An ethoxy, propoxy reaction system

Abstract

The application discloses an ethylene-propylene oxyalkylation reaction system, which comprises a reaction kettle, wherein the reaction kettle comprises a first reaction cavity and a second reaction cavity which are sequentially communicated; a plurality of uniform material pipes which are in communication are arranged in the first reaction cavity; the uniform material pipes are in annular structure and a plurality of first nozzles are arranged at equal intervals along the circumferential direction of the uniform material pipes; a feeding cavity is arranged on the outer side of the first reaction cavity; a plurality of discharge pipes are arranged on the feeding cavity at equal intervals along the circumferential direction of the feeding cavity; and a discharge port is arranged at the bottom end of the second reaction cavity; the discharge port is communicated with a first circulating pipeline and a second circulating pipeline which are located on the outer side of the reaction kettle; a shielding pump is arranged on the first circulating pipeline and the second circulating pipeline and the flow ratio of the two is 1:2; the outlet of the first circulating pipeline is inserted into the second reaction cavity; the outlet of the second circulating pipeline penetrates through the first reaction cavity and is communicated with the uniform material pipes; and the first circulating pipeline and the second circulating pipeline are respectively matched with a first heat exchanger which is used for heat exchange of the materials in the first circulating pipeline and the second circulating pipeline, so that the growth ratio of the entire addition reaction is effectively increased.

Description

Technical Field

[0001] This invention relates to the field of eth / propoxylation reaction system technology, and in particular to an eth / propoxylation reaction system. Background Technology

[0002] In existing technologies, ethoxylation reactions—nucleophilic addition reactions of ethylene oxide / propane with compounds such as fatty alcohols, fatty acids, alkylphenols, fatty amines, and alkylamides—are collectively referred to as ethoxylation reactions. It is a very vigorous exothermic chemical reaction with considerable danger. Therefore, in industrial production, strict control of the reaction intensity and effective heat removal measures must be implemented. The reaction mechanism is as follows: A) Ethoxylation of alcohol ethers: ROH + nCH2CH2O — RO(CH2CH2O)nH + Q; B) Ethoxylation of alkylphenol ethers: RC2H4OH + nCH2CH2O — RC2H4O(CH2CH2O)nH + Q; Specific ethoxylation reaction forms include: a) stirred tank reactor, b) spray contact reactor; depending on the product type, chain growth ratio, and scale, it can be divided into first-generation, second-generation, and third-generation reaction systems. Fourth-generation reactor systems have not been widely adopted. However, stirred tank reactors have been gradually phased out of the market due to their rudimentary equipment, low level of automation, poor product quality, and the inevitable wear of seals on the stirring shaft which may cause sparks, resulting in low safety performance.

[0003] Traditional ethoxylation process description: 1) Initiator preparation (raw materials and catalyst); Initiator pre-reaction and dehydration: Under nitrogen protection, the initiator is pumped into the reactor, and the catalyst is added. 2) Reaction; The system is evacuated and purged with nitrogen 1-3 times to ensure the oxygen content in the system is less than 10 PPM. 3) External circulation is activated, and the initiator is heated and dehydrated. 4) Cycloethylene addition reaction. 5) Maturation: After the cycloethylene addition is completed, a small amount of ethylene oxide remains in the gas phase and materials of the reactor, requiring maturation. The reactants continue to circulate for about 30 minutes until the cycloethylene is completely reacted. The degree of maturation is determined by the reactor pressure; maturation ends when the residual pressure of the reactor remains constant. 6) Cooling, neutralization, and degassing; After the reaction, the reactor is cooled to below 90 degrees Celsius, neutralized with a neutralizing agent, and the remaining gas in the reactor is discharged to the tail gas treatment unit.

[0004] A schematic diagram of a traditional single external circulation ethoxylation reaction system is shown below. Figure 1As shown, its disadvantages are: 1) It requires a large circulation volume at the beginning, and the minimum amount of initiator must be ensured, so the growth ratio of the addition reaction cannot be effectively scaled up. 2) It requires at least 8 cycles to complete the reaction of ethylene oxide to more than 99.9%, resulting in low reaction efficiency. 3) Due to the low reaction efficiency, the volume of the reactor cannot be effectively increased, a) resulting in relatively small production capacity, b) high unreacted EO content in the pipeline, which is a serious safety hazard. Once the pump leaks or the flange connection leaks, the consequences are unimaginable. c) Due to the low reaction efficiency, residual ethylene oxide is emitted into the tail gas treatment system, causing environmental problems.

[0005] In traditional dual-external-circulation eth / propoxylation reaction systems, the conventional dual-circulation combined external-circulation reactor uses two interconnected chamber tanks, such as... Figure 2 As shown, or a combination of a horizontal tank and a vertical reaction vessel can be used, such as... Figure 3 As shown, two centrifugal pumps are used to circulate the reaction into two reactors (horizontal plus horizontal, vertical plus horizontal) to increase the amount of reaction and improve the reaction efficiency. The main features of this reactor are: (1) It adopts a semi-batch operation mode (the raw material initiator and catalyst are added to the reactor at one time, while the specified amount of reactant EO is added continuously); (2) The heat of reaction is removed through an external heat exchanger, and the reaction temperature is accurately controlled; (3) The top of the reactor is the gas phase and the bottom is the liquid phase; (4) The liquid mixture at the bottom of the reactor enters the top of the reactor through external circulation, and after passing through the nozzle, it is atomized into fine droplets (dispersed phase) and diffuses into the EO gas phase (continuous phase) to ensure a high gas-liquid contact area; (5) A certain amount of inert protective gas nitrogen is introduced into the reactor to prevent EO from exploding and to inhibit its decomposition.

[0006] However, the traditional dual-circulation combined external circulation reaction system has the following disadvantages: 1) Although the combination of two reactors increases the amount of reaction per unit time, the reaction efficiency is not improved; 2) It still requires at least 8 cycles to complete more than 99% of the ethylene oxide reaction, resulting in long reaction time, low reaction efficiency, and relatively low safety performance; 3) a) Relatively small production capacity; b) High content of unreacted EO in the pipeline, which is a serious safety hazard. Once the pump or flange connection leaks, the consequences are unimaginable; c) Due to the problem of reaction efficiency, residual ethylene oxide is emitted into the tail gas treatment system, causing environmental problems. 4) Due to the horizontal tank setting, the reactor shape is unreasonable, and the interior is not polished, making it very difficult to clean the reactor, resulting in incomplete reaction, large wastewater volume, and large waste gas volume, which is not environmentally friendly; 5) Using two pumps and two circulation loops increases equipment investment costs. Summary of the Invention

[0007] The purpose of this invention is to provide an ethylene and propoxylation reaction system to solve the problems existing in the prior art. In the initial dropwise addition of ethylene oxide or propylene oxide, a small amount of initiator and catalyst are circulated using a first circulation pipeline. After the flow rate of ethylene oxide or propylene oxide is increased, the circulation amount of initiator and catalyst is increased using a second circulation pipeline, which effectively increases the growth ratio of the entire addition reaction.

[0008] To achieve the above objectives, the present invention provides the following solution: The present invention provides an ethoxylation reaction system, including a reaction vessel, the reaction vessel including a first reaction chamber and a second reaction chamber connected in sequence, the first reaction chamber being provided with a plurality of interconnected uniform feeding pipes, the uniform feeding pipes having an annular structure and being provided with a plurality of first nozzles at equal intervals along their circumference, each of the first nozzles facing the center of the first reaction chamber, a feeding chamber being provided on the outside of the first reaction chamber, the feeding chamber being provided with a plurality of discharge pipes distributed at equal intervals along their circumference, the discharge pipes passing through the first reaction chamber and facing the center of the first reaction chamber, and the feeding chamber being connected to a feeding mechanism, the feeding mechanism being provided with a feeding pump for pumping materials, the second reaction chamber being located below the first reaction chamber, and a discharge port being provided at the bottom end of the second reaction chamber;

[0009] The discharge port is connected to a first circulation pipeline and a second circulation pipeline located outside the reactor. Both the first and second circulation pipelines are connected to a shielded pump, and the flow ratio between the two is 1:2. The outlet of the first circulation pipeline extends into the second reaction chamber, and the outlet of the second circulation pipeline passes through the first reaction chamber and is connected to the uniform material pipe. Both the first and second circulation pipelines are equipped with a first heat exchanger for heat exchange of the internal materials.

[0010] Preferably, the discharge port is connected to the shielded pump, and the first circulation pipeline and the second circulation pipeline are connected in parallel at the outlet of the shielded pump.

[0011] Preferably, the first heat exchanger is a rotary plate heat exchanger.

[0012] Preferably, the outlet of the first circulation pipeline is connected to a spray pipe, the outlet end of the spray pipe passes through the first reaction chamber from top to bottom and extends into the second reaction chamber, and a Venturi tube is provided between the first circulation pipeline and the spray pipe to draw the remaining material in the feed chamber into the spray pipe.

[0013] Preferably, a first valve is provided at the inlet end of both the first circulation pipeline and the second circulation pipeline.

[0014] Preferably, a connecting pipe is connected between the discharge port and the shielded pump, and the connecting pipe is connected to an initiator supply pipeline, the outlet end of which is provided with a second valve.

[0015] Preferably, the discharge port is connected to a collection chamber, the radial cross-section of the collection chamber gradually decreases from top to bottom, and the connecting pipe is connected to the bottom end of the collection chamber.

[0016] Preferably, the uniform material tube includes a warp tube and at least one weft tube, the warp tube is connected to each of the weft tubes and is perpendicular to the weft tubes, the warp tube is connected to the first pipeline, and each of the first nozzles is disposed on the weft tube.

[0017] Preferably, the outlet end of the discharge pipe is connected to a second nozzle.

[0018] Preferably, the feeding mechanism is provided with a feeding pipe connected to the feeding pump, and the feeding pipe is also equipped with a second heat exchanger for exchanging heat with the material inside it.

[0019] The present invention achieves the following technical effects compared to the prior art:

[0020] First, by setting up a first circulation pipeline and a second circulation pipeline both connected to the outlet on the outside of the reactor, with a flow ratio of 1:2, the initiator is circulated through the first circulation pipeline in the earliest cycle, allowing for a smaller amount of initiator to react with the added ethylene oxide or propylene oxide. After the reaction has proceeded for a period of time, the feeding mechanism fully supplies the feed chamber, causing ethylene oxide or propylene oxide to be sprayed towards the center of the first reaction chamber through the feed chamber and the outlet pipe. At this time, the second circulation pipeline is activated, allowing the initiator, catalyst, and corresponding products to be sprayed towards the center of the first reaction chamber through the uniform distribution pipe and each first nozzle, making impact contact with the ethylene oxide and propylene oxide sprayed at the center of the first reaction chamber. This increases the amount of contact reaction between the two, thereby effectively increasing the growth ratio of the addition reaction.

[0021] Second, the discharge port is connected to a shielded pump, and the first circulation pipeline and the second circulation pipeline are connected in parallel at the outlet of the shielded pump. The first circulation pipeline and the second circulation pipeline share the same shielded pump to reduce the cost of use.

[0022] Third, the first heat exchanger is a rotary plate heat exchanger, which improves the efficiency of heat exchange for materials in the first and second circulation pipelines.

[0023] Fourth, the outlet of the first circulation pipeline is connected to an injection pipe. The outlet end of the injection pipe passes through the first reaction chamber from top to bottom and extends into the second reaction chamber. A Venturi tube is provided between the first circulation pipeline and the injection pipe to draw the remaining material in the feed chamber into the injection pipe. By setting the Venturi tube, a pressure difference is generated after the material in the first circulation pipeline enters the Venturi tube, and the remaining material in the feed chamber is drawn in. As a result, the unreacted ethylene oxide and propylene oxide react fully with the initiator in the injection pipe, which fully reduces the residual amount of ethylene oxide and propylene oxide and ensures the environmental protection effect of the entire device. Attached Figure Description

[0024] To more clearly illustrate the technical solutions in the embodiments of the present invention or the prior art, the drawings used in the embodiments will be briefly introduced below. Obviously, the drawings described below are only some embodiments of the present invention. For those skilled in the art, other drawings can be obtained based on these drawings without creative effort.

[0025] Figure 1 This is a schematic diagram of a traditional single external circulation ethoxylation reaction system;

[0026] Figure 2 Schematic diagram of a traditional dual external circulation ethoxylation reaction system Figure 1 ;

[0027] Figure 3 Schematic diagram of a traditional dual external circulation ethoxylation reaction system Figure 2 ;

[0028] Figure 4 This is a schematic diagram of the overall structure of the present invention;

[0029] Figure 5 This is a schematic diagram of the reactor structure of the present invention;

[0030] Among them, 1-first circulation pipeline, 2-second circulation pipeline, 3-reaction vessel, 4-first heat exchanger, 5-second heat exchanger, 6-shielded pump, 7-Venturi tube, 8-suction pipe, 9-feeding mechanism, 10-discharge pipe, 11-feeding chamber, 12-weft pipe, 13-meridian pipe, 14-first nozzle, 15-second reaction chamber, 16-first reaction chamber, 17-collection chamber. Detailed Implementation

[0031] The technical solutions of the embodiments of the present invention will be clearly and completely described below with reference to the accompanying drawings. Obviously, the described embodiments are only some embodiments of the present invention, and not all embodiments. Based on the embodiments of the present invention, all other embodiments obtained by those skilled in the art without creative effort are within the scope of protection of the present invention.

[0032] The purpose of this invention is to provide an ethylene and propoxylation reaction system to solve the problems existing in the prior art. In the initial dropwise addition of ethylene oxide or propylene oxide, a small amount of initiator and catalyst are circulated using a first circulation pipeline. After the flow rate of ethylene oxide or propylene oxide is increased, the circulation amount of initiator and catalyst is increased using a second circulation pipeline, which effectively increases the growth ratio of the entire addition reaction.

[0033] To make the above-mentioned objects, features and advantages of the present invention more apparent and understandable, the present invention will be further described in detail below with reference to the accompanying drawings and specific embodiments.

[0034] like Figures 1 to 5 As shown, this embodiment provides an ethoxylation reaction system, including a reaction vessel 3. The reaction vessel 3 includes a first reaction chamber 16 and a second reaction chamber 15 connected in sequence. The first reaction chamber 16 is provided with several interconnected uniform distribution pipes. The uniform distribution pipes have an annular structure and are provided with several first nozzles 14 at equal intervals along their circumference, so as to atomize the initiator and catalyst through the first nozzles 14. Each first nozzle 14 faces the center of the first reaction chamber 16, thereby allowing the atomized material to be introduced into the center. A feed chamber 11 is provided on the outside of the first reaction chamber 16, and several discharge pipes 1 are provided on the feed chamber 11 at equal intervals along its circumference. 0. The discharge pipe 10 passes through the first reaction chamber 16 and is positioned towards the center of the first reaction chamber 16. The material is evenly distributed through the feed chamber 11 and the discharge pipe 10. The feed chamber 11 is connected to the feeding mechanism 9, which is equipped with a feeding pump to provide power for the injection of ethylene oxide or propylene oxide. The second reaction chamber 15 is located below the first reaction chamber 16. The bottom of the second reaction chamber 15 is provided with a discharge port. That is, after the initiator reacts with ethylene oxide or propylene oxide in the first reaction chamber 16, the products and the remaining materials flow into the second reaction chamber 15 to carry out the remaining reaction and the accumulation of products.

[0035] The discharge port is connected to a first circulation pipe 1 and a second circulation pipe 2 located outside the reactor 3. Both the first circulation pipe 1 and the second circulation pipe 2 are connected to a shielded pump 6, and the flow ratio between the two is 1:2. The outlet of the first circulation pipe 1 extends into the second reaction chamber 15, and the outlet of the second circulation pipe 2 passes through the first reaction chamber 16 and is connected to the uniform material pipe. Both the first circulation pipe 1 and the second circulation pipe 2 are equipped with a first heat exchanger 4 for heat exchange of the materials inside. Through the heat exchange function of the first heat exchanger 4, heat can be removed and transferred in simultaneously. Specifically, during the initiator heating and dehydration stage, steam is introduced into the heat transfer pipe of the first heat exchanger 4 to transfer heat and exchange heat with the first circulation pipe 1 or the second circulation pipe 2 to heat the initiator in the two circulation pipes and dehydrate it. When ethylene oxide is introduced, cooling water is introduced into the heat transfer pipe of the first heat exchanger 4 to remove the heat generated by the addition reaction, so as to reuse the heat and reduce energy consumption. Preferably, the first circulation pipe 1 has a diameter of 80 mm, and the second circulation pipe 2 has a diameter of 125 mm. The flow rate ratio is controlled by adjusting the pipe diameter and its resistance. The first circulation pipe 1 is a small circulation, with a circulation volume half that of the second circulation pipe 2. When the addition reaction begins, the first circulation pipe 1 is used for small circulation first. Once a certain volume is reached, the second circulation pipe 2 is then opened for large circulation. This ensures that the addition reaction can proceed even with a small initial amount of initiator, thus increasing the growth rate of the addition reaction. Furthermore, the heat exchanger 4 on the first circulation pipe 1 has a heat exchange area of ​​35 m². 2 The heat exchange area of ​​the first heat exchanger 4 on the second circulation pipeline 2 is 45 m². 2 .

[0036] By setting a first circulation pipe 1 and a second circulation pipe 2, both connected to the discharge port, on the outside of the reactor 3, with a flow ratio of 1:2, the initiator is circulated through the first circulation pipe 1 in the earliest cycle, allowing for a smaller amount of initiator to react with the added ethylene oxide or propylene oxide. After the reaction has proceeded for a period of time, the feeding mechanism 9 fully supplies the feed chamber 11, causing ethylene oxide or propylene oxide to be sprayed towards the center of the first reaction chamber 16 through the feed chamber 11 and the discharge pipe 10. At this time, the second circulation pipe 2 is activated, allowing the initiator, catalyst, and corresponding products to be sprayed towards the center of the first reaction chamber 16 through the uniform distribution pipe and each first nozzle 14. This allows for impact contact with the ethylene oxide and propylene oxide sprayed at the center of the first reaction chamber 16, increasing the amount of contact reaction and ensuring a full reaction of the ethylene oxide or propylene oxide, thereby effectively increasing the growth ratio of the addition reaction. Furthermore, the entire device uses the combination of the first circulation pipeline 1 and the second circulation pipeline 2, which more rationally controls the circulation flow ratio than the traditional dual circulation, thereby improving the reaction efficiency. It achieves the reaction purpose with less energy circulation and uses one reactor 3 for reaction, instead of the traditional two devices that need to react at the same time. This is energy-saving, safe and efficient, thus achieving the maximum output with the minimum energy consumption.

[0037] The discharge port is connected to a shielded pump 6. The first circulation pipeline 1 and the second circulation pipeline 2 are connected in parallel at the outlet of the shielded pump 6. The first circulation pipeline 1 and the second circulation pipeline 2 share the same shielded pump 6 to reduce the cost of use.

[0038] Preferably, the first heat exchanger 4 is a rotary plate heat exchanger, which improves the efficiency of heat exchange for materials in the first circulation pipeline 1 and the second circulation pipeline 2.

[0039] In a preferred embodiment of the present invention, the outlet of the first circulation pipeline 1 is connected to a spray pipe. The outlet end of the spray pipe passes through the first reaction chamber 16 from top to bottom and extends into the second reaction chamber 15. A Venturi tube 7 is provided between the first circulation pipeline 1 and the spray pipe to draw the remaining material in the feed chamber 11 into the spray pipe. By setting the Venturi tube 7, a pressure difference is generated after the material in the first circulation pipeline 1 enters the Venturi tube 7, and the remaining material in the feed chamber 11 is drawn in. As a result, the unreacted ethylene oxide and propylene oxide react fully with the initiator in the spray pipe, effectively reducing the residual amount of ethylene oxide and propylene oxide and ensuring the environmental protection effect of the entire device. Preferably, a suction pipe 8 is connected between the Venturi tube 7 and the feed chamber 11.

[0040] Furthermore, the inlet ends of the first circulation pipeline 1 and the second circulation pipeline 2 are each equipped with a first valve, which can be opened according to different reaction stages.

[0041] Furthermore, a connecting pipe connects the discharge port to the shielded pump 6, and the connecting pipe is connected to the initiator supply pipeline. The initiator is polyether or the like. A second valve is provided at the outlet end of the initiator supply pipeline, so that the supply pipeline and the connecting pipe can be connected by opening the second valve, allowing the initiator to enter the reactor 3 and the two circulation pipelines.

[0042] In a preferred embodiment of the present invention, the discharge port is connected to a collection chamber 17, the radial cross section of the collection chamber 17 gradually decreases from top to bottom, and the connecting pipe is connected to the bottom end of the collection chamber 17. This allows for a limited initial dose to be introduced at the beginning of the reaction, and also ensures the liquid level of the initiator in the collection chamber 17, so as to prevent cavitation at the suction port of the shielded pump 6 under vacuum conditions.

[0043] Furthermore, the uniform material tube includes a meridional tube 13 and at least one lateral tube 12. The meridional tube 13 is connected to each lateral tube 12 and is perpendicular to the lateral tube 12. The meridional tube 13 is connected to the first pipeline. Each first nozzle 14 is disposed on the lateral tube 12 so as to convey material to each lateral tube 12 through the meridional tube 13, thereby achieving the first step of uniform material distribution of the initiator and catalyst. Then, through each first nozzle 14 on the lateral tube 12, the second step of uniform material distribution of the initiator and catalyst is achieved, and the uniformity of the atomization distribution of the initiator and catalyst is ensured.

[0044] Preferably, the outlet end of the discharge pipe 10 is connected to a second nozzle to fully atomize ethylene oxide or propylene oxide through the second nozzle.

[0045] The feeding mechanism 9 is equipped with a feeding pipe connected to the feeding pump. A second heat exchanger 5 is also installed on the feeding pipe to exchange heat with the material inside. The second heat exchanger 5 preheats the ethylene oxide or propylene oxide in the feeding pipe to ensure effective and sufficient reaction with the initiator. Preferably, the second heat exchanger is a swirl plate heat exchanger.

[0046] Any adaptive changes made according to actual needs are within the scope of protection of this invention.

[0047] It should be noted that, for those skilled in the art, it is obvious that the present invention is not limited to the details of the exemplary embodiments described above, and that the invention can be implemented in other specific forms without departing from the spirit or essential characteristics of the invention. Therefore, the embodiments should be considered illustrative and non-limiting in all respects, and the scope of the invention is defined by the appended claims rather than the foregoing description. Thus, all variations falling within the meaning and scope of equivalents of the claims are intended to be included within the present invention. No reference numerals in the claims should be construed as limiting the scope of the claims.

[0048] Specific examples have been used to illustrate the principles and implementation methods of this invention. The descriptions of the above embodiments are only for the purpose of helping to understand the method and core ideas of this invention. Furthermore, those skilled in the art will recognize that, based on the ideas of this invention, there will be changes in the specific implementation methods and application scope. Therefore, the content of this specification should not be construed as a limitation of this invention.

Claims

1. An ethoxy, propoxy, oxylation reaction system characterized by, The utility model provides a reaction kettle, which comprises a first reaction cavity and a second reaction cavity connected in sequence, a plurality of communicating homogenizing pipes are arranged in the first reaction cavity, the homogenizing pipes are annular structures and are provided with a plurality of first nozzles at equal intervals along the circumferential direction, each first nozzle is directed to the center of the first reaction cavity, a feeding cavity is arranged on the outer side of the first reaction cavity, a plurality of discharge pipes are arranged on the feeding cavity at equal intervals along the circumferential direction, the discharge pipes pass through the first reaction cavity and are directed to the center of the first reaction cavity, and the feeding cavity is connected with a feeding mechanism, the feeding mechanism is provided with a feeding pump for pumping materials, and the second reaction cavity is located below the first reaction cavity; the second reaction cavity is provided with a discharge port at the bottom end; the discharge port is connected with a first circulating pipeline and a second circulating pipeline located outside the reaction kettle, the first circulating pipeline and the second circulating pipeline are both connected with a shielding pump, the flow ratio of the two is 1:2, the outlet of the first circulating pipeline extends into the second reaction cavity, the outlet of the second circulating pipeline passes through the first reaction cavity and is connected with the homogenizing pipes, and the first circulating pipeline and the second circulating pipeline are both matched with a first heat exchanger for heat exchange of materials in the first circulating pipeline and the second circulating pipeline; the outlet of the first circulating pipeline is connected with a jet pipe, the outlet end of the jet pipe passes through the first reaction cavity from top to bottom and extends into the second reaction cavity, and a Venturi tube is arranged between the first circulating pipeline and the jet pipe to suck the remaining materials in the feeding cavity into the jet pipe; the homogenizing pipes comprise a warp pipe and at least one weft pipe, the warp pipe is connected with each weft pipe, the warp pipe is perpendicular to the weft pipe, the warp pipe is connected with the first circulating pipeline, and each first nozzle is arranged on the weft pipe. The discharge port is connected with the shielding pump, and the first circulating pipeline and the second circulating pipeline are connected in parallel at the outlet of the shielding pump. The first heat exchanger is a rotating plate heat exchanger. The inlet end of the first circulating pipeline and the second circulating pipeline is provided with a first valve.

2. The ethoxy, propoxy, or ethoxypropoxy reaction system of claim 1, wherein, A connecting pipe is connected between the discharge port and the shielding pump, the connecting pipe is connected with a starter supply pipeline, and the outlet end of the starter supply pipeline is provided with a second valve.

3. The ethoxy, propoxy, or ethoxypropoxy reaction system of claim 2, wherein, The discharge port is connected with a material collecting cavity, the radial cross section of the material collecting cavity gradually decreases from top to bottom, and the connecting pipe is connected to the bottom end of the material collecting cavity.

4. The ethoxy, propoxy, or ethoxypropoxy reaction system of claim 3, wherein, The outlet end of the discharge pipe is connected with a second nozzle.

5. The ethoxy, propoxy, or ethoxypropoxy reaction system of claim 4, wherein, The feeding mechanism is provided with a feeding pipe connected with the feeding pump, and the feeding pipe is also matched with a second heat exchanger for heat exchange of materials in the feeding pipe.

6. The ethoxy, propoxy, or ethoxypropoxy reaction system of claim 5, wherein, ​ 7. The ethoxy, propoxy, or ethoxypropoxy reaction system of claim 6, wherein, ​ 8. The ethoxy, propoxy, or ethoxypropoxy reaction system of claim 7, wherein, ​

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