendliness and the like is increasing, so that more severe requirements on energy conservation, emission reduction, consumption reduction and high efficiency are provided in the research and development and production of chemical and pharmaceutical products.
As mentioned above, ethyl 6-carbonyl-8-chlorooctanoate is an important pharmaceutical intermediate in the production of lipoic acid. The chemical structure is shown as the following formula:
the current main method for producing 6-carbonyl-8-chloro ethyl caprylate is as follows: in a reaction kettle, 6-chloro-6-oxoethyl hexanoate is used as a raw material, aluminum trichloride is used as a catalytic action, ethylene gas is introduced for alkylation reaction, and the reaction is carried out in a gas-liquid two-phase environment, and the reaction process needs 2 times of excess ethylene, so that the problems of low production efficiency, unstable product quality and large potential safety hazard of excess ethylene are caused, and the requirements of modern industrial production are not met. However, if the 6-carbonyl-8-chlorooctanoic acid ethyl ester is produced on the basis of meeting the requirements of high yield, low energy consumption, stability and safety and environment protection, reasonable equipment configuration inevitably plays a key role, and the technical scheme to be described below is generated under the background.
Disclosure of Invention
The invention aims to provide a 6-carbonyl-8-chloro ethyl caprylate synthesizing device which is beneficial to meeting the continuous synthesis requirement, providing a foundation for improving the preparation efficiency, ensuring the consistency and stability of the quality of the prepared product, obviously improving the yield, reducing the energy consumption and the emission, embodying the green and environmental protection, and conveniently embodying the safety so as to avoid hidden danger.
The invention also aims to provide a method for synthesizing 6-carbonyl-8-chloro ethyl caprylate by using the 6-carbonyl-8-chloro ethyl caprylate synthesis device, which has the advantages of short process steps, capability of guaranteeing the consistency and stability of the quality, high yield, low energy consumption, less emission, environmental protection and safety, and can be comprehensively embodied.
The invention has the primary task that the synthesis device of the 6-carbonyl-8-chloro ethyl caprylate comprises a complexing liquid supply mechanism, an ethylene gas supply mechanism and a reaction mechanism, wherein the complexing liquid supply mechanism comprises a complexing liquid preparation kettle, a complexing liquid temporary storage kettle, a complexing liquid metering pump, a damping buffer, a complexing liquid conveying pipeline one-way valve and a mixed liquid conveying pump, a complexing liquid preparation kettle feeding port is arranged at the upper part of the complexing liquid preparation kettle, a complexing liquid preparation kettle discharging port is formed at the bottom of the complexing liquid preparation kettle, the complexing liquid preparation kettle discharging port is connected with a mixed liquid conveying pump inlet port of a mixed liquid conveying pump through a complexing liquid preparation kettle discharging port conveying pipe, the mixed liquid conveying pump discharging port of the mixed liquid conveying pump is connected with a complexing liquid temporary storage kettle feeding port at the top of the complexing liquid temporary storage kettle through a mixed liquid conveying pump discharging port pipeline, a discharge port of the complexing liquid temporary storage kettle at the bottom of the complexing liquid temporary storage kettle is connected with a feed port of a complexing liquid metering pump of the complexing liquid metering pump through a complexing liquid temporary storage kettle discharge port pipeline, a discharge port of the complexing liquid metering pump is connected with the reaction mechanism through a complexing liquid metering pump conveying pipeline, a damping buffer and a complexing liquid conveying pipeline one-way valve are connected to the complexing liquid metering pump conveying pipeline, wherein the position of the complexing liquid conveying pipeline one-way valve on the complexing liquid metering pump conveying pipeline is positioned between the damping buffer and the reaction mechanism; the ethylene gas supply mechanism comprises an ethylene compressor, an ethylene buffer tank and an ethylene buffer tank outlet pipeline one-way valve, wherein an ethylene compressor inlet of the ethylene compressor is connected with an ethylene gas supply source pipeline through an ethylene compressor inlet pipeline, an ethylene compressor outlet of the ethylene compressor is connected with an ethylene buffer tank inlet of the ethylene buffer tank through an ethylene compressor outlet pipeline, an ethylene buffer tank outlet of the ethylene buffer tank is connected with the reaction mechanism through an ethylene buffer tank outlet pipeline, and the ethylene buffer tank outlet pipeline one-way valve is connected to an ethylene buffer tank outlet pipeline; the reaction mechanism comprises a premixer, a static mixer, a heat exchanger and a hydrolysis kettle, the premixer is connected with the inlet end of the static mixer, the complex liquid metering pump conveying pipeline and the ethylene buffer tank outlet pipeline are connected with the premixer, the outlet end of the static mixer is connected with the heat exchanger inlet end of the static mixer outlet end pipeline heat exchanger, and the heat exchanger outlet end of the heat exchanger is connected with the hydrolysis kettle through the heat exchanger outlet end pipeline.
In a specific embodiment of the present invention, a complexing liquid preparation kettle discharge port conveying pipe control valve and a complexing liquid preparation kettle discharge port conveying pipe check valve are arranged on the pipeline of the complexing liquid preparation kettle discharge port conveying pipe, and the position of the complexing liquid preparation kettle discharge port conveying pipe check valve on the pipeline of the complexing liquid preparation kettle discharge port conveying pipe is located between the complexing liquid preparation kettle discharge port conveying pipe control valve and the mixed liquid conveying pump inlet of the mixed liquid conveying pump.
In another specific embodiment of the present invention, the damping buffer is a pulse diaphragm type damping buffer with a pressure gauge and used for reducing pulses caused by the complexing liquid metering pump, and a damping buffer connecting pipe check valve is arranged on a pipe of a damping buffer connecting pipe connected with the complexing liquid metering pump conveying pipe of the damping buffer; and a pressure display device and a safety valve are arranged at the discharge port of the complexing liquid metering pump.
In another specific embodiment of the present invention, a hydrolysis kettle inlet and a hydrolysis kettle tail gas outlet are formed at the top of the hydrolysis kettle, a hydrolysis kettle inlet valve is disposed at one end of the heat exchanger outlet end pipeline, which is connected with the hydrolysis kettle inlet, a hydrolysis kettle tail gas outlet is connected with the hydrolysis kettle tail gas outlet, and a tail gas outlet valve is disposed on the hydrolysis kettle tail gas outlet.
In yet another embodiment of the present invention, the static mixer is an SV type static mixer.
Another object of the present invention is to provide a method for synthesizing ethyl 6-carbonyl-8-chlorooctanoate from an apparatus for synthesizing ethyl 6-carbonyl-8-chlorooctanoate, comprising the steps of:
A) preparing complexing liquid, firstly introducing 6-chloro-6-oxoethyl hexanoate and dichloroethane as reaction raw materials into a complexing liquid preparation kettle from a complexing liquid preparation kettle feed inlet at the upper part of a complexing liquid preparation kettle of a complexing liquid supply mechanism through a pipeline, then introducing anhydrous aluminum trichloride into the complexing liquid preparation kettle from a complexing liquid preparation kettle feed inlet through a pipeline to obtain complexing liquid, introducing the complexing liquid into a mixed liquid conveying pump from a mixed liquid conveying pump inlet through a complexing liquid preparation kettle discharge outlet conveying pipe connected between a complexing liquid preparation kettle discharge outlet at the bottom of the complexing liquid preparation kettle and a mixed liquid conveying pump inlet of a mixed liquid conveying pump, introducing the mixed liquid into the complexing liquid temporary storage kettle from a complexing liquid temporary storage kettle feed inlet at the top of the complexing liquid temporary storage kettle through a mixed liquid conveying pump discharge outlet pipeline of the mixed liquid conveying pump, leading the complex liquid temporary storage kettle to a liquid inlet of a complex liquid metering pump of the complex liquid metering pump through a complex liquid temporary storage kettle discharge port pipeline connected with a complex liquid temporary storage kettle discharge port at the bottom of the complex liquid temporary storage kettle, and conveying the complex liquid metering pump to a premixer of a reaction mechanism through a complex liquid metering pump conveying pipeline from the liquid inlet of the complex liquid metering pump, wherein a damping buffer and a complex liquid conveying pipeline one-way valve are respectively connected to the complex liquid metering pump conveying pipeline, and the position of the complex liquid conveying pipeline one-way valve on the complex liquid metering pump conveying pipeline is positioned between the damping buffer and the premixer of the reaction mechanism;
B) preparing a reaction material to be synthesized, conveying ethylene to an inlet of an ethylene compressor of the ethylene compressor by an inlet pipeline of the ethylene compressor, which is connected with an ethylene gas supply source pipeline and is also connected with an inlet of the ethylene compressor of an ethylene gas supply mechanism, conveying the ethylene to an ethylene buffer tank from an opening of the ethylene buffer tank by an outlet pipeline of the ethylene compressor, which is connected with an outlet of the ethylene compressor, and conveying the ethylene to a premixer of the reaction mechanism by an outlet pipeline of the ethylene buffer tank, which is connected with a check valve of the outlet pipeline of the ethylene buffer tank, so as to obtain the reaction material to be synthesized;
C) and D), synthesizing a finished product, namely leading the reaction material to be synthesized in the premixer in the step B) into a static mixer from the inlet end of the static mixer, leading the reaction material to be synthesized into a heat exchanger from the inlet end of the heat exchanger through a pipeline at the outlet end of the static mixer connected with the outlet end of the static mixer, leading the reaction material to be synthesized into a hydrolysis kettle through a pipeline at the outlet end of the heat exchanger connected with the outlet end of the heat exchanger, and obtaining the 6-carbonyl-8-chloro ethyl caprylate through layering.
In still another embodiment of the present invention, the mol ratio of ethyl 6-chloro-6-oxohexanoate, anhydrous aluminum trichloride and dichloroethane in the step A) is 1: 1.6-2.5: 8-10; the flow rate of the complexing liquid is 9000-11000 ml/min; the pressure of the damping buffer is 0.3-0.7 MPa.
In a more specific embodiment of the present invention, the pressure of the ethylene gas in step B) is 0.15 to 0.25MPa greater than the pressure of the damping buffer in step A), and the flow rate of the ethylene gas is 14 to 18L/min; the temperature of the jacket water bath of the static mixer in the step C) is 65-78 ℃, and the retention time of the materials in the static mixer is 15-60 s.
In a further specific embodiment of the invention, the temperature of the reaction material to be synthesized after heat exchange by the heat exchanger in step C) is 0 to 25 ℃; the hydrolysis temperature of the hydrolysis kettle is 0-25 ℃.
In a still more specific embodiment of the present invention, the static mixer described in step C) is internally formed with a hole passage which is a spiral-up hole passage, and the static mixer is formed by connecting four tubes each having a pipe diameter of DN25mm and a length of 1000mm in series.
The technical scheme provided by the invention has the technical effects that: because the complexing liquid supply mechanism and the ethylene gas supply mechanism are simultaneously connected with the reaction mechanism, the kettle type intermittent reaction in the prior art can be changed into continuous flow reaction, basic guarantee is provided for improving the preparation efficiency, the consistency and the stability of the product quality under the continuous flow reaction can be guaranteed, the yield can be improved, the energy and the cost can be saved, and the emission is reduced, so that the green, environment-friendly and safe effects are realized; the preparation method can introduce raw materials of 6-chloro-6-oxoethyl hexanoate, dichloroethane and anhydrous aluminum trichloride into a complexing liquid preparation kettle to obtain complexing liquid, and then sequentially convey the complexing liquid temporary storage kettle and a complexing liquid metering pump to a reaction mechanism, and further introduce ethylene gas into the reaction mechanism sequentially through an ethylene compressor and a static mixer, so that the 6-chloro-6-oxoethyl hexanoate and ethylene can continuously perform gas-liquid two-phase reaction, the molar ratio consumed by the reaction of the ethylene and the 6-chloro-6-oxoethyl hexanoate can be reduced from 2.4: 1 to 1.3: 1, and the technical effect of the 6-carbonyl-8-chloroethyl octanoate synthesis device can be comprehensively embodied.
Drawings
FIG. 1 is a schematic diagram of a 6-carbonyl-8-ethyl chlorooctanoate synthesis apparatus according to the present invention.
Detailed Description
Example 1:
the method for synthesizing the ethyl 6-carbonyl-8-chlorooctanoate by using the ethyl 6-carbonyl-8-chlorooctanoate synthesis device shown in figure 1 comprises the following steps:
A) preparing complex liquid, firstly, respectively introducing 6-chloro-6-oxoethyl hexanoate and dichloroethane as reaction raw materials into a complex liquid preparation kettle 11 through respective pipelines, namely a 6-chloro-6-oxoethyl hexanoate conveying pipeline provided with a valve and a dichloroethane conveying pipeline also provided with a valve from a complex liquid preparation kettle feed port 111 at the upper part of a complex liquid preparation kettle 11 of a structural system of a complex liquid supply mechanism 1, wherein the complex liquid preparation kettle 11 has two sets with completely same structures as shown in figure 1 so as to fully ensure uninterrupted conveying of 6-chloro-6-oxoethyl hexanoate and dichloroethane mixture, specifically, when materials in one set of complex liquid preparation kettle tend to be used up, the materials in the other set of complex liquid preparation kettle are started, and the complex liquid preparation kettle which tends to be used up is positioned in the 6-chloro-6-oxoethyl hexanoate conveying pipeline The feeding state of the feeding pipeline and the dichloroethane conveying pipeline, closing the valve when full conveying, so that two complexing liquid preparation kettles alternately and continuously supply materials to a subsequent station, introducing anhydrous aluminum trichloride into the complexing liquid preparation kettle 11 from a complexing liquid preparation kettle feeding port 111 through a pipeline to obtain complexing liquid, introducing the complexing liquid into the mixed liquid conveying pump 16 from a mixed liquid conveying pump inlet port through a complexing liquid preparation kettle discharging port conveying pipe 1121 between a complexing liquid preparation kettle discharging port 112 connected to the bottom of the complexing liquid preparation kettle 11 and a mixed liquid conveying pump inlet port of the mixed liquid conveying pump 16, introducing the mixed liquid into the complexing liquid temporary storage kettle 12 from a complexing liquid temporary storage kettle feeding port 121 at the top of the complexing liquid temporary storage kettle 12 through a mixed liquid conveying pump discharging port pipeline 161 by a mixed liquid conveying pump discharging port conveying pipe 1221 connected with a complexing liquid temporary storage kettle discharging port 122 at the bottom of the complexing liquid temporary storage kettle 12 13, a liquid inlet of the complexing liquid metering pump, which is conveyed to a premixer 31 of the reaction mechanism 3 through a complexing liquid metering pump conveying pipeline 131 from the liquid inlet of the complexing liquid metering pump, wherein the complexing liquid metering pump conveying pipeline 131 is respectively connected with a damping buffer 14 and a complexing liquid conveying pipeline one-way valve 15, the position of the complexing liquid conveying pipeline one-way valve 15 on the complexing liquid metering pump conveying pipeline 131 is positioned between the damping buffer 14 and the premixer 31 of the reaction mechanism 3, in the embodiment, the mol ratio of the 6-chloro-6-oxoethyl hexanoate, the anhydrous aluminum trichloride and the dichloroethane is 1: 1.83: 9.5, the flow rate of the complexing liquid is 9000ml/min, the pressure of the damping buffer 14 is 0.5MPa, and as shown in fig. 1, a complexing liquid preparation kettle discharge port conveying pipe control valve 11211 and a complexing liquid preparation kettle discharge port non-return conveying pipe are arranged on the pipeline of the complexing liquid preparation kettle discharge port conveying pipe 1121 A valve 11212, in which the position of the complex liquid preparation tank discharge port delivery pipe check valve 11212 on the pipe of the complex liquid preparation tank discharge port delivery pipe 1121 is located between the complex liquid preparation tank discharge port delivery pipe control valve 11211 and the mixed liquid delivery pump inlet port of the mixed liquid delivery pipe 16, and further, the damping buffer 14 is a pulse diaphragm type damping buffer with a pressure gauge for reducing the pulse caused by the complex liquid metering pump 13, a damping buffer connection pipe check valve 1411 is provided on the pipe of the damping buffer connection pipe 141, to which the damping buffer 14 is connected to the complex liquid metering pump delivery pipe 131, and a pressure display device 132 (such as a pressure gauge) and a safety valve 133 are provided at the position of the complex liquid metering pump discharge port of the complex liquid metering pump 13;
B) a reactant to be synthesized is prepared, ethylene, i.e., ethylene gas, is fed to the ethylene compressor inlet 211 of the ethylene compressor 21 from an ethylene compressor inlet line 2111 connected to an ethylene gas supply source, e.g., an ethylene gas storage tank line, and also connected to the ethylene compressor inlet 211 of the ethylene compressor 21 of the structural system of the ethylene gas supply means 2, the reaction material to be synthesized is obtained by delivering the reaction material from the ethylene buffer tank port 221 to the ethylene buffer tank 22 through an ethylene compressor outlet pipe 2121 connected to the ethylene compressor outlet 212 of the ethylene compressor 21, and delivering the reaction material to the premixer 31 of the reaction mechanism 3 through an ethylene buffer tank outlet pipe 2221 connected to the ethylene buffer tank outlet 222 of the ethylene buffer tank 22, wherein, an ethylene buffer tank outlet pipeline check valve 23 is connected to the ethylene buffer tank outlet pipeline 2221, as can be seen from the description of this step and the description of step a): the material entering the premixer 31 in the step A) is in a liquid phase, while the material entering the premixer 31 in the step B) is in a gas phase, and the reaction material to be synthesized is formed by the gas-liquid two-phase material, wherein the pressure of the ethylene gas in the step is controlled to be 0.5MPa, the pressure of the damping buffer 14 is 0.35MPa, namely the pressure of the ethylene gas is 0.15MPa greater than the pressure of the damping buffer 14 in the step A), and the flow rate of the ethylene gas in the step is 16L/min;
C) synthesizing a finished product, namely introducing the reaction material to be synthesized in the premixer 31 in the step B) into a static mixer 32 from an inlet end of the static mixer 32, introducing the reaction material to be synthesized into a heat exchanger 33 from an inlet end of the heat exchanger through a pipeline 321 at an outlet end of the static mixer connected with an outlet end of the static mixer 32, introducing the reaction material to be synthesized into a hydrolysis kettle 34 through a pipeline 331 at an outlet end of the heat exchanger connected with an outlet end of the heat exchanger 33, layering and distilling to obtain the finished product, namely 6-carbonyl-8-ethyl chlorooctanoate, wherein the gas-phase analysis purity of the 6-carbonyl-8-ethyl chlorooctanoate is 97.69%, the gas-phase analysis purity of the unreacted raw material is 1.93%, and the impurity content is 0.37%, the water bath temperature of a jacket of the static mixer 32 in the step is 70 ℃, the residence time of the reaction material in the static mixer 32 is controlled to be 40s, the temperature of the reaction, the hydrolysis temperature of the hydrolysis kettle 34 is 0 ℃, a pore passage is formed inside the static mixer 32, the pore passage is a spiral rising pore passage, the static mixer 32 is formed by connecting four pipes with the pipe diameter of DN25mm and the length of 1000mm in series, as shown in figure 1, a hydrolysis kettle feed inlet 341 and a hydrolysis kettle tail gas outlet 342 are formed at the top of the hydrolysis kettle 34, a hydrolysis kettle feed inlet valve 3311 is arranged at one end of the heat exchanger outlet end pipeline 331 matched and connected with the hydrolysis kettle feed inlet 341, a hydrolysis kettle tail gas outlet pipe 3421 is matched and connected with the hydrolysis kettle tail gas outlet pipe 342, and a tail gas outlet valve 34211 is arranged on the hydrolysis kettle tail gas outlet pipe 3421.
Example 2:
only changing the mol ratio of the 6-chloro-6-oxoethyl hexanoate, the anhydrous aluminum trichloride and the dichloroethane in the step A) to 1: 1.6: 10, changing the flow of the complexing liquid to 11000L/min, and changing the pressure of the damping buffer 14 to 0.7 MPa; only changing the pressure of the ethylene gas in the step B) to 0.8MPa, changing the pressure of the damping buffer 14 to 0.6MPa, wherein the pressure of the ethylene gas is 0.2MPa higher than the pressure of the damping buffer 14, and changing the flow rate of the ethylene gas to 14L/min; only the jacket water bath temperature of the static mixer 32 in the step C) was changed to 65 ℃, the residence time of the material in the static mixer 32 was changed to 60s, the temperature of the reaction material to be synthesized after heat exchange by the heat exchanger 33 was changed to 25 ℃, the hydrolysis temperature of the hydrolysis kettle 34 was changed to 10 ℃, the gas phase analytical purity of ethyl 6-carbonyl-8-chlorooctanoate was 96.07%, the unreacted raw material was 3.48%, and the impurities were 0.44%, and the rest was the same as described in example 1.
Example 3:
only changing the mol ratio of the 6-chloro-6-oxoethyl hexanoate, the anhydrous aluminum trichloride and the dichloroethane in the step A) to 1: 2.5: 8, changing the flow of the complexing liquid to 10000L/min, and changing the pressure of the damping buffer 14 to 0.3 MPa; only changing the pressure of the ethylene gas in the step B) to 0.9MPa, changing the pressure of the damping buffer 14 to 0.65MPa, wherein the pressure of the ethylene gas is 0.25MPa greater than the pressure of the damping buffer 14, and changing the flow rate of the ethylene gas to 18L/min; only the jacket water bath temperature of the static mixer 32 in the step C) was changed to 78 ℃, the residence time of the material in the static mixer 32 was changed to 15s, the temperature of the reaction material to be synthesized after heat exchange by the heat exchanger 33 was changed to 10 ℃, the hydrolysis temperature of the hydrolysis kettle 34 was changed to 25 ℃, the gas phase analysis purity of ethyl 6-carbonyl-8-chlorooctanoate was 96.43%, the unreacted raw material was 4.22%, and the impurities were 0.6%, and the rest was the same as described in example 1.
Claims (10)
1. A6-carbonyl-8-ethyl chlorooctoate synthesizer is characterized by comprising a complexing liquid supply mechanism (1), an ethylene gas supply mechanism (2) and a reaction mechanism (3), wherein the complexing liquid supply mechanism (1) comprises a complexing liquid preparation kettle (11), a complexing liquid temporary storage kettle (12), a complexing liquid metering pump (13), a damping buffer (14), a complexing liquid conveying pipeline one-way valve (15) and a mixed liquid conveying pump (16), a complexing liquid preparation kettle feed inlet (111) is formed in the upper part of the complexing liquid preparation kettle (11), a complexing liquid preparation kettle discharge outlet (112) is formed in the bottom of the complexing liquid preparation kettle (11), the complexing liquid preparation kettle discharge outlet (112) is connected with a mixed liquid conveying pump inlet of a mixed liquid conveying pump (16) through a complexing liquid preparation kettle discharge outlet conveying pipe (1121), a mixed liquid conveying pump discharge port of the mixed liquid conveying pump (16) is connected with a complexing liquid temporary storage kettle feed port (121) at the top of the complexing liquid temporary storage kettle (12) through a mixed liquid conveying pump discharge port pipeline (161), a complexing liquid temporary storage kettle discharge port (122) at the bottom of the complexing liquid temporary storage kettle (12) is connected with a complexing liquid metering pump feed inlet of a complexing liquid metering pump (13) through a complexing liquid temporary storage kettle discharge port pipeline (1221), the discharge port of the complexing liquid metering pump (13) is connected with the reaction mechanism (3) through a complexing liquid metering pump conveying pipeline (131), a damping buffer (14) and a one-way valve (15) of the complexing liquid conveying pipeline are connected on the complexing liquid metering pump conveying pipeline (131), the position of the complexing liquid conveying pipeline one-way valve (15) on the complexing liquid metering pump conveying pipeline (131) is positioned between the damping buffer (14) and the reaction mechanism (3); the ethylene gas supply mechanism (2) comprises an ethylene compressor (21), an ethylene buffer tank (22) and an ethylene buffer tank outlet pipeline one-way valve (23), wherein an ethylene compressor inlet (211) of the ethylene compressor (21) is connected with an ethylene gas supply source pipeline through an ethylene compressor inlet pipeline (2111), an ethylene compressor outlet (212) of the ethylene compressor (21) is connected with an ethylene buffer tank inlet (221) of the ethylene buffer tank (22) through an ethylene compressor outlet pipeline (2121), an ethylene buffer tank outlet (222) of the ethylene buffer tank (22) is connected with the reaction mechanism (3) through an ethylene buffer tank outlet pipeline (2221), and the ethylene buffer tank outlet pipeline one-way valve (23) is connected to the ethylene buffer tank outlet pipeline (2221); the reaction mechanism (3) comprises a premixer (31), a static mixer (32), a heat exchanger (33) and a hydrolysis kettle (34), wherein the premixer (31) is connected with the inlet end of the static mixer (32), the complex liquid metering pump conveying pipeline (131) and the ethylene buffer tank outlet pipeline (2221) are connected with the premixer (31), the outlet end of the static mixer (32) is connected with the heat exchanger inlet end of the heat exchanger (33) through the static mixer outlet end pipeline (321), and the heat exchanger outlet end of the heat exchanger (33) is connected with the hydrolysis kettle (34) through the heat exchanger outlet end pipeline (331).
2. The apparatus for synthesizing ethyl 6-carbonyl-8-chlorooctanoate according to claim 1, wherein a complex liquid preparation kettle discharge port delivery pipe control valve (11211) and a complex liquid preparation kettle discharge port delivery pipe check valve (11212) are disposed on a pipeline of the complex liquid preparation kettle discharge port delivery pipe (1121), and a position of the complex liquid preparation kettle discharge port delivery pipe check valve (11212) on the pipeline of the complex liquid preparation kettle discharge port delivery pipe (1121) is located between the complex liquid preparation kettle discharge port delivery pipe control valve (11211) and a mixed liquid delivery pump inlet of the mixed liquid delivery pump (16).
3. The apparatus for synthesizing ethyl 6-carbonyl-8-chlorooctanoate according to claim 1, wherein the damping buffer (14) is a pulse diaphragm type damping buffer having a pressure gauge and used for reducing pulses caused by the complex liquid metering pump (13), and a damping buffer connection pipe check valve (1411) is provided on a pipe of a damping buffer connection pipe (141) connecting the damping buffer (14) and the complex liquid metering pump delivery pipe (131); and a pressure display device (132) and a safety valve (133) are arranged at the discharge hole of the complexing liquid metering pump (13).
4. The apparatus for synthesizing ethyl 6-carbonyl-8-chlorooctanoate according to claim 1, wherein a hydrolysis reactor inlet (341) and a hydrolysis reactor tail gas outlet (342) are formed at the top of the hydrolysis reactor (34), a hydrolysis reactor inlet valve (3311) is disposed at the end of the heat exchanger outlet pipeline (331) connected to the hydrolysis reactor inlet (341), a hydrolysis reactor tail gas outlet (3421) is connected to the hydrolysis reactor tail gas outlet (342), and a tail gas outlet valve (34211) is disposed on the hydrolysis reactor tail gas outlet (3421).
5. The apparatus for synthesizing ethyl 6-carbonyl-8-chlorooctanoate according to claim 1, wherein the static mixer is an SV type static mixer.
6. A method for synthesizing 6-carbonyl-8-chloro ethyl caprylate by a 6-carbonyl-8-chloro ethyl caprylate synthesis device is characterized by comprising the following steps:
A) preparing complexing liquid, firstly introducing 6-chloro-6-oxoethyl hexanoate and dichloroethane as reaction raw materials into a complexing liquid preparation kettle (11) from a complexing liquid preparation kettle feed inlet (111) at the upper part of a complexing liquid preparation kettle (11) of a complexing liquid supply mechanism (1) through a pipeline, then introducing anhydrous aluminum trichloride into the complexing liquid preparation kettle (11) from the complexing liquid preparation kettle feed inlet (111) through a pipeline to obtain the complexing liquid, then introducing the complexing liquid into a mixed liquid conveying pump (16) from a mixed liquid inlet through a complexing liquid preparation kettle discharge outlet conveying pipe (1121) connected between a complexing liquid preparation kettle discharge outlet (112) at the bottom of the complexing liquid preparation kettle (11) and a mixed liquid conveying pump inlet of the mixed liquid conveying pump (16), and pumping out the complexing liquid temporary storage conveying pump (16) at the top of the complexing liquid preparation kettle (12) from the mixed liquid conveying temporary storage conveying A feeding port (121) is introduced into a complexing liquid temporary storage kettle (12), then the complexing liquid temporary storage kettle is introduced to a liquid inlet of a complexing liquid metering pump (13) through a complexing liquid temporary storage kettle discharge port pipeline (1221) connected with a complexing liquid temporary storage kettle discharge port (122) at the bottom of the complexing liquid temporary storage kettle (12), the liquid inlet of the complexing liquid metering pump (13) is conveyed to a premixer (31) of a reaction mechanism (3) through a complexing liquid metering pump conveying pipeline (131), wherein the complexing liquid metering pump conveying pipeline (131) is respectively connected with a damping buffer (14) and a complexing liquid conveying pipeline one-way valve (15), and the position of the complexing liquid conveying pipeline one-way valve (15) on the complexing liquid metering pump conveying pipeline (131) is positioned between the damping buffer (14) and the premixer (31) of the reaction mechanism (3);
B) preparing a reactant to be synthesized, feeding ethylene to an ethylene compressor inlet (211) of an ethylene compressor (21) from an ethylene compressor inlet line (2111) connected to an ethylene gas supply source line and simultaneously connected to the ethylene compressor inlet (211) of the ethylene compressor (21) of an ethylene gas supply mechanism (2), an outlet pipeline (2121) of the ethylene compressor, which is connected with an outlet (212) of the ethylene compressor (21), is conveyed to the ethylene buffer tank (22) from an ethylene buffer tank opening (221), and then conveyed to a premixer (31) of the reaction mechanism (3) through an outlet pipeline (2221) of the ethylene buffer tank, which is connected with an outlet (222) of the ethylene buffer tank (22), wherein, an outlet pipeline one-way valve (23) of the ethylene buffer tank is connected on the outlet pipeline (2221) of the ethylene buffer tank to obtain a reaction material to be synthesized;
C) and (3) synthesizing a finished product, namely introducing the reaction material to be synthesized in the premixer (31) in the step B) into the static mixer (32) from the inlet end of the static mixer (32), introducing the reaction material to be synthesized into the heat exchanger (33) from the inlet end of the heat exchanger (33) through a static mixer outlet end pipeline (321) connected with the outlet end of the static mixer (32), introducing the reaction material to be synthesized into a hydrolysis kettle (34) through a heat exchanger outlet end pipeline (331) connected with the heat exchanger outlet end of the heat exchanger (33), and obtaining the 6-carbonyl-8-chlorooctanoic acid ethyl ester through layering and distillation.
7. The method for synthesizing ethyl 6-carbonyl-8-chlorooctanoate by using the apparatus for synthesizing ethyl 6-carbonyl-8-chlorooctanoate according to claim 6, wherein the mol ratio of ethyl 6-chloro-6-oxohexanoate, anhydrous aluminum trichloride and dichloroethane in the step A) is 1: 1.6 to 2.5: 8 to 10; the flow rate of the complexing liquid is 9000-11000 ml/min; the pressure of the damping buffer (14) is 0.3-0.7 MPa.
8. The method for synthesizing ethyl 6-carbonyl-8-chlorooctanoate by the apparatus for synthesizing ethyl 6-carbonyl-8-chlorooctanoate according to claim 6, wherein the pressure of the ethylene gas in the step B) is 0.15 to 0.25MPa greater than the pressure of the damping buffer (14) in the step A), and the flow rate of the ethylene gas is 14 to 18L/min; the jacket water bath temperature of the static mixer (32) in the step C) is 65-78 ℃, and the retention time of the materials in the static mixer (32) is 15-60 s.
9. The method for synthesizing ethyl 6-carbonyl-8-chlorooctanoate by the apparatus for synthesizing ethyl 6-carbonyl-8-chlorooctanoate according to claim 6, wherein the temperature of the reaction material to be synthesized after heat exchange by the heat exchanger (33) in step C) is 0 to 25 ℃; the hydrolysis temperature of the hydrolysis kettle (34) is 0-25 ℃.
10. The method for synthesizing ethyl 6-carbonyl-8-chlorooctanoate by using the apparatus for synthesizing ethyl 6-carbonyl-8-chlorooctanoate according to claim 6, wherein the static mixer (32) in the step C) is formed with a hole passage inside, the hole passage is a spiral-up hole passage, and the static mixer (32) is formed by connecting four pipes each having a pipe diameter of DN25mm and a length of 1000mm in series.
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| CN102731307A (en) * | 2012-07-17 | 2012-10-17 | 江苏同禾药业有限公司 | Preparation method of ethyl 6-oxo-8-chloro-caprylate |
| CN108774209A (en) * | 2018-08-03 | 2018-11-09 | 苏州富士莱医药股份有限公司 | A method of lipoic acid ethyl ester is prepared using tubular reactor |
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| CN102731307A (en) * | 2012-07-17 | 2012-10-17 | 江苏同禾药业有限公司 | Preparation method of ethyl 6-oxo-8-chloro-caprylate |
| CN108774209A (en) * | 2018-08-03 | 2018-11-09 | 苏州富士莱医药股份有限公司 | A method of lipoic acid ethyl ester is prepared using tubular reactor |
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| CN114644558A (en) * | 2022-03-31 | 2022-06-21 | 福州大学 | Method for continuously synthesizing 6-hydroxy-8-chloro ethyl caprylate by taking monoethyl adipate as raw material in multiple steps |
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