A device for increasing the crude ester content in the production process of methyl chloroacetate.

Abstract

This utility model relates to the field of chemical production equipment technology, and discloses a device for increasing the crude ester content in the production process of methyl chloroacetate, including: a batching kettle, an esterification kettle, an esterification tower, an ester-water separator, an esterification aqueous phase tank, and an esterification ester phase tank. The gas phase pipe of the esterification kettle is connected to the esterification tower, and the top pipe of the esterification tower is connected to the ester-water separator via a condenser. The extraction water pipe is connected to the lower layer ester material outlet pipe of the ester-water separator. The aqueous phase pipe of the ester-water separator is connected to the esterification aqueous phase tank, and the ester material pipe is connected to the esterification ester phase tank via the extraction water pipe. The overflow pipe of the esterification ester phase tank is connected to the esterification aqueous phase tank, and the bottom pipe is connected to the crude ester intermediate tank. This utility model achieves the stepwise purification and extraction of microemulsified crude ester products through multi-stage static separation, intermediate-stage water injection extraction, and aqueous phase sedimentation pipeline layout, reducing the loss of oil phase caused by wastewater discharge; at the same time, it utilizes the water washing structure embedded in the pipe to remove alcohol impurities, maintains stable transfer of the multiphase flow interface, and improves the final crude ester yield.

Description

Technical Field

[0001] This application relates to the field of chemical production equipment technology, specifically to a device for increasing the crude ester content in the production process of methyl chloroacetate. Background Technology

[0002] Methyl chloroacetate is mainly produced by the liquid-phase esterification reaction of chloroacetic acid and methanol. The mixed system produced in the reaction stage contains the target ester, generated water, and excess unconverted methanol, exhibiting a multi-component azeotropic state. To meet the feed specifications of the final distillation section, the mixed gaseous material generated by the reaction needs to undergo cooling phase change and primary oil-water separation.

[0003] Existing processes often rely on a single condenser paired with a single-stage water separator for static stratification. Residual methanol in the mixture exhibits significant solubilizing properties, causing a large amount of free and microemulsified methyl chloroacetate to miscibly remain at the aqueous interface. Conventional single-stage settling operations cannot disrupt the micro-equilibrium of the liquid-liquid two-phase distribution, resulting in a significant amount of recoverable crude ester material being directly discharged and lost along with the upper wastewater, thus reducing the overall material yield. The upstream gas-phase separation unit lacks a physical interception zone for heavy components, allowing unreacted high-boiling-point acid components to easily penetrate the downstream condenser network with the gas flow, resulting in a high impurity content in the final collected crude ester.

[0004] Therefore, this invention proposes a device for increasing the crude ester content during the production of methyl chloroacetate to address the shortcomings of existing technologies. Utility Model Content

[0005] In view of the problems existing in the separation device for the production of methyl chloroacetate, such as the reliance on a single condenser and water separator leading to the retention of microemulsified crude ester in the aqueous phase and its loss with the wastewater discharge, and the lack of physical interception of heavy components in the gas phase separation unit causing unreacted acid to penetrate and resulting in high impurities in the crude ester produced, this utility model aims to provide a device with an improved structure that can effectively solve the above problems and increase the crude ester content in the production process of methyl chloroacetate.

[0006] This utility model provides a device for increasing the crude ester content in the production process of methyl chloroacetate, including: a batching kettle, a raw material feed pipe, a batching kettle feed pump, a high-level tank for mixed liquid, an esterification kettle, an esterification tower, a condenser, an ester-water separator, an esterification aqueous phase tank, an esterification ester phase tank, and a crude ester intermediate tank; as well as the core innovative component, an extraction water pipe.

[0007] The batching vessel and the sedimentation and separation tanks at each stage together form a multiphase interface splitting and separation structure connected by a material fluid pipeline network.

[0008] Furthermore, the raw material feed pipe is connected to the upper part of the batching kettle, the bottom outlet of the batching kettle is connected to the feed inlet of the batching kettle feed pump via a pipe, the outlet of the batching kettle feed pump is connected to the top inlet of the high-level mixing tank via a pipe, and the bottom overflow pipe of the high-level mixing tank is connected to the upper inlet of the esterification kettle; the top gas phase pipe of the esterification kettle is connected to the bottom of the esterification tower, the top gas phase outlet pipe of the esterification tower is connected to the feed end of the condenser, and the bottom liquid outlet pipe of the condenser is connected to the top of the ester-water separator. The extraction water pipe is connected to the lower ester material discharge pipe of the ester-water separator; the upper aqueous phase discharge pipe of the ester-water separator is connected to the top of the esterification aqueous phase tank; the lower ester material discharge pipe of the ester-water separator is connected to the top of the esterification ester phase tank via the extraction water pipe; the upper overflow pipe of the esterification ester phase tank is connected to the side wall of the esterification aqueous phase tank; the bottom discharge pipe of the esterification ester phase tank is connected to the top of the crude ester intermediate tank; and the bottom sedimentation discharge pipe of the esterification aqueous phase tank is connected to the side wall of the crude ester intermediate tank.

[0009] The gas phase outlet pipe at the top of the batching vessel is connected to the air inlet of the batching vessel cooler, and the reflux liquid outlet pipe at the bottom of the batching vessel cooler is connected to the inside of the batching vessel. The shell and tube heat exchange structure is used to force the heated and volatilized gas phase material to cool down and liquefy and guide it back to the batching reaction zone.

[0010] The device for increasing the crude ester content in the methyl chloroacetate production process also includes a methanol replenishment tank. The discharge pipe at the bottom of the methanol replenishment tank is connected to the middle of the side wall of the esterification reactor, and liquid alcohol material is replenished at constant pressure to the heated and boiling reaction liquid phase main area.

[0011] A forced cooler is fixedly inserted inside the top of the esterification tower. It is used to cool the rising mixed gas phase by relying on the surface of the heat exchange tube bundle and to form a local condensation zone at the top of the tower to intercept high-boiling-point droplets.

[0012] The device for increasing the crude ester content in the methyl chloroacetate production process also includes a crude ester transfer pump. The inlet of the crude ester transfer pump is connected to the outlet at the bottom of the crude ester intermediate tank, and the outlet pipe of the crude ester transfer pump is connected to the feed pipeline of the distillation process.

[0013] The overflow pipe at the bottom of the high-level tank of the mixture is at a higher level than the feed inlet at the top of the esterification reactor, creating a gravitational potential energy difference that drives the fluid to overcome the frictional resistance along the pipeline and discharge it into the downstream working chamber.

[0014] The discharge pipe at the bottom of the methanol replenishment tank is at a higher level than the inlet at the middle of the side wall of the esterification reactor, providing static pressure potential energy support for the non-powered fluid transport network.

[0015] The outlet end of the extraction water pipe extends to the center of the ester material outlet pipe in the lower layer of the ester water separator, so that the incoming cleaning medium diffuses outward along the radial section of the pipe to fully wash away the methanol impurities dissolved inside the crude ester.

[0016] The horizontal height of the inlet of the overflow pipe at the top of the esterification tank is higher than the horizontal height of the inlet on the side wall of the esterification water tank, guiding the upper light phase liquid to flow across the weir plate at the pipe opening and into the secondary settling chamber by relying on the natural liquid level difference.

[0017] The bottoms of the batching tank, the high-level mixing tank, the esterification tank, the esterification aqueous phase tank, the esterification ester phase tank, and the crude ester intermediate tank are all supported on the same horizontal ground reference surface, eliminating shear deformation stress caused by uneven equipment heights at pipeline interfaces and unifying the drainage elevation reference.

[0018] Compared with the prior art, this application has at least the following beneficial effects: 1. This utility model relies on the layout of primary ester-water separation, intermediate stage water injection extraction, and downstream long-cycle aqueous phase sedimentation connecting pipeline to achieve stepwise purification and extraction of dissolved and microemulsified reaction products in the aqueous system. This reduces the loss ratio caused by the separation and discharge of crude ester liquid with wastewater and improves the overall utilization rate of raw materials and the yield of materials in the system.

[0019] 2. This utility model uses a local heat exchange and cooling component configured in the vapor phase outlet area at the top of the tower to intercept the high-boiling-point unreacted raw materials carried by the escaping mixed vapor, forcing the heavy component droplets to flow back down to the bottom heated reaction zone. This reduces the loss of unconverted acid components at the front end while controlling the vapor-liquid equilibrium temperature at the top of the distillation tower. Attached Figure Description

[0020] To more intuitively illustrate the prior art and this application, exemplary drawings are provided below. It should be understood that the specific shapes and structures shown in the drawings should not generally be regarded as limiting conditions for implementing this application; for example, based on the technical concept disclosed in this application and the exemplary drawings, those skilled in the art are able to easily make conventional adjustments or further optimizations to the addition / reduction / classification, specific shapes, positional relationships, connection methods, size ratios, etc. of certain units (components).

[0021] Figure 1 This is a three-dimensional schematic diagram of a device for increasing the crude ester content in the production process of methyl chloroacetate according to the present invention; Figure 2 This is a schematic diagram of the bottom structure of a device for increasing the crude ester content during the production of methyl chloroacetate according to this utility model; Figure 3 This is a schematic diagram of the forced cooler of a device for increasing the crude ester content in the production process of methyl chloroacetate according to this utility model.

[0022] Explanation of reference numerals in the attached figures: 1. Batching vessel; 2. Batching vessel cooler; 3. Batching vessel feed pump; 4. Mixture high-level tank; 5. Esterification vessel; 6. Methanol replenishment high-level tank; 7. Esterification tower; 8. Forced cooler; 9. Condenser; 10. Ester-water separator; 11. Extraction water pipe; 12. Esterification aqueous phase tank; 13. Esterification ester phase tank; 14. Crude ester intermediate tank; 15. Crude ester transfer pump; 16. Raw material feed pipe. Detailed Implementation

[0023] To make the objectives, technical solutions, and advantages of this utility model clearer, the technical solutions in the embodiments of this utility model will be clearly and completely described below with reference to the accompanying drawings. Obviously, the described embodiments are only a part of the embodiments of this utility model, and not all of them. All other embodiments obtained by those skilled in the art based on the embodiments of this utility model without creative effort are within the scope of protection of this utility model. Example

[0024] Please refer to Figures 1 to 3 This utility model provides a device for increasing the crude ester content during the production of methyl chloroacetate, aiming to solve the problems in the prior art where the lack of a multi-stage stratified recovery process in esterification production leads to the loss of crude ester material dissolved in the aqueous phase and poor impurity separation results in low product purity. The device for increasing the crude ester content in the production process of methyl chloroacetate includes a batching tank 1 and a raw material feed pipe 16 connected to the upper part of the batching tank 1. The batching tank 1 is used to mix the fed methyl chloroacetate with methanol in the liquid phase. The bottom outlet of the batching tank 1 is connected to the inlet of the batching tank feed pump 3 through a pipeline. The batching tank feed pump 3 is used to provide fluid dynamic pressure for the pipeline transportation of the mixed liquid. The discharge port of the batching tank feed pump 3 is connected to the top inlet of the high-level mixing tank 4 through a pipeline. The high-level mixing tank 4 is used for high-level temporary storage of the mixture. The bottom overflow pipe of the high-level mixing tank 4 is connected to the upper inlet of the esterification tank 5. The esterification tank 5 is used to contain the reactants and provide the closed heating space required for the esterification reaction. The top gas phase pipe of the esterification reactor 5 is connected to the bottom of the esterification tower 7. The esterification tower 7 is used to perform vapor-liquid contact and mass heat exchange on the gas phase mixture generated by the reaction. The top gas phase outlet pipe of the esterification tower 7 is connected to the feed end of the condenser 9. The condenser 9 is used to exchange heat with the high-temperature steam sent from the gas phase pipe, cool it down and liquefy it into a mixture. The bottom liquid outlet pipe of the condenser 9 is connected to the top of the ester-water separator 10. The ester-water separator 10 is used to perform initial gravity settling and stratification of the liquid mixture by utilizing the density difference of the materials. Extraction water pipe 11 is connected to the lower ester material discharge pipe of ester water separator 10. Extraction water pipe 11 is used to simultaneously draw clean water into the crude ester liquid flowing through the pipe for washing methanol impurities. The upper aqueous phase discharge pipe of ester water separator 10 is connected to the top of esterification aqueous phase tank 12. The lower ester material discharge pipe of ester water separator 10 is connected to the top of esterification ester phase tank 13 through extraction water pipe 11. Esterification ester phase tank 13 is used for secondary purification and stratification of the crude ester mixture after water washing. The overflow pipe at the top of the esterification ester phase tank 13 is connected to the side wall of the esterification aqueous phase tank 12. The esterification aqueous phase tank 12 is used to retain the aqueous phase liquid that flows in from the front end for a long time so as to settle the trace amount of crude ester entrained at the bottom. The discharge pipe at the bottom of the esterification ester phase tank 13 is connected to the top of the crude ester intermediate tank 14. The sedimentation discharge pipe at the bottom of the esterification aqueous phase tank 12 is connected to the side wall of the crude ester intermediate tank 14. The crude ester intermediate tank 14 is used to centrally receive and temporarily store the qualified crude ester liquid separated and settled from each branch pipe.

[0025] To solve the above-mentioned technical problems, the device for increasing the crude ester content in the methyl chloroacetate production process also includes a forced cooler 8. The forced cooler 8 is fixedly inserted into the top of the esterification tower 7. The forced cooler 8 uses the heat exchange surface of the refrigerant to cool the rising mixed steam and form a local condensation zone at the top of the tower so that the high-boiling-point chloroacetic acid droplets that escape fall back to the lower part of the esterification tower 7.

[0026] The gas phase outlet pipe at the top of the batching vessel 1 is connected to the gas inlet of the batching vessel cooler 2, and the reflux liquid outlet pipe at the bottom of the batching vessel cooler 2 is connected to the inside of the batching vessel 1. The batching vessel cooler 2 is used to receive the methanol vapor that is heated and volatilized during the mixing process of the batching vessel 1 and to force it to liquefy and guide it back to the batching liquid phase zone to circulate and participate in the mixing.

[0027] The bottom discharge pipe of the methanol replenishment tank 6 is connected to the middle of the side wall of the esterification reactor 5. The methanol replenishment tank 6 is used to replenish liquid methanol solution into the esterification reactor 5 at a constant pressure and volume during the heated reaction process of the system. In order to construct a fluid pipeline network that relies on gravitational potential energy to transport materials, the horizontal height of the overflow pipe at the bottom of the mixed liquid high-level tank 4 is higher than the horizontal height of the feed inlet at the top of the esterification reactor 5, and the horizontal height of the discharge pipe at the bottom of the methanol replenishment tank 6 is higher than the horizontal height of the feed inlet at the middle of the side wall of the esterification reactor 5.

[0028] The outlet end of the extraction water pipe 11 extends to the center of the lower ester material outlet pipe of the ester water separator 10. This embedded plug-in pipe structure allows the incoming washing water to radially permeate and diffuse along the cross-sectional axis of the ester material fluid pipe to the outer boundary to wash away methanol impurities dissolved in the crude ester of the oil phase.

[0029] The horizontal height of the inlet of the overflow pipe at the top of the esterification tank 13 is higher than the horizontal height of the inlet on the side wall of the esterification water tank 12. This fluid height difference pipeline design guides the upper layer of ester-containing water liquid that has undergone secondary static separation to flow over the baffle and into the esterification water tank 12 for long-term sedimentation and recovery by relying on the natural liquid level difference. The feed inlet of the crude ester transfer pump 15 is connected to the bottom outlet of the crude ester intermediate tank 14, and the discharge pipe of the crude ester transfer pump 15 is connected to the feed pipeline of the distillation process. The crude ester transfer pump 15 is used to apply positive pressure of pumping fluid to discharge qualified bottom-purified crude ester.

[0030] The bottoms of the batching vessel 1, the high-level mixing tank 4, the esterification vessel 5, the esterification aqueous phase tank 12, the esterification ester phase tank 13, and the crude ester intermediate tank 14 are all supported on the same horizontal ground reference surface. This flat-bottom support installation form establishes a unified structural reference for the elevation design of the gravity drainage pipeline network of the entire set of reaction vessels and the static settling tank components.

[0031] Based on the above embodiments, the present invention may further include the following preferred technical solutions: In a preferred embodiment, in order to retain high-boiling-point reactants and control the vapor-liquid equilibrium temperature at the top of the tower, the outer flange of the forced cooler 8 is sealed and locked to the top opening of the esterification tower 7. The forced cooler 8 is equipped with a cooling medium tube bundle, and the outer wall of the heat exchange tube bundle contacts the rising mixed gas phase to force the heavy component chloroacetic acid to drip back into the liquid phase reaction zone.

[0032] In a preferred embodiment, in order to recover the light components that volatilize during the batching stage, the gas phase outlet pipe at the top of the batching vessel 1 is connected to the gas inlet of the batching vessel cooler 2 via a flange, and the reflux liquid outlet pipe at the bottom of the batching vessel cooler 2 is connected to the interior of the batching vessel 1. Circulating cooling water flows in the shell side of the batching vessel cooler 2 to quickly exchange heat and cool down the high-temperature methanol vapor entering the tube side, transforming it into a liquid phase.

[0033] In a preferred embodiment, in order to maintain a constant molar ratio in the internal system of the esterification reaction vessel, the bottom discharge pipe flange of the methanol replenishment tank 6 is connected to the middle of the side wall of the esterification vessel 5. The liquid inlet position in the middle allows the liquid methanol replenishment liquid to quickly penetrate the gas-liquid interface and integrate into the main body of the boiling reaction liquid phase.

[0034] In a preferred embodiment, in order to construct a fluid transport network that does not require power pumping, the horizontal height of the overflow pipe at the bottom of the high-level tank 4 is higher than the horizontal height of the feed inlet at the top of the esterification vessel 5, and the horizontal height of the discharge pipe at the bottom of the high-level tank 6 for adding methanol is higher than the horizontal height of the feed inlet at the middle of the side wall of the esterification vessel 5. The gravity potential energy difference drives the fluid to overcome the frictional resistance along the pipeline and smoothly pour it into the downstream working chamber.

[0035] In a preferred embodiment, in order to increase the specific surface area of ​​mass transfer in liquid-liquid extraction, the outlet end of the extraction water pipe 11 extends to the center of the lower ester material outlet pipe of the ester water separator 10. The washing water diffuses outward along the radial section of the pipe through the insertion port and cuts and mixes with the downward moving crude ester fluid.

[0036] In a preferred embodiment, in order to achieve continuous self-overflow splitting of the phase-separated liquid, the horizontal height of the inlet of the overflow pipe at the top of the esterification phase tank 13 is higher than the horizontal height of the inlet on the side wall of the esterification water phase tank 12. The height difference of the pipe network drives the upper light phase alcohol-containing aqueous solution, after physical settling and stratification, to continuously overflow the overflow pipe weir and fall into the secondary long-period settling chamber.

[0037] In a preferred embodiment, in order to ensure the stable operation of the gravity diversion system and eliminate the shear deformation stress caused by uneven settlement of the equipment at the pipeline interface, the bottoms of the batching tank 1, the high-level mixing tank 4, the esterification tank 5, the esterification aqueous phase tank 12, the esterification ester phase tank 13, and the crude ester intermediate tank 14 are all supported on the same horizontal ground reference surface. The inlet of the crude ester transfer pump 15 is connected to the outlet at the bottom of the crude ester intermediate tank 14, and the end of the outlet pipe of the crude ester transfer pump 15 is connected to the feed pipeline of the distillation process.

[0038] Working principle: Chloroacetic acid and methanol liquid raw materials are discharged into the mixing tank 1 through the raw material feed pipe 16 and stirred. The methanol vapor that is heated and volatilized rises along the gas phase pipeline to the gas inlet of the mixing tank cooler 2. It is cooled and liquefied by heat exchange with the circulating cooling water in the shell side. After liquefaction, it falls back into the liquid phase of the mixing tank 1 through the bottom return liquid outlet pipeline to participate in the circulating mixing.

[0039] The mixed liquid is pressurized and pumped by the feed pump 3 to the high-level tank 4 for temporary storage. The liquid is continuously injected into the esterification tank 5 by the spatial gravitational potential energy difference formed by the horizontal height of the bottom overflow pipe being higher than the horizontal height of the feed inlet at the top of the esterification tank 5. At the same time, the methanol replenishment tank 6 uses the hydrostatic pressure of the bottom discharge pipe being higher than the horizontal height of the feed inlet in the middle of the side wall of the esterification tank 5 to continuously replenish the methanol solution into the esterification tank 5. The material is heated to the boiling state in the esterification tank 5 and undergoes a liquid phase esterification reaction to produce ternary azeotropic vapor, which rises and enters the esterification tower 7.

[0040] The rising gaseous mixture encounters the surface of the forced cooler 8 inside the esterification tower 7 and undergoes heat exchange and cooling. The high-boiling-point chloroacetic acid component is intercepted by the local condensation zone and turns into droplets that fall back to the bottom reaction zone. The low-boiling-point crude ester gaseous material that passes through the barrier of the forced cooler 8 flows into the condenser 9 through the fluid pipeline and undergoes heat exchange to change into a liquid fluid before being introduced into the chamber of the ester-water separator 10.

[0041] The material is statically separated into layers by density gradient inside the ester-water separator 10. The less dense alcohol-containing aqueous phase floats to the top and is discharged into the esterification aqueous phase tank 12 through the overflow pipe. The more dense crude ester heavy phase sinks and is discharged into the bottom pipe. Simultaneously, clean water is continuously injected into the core of the crude ester liquid flow through the extraction water pipe 11, which extends from the liquid outlet end to the center of the lower layer ester material discharge pipe of the ester-water separator 10, to perform a radial diffusion washing action to remove residual water-soluble methanol impurities.

[0042] After washing with water, the emulsified crude ester solution flows into the esterification phase tank 13 for secondary gravity phase separation and settling. Due to the geometric difference in the height of the inlet of the liquid being higher than that of the inlet of the side wall of the esterification water phase tank 12, the surface alcohol-containing washing water continuously flows across the weir plate of the pipe into the esterification water phase tank 12 for extended period of particle sedimentation. The purified crude ester at the bottom of the esterification phase tank 13 and the liquid methyl ester that slowly settles and accumulates at the bottom of the esterification water phase tank 12 are guided together into the crude ester intermediate tank 14 for centralized storage. Finally, the crude ester is pumped out to the feed pipeline of the distillation process by the crude ester transfer pump 15 to establish positive pressure.

[0043] The above content is only a specific embodiment of this utility model. The protection scope of this utility model is not limited thereto. Any changes or substitutions that can be easily conceived by those skilled in the art within the scope of the technology disclosed in this utility model should be included within the protection scope of this utility model. The protection scope of this utility model shall be subject to the final approved content.

Claims

1. An apparatus for increasing the crude ester content in the production process of methyl chloroacetate, comprising a batching tank (1) and a pipeline connected to a raw material feed pipe (16) at the top of the batching tank (1); characterized in that, The bottom outlet of the mixing tank (1) is connected to the inlet of the mixing tank feed pump (3) via a pipe. The outlet of the mixing tank feed pump (3) is connected to the top inlet of the high-level mixing tank (4) via a pipe. The overflow pipe at the bottom of the high-level mixing tank (4) is connected to the upper inlet of the esterification tank (5). The top gas phase pipe of the esterification tank (5) is connected to the bottom of the esterification tower (7). The top gas phase outlet pipe of the esterification tower (7) is connected to the inlet of the condenser (9). The bottom liquid outlet pipe of the condenser (9) is connected to the top of the ester-water separator (10). The extraction water pipe (11) is inserted through and connected to the... The lower layer of the ester-water separator (10) has an ester material discharge pipe; the upper layer of the ester-water separator (10) has an aqueous phase discharge pipe connected to the top of the esterification aqueous phase tank (12); the lower layer of the ester-water separator (10) has an ester material discharge pipe connected to the top of the esterification ester phase tank (13) via the extraction water pipe (11); the upper part of the esterification ester phase tank (13) has an overflow pipe connected to the side wall of the esterification aqueous phase tank (12); the bottom of the esterification ester phase tank (13) has a discharge pipe connected to the top of the crude ester intermediate tank (14); and the bottom of the esterification aqueous phase tank (12) has a sedimentation discharge pipe connected to the side wall of the crude ester intermediate tank (14).

2. The apparatus for increasing the crude ester content in the production process of methyl chloroacetate according to claim 1, characterized in that, The top gas phase outlet pipe of the batching vessel (1) is connected to the air inlet of the batching vessel cooler (2), and the bottom reflux liquid outlet pipe of the batching vessel cooler (2) is connected to the interior of the batching vessel (1).

3. The apparatus for increasing the crude ester content in the production process of methyl chloroacetate according to claim 1, characterized in that, The bottom discharge pipe of the methanol replenishment tank (6) is connected to the middle of the side wall of the esterification reactor (5).

4. The apparatus for increasing the crude ester content in the production process of methyl chloroacetate according to claim 1, characterized in that, A forced cooler (8) is fixedly inserted into the top of the esterification tower (7).

5. The apparatus for increasing the crude ester content in the production process of methyl chloroacetate according to claim 1, characterized in that, The inlet of the crude ester transfer pump (15) is connected to the bottom outlet of the crude ester intermediate tank (14), and the outlet pipe of the crude ester transfer pump (15) is connected to the feed line of the distillation process.

6. The apparatus for increasing the crude ester content in the production process of methyl chloroacetate according to claim 1, characterized in that, The overflow pipe at the bottom of the high-level tank (4) is at a higher level than the feed inlet at the top of the esterification vessel (5).

7. The apparatus for increasing the crude ester content in the production process of methyl chloroacetate according to claim 3, characterized in that, The discharge pipe at the bottom of the methanol replenishment tank (6) is at a higher level than the feed inlet at the middle of the side wall of the esterification reactor (5).

8. The apparatus for increasing the crude ester content in the production process of methyl chloroacetate according to claim 1, characterized in that, The outlet end of the extraction water pipe (11) extends into the center of the ester material outlet pipe in the lower layer of the ester water separator (10).

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