Ethoxylation and propoxylation reaction system

Abstract

The present invention discloses an ethoxylation and propoxylation reaction system, and relates to the technical field of ethoxylation and propoxylation reaction, the ethoxylation and propoxylation reaction system comprises a reaction kettle, the reaction kettle is connected with a material supply system, the material supply system is used for conveying raw materials and an initiator into the reaction kettle, and a circulation discharge port of the reaction kettle is connected to an input end of a circulation pump through a discharge pipe. The output end of the circulating pump is connected with a tubular circulating pipeline and a spray circulating pipeline in parallel; a tubular circulating heater and a tubular circulating cooler are arranged on the tubular circulating pipeline, and fluid on the tubular circulating pipeline can flow through a first heat exchange channel of the tubular circulating heater and a first heat exchange channel of the tubular circulating cooler in sequence; a spray circulation heater and a spray circulation cooler are arranged on the spray circulation pipeline, and fluid on the spray circulation pipeline can flow through the first heat exchange channels of the spray circulation heater and the spray circulation cooler in sequence. According to the invention, continuous conversion between a heating working process and a cooling working process can be realized.

Description

Technical Field

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

[0002] The nucleophilic addition reactions of ethylene oxide / propane with fatty alcohols, fatty acids, alkylphenols, fatty amines, alkylamides, and other compounds are collectively known as ethoxy / propylation reactions. These are highly vigorous exothermic chemical reactions with considerable danger. Therefore, strict control of the reaction intensity and effective heat removal measures are essential in industrial production. The reaction mechanisms are 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. Based on product type, chain growth ratio, and scale, reaction systems can be classified into first-generation, second-generation, and third-generation 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] The existing ethoxylation reaction system, as shown in patent number CN116832761A, includes a reactor comprising a first reaction chamber and a second reaction chamber connected in sequence. The first reaction chamber contains several interconnected uniform distribution pipes, each with a ring-shaped structure and several first nozzles evenly spaced along its circumference. An inlet chamber is located outside the first reaction chamber, and several outlet pipes are evenly distributed along its circumference on the inlet chamber. An outlet is located at the bottom of the second reaction chamber. The outlet is connected to a first circulation pipe and a second circulation pipe located outside the reactor. Both the first and second circulation pipes are connected to a shielded pump with a flow rate ratio of 1:2. The outlet of the first circulation pipe extends into the second reaction chamber, and the outlet of the second circulation pipe passes through the first reaction chamber and connects to the uniform distribution pipes. Both the first and second circulation pipes are equipped with first heat exchangers for heat exchange of the internal materials, effectively increasing the growth ratio of the entire addition reaction.

[0005] However, in the aforementioned patents, both heating and cooling utilize a single rotary plate heat exchanger. This setup has a significant drawback: steam is used during the initiator heating stage, and cooling is required after the initiator releases heat through the addition of ethylene oxide or propylene oxide. The heating and cooling processes are discontinuous, and water is needed to remove the steam from the heat exchanger before cooling. Therefore, there is no stable temperature curve from heating up, dehydration, to cooling down, making continuous, fully automated control difficult—a major disadvantage for modern industry.

[0006] Therefore, there is an urgent need in this field for a novel ethoxylation reaction system to solve the above problems. Summary of the Invention

[0007] The purpose of this invention is to provide an ethoxylation reaction system to solve the problems existing in the prior art, which can realize continuous switching from heating to cooling, thereby achieving continuous fully automatic control.

[0008] To achieve the above objectives, the present invention provides the following solution:

[0009] This invention discloses an ethoxylation reaction system, including a reaction vessel. The reaction vessel is connected to a feeding system for conveying raw materials and initiators into the reaction vessel. The circulation outlet of the reaction vessel is connected to the input end of a circulation pump via a discharge pipe. The output end of the circulation pump is connected in parallel to a tubular circulation pipeline and a spray circulation pipeline. The ends of the tubular circulation pipeline and the spray circulation pipeline furthest from the circulation pump are both connected to the interior of the reaction vessel.

[0010] The tubular circulation pipeline is equipped with a tubular circulation heater and a tubular circulation cooler. Fluid in the tubular circulation pipeline can flow sequentially through the first heat exchange channels of the tubular circulation heater and the tubular circulation cooler. High-temperature heating oil can be introduced into the second heat exchange channel of the tubular circulation heater, and low-temperature cooling oil can be introduced into the second heat exchange channel of the tubular circulation cooler. The spray circulation pipeline is equipped with a spray circulation heater and a spray circulation cooler. Fluid in the spray circulation pipeline can flow sequentially through the first heat exchange channels of the spray circulation heater and the spray circulation cooler. High-temperature heating oil can be introduced into the second heat exchange channel of the spray circulation heater, and low-temperature cooling oil can be introduced into the second heat exchange channel of the spray circulation cooler.

[0011] Preferably, the tubular circulating heater, the tubular circulating cooler, the spray circulating heater, and the spray circulating cooler are all shell-and-tube heat exchangers.

[0012] Preferably, the circulating pump is a magnetic pump, a centrifugal pump, or a canned motor pump.

[0013] Preferably, the lower end of the reactor is provided with a collection chamber, the upper end cross-sectional dimension of the collection chamber is larger than the lower end cross-sectional dimension of the collection chamber, and the circulation outlet of the collection chamber is connected to the input end of the circulation pump through a discharge pipe.

[0014] Preferably, the interior of the reactor includes an upper reaction chamber and a lower reaction chamber, with the upper reaction chamber located above the lower reaction chamber.

[0015] Preferably, the upper reaction chamber is provided with a reactant meridional tube, a plurality of reactant zonal tubes are connected to the reactant meridional tube, a plurality of zonal tube nozzles are spaced apart on the reactant zonal tubes, and the spray circulation pipeline is connected to the reactant meridional tube.

[0016] Preferably, a raw material supply chamber is provided outside the upper reaction chamber, and multiple supply nozzles are connected to the raw material supply chamber, which can spray material into the upper reaction chamber.

[0017] Preferably, the feeding system includes a raw material feeding pipeline, a preheater is provided on the raw material feeding pipeline, and the output end of the raw material feeding pipeline is connected to the raw material feeding chamber.

[0018] Preferably, the tubular circulation pipeline is connected to an injector at one end near the reactor. The injector is connected to an injection pipe and a suction pipe. The end of the injection pipe away from the injector extends into the lower reaction chamber, and the end of the suction pipe away from the injector communicates with the raw material supply chamber.

[0019] Preferably, the tubular circulation pipeline is connected to an initiator supply pipeline, and the reactor is provided with an initiator addition port.

[0020] The present invention achieves the following technical effects compared to the prior art:

[0021] This invention incorporates a tubular circulating heater and a tubular circulating cooler within a tubular circulating pipeline, and a spray circulating heater and a spray circulating cooler within a spray circulating pipeline. The method involves heating the initiator with high-temperature heating oil and cooling it with low-temperature cooling oil to remove the heat of the addition reaction. Specifically, the initiator is heated and dehydrated by the tubular circulating heater using high-temperature heating oil. Once the initiation temperature is reached, the hot oil in the tubular circulating heater is drained, and then low-temperature cooling oil is added through the tubular circulating cooler to remove the exothermic heat of the addition reaction. This continuous heat transfer into and out of the material allows for fully automated control via temperature setting and stratified control. Attached Figure Description

[0022] 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.

[0023] Figure 1 This is a schematic diagram of the structure of the ethyl and propoxylation reaction system according to an embodiment of the present invention;

[0024] Figure 2 This is a schematic diagram of the tubular circulation pipeline in the ethoxylation reaction system of this invention.

[0025] Figure 3 This is a schematic diagram of the spray circulation pipeline in the ethoxylation reaction system of this invention.

[0026] Figure 4 This is a schematic diagram of the reactor structure in the ethyl and propoxylation reaction system of this invention.

[0027] In the diagram: 1-Reaction vessel; 101-Upper reaction chamber; 102-Lower reaction chamber; 103-Reactant meridional pipe; 104-Reactant zonal pipe; 105-Raw material feeding chamber; 2-Tube-type circulation pipeline; 201-Tube-type circulation heater; 202-Tube-type circulation cooler; 3-Spray circulation pipeline; 301-Spray circulation heater; 302-Spray circulation cooler; 4-Raw material feeding pipeline; 401-Preheater; 5-Circulation pump; 6-Collection chamber; 7-Initiator feeding pipeline; 8-Ejector; 801-Injection pipe; 802-Suction pipe. Detailed Implementation

[0028] 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.

[0029] The purpose of this invention is to provide an ethoxylation reaction system to solve the problems existing in the prior art, which can realize continuous switching from heating to cooling, thereby achieving continuous fully automatic control.

[0030] 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.

[0031] like Figures 1-4 As shown, this invention provides an ethoxylation reaction system, including a reactor 1, wherein the reactor 1 can adopt an existing reactor 1 structure. The reactor 1 is connected to a feeding system for conveying raw materials and initiators into the reactor 1, wherein the raw materials can be EO / PO (ethylene oxide / propylene oxide). The circulation outlet of the reactor 1 is connected to the input end of a circulation pump 5 via a discharge pipe. The output end of the circulation pump 5 is connected in parallel to a tubular circulation pipeline 2 and a spray circulation pipeline 3. Corresponding switching valves are provided on the tubular circulation pipeline 2 and the spray circulation pipeline 3 to control the flow in each pipeline. The flow ratio of the tubular circulation pipeline 2 to the spray circulation pipeline 3 is 1:2. The material flowing out of the reactor 1 can flow into the tubular circulation pipeline 2 and / or the spray circulation pipeline 3 through the circulation pump 5. The ends of the tubular circulation pipeline 2 and the spray circulation pipeline 3 furthest from the circulation pump 5 are both connected to the interior of the reactor 1.

[0032] The difference from the prior art is that the tubular circulation pipeline 2 is equipped with a tubular circulation heater 201 and a tubular circulation cooler 202. The fluid from the circulation pump 5 on the tubular circulation pipeline 2 can flow through the first heat exchange channel of the tubular circulation heater 201 and the tubular circulation cooler 202 in sequence. The second heat exchange channel of the tubular circulation heater 201 can be introduced with high-temperature heating oil with a temperature of above 250°C. The second heat exchange channel of the tubular circulation cooler 202 can be introduced with low-temperature cooling oil with a temperature of below 30°C. Similarly, the spray circulation pipeline 3 is equipped with a spray circulation heater 301 and a spray circulation cooler 302. The fluid from the circulation pump 5 on the spray circulation pipeline 3 can flow through the first heat exchange channel of the spray circulation heater 301 and the spray circulation cooler 302 in sequence. The second heat exchange channel of the spray circulation heater 301 can be filled with high-temperature heating oil with a temperature of above 250°C. The second heat exchange channel of the spray circulation cooler 302 can be filled with low-temperature cooling oil with a temperature of below 30°C.

[0033] In practical use, the initiator is first added to the reactor 1 through the feeding system. Then, the circulation pump 5 is started, the tubular circulation line 2 is opened, and the spray circulation line 3 is closed. This allows the mixture to circulate at a low flow rate through the tubular circulation line 2. Once a certain amount is reached, the spray circulation line 3 is opened for a larger circulation. The purpose is to allow the addition reaction to occur even when only a small amount of initiator is initially circulated, thus increasing the growth ratio of the addition reaction. During the circulation process, raw materials (i.e., ethylene oxide or propylene oxide) also need to be added. While the initiator is in a heated and dehydrated state, the tubular circulation heater 201 and the spray circulation heater 301 are started. High-temperature heating oil is supplied to the second heat exchange channel through external pipelines, allowing the tubular circulation heater 201 and the spray circulation heater 301 to heat the fluid passing through the first heat exchange channel, thus heating and dehydrating the mixture. When the temperature reaches the expected level and cooling is required, the tubular circulating heater 201 and the spray circulating heater 301 should be shut down promptly, while the tubular circulating cooler 202 and the spray circulating cooler 302 should be turned on. Low-temperature cooling oil, supplied to the second heat exchange channel through external pipelines, removes the heat generated by the addition reaction, allowing for secondary heat utilization and reducing energy consumption. Because the heating and cooling processes utilize two different devices, these two processes can be switched quickly and continuously, achieving continuous fully automatic control.

[0034] In this embodiment, the tubular circulating heater 201, tubular circulating cooler 202, spray circulating heater 301, and spray circulating cooler 302 are all existing shell-and-tube heat exchangers. Since shell-and-tube heat exchangers are an existing and very common type of heat exchanger, their specific structures will not be described in detail here. As is well known, a shell-and-tube heat exchanger includes a shell side and a tube side. The tubular circulating pipe 2 and the spray circulating pipe 3 are both connected to the tube side of the shell-and-tube heat exchanger (i.e., the first heat exchange channel mentioned above), while the high-temperature heating oil or low-temperature cooling oil from the external pipes are connected to the shell side of the shell-and-tube heat exchanger (i.e., the second heat exchange channel mentioned above).

[0035] In this embodiment, the circulating pump 5 includes, but is not limited to, existing magnetic pumps, centrifugal pumps, or canned pumps, in order to meet the requirement of no leakage during operation.

[0036] In this embodiment, the lower end of the reactor 1 is provided with a material collection chamber 6. The material collection chamber 6 and the reactor 1 are an integral structure, and the circulation outlet of the material collection chamber 6 (i.e. the circulation outlet of the reactor 1 mentioned above) is connected to the input end of the circulation pump 5 through the discharge pipe.

[0037] It should be noted that the upper cross-sectional dimension of the collection chamber 6 is larger than the lower cross-sectional dimension of the collection chamber 6. Specifically, it can be an inverted conical structure or an inverted beer bottle shape. The reason for this structure is to ensure that even when the initial dosage is small at the beginning of the reaction, the reactants can reach a certain height, increasing the fluid pressure flowing out of the collection chamber 6, thereby avoiding cavitation at the inlet of the circulating pump 5 due to insufficient pressure.

[0038] In this embodiment, the reactor 1 includes an upper reaction chamber 101 and a lower reaction chamber 102, which are connected and the upper reaction chamber 101 is located above the lower reaction chamber 102. After the initiator reacts with ethylene oxide or propylene oxide in the upper reaction chamber 101, the products and remaining materials flow into the lower reaction chamber 102 for further reaction and product aggregation.

[0039] It should be noted that the top of the upper chamber 101 of the reaction vessel is also connected to a nitrogen inlet pipe, a vent pipe, a vacuum pipe, and a rupture disc vent line. The nitrogen inlet pipe is used to introduce nitrogen gas, thereby venting the air in the reaction vessel 1 through the vent pipe; the vacuum pipe is equipped with a vacuum pump to evacuate the nitrogen gas in the reaction vessel 1; and the rupture disc vent line has a rupture disc installed on it, which can release pressure when the pressure in the reaction vessel 1 is too high.

[0040] In this embodiment, the upper reaction chamber 101 is equipped with a reactant meridional pipe 103, to which a plurality of reactant zonal pipes 104 are connected. The axial direction of the reactant meridional pipe 103 is perpendicular to the axial direction of the reactant zonal pipes 104. At least one reactant zonal pipe 104 is provided, and each reactant zonal pipe 104 is connected to the reactant meridional pipe 103. Multiple zonal nozzles are spaced apart on the reactant zonal pipes 104, and each zonal nozzle sprays towards the center of the upper reaction chamber 101. The spray circulation pipeline 3 is connected to the reactant meridional pipe 103.

[0041] During the circulation process, the circulating pump 5 delivers the reactants through the spray circulation pipeline 3 to the reactant meridional pipe 103, and then the reactants are delivered from the reactant meridional pipe 103 to the various reactant zonal pipes 104, achieving the first step of homogenizing the initiator and catalyst. Then, the reactant zonal pipes 104 deliver the reactants to the various zonal nozzles, achieving the second step of homogenizing the initiator and catalyst, and ensuring the uniformity of the atomization distribution of the initiator and catalyst. Finally, the various zonal nozzles spray the atomized material towards the center of the upper reaction chamber 101.

[0042] In this embodiment, an annular raw material supply chamber 105 is provided on the outer side of the upper reaction chamber 101. Multiple supply nozzles are connected to the raw material supply chamber 105. The supply nozzles are also spaced apart, and the head of the supply nozzle can pass through the side wall of the upper reaction chamber 101, so that the supply nozzle can spray material towards the center of the upper reaction chamber 101, thereby achieving uniform distribution of raw materials and uniform mixing with the reaction material sprayed from the latitudinal nozzle.

[0043] In this embodiment, the feeding system includes a raw material feeding pipeline 4, which is equipped with a switch valve and a feeding pump. The feeding pump provides the conveying power, and the switch valve is used to control the flow in the pipeline. A preheater 401 is provided on the raw material feeding pipeline 4. The input end of the raw material feeding pipeline 4 is the raw material source (i.e., a storage container for ethylene oxide or propylene oxide), and the output end of the raw material feeding pipeline 4 is connected to the raw material feeding chamber 105.

[0044] In actual use, the raw materials can be preheated by the preheater 401 under the power of the feed pump, so that they are closer to the temperature conditions most suitable for the reaction, before being transported to the raw material feed chamber 105.

[0045] Among them, the preheater 401 is an existing heat exchanger structure, which can also be an existing shell and tube heat exchanger. Its tube side is used for the flow of raw materials, while the shell side can be used to introduce external preheating oil or preheating water. The temperature of the preheating oil or preheating water is not higher than 100℃, so as to give the raw materials an appropriate preheating effect, so that the reaction can be carried out faster and the reaction rate can be improved.

[0046] In this embodiment, the end of the tubular circulation pipeline 2 closest to the reactor 1 (i.e., the outlet end of the tubular circulation pipeline 2) is connected to the inlet end of the ejector 8, which is a conventional venturi tube. The ejector 8 is also connected to an injection pipe 801 and a suction pipe 802. The end of the injection pipe 801 furthest from the ejector 8 (i.e., the outlet end of the injection pipe 801) extends into the lower reaction chamber 102, and the inlet end of the injection pipe 801 is connected to the ejector 8. The end of the suction pipe 802 furthest from the ejector 8 (i.e., the inlet end of the suction pipe 802) is connected to the raw material feeding chamber 105, and the outlet end of the suction pipe 802 is connected to the ejector 8.

[0047] In actual use, the material from the tubular circulation line 2 flows into the injector 8, and then flows into the lower reaction chamber 102 through the injector 8 and the injection pipe 801. During this process, the material from the tubular circulation line 2 generates a pressure difference after entering the venturi tube, and the remaining material in the raw material supply chamber 105 is drawn out through the suction pipe 802. As a result, the unreacted ethylene oxide or propylene oxide will fully react with the initiator in the injection pipe 801, which significantly reduces the residual amount of ethylene oxide or propylene oxide and ensures the environmental protection effect of the entire device.

[0048] In this embodiment, an initiator supply line 7 is connected to the tubular circulation line 2, and an initiator addition port is provided on the reactor 1. This allows the initiator to be either transported to the tubular circulation line 2 via the initiator supply line 7 and then flow into the reactor 1, or it can be directly poured into the reactor 1 via the initiator addition port. A catalyst addition port is also provided on the side wall of the reactor 1 for adding catalyst.

[0049] 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 ethoxylation reaction system, comprising a reaction vessel, wherein the reaction vessel is connected to a feeding system for supplying raw materials and initiators to the reaction vessel, the circulation outlet of the reaction vessel is connected to the input end of a circulation pump via a discharge pipe, and the output end of the circulation pump is connected in parallel to a tubular circulation pipeline and a spray circulation pipeline, wherein the ends of the tubular circulation pipeline and the spray circulation pipeline furthest from the circulation pump are both connected to the interior of the reaction vessel; Its features are: The tubular circulation pipeline is equipped with a tubular circulation heater and a tubular circulation cooler. Fluid in the tubular circulation pipeline can flow sequentially through the first heat exchange channels of the tubular circulation heater and the tubular circulation cooler. High-temperature heating oil can be introduced into the second heat exchange channel of the tubular circulation heater, and low-temperature cooling oil can be introduced into the second heat exchange channel of the tubular circulation cooler. The spray circulation pipeline is equipped with a spray circulation heater and a spray circulation cooler. Fluid in the spray circulation pipeline can flow sequentially through the first heat exchange channels of the spray circulation heater and the spray circulation cooler. High-temperature heating oil can be introduced into the second heat exchange channel of the spray circulation heater, and low-temperature cooling oil can be introduced into the second heat exchange channel of the spray circulation cooler.

2. The ethoxylation reaction system according to claim 1, characterized in that: The tubular circulating heater, tubular circulating cooler, spray circulating heater, and spray circulating cooler are all shell-and-tube heat exchangers.

3. The ethoxylation reaction system according to claim 1, characterized in that: The circulating pump is a magnetic pump, a centrifugal pump, or a canned pump.

4. The ethoxylation reaction system according to claim 1, characterized in that: The lower end of the reactor is provided with a material collection chamber. The upper cross-sectional dimension of the material collection chamber is larger than the lower cross-sectional dimension of the material collection chamber. The circulation outlet of the material collection chamber is connected to the input end of the circulation pump through a discharge pipe.

5. The ethoxylation reaction system according to claim 1, characterized in that: The reactor contains an upper reaction chamber and a lower reaction chamber, with the upper reaction chamber located above the lower reaction chamber.

6. The ethoxylation reaction system according to claim 5, characterized in that: The upper reaction chamber is equipped with a reactant meridional tube, which is connected to several reactant zonal tubes. Multiple zonal nozzles are spaced apart on the reactant zonal tubes, and the spray circulation pipeline is connected to the reactant meridional tube.

7. The ethoxylation reaction system according to claim 5, characterized in that: The upper reaction chamber is provided with a raw material supply chamber on its outer side. The raw material supply chamber is connected to a plurality of supply nozzles, which can spray material into the upper reaction chamber.

8. The ethoxylation reaction system according to claim 7, characterized in that: The feeding system includes a raw material feeding pipeline, a preheater is provided on the raw material feeding pipeline, and the output end of the raw material feeding pipeline is connected to the raw material feeding chamber.

9. The ethoxylation reaction system according to claim 7, characterized in that: The tubular circulation pipeline is connected to an injector at one end near the reactor. The injector is connected to an injection pipe and a suction pipe. The end of the injection pipe away from the injector extends into the lower reaction chamber, and the end of the suction pipe away from the injector is connected to the raw material supply chamber.

10. The ethoxylation reaction system according to claim 1, characterized in that: The tubular circulation pipeline is connected to an initiator supply pipeline, and the reactor is equipped with an initiator addition port.

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