CN110170285A - Synthesize the method and application of devolatilizer and continuous synthesis devolatilization - Google Patents

Abstract

The invention relates to the technical field of resin synthesis reaction and devolatilization production, and discloses a synthetic devolatilizer and a method and application for continuous synthesis and devolatilization. The reactor includes a synthesis reaction section (1), a devolatilization section (2) and a vacuum unit; wherein, the synthesis reaction section (1) is used for synthesis reaction; the devolatilization section (2) has a cavity for Devolatilization of the synthetic product synthesized in the synthesis reaction section (1); the vacuum unit is used to provide the vacuum degree required by the synthesis reaction section (1) and the devolatilization section (2); the synthesis The outlet of the reaction section (1) is connected with the inlet of the devolatilization section (2), so that the synthetic product synthesized in the synthesis reaction section (1) can directly fall into the devolatilization section (2) for devolatization. wave. The synthetic devolatilizer of the invention realizes continuous production, has high vaporization efficiency, small heat loss, low equipment investment and low maintenance cost.

Description

Method and application of synthetic devolatilizer and continuous synthetic devolatilization

technical field

The invention relates to the technical field of resin synthesis reaction and devolatilization production, in particular to a synthetic devolatilizer and a method and application for continuous synthesis and devolatilization.

Background technique

In the current production technology process such as resin synthesis reaction and removal of volatile solvents, the raw materials are usually sent to the reaction kettle to synthesize the crude resin, and then the crude resin containing the volatile solvent is transported to the atmospheric distillation kettle through a high temperature pump. , atmospheric distillation column, atmospheric pressure decolorization kettle and other equipment, and then further devolatilization and decolorization. However, the above-mentioned resin synthesis reaction and solvent removal device all have shortcomings, which are mainly as follows: 1. A single resin synthesis reactor operates intermittently, with small production scale and high energy consumption; 2. The subsequent design of the atmospheric distillation still process is a batch process , which increases the power consumption of high-temperature medium transportation, and the heat loss is large, and it cannot meet the requirements of continuous production of resin products and continuous devolatilization and decolorization; 3. Atmospheric pressure distillation towers and atmospheric pressure decolorization kettles in the process of devolatilization and decolorization, the vaporization effect Without negative pressure, the vaporization effect is good, and the heat consumption of the heating medium is also increased, and the trays in the atmospheric distillation column are easily damaged, and the equipment maintenance cost is increased. The reason for these problems is that the current technology cannot effectively integrate the resin synthesis reaction with the removal of volatile solvents, decolorization and other processes to achieve continuous unit operation.

SUMMARY OF THE INVENTION

The purpose of the present invention is to overcome the problems of the prior art that the resin synthesis devolatilization cannot be carried out continuously, etc., and provides a novel synthetic devolatilization with continuous production, high vaporization efficiency, little heat loss, less equipment investment and low maintenance costs. A method of devolatilization for continuous synthesis and continuous synthesis.

In order to achieve the above object, one aspect of the present invention provides a synthesis devolatilizer, the reactor includes a synthesis reaction section, a devolatilization section and a vacuum unit;

Wherein, the synthesis reaction section is used for synthesis reaction;

The devolatilization section has a cavity for devolatilization of the synthetic product synthesized in the synthesis reaction section;

The vacuum unit is used to provide the vacuum degree required by the synthesis reaction section and the devolatilization section;

The synthesis reaction section is arranged above the devolatilization section, and the outlet of the synthesis reaction section is connected with the inlet of the devolatilization section, so that the synthesis product synthesized in the synthesis reaction section can directly fall into the devolatilization section. The devolatilization section is used for devolatilization.

Preferably, the height of the cavity of the devolatilization section is above 4m, preferably 5-7m.

Preferably, the upper part of the devolatilization section is provided with a volatiles outlet, and the volatiles outlet is used to lead out the volatiles obtained by devolatilization.

Preferably, the volatiles outlet is connected to one or more volatiles separation units, and the volatiles separation unit includes a condenser and a gas-liquid separator connected in sequence; the volatiles inlet of the condenser is connected to the volatiles outlet or The gas-phase outlet of the gas-liquid separator of the previous-stage volatile matter separation unit, and the volatile matter outlet of the condenser is connected to the inlet of the gas-liquid separator.

Preferably, the volatiles separation unit is connected to the vacuum unit, and the vacuum unit is used to provide the vacuum degree required by the synthesis reaction section, the devolatilization section and the volatiles separation unit.

Preferably, the outside of the devolatilization section is provided with a jacket, and the outside of the synthesis reaction section is provided with a heating unit.

Preferably, the top of the synthesis reaction section is provided with a material inlet, and the bottom of the devolatilization section is provided with a material outlet.

Preferably, both the synthesis reaction section and the devolatilization section are set in a cylindrical shape, and the bottom of the devolatilization section is set in an inverted cone shape.

Preferably, the upper part of the synthesis reaction section is further provided with a vent.

The second aspect of the present invention provides a method for continuous synthesis and devolatilization, the method is carried out using the above-mentioned synthesis devolatilizer of the present invention, wherein after the reaction material is subjected to the synthesis reaction in the synthesis reaction section, the obtained synthesis product directly falls into the The devolatilization section is devolatilized.

Preferably, the reaction conditions in the synthesis reaction section include: the temperature is 100-150°C, and the pressure is 0.1-0.3MPa; more preferably, the temperature is 105-115°C, and the pressure is 0.1-0.2MPa.

Preferably, the devolatilization conditions of the devolatilization section (2) include: a temperature of 200-250° C. and a pressure of -0.098 to -0.08 MPa.

Preferably, the method is used for the synthesis of resin, more preferably, the resin is an SMA functionalized resin.

The third aspect of the present invention provides the application of the above-mentioned synthetic devolatilizer or the method for continuous synthetic devolatilization in resin preparation.

Through the above technical solutions, the synthetic devolatilizer and the method for continuous synthetic devolatilization provided by the present invention utilize a single device to complete the synthesis reaction and the volatile removal process, achieve an effective combination of synthesis and devolatilization, realize continuous production, and reduce The equipment investment is reduced, the heat loss generated in the intermediate process is reduced, and the vaporization efficiency is improved, which can meet the needs of high-efficiency and continuous production in large-scale production. The synthetic devolatilizer provided by the invention adopts a vacuum environment for feeding, and a negative pressure system is used for reverse vaporization in the process of removing volatiles, so as to improve the vaporization efficiency.

The synthetic devolatilizer provided by the invention integrates the resin reaction and volatiles removal into one device by effectively controlling the reaction temperature and pressure of the resin synthesis reaction section, and eliminates the intermediate equipment such as distillation kettle, decolorization kettle, distillation tower, etc. It saves the equipment investment, avoids the maintenance work of frequent cleaning of the distillation column or even dismantling the column section, and reduces the maintenance cost.

Description of drawings

Fig. 1 is the structural representation of the synthetic devolatilizer of the present invention.

Description of reference numerals

1. Synthesis reaction section 2. Devolatilization section 3. Condenser

4. Gas-liquid separator 5. Material inlet 6. Volatile outlet

7. Material outlet 8. The first heat transfer oil inlet 9. The first heat transfer oil outlet

10. Vent port 11. Drain port 12. Sight glass port

13. Pressure gauge port 14. Thermometer port 15. Jacket thermometer port

16. Reinforcing plate 17. Expansion joint 18. Circulating fluid inlet

19. Circulating liquid outlet 20. Condensing inlet 21. Condensing outlet

22. Gas outlet 23. Vacuum port 24. Solvent outlet

25. The second heat transfer oil inlet 26. The second heat transfer oil outlet

Detailed ways

The endpoints of ranges and any values disclosed herein are not limited to the precise ranges or values, which are to be understood to encompass values proximate to those ranges or values. For ranges of values, the endpoints of each range, the endpoints of each range and the individual point values, and the individual point values can be combined with each other to yield one or more new ranges of values that Ranges should be considered as specifically disclosed herein.

The synthesis devolatilizer provided by the present invention, as shown in FIG. 1 , the reactor includes a synthesis reaction section 1, a devolatilization section 2 and a vacuum unit; wherein, the synthesis reaction section 1 is used for synthesis reaction; the devolatilization section 2 has a cavity for devolatilization of the synthetic product synthesized in the synthesis reaction section 1; the vacuum unit is used to provide the vacuum degree required by the synthesis reaction section 1 and the devolatilization section 2; the The synthesis reaction section 1 is arranged above the devolatilization section 2, and the outlet of the synthesis reaction section 1 is connected to the inlet of the devolatilization section 2, so that the synthetic product synthesized in the synthesis reaction section 1 can be directly Fall into the devolatilization section 2 for devolatilization.

The structure of the synthesis reaction section 1 is not particularly limited, as long as the conditions required for the synthesis reaction can be provided. Preferably, a heating unit is provided outside the synthesis reaction section 1, and the heating unit is used to heat the synthesis reaction section 1 to provide the temperature of the synthesis reaction. The heating unit may include a heating pipe (such as a heating pipe) disposed outside the heating synthesis reaction section 1, the lower part of the heating pipe may be provided with a first heat transfer oil inlet 8, and the upper part may be provided with a first heat transfer oil. Exit 9.

According to a specific embodiment of the present invention, the synthesis reaction section 1 may have a shell-and-tube structure, and the tube side is used for introducing reaction materials, and the shell side is used for introducing heating medium such as heat transfer oil. In order to ensure the structural stability of the synthesis reaction section 1 , an expansion joint 17 is preferably provided in the middle of the heating unit. In addition, preferably, the upper part of the heating unit is further provided with a vent 10, and the lower part of the heating unit is also provided with a clean outlet 12.

In order to provide the time for the synthesis reaction, preferably, the height of the synthesis reaction section 1 is 2-10m, preferably 4-8m, more preferably 6m.

In the present invention, the cavity of the devolatilization section 2 makes the synthetic product in a reduced-pressure heating environment during the falling process to complete the devolatilization. Therefore, when the synthetic devolatilizer of the present invention is used for synthesis and devolatilization, the devolatilization is performed. The process can achieve good results without stirring, etc., with high processing efficiency and reduced costs. Preferably, a jacket is provided on the outside of the devolatilization section 2, and the jacket is used to heat the devolatilization section 2 to provide the temperature required for devolatilization. The upper part of the jacket can be provided with a second heat-conducting oil outlet 26, the lower part can be provided with a second heat-conducting oil inlet 25, and the jacket can also be provided with a jacket thermometer port 15 for detecting the heat-conducting oil in the jacket. temperature. In order to improve the strength of the devolatilization section 2, reinforcing plates 16 are preferably arranged in the jacket. The reinforcing plates 16 are preferably arranged at equal distances, and the distance is preferably 100-500mm, more preferably 200-400mm, eg 350mm.

Preferably, the synthesis reaction section 1 is directly connected above the devolatilization section 2, for example, it can be connected by a flange. In addition, in order to ensure the pressure of the synthesis reaction section 1 and the devolatilization section 2, it is necessary to seal the synthesis reaction section 1 and the devolatilization section 2, for example, a rubber gasket can be provided for sealing.

In order to provide sufficient devolatilization time, preferably, the cavity height of the devolatilization section 2 is 4m or more, preferably 5-7m, more preferably 5-6.5m. In addition, the inner diameter of the devolatilization section 2 is preferably 1.0-2.0 m, more preferably 1.2-1.7 m, and still more preferably 1.5 m.

According to the present invention, preferably, a material inlet 5 is arranged at the top of the synthesis reaction section 1, and a volatile outlet 6 is arranged at the upper part of the devolatilization section 2, and the volatile outlet 6 is used to export the volatilization obtained by devolatilization. The bottom of the devolatilization section 2 is provided with a material outlet 7, and the material outlet 7 is used to derive the synthetic devolatilized product.

In addition, the synthesis reaction section 1 is preferably arranged in a cylindrical shape, and the devolatilization section 2 preferably has a cylindrical upper portion and an inverted cone-shaped lower portion. Preferably, the upper height of the devolatilization section 2 is 3.5-4m, the lower apex angle of the inverted cone of the devolatilization section 2 is 50°-70°, more preferably 60°, and the height is 1-2, more preferably 1.5m . In addition, the upper part of the devolatilization section 2 is preferably pressed with an elliptical head, and the bottom part is preferably set as an inverted cone. Preferably, the pressure-receiving parts of the devolatilization section 2 are made of stainless steel.

In addition, the top of the devolatilization section 2 is preferably provided with a sight glass port 12, which is convenient for observing the resin generation and devolatilization state. In addition, it is also preferable to have a thermometer port 14 and a pressure gauge port 13 as required, and the thermometer port 14 is convenient for detection. For the temperature in the devolatilization section, the pressure gauge port 13 is convenient for detecting the pressure in the devolatilization section. The thermometer port 14 may be arranged at the upper and/or lower portion of the devolatilization section 2 , and the pressure gauge port 13 may be arranged at the upper portion of the devolatilization section 2 .

According to a preferred embodiment of the present invention, the volatile outlet 6 is connected to one or more volatile separation units, and the volatile separation unit includes a condenser 3 and a gas-liquid separator 4 that are connected in sequence; The volatiles inlet 20 is connected to the volatile outlet 6 or the gas-phase outlet 22 of the gas-liquid separator 4 of the previous stage volatiles separation unit, and the volatiles outlet 21 of the condenser 3 is connected to the gas-liquid separator 4 Entrance.

The condenser 3 and the gas-liquid separator 4 are not particularly limited, as long as the volatiles in the gas phase obtained by devolatilization can be separated. Preferably, the upper part of the condenser 3 is provided with a condensation inlet 20 for introducing volatiles, and the lower part of the condenser 3 is provided with a condensation outlet 21 for leading out the condensed volatiles. The outside of the condenser 3 can be provided with a cooling structure, for example, a jacket type cooling structure can be used. The gas phase is cooled by countercurrent circulation. The circulating liquid used in the jacket cooling structure can be water, chilled water, etc. as long as it provides sufficient cooling effect. The gas-liquid separator 4 can be a gas-liquid separation tank or the like, and the bottom of the gas-liquid separator 4 is provided with a solvent outlet 24 for recovering the solvent.

When using a two-stage volatiles separation unit, in the first-stage volatiles separation unit, the gas-phase volatiles pass through the tube side of the condenser 3 and are cooled by the circulating water introduced into the shell side, and then pass through the gas-liquid separator 4 to separate the liquid phase. Volatiles; then, the gas phase part enters the second-stage volatiles separation unit, and is deeply condensed by the chilled water introduced into the 3-stage condenser and from the shell-side, so as to effectively condense the volatiles; after the second-stage volatiles separation unit The liquid-phase volatiles condensed by the condenser 3 enter the recovery tank.

According to a preferred embodiment of the present invention, the volatile separation unit is connected to the vacuum unit, and the vacuum unit is used to provide the synthesis reaction section 1, the devolatilization section 2 and the volatile separation unit required vacuum. In the case of using multiple volatile separation units, the volatile outlet of the last volatile separation unit is used as the vacuum hole 23, and the vacuum hole 23 is connected to the vacuum unit. Specifically, the volatile separation unit is connected to the vacuum unit through a vacuum port 23 .

The second aspect of the present invention provides a method for continuous synthesis and devolatilization, which is carried out using the above-mentioned synthesis devolatilizer of the present invention; wherein, after the reaction material undergoes a synthesis reaction in the synthesis reaction section 1, the obtained synthesis product directly drops into the devolatilization section 2 for devolatilization.

In the present invention, the synthetic product synthesized in the synthesis reaction section 1 enters the devolatilization section 2, and the solution containing the synthetic product is rapidly heated to the temperature required for devolatilization by the external heat-conducting oil of the devolatilization section 2, and rapidly in a foamed state Entering the devolatilizer, the excess unreacted raw materials and the solvent that does not participate in the reaction are discharged from the top of the devolatilizer in gaseous form, and the molten synthetic product after degassing falls into the bottom of the devolatilizer,

The method for continuous synthesis and devolatilization of the present invention can be used in the preparation of resins and other reactions that require synthesis and devolatilization at the same time, and can greatly improve the efficiency of preparation; it is preferably used for synthetic resins, and more preferably used for synthesizing SMA functionalized resins. Specifically, when synthesizing the SMA functionalized resin, the reaction materials include: styrene, acrylonitrile and ethylbenzene. The flow rate of introducing the reaction material into the synthesis reaction section 1 can be selected according to the structure of the synthesis reaction section 1 and the required reaction time, for example, it can be 0.1-0.3 m/s.

According to the present invention, the reaction conditions in the synthesis reaction section 1 may include: the temperature is 100-150°C, and the pressure is 0.1-0.3MPa; preferably, the temperature is 100-120°C, and the pressure is 0.1-0.3MPa; more preferably Ground, the temperature is 105-115°C, and the pressure is 0.1-0.2MPa, for example, the temperature is 110±5°C, and the temperature is 0.15MPa. According to the present invention, the devolatilization conditions of the devolatilization section 2 may include: the temperature is 200-250°C, and the pressure is -0.098～-0.08MPa; preferably, the temperature is 210-230°C, and the pressure is -0.098～-0.09 MPa; more preferably, the temperature is 220°C and the pressure is -0.095MPa.

In order to provide the conditions for the above reaction and devolatilization, preferably, the temperature of the heat transfer oil used in the heating unit of the synthesis reaction section 1 is 120-200°C, preferably 130-160°C, and the pressure is 0.1-0.5Mpa; the The temperature of the heat transfer oil in the jacket of the devolatilization section 2 is 230-320°C, preferably 260-280°C, and the pressure is 0.05-0.15MPa.

The third aspect of the present invention provides the application of the above-mentioned synthetic devolatilizer or the method for continuous synthetic devolatilization in resin preparation.

The present invention will be described in detail below by means of examples.

The SMA functionalized resin is prepared by a synthetic devolatilizer as shown in Figure 1, the reactor includes a synthesis reaction section 1, a devolatilization section 2, a two-stage volatile separation unit and a vacuum unit.

The synthesis reaction section 1 is used for synthesis reaction, and is provided with a heating unit composed of a heating tube on the outside. The upper part of the heating unit is also provided with a vent 10 , and the lower part is also provided with a clean outlet 12 . An expansion joint 17 is also provided in the middle of the heating unit.

The devolatilization section 2 has a cavity for devolatilization of the synthetic product synthesized in the synthesis reaction section 1, the height of the cavity is 5m, and the inner diameter is 1.5m. The outside of the devolatilization section 2 is provided with a jacket, the jacket is used to heat the devolatilization section 2, and the upper part of the jacket is provided with a second heat-conducting oil outlet 26 for introducing heat-conducting oil and a clamp for setting a thermometer. The lower part of the thermometer port 15 is provided with a second heat-conducting oil inlet 25 for leading out the heat-conducting oil. The inside of the jacket is provided with a reinforcing plate 16 (which is horizontally arranged around the outer circumference of the jacket, with a longitudinal interval of 350 mm).

Described synthesis reaction section 1 is cylindrical, the upper part of described devolatilization section 2 is cylindrical (inner height 3.5m), the lower part is inverted cone (inner height 3.5m, apex angle 60°), described synthesis reaction section 1 and the upper part of the devolatilization section 2 both use elliptical heads to press. The top of the synthesis reaction section 1 is provided with a material inlet 5, the upper part of the devolatilization section 2 is provided with a volatiles outlet 6, and the bottom of the devolatilization section 2 is provided with a material outlet 7 for deriving synthetic devolatilization. product.

The synthesis reaction section 1 is directly arranged above the devolatilization section 2 to form the body of the synthesis devolatilizer, and the outlet of the synthesis reaction section 1 is connected to the inlet of the devolatilization section 2 through a flange, so that in the The synthetic product synthesized in the synthesis reaction section 1 can directly fall into the devolatilization section 2 for devolatilization.

Two-stage volatile matter separation units are connected in series with the volatile matter outlet 6 for separation of volatile matter. Volatile separation units at all levels include a condenser 3 and a gas-liquid separator 4. The upper part of the condenser 3 is provided with a condensation inlet 20 for introducing volatiles, and the lower part of the condenser 3 is provided with a condensation outlet 21 for In order to export the condensed volatiles, a jacket cooling structure is arranged outside the condenser 3 , the lower part of the jacket is provided with a circulating liquid inlet 18 , and the upper part is provided with a circulating liquid outlet 19 . In addition, the volatile inlet 20 of the condenser 3 of the first-stage volatile separation unit is connected to the volatile outlet 6, and the volatile inlet 20 of the condenser 3 of the second-stage volatile separation unit is connected to the first-stage volatile separation unit The gas phase outlet 22 of the gas-liquid separator 4.

The vacuum unit (vacuum pump) is connected to the gas-phase outlet 22 of the gas-liquid separator 4 of the second-stage volatile matter separation unit, and is used to provide the vacuum degree required by the synthesis reaction section 1 and the devolatilization section 2 .

Turn on the vacuum pump, introduce the reaction material at a speed of 0.2m/s through the material inlet 5, and introduce 140°C heat-conducting oil into the jacket of the synthesis reaction section 1, so that the conditions of the synthesis reaction are temperature 110°C, time 5min, pressure 0.15MPa . The synthetic product obtained by the synthesis reaction can be directly dropped into the devolatilization section 2 for devolatilization, and the heating unit of the devolatilization section 2 is fed with heat-conducting oil at 270 °C, so that the conditions of the devolatilization are the temperature of 220 °C, the time of 0.5 min, and the pressure. -0.095MPa. The product obtained by devolatilization is led out from the material outlet 7, the volatiles are introduced into the two-stage volatiles separation unit from the volatiles outlet 6, and condensed water is introduced into the condenser 3 of the first-stage volatiles separation unit for condensation, and then in the gas-liquid The gas-liquid separation is carried out in the separator 4 , and then chilled water is introduced into the condenser 3 of the second-stage volatile matter separation unit for condensation, and then the gas-liquid separation is carried out in the gas-liquid separator 4 . The resulting solvent is drawn from the solvent outlet 24 of the gas-liquid separator 4 of the two-stage volatiles separation unit.

The preferred embodiments of the present invention have been described above in detail, however, the present invention is not limited thereto. Within the scope of the technical concept of the present invention, a variety of simple modifications can be made to the technical solutions of the present invention, including the combination of various technical features in any other suitable manner. These simple modifications and combinations should also be regarded as the content disclosed in the present invention. All belong to the protection scope of the present invention.

Claims (10)

1. a kind of synthesis devolatilizer, which is characterized in that the reactor includes synthetic reaction section (1), devolatilization section (2) and vacuum list Member；

Wherein, the synthetic reaction section (1) is used for synthetic reaction；

The devolatilization section (2) has cavity, the devolatilization for the synthetic product that synthesis obtains in the synthetic reaction section (1)；

The vacuum unit is used to provide the described the vacuum degree that synthetic reaction section (1) and the devolatilization section (2) need；

The synthetic reaction section (1) is set to the top of the devolatilization section (2), the outlet of the synthetic reaction section (1) with it is described The entrance of devolatilization section (2) connects, so that can fall directly into the synthetic product that the middle synthesis of the synthetic reaction section (1) obtains described Devolatilization section (2) carries out devolatilization.

2. synthesis devolatilizer according to claim 1, wherein the height of the cavity of the devolatilization section (2) is 4m or more, excellent It is selected as 5-7m；

Preferably, the top of the devolatilization section (2) is provided with volatiles outlet (6), and the volatiles outlet (6) is de- for exporting The volatile matter waved.

3. synthesis devolatilizer according to claim 2, wherein volatilization more than volatiles outlet (6) the connection level-one Object separative unit, the volatile matter separative unit include sequentially connected condenser (3) and gas-liquid separator (4)；

The volatile matter import (20) of the condenser (3) connects the volatiles outlet (6) or the previous stage volatile matter point The gaseous phase outlet (22) of gas-liquid separator (4) from unit,

The volatiles outlet (21) of the condenser (3) connects the entrance of the gas-liquid separator (4).

4. synthesis devolatilizer according to claim 3, wherein the volatile matter separative unit and the vacuum unit connect It connects, the vacuum unit is used to provide the described synthetic reaction section (1), the devolatilization section (2) and the volatile matter separative unit and needs The vacuum degree wanted.

5. synthesis devolatilizer described in any one of -5 according to claim 1, wherein the external setting of the devolatilization section (2) There is collet, the outside of the synthetic reaction section (1) is provided with heating unit.

6. synthesis devolatilizer described in any one of -5 according to claim 1, wherein the top of the synthetic reaction section (1) It is provided with material inlet (5), the bottom of the devolatilization section (2) is provided with material outlet (7)；

Preferably, the synthetic reaction section (1) and the devolatilization section (2) are disposed as cylindrical shape, the bottom of the devolatilization section (2) It is set as back taper；

Preferably, the top of the synthetic reaction section (1) is additionally provided with drain (10).

7. a kind of method of continuous synthesis devolatilization, which is characterized in that this method uses described in any one of claim 1-6 Devolatilizer is synthesized to carry out；

Wherein, after the synthetic reaction section (1) carries out synthetic reaction, obtained synthetic product falls directly into described reaction mass Devolatilization section (2) carries out devolatilization.

8. according to the method described in claim 7, wherein, the reaction condition in the synthetic reaction section (1) includes: that temperature is 100-150 DEG C, pressure 0.1-0.3MPa；It is highly preferred that temperature is 105-115 DEG C, pressure 0.1-0.2MPa；

Preferably, the devolatilization condition of the devolatilization section (2) include: temperature be 200-250 DEG C, pressure be -0.098~- 0.08MPa。

9. method according to claim 7 or 8, wherein the method is used for the synthesis of resin, and the resin is SMA function Resin can be changed.

10. continuous described in any one of synthesis devolatilizer or claim 7-9 described in any one of claim 1-6 Synthesize application of the method for devolatilization in resin preparation.