CN213493686U

CN213493686U - Hydroxyl ether reaction system

Info

Publication number: CN213493686U
Application number: CN202022130459.7U
Authority: CN
Inventors: 向英; 李波; 王剑宇; 兰剑平; 王娟; 张丹
Original assignee: Chongqing Chemical Research Institute Materials Technology Co ltd; Chongqing Chemical Research Institute Co Ltd
Current assignee: Chongqing Chemical Research Institute Materials Technology Co ltd; Chongqing Chemical Research Institute Co Ltd
Priority date: 2020-09-24
Filing date: 2020-09-24
Publication date: 2021-06-22
Anticipated expiration: 2030-09-24

Abstract

A hydroxyether reaction system comprises a reaction kettle, a distillation tower, a condenser, a vacuum unit, a first distillation tank, a second distillation tank and a third distillation tank, wherein a tower bottom feed inlet of the distillation tower is connected with the top of a kettle body through a first pipeline, a tower top steam outlet is connected with a process medium inlet of the condenser through a second pipeline, a process medium exhaust port of the condenser is connected with the vacuum unit, a process medium liquid outlet of the condenser is connected with a third pipeline, a fourth pipeline, a fifth pipeline, a sixth pipeline and a seventh pipeline in parallel, the third pipeline is connected with the top of the side wall of the distillation tower, the fourth pipeline is connected with the middle of the side wall of the distillation tower, the fifth pipeline is connected with the first distillation tank, the sixth pipeline is connected with the second distillation tank, and the seventh pipeline is connected with the third distillation tank. The utility model has simple structure and low operation cost, can effectively improve the utilization rate of the raw material of the synthetic hydroxyether, and has low component separation cost.

Description

Hydroxyl ether reaction system

Technical Field

The utility model relates to the field of chemical industry, in particular to hydroxyether reaction system.

Background

The chemical enterprises use butanediol and acetylene as raw materials to synthesize the hydroxyether product under the action of a potassium hydroxide cocatalyst.

Butanediol is used as a liquid raw material, acetylene is used as a gas raw material, and after the two raw materials enter a reaction kettle, the contact area between the gas raw material and the liquid raw material is small, the contact time is short, so that the utilization rate of the raw materials is low, the synthesis efficiency of hydroxyether is low, and the large-scale synthesis of hydroxyether is not facilitated.

In addition, the synthesized material is discharged in a liquid state and then is distilled and separated by a distillation tower, which causes serious waste of heat.

Therefore, how to synthesize hydroxyether by using butanediol and acetylene with high efficiency is a problem to be solved by those skilled in the art.

Disclosure of Invention

The utility model aims at the not enough of prior art, provide a hydroxyether reaction system, its simple structure, running cost are low, can effectively improve the utilization ratio of synthetic hydroxyether raw materials, and the component separation is with low costs.

The technical scheme of the utility model is that: a hydroxyether reaction system comprises a reaction kettle, a distillation tower, a condenser, a vacuumizing device, a first distillation tank, a second distillation tank and a third distillation tank, wherein the reaction kettle comprises a kettle body, a heat exchange coil, an air-entrapping ring pipe and a stirring device, a feeding pipe is arranged at the top of the kettle body and is used for being connected with a butanediol source, a heating interlayer is arranged on the peripheral wall of the kettle body, the heat exchange coil is positioned in the inner space of the kettle body, stirring blades of the stirring device are positioned in the inner space of the heat exchange coil, the air-entrapping ring pipe is arranged in the inner space of the kettle body and is positioned below the heat exchange coil, a plurality of air-entrapping holes are arranged at the bottom of the air-entrapping ring pipe and are uniformly distributed along the circumferential direction of the air-entrapping ring pipe, the air-entrapping ring pipe is connected with an acetylene source through an air-entrapping pipe, a tower bottom feeding port of the distillation tower is, the process medium exhaust port of the condenser is connected with the vacuumizing device through a vacuum buffer tank, a process medium liquid discharge port of the condenser is connected with a third pipeline, a fourth pipeline, a fifth pipeline, a sixth pipeline and a seventh pipeline in parallel, a third valve is arranged at the downstream end of the third pipeline and is connected with the top of the side wall of the distillation tower, a fourth valve is arranged at the downstream end of the fourth pipeline and is connected with the middle of the side wall of the distillation tower, a fifth valve is arranged on the fifth pipeline and is connected with a first fraction tank, a sixth valve is arranged on the sixth pipeline and is connected with a second fraction tank, and a seventh valve is arranged on the seventh pipeline and is connected with a third fraction tank.

The bottom of the kettle body is provided with a slag discharge pipe, and a first valve is arranged on the slag discharge pipe.

The number of the gas adding pipes is two, each gas adding pipe is provided with a second valve, the upstream ends of the two gas adding pipes are used for being connected with an acetylene source, and the downstream ends of the two gas adding pipes are connected with the gas adding ring pipe respectively and are positioned at the two ends of the gas adding ring pipe with the same diameter.

The top of the kettle body is provided with an emptying pipe for connecting with a tail gas system, and the emptying pipe is provided with an emptying valve.

The first pipeline is coated with a heat insulation layer.

And a liquid outlet at the bottom of the distillation tower is connected with the top of the kettle body through an eighth pipeline, and an eighth valve is arranged on the eighth pipeline.

And the eighth pipeline is provided with a first guide shower pipe in parallel and positioned at the upstream of the eighth valve, and the first guide shower pipe is provided with a first guide shower valve.

The eighth pipeline is provided with a first nitrogen pipe in parallel, the first nitrogen pipe is positioned at the downstream of the eighth valve, the upstream end of the first nitrogen pipe is used for being connected with a nitrogen source, and the first nitrogen pipe is sequentially provided with a first check valve and a ninth valve from the upstream to the downstream.

The first fraction tank, the second fraction tank and the third fraction tank are respectively connected with the vacuum buffer tank through pipelines, the top of each fraction tank is respectively provided with a second nitrogen pipe, the upstream of each second nitrogen pipe is used for being connected with a nitrogen source, and each second nitrogen pipe is sequentially provided with a second one-way valve and a tenth valve from the upstream to the downstream.

And second guide showering pipes are respectively arranged at the bottoms of the first distillation tank, the second distillation tank and the third distillation tank, and second guide showering valves are respectively arranged on the second guide showering pipes.

Adopt above-mentioned technical scheme to have following beneficial effect:

1. the hydroxyether reaction system comprises a reaction kettle, a distillation tower, a condenser, a vacuumizing device, a first distillation tank, a second distillation tank and a third distillation tank, wherein the reaction kettle is used as a space for synthesizing hydroxyether from raw materials, the distillation tower is used for separating materials synthesized in the reaction kettle, and the condenser and the vacuumizing device are matched to liquefy components obtained by distillation in the distillation tower to obtain separated components. The reaction kettle comprises a kettle body, a heat exchange coil, an air-entrapping ring pipe and a stirring device, wherein the heat exchange coil is used for heating or cooling the raw materials in the kettle body, the actual requirements of enterprises are met, the stirring device is used for uniformly mixing materials, local overheating is avoided, and the air-entrapping ring pipe is used for providing acetylene gas to the kettle body. The top of the cauldron body is equipped with the inlet pipe for be connected with the butanediol source, the butanediol passes through the inlet pipe and provides the butanediol liquid to the cauldron is internal. The heating interlayer is arranged on the peripheral wall of the kettle body and used for heating the raw materials in the kettle body so as to meet the reaction condition of synthesizing the hydroxyether. The heat exchange coil is located the interior vacancy of the kettle body, and the stirring blades of the stirring device are located the interior vacancy of the heat exchange coil, namely, the temperature of materials in the kettle body can be effectively adjusted by utilizing the interior vacancy of the stirring blades and the heat exchange coil at the periphery of the stirring blades, and the actual requirements of enterprises are met. The gas-filling ring pipe is arranged in the kettle body and is positioned below the heat exchange coil pipe, the bottom of the gas-filling ring pipe is provided with a plurality of gas-filling holes, the gas-filling holes are uniformly distributed along the circumferential direction of the gas-filling ring pipe, the gas-filling ring pipe is connected with an acetylene source through a gas-filling pipe, the acetylene gas provided by the acetylene source to the gas-filling ring pipe enters the gas-filling ring pipe and then is discharged downwards from the gas-filling holes, the gas-filling ring pipe is positioned below the heat exchange coil pipe and the stirring blades, the specific gravity of the acetylene gas is light, the acetylene gas entering the kettle body firstly moves downwards, is firstly mixed with the butanediol and then ascends under the action of buoyancy, is stirred and is secondly mixed with the butanediol, the contact time and the contact area of the acetylene gas and the butanediol can be effectively prolonged, the synthesis efficiency of the butanediol and the acetylene gas is improved, in addition, the gas, ensuring the stability of acetylene gas filling. The method is characterized in that a tower bottom feed inlet of the distillation tower is connected with the top of a kettle body through a first pipeline, a tower top steam outlet of the distillation tower is connected with a process medium inlet of a condenser through a second pipeline, a process medium exhaust port of the condenser is connected with a vacuumizing device through a vacuum buffer tank, after the reaction is finished, the temperature in the kettle is high, the vacuumizing device is started to enable the air in the distillation tower and the kettle body to be negative pressure, and the synthesized material enters the rectification tower in a vapor state under the conditions of high temperature and negative pressure. The process medium liquid outlet of the condenser is connected with a third pipeline, a fourth pipeline, a fifth pipeline, a sixth pipeline and a seventh pipeline in parallel, a third valve is arranged at the downstream end of the third pipeline and connected with the top of the side wall of the distillation tower, a fourth valve is arranged at the downstream end of the fourth pipeline and connected with the middle of the side wall of the distillation tower, partial fraction is refluxed to the top of the distillation tower, the purity of the fraction is improved, the actual requirement is met, and high-boiling-point impurities in the fraction can be effectively reduced by refluxing the partial fraction to the middle of the distillation tower. The fifth pipeline is provided with a fifth valve and is connected with the first distillation tank, the sixth pipeline is provided with a sixth valve and is connected with the second distillation tank, the seventh pipeline is provided with a seventh valve and is connected with the third distillation tank, different distillation tanks are used for respectively receiving fractions with different temperature sections by opening and closing different valves, generally, the first distillation tank is used for receiving front fractions, the second distillation tank is used for receiving hydroxyether to obtain semi-finished products, the purity is 80-90%, and the third distillation tank is used for receiving high-boiling-point components. And completing the separation of the materials.

2. The bottom of the kettle body is provided with a slag discharge pipe, the slag discharge pipe is provided with a first valve, potassium hydroxide added into the kettle body is used as a catalyst, the potassium hydroxide cannot be discharged in a vapor state along with materials obtained by synthesis in the kettle body, and the potassium hydroxide can be discharged out of the kettle body through the slag discharge pipe after being polluted for centralized treatment.

3. The number of the gas adding pipes is two, each gas adding pipe is provided with a second valve, the upstream ends of the two gas adding pipes are used for being connected with an acetylene source, the downstream ends of the two gas adding pipes are connected with a gas adding ring pipe respectively, the two gas adding pipes can be arranged for mutual backup, the continuity and the stability of gas supply are improved, the gas adding pipes are arranged at the two ends of the gas adding ring pipe simultaneously, the pressure stability of each gas adding hole can be improved, the pressure of acetylene gas discharged from each gas adding hole is higher, the stability is realized, the even distribution of the acetylene gas in the kettle body is ensured, and the synthesis efficiency of the acetylene and the butanediol is improved.

4. The top of the kettle body is provided with an emptying pipe for connecting with a tail gas system, and the emptying pipe is provided with an emptying valve for opening as required or under emergency to relieve the pressure of the reaction kettle.

5. And a liquid outlet at the bottom of the distillation tower is connected with the top of the kettle body through an eighth pipeline, an eighth valve is arranged on the eighth pipeline, a first guide shower pipe is arranged on the eighth pipeline in parallel and is positioned at the upstream of the eighth valve, and a first guide shower valve is arranged on the first guide shower pipe. The residual components in the distillation tower, such as butanediol, can be returned to the reaction kettle through the eighth pipeline to be used as raw materials for reuse, and the residual components in the distillation tower can also be discharged to be used for centralized treatment by opening the guide shower valve.

The following further description is made with reference to the accompanying drawings and detailed description.

Drawings

Fig. 1 is a schematic structural view of the present invention;

FIG. 2 is a partial view taken at M of FIG. 1;

fig. 3 is a bottom schematic view of the gas-filling ring pipe of the present invention.

In the drawing, 1 is a first distillation tank, 2 is a second distillation tank, 3 is a third distillation tank, 4 is a reaction kettle, 41 is a kettle body, 42 is a heat exchange coil, 43 is an air-filling ring pipe, 44 is a stirring device, 45 is a feeding pipe, 46 is an air-filling hole, 47 is an air-filling pipe, 48 is a slag-discharging pipe, 49 is a emptying pipe, 5 is a distillation tower, 6 is a condenser, 7 is a vacuumizing device, 8 is a vacuum buffer tank, 9 is a first shower guide pipe, 10 is a first shower guide valve, 11 is a first nitrogen pipe, 12 is a first check valve, 13 is a second nitrogen pipe, 14 is a second check valve, 15 is a second shower guide pipe, 16 is a second shower guide valve, 101 is a first pipeline, 102 is a second pipeline, 103 is a third pipeline, 104 is a fourth pipeline, 105 is a fifth pipeline, 106 is a sixth pipeline, 107 is a seventh pipeline, 108 is an eighth pipeline, a first valve, b is a second valve, and c is a third valve, d is the fourth valve, e is the fifth valve, f is the sixth valve, g is the seventh valve, h is the eighth valve, i is the ninth valve, j is the tenth valve.

Detailed Description

The utility model discloses in, do not specifically mark the equipment or the device of structure, be the conventional equipment or the device in chemical industry field usually, the connected mode that does not specifically mark adopts the conventional mode in chemical industry field or the producer to guide the mode to connect usually.

Referring to fig. 1-3, a particular embodiment of a hydroxyether reaction system is shown. The hydroxyether reaction system comprises a reaction kettle 4, a distillation tower 5, a condenser 6, a vacuumizing device 7, a first fraction tank 1, a second fraction tank 2 and a third fraction tank 3. The reaction kettle 4 comprises a kettle body 41, a heat exchange coil 42, an air-entrapping annular pipe 43 and a stirring device 44, wherein the kettle body is usually supported on a floor slab, so that the upper part of the kettle body is positioned above the floor slab, the lower part of the kettle body is positioned below the floor slab, in order to facilitate discharging of residual solids in the kettle body, such as added potassium hydroxide, a slag discharge pipe 48 is arranged at the bottom of the kettle body 41, and a first valve a is arranged on the slag discharge pipe 48. The top of cauldron body 41 is equipped with inlet pipe 45 for with the butanediol source continuous, usually, the cauldron body still is provided with and throws the material lid, conveniently adds the potassium hydroxide cocatalyst to the cauldron internal. Be equipped with on the periphery wall of the cauldron body 41 and heat the intermediate layer, the air inlet that heats the intermediate layer is located the top that heats the intermediate layer, and the fluid-discharge outlet that heats the intermediate layer is located the bottom that heats the intermediate layer, and the heating medium that heats the intermediate layer and use is industrial steam, and is exothermic through the industrial steam condensation, heats the internal sky of cauldron and heaies up, in order to improve industrial steam's utilization efficiency, reduces the heat and scatters and disappears, is equipped with the heat preservation on the heating intermediate layer outer wall. The heat exchange coil 42 is located in the inner cavity of the kettle body 41, specifically, a pipe orifice at the upper part of the heat exchange coil is a heat exchange medium outlet, a pipe orifice at the lower part of the heat exchange coil is a heat exchange medium inlet, and circulating hot water or cold water is used for heating or cooling the material in the inner cavity of the kettle body, so that the actual requirements of enterprises are effectively met. The stirring blades of the stirring device 44 are positioned in the hollow space of the heat exchange coil 42. The air-entrapping ring pipe 43 is arranged in the kettle body 41 and is positioned below the heat exchange coil 42, a plurality of air-entrapping holes 46 are formed in the bottom of the air-entrapping ring pipe 43, the air-entrapping holes 46 are uniformly distributed along the circumferential direction of the air-entrapping ring pipe 43, the air-entrapping ring pipe 43 is connected with an acetylene source through an air-entrapping pipe 47, and generally, in order to improve the charging uniformity of acetylene gas and improve the use efficiency of acetylene as much as possible, the smaller the aperture of the air-entrapping hole is, the larger the number of the air-entrapping holes is, and the balance is made between the aperture and the number. The central lines of the air-entraining circular pipe and the heat exchange coil pipe are in the same line with the stirring shaft of the stirring device. A feeding hole at the bottom of the distillation tower 5 is connected with the top of the kettle body 41 through a first pipeline 101, specifically, the first pipeline 101 is coated with a heat-insulating layer, in order to return the residual butanediol in the distillation tower to the reaction kettle for reuse as a raw material, a liquid outlet at the bottom of the distillation tower 5 is connected with the top of the kettle body 41 through an eighth pipeline 108, an eighth valve h is arranged on the eighth pipeline 108, generally, a first drenching guide pipe 9 is also required to be arranged on the eighth pipeline 108 in parallel and is positioned at the upstream of the eighth valve h, a first drenching guide valve 10 is arranged on the first drenching guide pipe 9, in order to ensure the production safety, a first nitrogen pipe 11 is arranged on the eighth pipeline 108 in parallel, the first nitrogen pipe 11 is located at the downstream of the eighth valve h, the upstream end of the first nitrogen pipe 11 is used for being connected with a nitrogen source, and the first nitrogen pipe 11 is sequentially provided with a first check valve 12 and a ninth valve i from the upstream to the downstream. The top outlet of the distillation column 5 is connected via a second line 102 to the process medium inlet of the condenser 6. A process medium exhaust port of the condenser 6 is connected with the vacuum pumping device 7 through a vacuum buffer tank 8, a process medium liquid outlet of the condenser 6 is connected with a third pipeline 103, a fourth pipeline 104, a fifth pipeline 105, a sixth pipeline 106 and a seventh pipeline 107 in parallel, a downstream end of the third pipeline 103 is provided with a third valve c which is connected with the top of the side wall of the distillation tower 5, a downstream end of the fourth pipeline 104 is provided with a fourth valve d which is connected with the middle part of the side wall of the distillation tower 5, the fifth pipeline 105 is provided with a fifth valve e which is connected with the first fraction tank 1, the sixth pipeline 106 is provided with a sixth valve f which is connected with the second fraction tank 2, the seventh pipeline 107 is provided with a seventh valve g which is connected with the third fraction tank 3, the first fraction tank 1, the second fraction tank 2 and the third fraction tank 3 are respectively connected with the vacuum buffer tank 8 through pipelines, the top of each fraction tank is respectively provided with a second nitrogen pipe 13, the upstream of each second nitrogen pipe 13 is used for connecting with a nitrogen source, and each second nitrogen pipe 13 is provided with a second check valve 14 and a tenth valve j in sequence from the upstream to the downstream. And second guiding and sprinkling pipes 15 are respectively arranged at the bottoms of the first distillation tank 1, the second distillation tank 2 and the third distillation tank 3, and a second guiding and sprinkling valve 16 is respectively arranged on each second guiding and sprinkling pipe 15.

Further, in order to release pressure according to needs or in an emergency state, an emptying pipe 49 is arranged at the top of the kettle body 41 and used for being connected with an exhaust system, and an emptying valve is arranged on the emptying pipe 49.

The utility model discloses a theory of operation does, the butanediol passes through the inlet pipe and provides the butanediol liquid to the cauldron is internal, agitating unit, heating intermediate layer work, acetylene gets into the air entrainment ring canal through the gas-filling pipe after, discharge downwards from the air entrainment hole, be located heat transfer coil pipe, stirring vane's below, the acetylene gas that gets into the internal portion of cauldron at first moves downwards, mix the back with the butanediol for the first time, then rise under buoyancy, and stir, mix with the butanediol secondary, long with the contact time of butanediol, area of contact is big, obtain the hydroxyether with the butanediol synthesis. After the synthesis is finished, the distillation tower is vacuumized through a vacuumizing device and is connected with the space in the kettle body, the synthesized material enters the distillation tower in a vapor state under the conditions of high temperature and negative pressure, different components are discharged out of the distillation tower in a vapor state under specific parameters by controlling parameters of the distillation tower due to different boiling points of the components and enter a condenser to be condensed into a liquid state, and a liquid fraction part reflows to the top of the distillation tower to improve the purity of the fraction and meet the actual requirement, and the liquid fraction part reflows to the middle of the distillation tower, so that high-boiling-point impurities in the fraction can be effectively reduced. Different fraction tanks are utilized to respectively receive fractions of different temperature sections by opening and closing different valves, generally, a first fraction tank is used for receiving front fraction, a second fraction tank is used for receiving hydroxyether to obtain a semi-finished product with the purity of 80-90%, and a third fraction tank is used for receiving high-boiling components. And completing the separation of the materials.

Claims

1. A hydroxyether reaction system, characterized by: comprises a reaction kettle (4), a distillation tower (5), a condenser (6), a vacuum extractor (7), a first fraction tank (1), a second fraction tank (2) and a third fraction tank (3),

the reaction kettle (4) comprises a kettle body (41), a heat exchange coil (42), an air-entrapping loop (43) and a stirring device (44),

a feeding pipe (45) is arranged at the top of the kettle body (41) and is used for connecting with a butanediol source, a heating interlayer is arranged on the peripheral wall of the kettle body (41),

the heat exchange coil (42) is positioned in the inner space of the kettle body (41), the stirring blades of the stirring device (44) are positioned in the inner space of the heat exchange coil (42),

the gas-filling ring pipe (43) is arranged in the kettle body (41) and is positioned below the heat exchange coil (42), a plurality of gas-filling holes (46) are arranged at the bottom of the gas-filling ring pipe (43), the gas-filling holes (46) are uniformly distributed along the circumferential direction of the gas-filling ring pipe (43), the gas-filling ring pipe (43) is connected with an acetylene source through a gas-filling pipe (47),

a feed inlet at the bottom of the distillation tower (5) is connected with the top of the kettle body (41) through a first pipeline (101), a steam outlet at the top of the distillation tower (5) is connected with a process medium inlet of the condenser (6) through a second pipeline (102),

a process medium exhaust port of the condenser (6) is connected with a vacuumizing device (7) through a vacuum buffer tank (8), a process medium liquid outlet of the condenser (6) is connected with a third pipeline (103), a fourth pipeline (104), a fifth pipeline (105), a sixth pipeline (106) and a seventh pipeline (107) in parallel, a downstream end of the third pipeline (103) is provided with a third valve (c), is connected with the top of the side wall of the distillation tower (5), the downstream end of the fourth pipeline (104) is provided with a fourth valve (d), is connected with the middle part of the side wall of the distillation tower (5), a fifth valve (e) is arranged on the fifth pipeline (105), and is connected with the first fraction tank (1), a sixth valve (f) is arranged on the sixth pipeline (106), and is connected with the second fraction tank (2), and a seventh valve (g) is arranged on a seventh pipeline (107) and is connected with the third fraction tank (3).

2. The hydroxyether reaction system of claim 1, wherein: the bottom of the kettle body (41) is provided with a slag discharge pipe (48), and the slag discharge pipe (48) is provided with a first valve (a).

3. The hydroxyether reaction system of claim 1, wherein: the number of the air adding pipes (47) is two, each air adding pipe (47) is provided with a second valve (b), the upstream ends of the two air adding pipes (47) are used for being connected with an acetylene source, and the downstream ends of the two air adding pipes (47) are connected with the air adding ring pipe (43) respectively and are positioned at two ends of the air adding ring pipe (43) with the same diameter.

4. The hydroxyether reaction system of claim 1, wherein: the top of the kettle body (41) is provided with an emptying pipe (49) for connecting with an exhaust system, and the emptying pipe (49) is provided with an emptying valve.

5. The hydroxyether reaction system of claim 1, wherein: the first pipeline (101) is coated with an insulating layer.

6. The hydroxyether reaction system of claim 1, wherein: and a liquid outlet at the bottom of the distillation tower (5) is connected with the top of the kettle body (41) through an eighth pipeline (108), and an eighth valve (h) is arranged on the eighth pipeline (108).

7. The hydroxyether reaction system of claim 6, wherein: and a first guide shower pipe (9) is arranged on the eighth pipeline (108) in parallel and is positioned at the upstream of the eighth valve (h), and a first guide shower valve (10) is arranged on the first guide shower pipe (9).

8. The hydroxyether reaction system of claim 6, wherein: and the eighth pipeline (108) is provided with a first nitrogen pipe (11) in parallel, the first nitrogen pipe (11) is positioned at the downstream of the eighth valve (h), the upstream end of the first nitrogen pipe (11) is used for being connected with a nitrogen source, and the first nitrogen pipe (11) is sequentially provided with a first check valve (12) and a ninth valve (i) from the upstream to the downstream.

9. The hydroxyether reaction system of claim 1, wherein: the first distillation tank (1), the second distillation tank (2) and the third distillation tank (3) are respectively connected with a vacuum buffer tank (8) through pipelines, the top of each distillation tank is respectively provided with a second nitrogen pipe (13), the upstream of each second nitrogen pipe (13) is used for being connected with a nitrogen source, and each second nitrogen pipe (13) is sequentially provided with a second one-way valve (14) and a tenth valve (j) from upstream to downstream.

10. The hydroxyether reaction system of claim 1, wherein: and second guide showering pipes (15) are respectively arranged at the bottoms of the first distillation tank (1), the second distillation tank (2) and the third distillation tank (3), and second guide showering valves (16) are respectively arranged on the second guide showering pipes (15).