CN112661735A - Continuous production system and method for methyl tetrahydrophthalic anhydride - Google Patents
Continuous production system and method for methyl tetrahydrophthalic anhydride Download PDFInfo
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- MWSKJDNQKGCKPA-UHFFFAOYSA-N 6-methyl-3a,4,5,7a-tetrahydro-2-benzofuran-1,3-dione Chemical compound C1CC(C)=CC2C(=O)OC(=O)C12 MWSKJDNQKGCKPA-UHFFFAOYSA-N 0.000 title claims abstract description 29
- 238000010924 continuous production Methods 0.000 title claims abstract description 23
- 238000000034 method Methods 0.000 title claims abstract description 18
- 229910052799 carbon Inorganic materials 0.000 claims abstract description 54
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims abstract description 53
- FPYJFEHAWHCUMM-UHFFFAOYSA-N maleic anhydride Chemical compound O=C1OC(=O)C=C1 FPYJFEHAWHCUMM-UHFFFAOYSA-N 0.000 claims abstract description 31
- 239000003054 catalyst Substances 0.000 claims abstract description 27
- 239000007788 liquid Substances 0.000 claims abstract description 24
- 238000003860 storage Methods 0.000 claims abstract description 23
- 238000004519 manufacturing process Methods 0.000 claims abstract description 7
- 238000010438 heat treatment Methods 0.000 claims description 23
- 238000006317 isomerization reaction Methods 0.000 claims description 14
- 239000010408 film Substances 0.000 claims description 11
- 238000003786 synthesis reaction Methods 0.000 claims description 10
- 239000010409 thin film Substances 0.000 claims description 9
- 230000015572 biosynthetic process Effects 0.000 claims description 7
- 238000012806 monitoring device Methods 0.000 claims description 6
- 238000012544 monitoring process Methods 0.000 claims description 6
- 238000009413 insulation Methods 0.000 claims description 2
- 238000005086 pumping Methods 0.000 claims description 2
- 238000006243 chemical reaction Methods 0.000 abstract description 13
- 230000008569 process Effects 0.000 abstract description 9
- 238000005265 energy consumption Methods 0.000 abstract description 2
- 125000004432 carbon atom Chemical group C* 0.000 abstract 1
- 239000000047 product Substances 0.000 description 25
- 239000000463 material Substances 0.000 description 10
- 239000002994 raw material Substances 0.000 description 6
- 238000010923 batch production Methods 0.000 description 3
- 239000003822 epoxy resin Substances 0.000 description 3
- 230000014759 maintenance of location Effects 0.000 description 3
- 229920000647 polyepoxide Polymers 0.000 description 3
- 239000000376 reactant Substances 0.000 description 3
- RRHGJUQNOFWUDK-UHFFFAOYSA-N Isoprene Chemical compound CC(=C)C=C RRHGJUQNOFWUDK-UHFFFAOYSA-N 0.000 description 2
- LPXKXYATZPHDJU-UHFFFAOYSA-N O.O.O.O.O.[C] Chemical compound O.O.O.O.O.[C] LPXKXYATZPHDJU-UHFFFAOYSA-N 0.000 description 2
- 230000008859 change Effects 0.000 description 2
- 238000001816 cooling Methods 0.000 description 2
- 238000004821 distillation Methods 0.000 description 2
- 239000012467 final product Substances 0.000 description 2
- LNEPOXFFQSENCJ-UHFFFAOYSA-N haloperidol Chemical compound C1CC(O)(C=2C=CC(Cl)=CC=2)CCN1CCCC(=O)C1=CC=C(F)C=C1 LNEPOXFFQSENCJ-UHFFFAOYSA-N 0.000 description 2
- 238000000199 molecular distillation Methods 0.000 description 2
- 238000011084 recovery Methods 0.000 description 2
- 238000007670 refining Methods 0.000 description 2
- 239000011265 semifinished product Substances 0.000 description 2
- PMJHHCWVYXUKFD-SNAWJCMRSA-N (E)-1,3-pentadiene Chemical group C\C=C\C=C PMJHHCWVYXUKFD-SNAWJCMRSA-N 0.000 description 1
- LWMIDUUVMLBKQF-UHFFFAOYSA-N 4-methyl-3a,4,5,7a-tetrahydro-2-benzofuran-1,3-dione Chemical compound CC1CC=CC2C(=O)OC(=O)C12 LWMIDUUVMLBKQF-UHFFFAOYSA-N 0.000 description 1
- JDBDDNFATWXGQZ-UHFFFAOYSA-N 5-methyl-3a,4,5,7a-tetrahydro-2-benzofuran-1,3-dione Chemical compound C1=CC(C)CC2C(=O)OC(=O)C12 JDBDDNFATWXGQZ-UHFFFAOYSA-N 0.000 description 1
- 229920002732 Polyanhydride Polymers 0.000 description 1
- 239000002253 acid Substances 0.000 description 1
- 238000005452 bending Methods 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 239000000945 filler Substances 0.000 description 1
- 238000007710 freezing Methods 0.000 description 1
- 230000008014 freezing Effects 0.000 description 1
- 239000008187 granular material Substances 0.000 description 1
- 230000036541 health Effects 0.000 description 1
- 238000005286 illumination Methods 0.000 description 1
- 230000007774 longterm Effects 0.000 description 1
- 231100000053 low toxicity Toxicity 0.000 description 1
- 238000002844 melting Methods 0.000 description 1
- 230000008018 melting Effects 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000005457 optimization Methods 0.000 description 1
- PMJHHCWVYXUKFD-UHFFFAOYSA-N piperylene Natural products CC=CC=C PMJHHCWVYXUKFD-UHFFFAOYSA-N 0.000 description 1
- 239000002952 polymeric resin Substances 0.000 description 1
- 238000006116 polymerization reaction Methods 0.000 description 1
- 238000004382 potting Methods 0.000 description 1
- 238000007086 side reaction Methods 0.000 description 1
- 239000011949 solid catalyst Substances 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 229920003002 synthetic resin Polymers 0.000 description 1
- 230000009466 transformation Effects 0.000 description 1
- 238000005292 vacuum distillation Methods 0.000 description 1
- 238000004017 vitrification Methods 0.000 description 1
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Abstract
The invention discloses a continuous production system and a continuous production method of methyl tetrahydrophthalic anhydride, wherein the production system comprises a tower reactor, a carbon five storage tank, a maleic anhydride storage tank, a film evaporator, a carbon five receiving tank, an adiabatic evaporator and a finished product tank, the carbon five storage tank is connected with the tower reactor through a first magnetic pump, the maleic anhydride storage tank is connected with the tower reactor through a second magnetic pump, the tower reactor is connected with the film evaporator, the film evaporator comprises a steam outlet and a liquid outlet, the steam outlet is connected with the carbon five receiving tank through a first condenser, the liquid outlet is connected with the adiabatic evaporator, a catalyst fixer is arranged between the liquid outlet and the adiabatic evaporator, and the adiabatic evaporator is connected with a second condenser through a third magnetic pump and then is connected with the finished product tank. The continuous production system of the methyl tetrahydrophthalic anhydride really realizes the continuous production of the methyl tetrahydrophthalic anhydride, improves the efficiency by about 200 percent compared with the traditional process, has more thorough reaction, reduces the investment of five carbon atoms, reduces the energy consumption, and improves the yield and the quality of the product.
Description
Technical Field
The invention belongs to the technical field of chemical industry, and particularly relates to a continuous production system and method for methyl tetrahydrophthalic anhydride.
Background
The liquid methyl tetrahydrophthalic anhydride has the characteristics of light color, low volatility, low toxicity, stable performance, low freezing point, long-term closed storage at room temperature, low viscosity, good intermiscibility with various epoxy resins and the like, and a condensate thereof has excellent electrical property and heat resistance, forms an insulating potting material and a castable material with the epoxy resins, fillers and the like, and is widely applied to the fields of electronic and electrical industry, aerospace and aviation industry and the like. The methyl tetrahydrophthalic anhydride is prepared by the polymerization reaction of maleic anhydride, piperylene and isoprene in carbon five, the product has 2 isomers, namely 4-methyl tetrahydrophthalic anhydride and 3-methyl tetrahydrophthalic anhydride, the melting points are 65 ℃ and 63 ℃ respectively, the product is rarely used alone as a curing agent, and the actual product is a liquid mixture of various isomers.
At present, the method for producing the methyl tetrahydrophthalic anhydride at home and abroad is mainly a batch production process, the automation degree is low, meanwhile, in the former synthesis process of maleic anhydride and carbon pentahydrate, carbon pentahydrate autopolymer is generated due to long-time stay reaction in a kettle, the reaction kettle needs to be cleaned frequently, and simultaneously, a large amount of polyanhydride is generated after distillation, so that the problems of poor product quality stability, low efficiency, low yield and the like are caused.
The Chinese patent application with the application number of 201711220925.7 discloses a device for continuously producing methyl tetrahydrophthalic anhydride, which only adds a detector and other testing devices on the basis of the existing batch production process and does not really realize the continuous production of the methyl tetrahydrophthalic anhydride.
The Chinese patent application with the application number of 201811320465.X discloses a process device for refining methyl tetrahydrophthalic anhydride by chemical synthesis isomeric molecular distillation, which comprises an ultrasonic synthesis reaction kettle, a magnetic isomeric reaction kettle, a methyl tetrahydrophthalic anhydride cooling kettle, a short-path molecular distiller, a light fraction methyl tetrahydrophthalic anhydride tank, a heavy fraction polymeric resin tank and the like, wherein isomeric methyl tetrahydrophthalic anhydride is obtained through the magnetic isomeric reaction kettle, and isomeric methyl tetrahydrophthalic anhydride enters the short-path molecular distiller through cooling for refining, so that the novel energy-saving and consumption-reducing methyl tetrahydrophthalic anhydride molecular distillation clean low-carbon process is achieved. After the semi-finished product in the first kettle is synthesized in the synthesis reaction kettle, the semi-finished product enters the magnetic isomerization reaction kettle and the like in sequence, namely the whole reaction is carried out in batches, so the process belongs to the optimization and upgrading of the batch production process, the continuous production of the methyl tetrahydrophthalic anhydride is not really realized, and the problem of low efficiency exists.
Disclosure of Invention
In order to solve the technical problems, the invention adopts the technical scheme that: the continuous production system of the methyl tetrahydrophthalic anhydride comprises a tower reactor, a carbon five storage tank, a maleic anhydride storage tank, a film evaporator, a carbon five receiving tank, an adiabatic evaporator and a finished product tank, wherein the carbon five storage tank is connected with the tower reactor through a first magnetic pump, the maleic anhydride storage tank is connected with the tower reactor through a second magnetic pump, the tower reactor is connected with the film evaporator, the film evaporator comprises a steam outlet and a liquid outlet, the steam outlet is connected with the carbon five receiving tank through a first condenser, the liquid outlet is connected with the adiabatic evaporator, a catalyst fixer is arranged between the liquid outlet and the adiabatic evaporator, and the adiabatic evaporator is connected with the finished product tank after being connected with a second condenser through a third magnetic pump.
Preferably, a first flow meter is arranged between the first magnetic pump and the tower reactor, and a second flow meter is arranged between the second magnetic pump and the tower reactor.
Preferably, the production system further comprises a monitoring control system, the monitoring control system comprises a DCS, the DCS is connected with the first flowmeter and the second flowmeter, and the first magnetic pump, the second magnetic pump and the third magnetic pump are respectively connected with the DCS.
Preferably, the tower reactor is divided into a plurality of sections from top to bottom, each section is provided with a heating device and a temperature monitoring device, and the heating device and the temperature monitoring device are respectively connected with the DCS.
Preferably, the liquid outlet is connected with the heat-insulating evaporator through a heat-conducting oil heating jacket sleeve, the catalyst fixer is arranged on the heat-conducting oil heating jacket sleeve, and the temperature of the heat-conducting oil heating jacket sleeve is controlled by DCS.
The continuous production method of the methyl tetrahydrophthalic anhydride uses the continuous production system and comprises the following steps: storing carbon five in a carbon five storage tank, storing maleic anhydride in a maleic anhydride storage tank, and conveying specified amounts of the carbon five and the maleic anhydride to a tower reactor by using a first metering pump and a second metering pump respectively, wherein the molar ratio of the maleic anhydride to the carbon five is 1: 1.03 to 1.10, controlling the synthesis temperature in the tower reactor to be 70 to 80 ℃, ensuring that the carbon five which is not reacted enters a thin film evaporator with the temperature controlled at 120 ℃ after the residence time in the tower reactor is 30 to 40 seconds, pumping and recovering the carbon five which is not reacted into a carbon five receiving tank after being condensed by a first condenser under the high vacuum state, introducing the liquid at the bottom of the thin film evaporator into a catalyst fixer with a catalyst for isomerization reaction at the temperature of 160 ℃ and 200 ℃, then entering a heat insulation evaporator with the temperature controlled at 140 ℃ and 130 ℃ and collecting the gasified product in a finished product tank after being condensed by a second condenser.
Preferably, the temperature of each stage in the column reactor is equal.
The invention has the beneficial effects that: the continuous production system of the methyl tetrahydrophthalic anhydride really realizes the continuous production of the methyl tetrahydrophthalic anhydride. Compared with the traditional process (one 10 m)3The reaction kettle can produce 4 batches of materials at most in 24 hours), the continuous production system can produce about 100 tons of products in one day, and the efficiency is improved by about 200%; the method has the advantages that the method is accurately measured according to the contents of maleic anhydride and carbon five, so that the reaction is more thorough, the investment of the carbon five is reduced, and the ratio is close to a theoretical value; the occupied area of the device is smaller under the same yield, the energy consumption is lower, and the problem of the transformation of the existing old factory is solved; the retention time of reactants is shortened, the yield of the catalyst product can reach 98.7 percent, and the yield is improved by about 5 percent; the quality stability of the product is improved, and the product does not change color in one year under the illumination condition; simultaneously, adopt novel large granule solid catalyst, guarantee that isomerization degree reaches more than 35%, catalyst remains when avoiding later stage vacuum distillation to influence product quality and yield in the cauldron. Meanwhile, the influence of catalyst residues in the kettle on the quality and yield of the product during later-stage reduced pressure distillation is avoided. The final product is tested, wherein the content of free acid is determined by general0.1 percent of the product is reduced to 0.04 percent, the vitrification temperature of the product and an epoxy resin system is increased to 105 ℃, the impact strength reaches 17-18 KJ/square meter, the tensile strength reaches 72MPa, and the bending strength reaches 130 MPa. The smell of the product is greatly reduced, and the method plays a great role in environmental impact and occupational health protection caused by downstream production.
Drawings
Fig. 1 is a schematic structural view of the present invention.
Detailed Description
The technical solutions of the present invention will be described clearly and completely with reference to the accompanying drawings, and it should be understood that the described embodiments are some, but not all embodiments of the present invention. All other embodiments, which can be derived by a person skilled in the art from the embodiments given herein without making any creative effort, shall fall within the protection scope of the present invention.
In the description of the present invention, it should be noted that the terms "center", "upper", "lower", "left", "right", "vertical", "horizontal", "inner", "outer", etc., indicate orientations or positional relationships based on the orientations or positional relationships shown in the drawings, and are only for convenience of description and simplicity of description, but do not indicate or imply that the device or element being referred to must have a particular orientation, be constructed and operated in a particular orientation, and thus, should not be construed as limiting the present invention. Furthermore, the terms "first," "second," and "third" are used for descriptive purposes only and are not to be construed as indicating or implying relative importance.
In the description of the present invention, it should be noted that, unless otherwise explicitly specified or limited, the terms "mounted," "connected," and "connected" are to be construed broadly, e.g., as meaning either a fixed connection, a removable connection, or an integral connection; can be mechanically or electrically connected; they may be connected directly or indirectly through intervening media, or they may be interconnected between two elements. The specific meanings of the above terms in the present invention can be understood in specific cases to those skilled in the art.
Example 1
As shown in fig. 1, the continuous production system of methyl tetrahydrophthalic anhydride comprises a tower reactor 7, a carbon five storage tank 1, a maleic anhydride storage tank 2, a film evaporator 8, a carbon five receiving tank 10, an adiabatic evaporator 12 and a finished product tank 15, wherein the carbon five storage tank 1 is connected with the tower reactor 7 through a first magnetic pump 3, the maleic anhydride storage tank 2 is connected with the tower reactor 7 through a second magnetic pump 4, the tower reactor 7 is connected with the film evaporator 8, the film evaporator 8 comprises a steam outlet and a liquid outlet, the steam outlet is connected with the carbon five receiving tank 10 through a first condenser 9, the liquid outlet is connected with the adiabatic evaporator 12, a catalyst fixer 11 is arranged between the liquid outlet and the adiabatic evaporator 12, and the adiabatic evaporator 12 is connected with a finished product tank 15 after being connected with a second condenser 14 through a third magnetic pump 13.
Further, a first flow meter 5 is arranged between the first magnetic pump 3 and the tower reactor 7, and a second flow meter 6 is arranged between the second magnetic pump 4 and the tower reactor 7.
Further, the production system further comprises a monitoring control system, the monitoring control system comprises a DCS16, a DCS16 is connected with the first flowmeter 5 and the second flowmeter 6, and the first magnetic pump 3, the second magnetic pump 4 and the third magnetic pump 13 are respectively connected with a DCS 16. The first flow meter 5 and the second flow meter 6 respectively control the carbon five and the maleic anhydride to enter the tower reactor 7 at set flow rates, so that the proportion of the carbon five and the maleic anhydride participating in the reaction in the tower reactor 7 is controlled, and the retention time of the materials in the tower reactor 7 is controlled.
Further, the tower reactor 7 is divided into a plurality of sections from top to bottom, each section is provided with a heating device and a temperature monitoring device, and the heating device and the temperature monitoring device are respectively connected with the DCS 16. And by adopting segmented temperature control, the temperature of each segment in the tower reactor 7 is similar, and the excessive reaction temperature change of the maleic anhydride and the carbon five in the tower reactor 7 is avoided. The maleic anhydride and the carbon five move from bottom to top in the tower reactor 7, the reaction is faster when the maleic anhydride and the carbon five at the lower end of the tower reactor 7 are contacted, the heat is released and increased rapidly in the reaction process, and the reaction is less when going upward, and the heat release is reduced gradually. And the adoption of segmented temperature control avoids the generation of side reaction caused by overhigh temperature when the maleic anhydride is contacted with the carbon five.
Further, the liquid outlet is connected with the heat-insulating evaporator 12 through a heat-conducting oil heating jacket pipe, the catalyst fixer 11 is installed on the heat-conducting oil heating jacket pipe, and the temperature of the heat-conducting oil heating jacket pipe is controlled by DCS. The heat conducting oil is used for heating the jacketed pipe to heat the material, so that the material can reach a set temperature when the material is subjected to isomerization reaction by using the catalyst in the catalyst fixer 11.
Raw material carbon five and maleic anhydride respectively enter a tower reactor 7 through a first flowmeter 5 and a second flowmeter 6 according to a set proportion, an outlet of the tower reactor 7 is connected with an inlet of a thin film evaporator 8, redundant carbon five components are separated and recovered at a certain temperature and vacuum degree, and the carbon five enters a carbon five recovery tank through a first condenser for recovery. And a material outlet of the thin film evaporator 8 is connected with a heat-conducting oil heating jacket pipe, and the heat-conducting oil heating jacket pipe is used for heating the material. Then the material is subjected to isomerization reaction by using the catalyst in the catalyst fixer 11, gasified in the adiabatic evaporator 12, and finally condensed by the second condenser 14 and collected in the finished product tank 15.
Example 2
The molar ratio of maleic anhydride to carbon five is 1: the raw material of 1.05 is respectively conveyed to the tower reactor by a first metering pump and a second metering pump at 5T/h, the synthesis temperature in the tower reactor is controlled to be 70-75 ℃, the reactant is ensured to stay in the tower reactor for 40 seconds and then enters a thin film evaporator with the temperature controlled to be 116-118 ℃, and the unreacted carbon five is extracted, condensed and recovered under the condition that the vacuum is more than-0.98 MPa. The liquid at the bottom enters a heat-conducting oil heating jacket pipe with the temperature of 170-175 ℃, enters a catalyst fixer with a catalyst after being heated for isomerization reaction, and then enters an insulating evaporator with the temperature controlled at 136-140 ℃. The gasified product is condensed and collected by a second condenser. The final product yield is 98.92%, and the isomerization depth is 36.7%.
Example 3
The molar ratio of maleic anhydride to carbon five is 1: the raw material of 1.10 is conveyed to a tower reactor by a metering pump at 4T/h, the synthesis temperature is controlled to be 70-73 ℃, the reactant is ensured to stay in the tower reactor for 30 seconds and then enters a film evaporator with the temperature controlled to be 112-115 ℃, and the unreacted carbon five is extracted, condensed and recovered under the condition that the vacuum is more than-0.98 MPa. The liquid at the bottom enters a heat-conducting oil heating jacket pipe with the temperature of 165-170 ℃, a catalyst fixer with a catalyst is used for isomerization reaction, then the liquid enters an adiabatic evaporator with the temperature of 132-135 ℃, and the gasified product is condensed and collected by a second condenser. Finally, the product yield is 98.73 percent, and the isomerization depth is 35.8 percent.
Example 4
The molar ratio of maleic anhydride to carbon five is 1: 1.03 is conveyed to a tower reactor by a metering pump at 5T/h, the synthesis temperature is controlled to be 75-80 ℃, the residence time in the tower reactor is ensured to be 40 seconds, then the raw materials enter a film evaporator with the temperature controlled to be 120-123 ℃, and unreacted carbon five is extracted, condensed and recovered under the condition that the vacuum is more than-0.98 MPa. The bottom liquid enters a heat-conducting oil heating jacket through a pipeline at the temperature of 175-180 ℃, is subjected to isomerization reaction in a catalyst fixer with a catalyst, then enters an insulating evaporator with the temperature controlled at 140-145 ℃, and is condensed and collected by a condenser. Finally, the product yield is 98.76%, and the isomerization depth is 38.9%.
Example 5
The molar ratio of maleic anhydride to carbon five is 1: the raw material of 1.05 is conveyed to the tower reactor by a metering pump at 5T/h, the synthesis temperature is controlled to be 70-75 ℃, the raw material enters a thin film evaporator 8 with the temperature controlled to be 120-123 ℃ after the retention time in the tower reactor 7 is 40 seconds, and the unreacted carbon five is extracted, condensed and recovered under the state that the vacuum is more than-0.98 MPa. The bottom liquid enters a heat-conducting oil heating jacket through a pipeline at the temperature of 220-225 ℃, is subjected to isomerization reaction in a catalyst fixer 11 with a catalyst, then enters an insulating evaporator with the temperature controlled at 136-140 ℃, and is condensed and collected by a condenser. Finally, the product yield is 99.03%, and the isomerization depth is 42.7%.
It should be noted that the technical features of the carbon five storage tank, the maleic anhydride storage tank, the magnetic pump, the flow meter, the tower reactor, the thin film evaporator, the condenser, the carbon five receiving tank, the catalyst holder, the adiabatic evaporator, etc. related to the present patent application should be regarded as the prior art, and the specific structure, the operation principle, the control mode and the spatial arrangement mode of the technical features may be selected conventionally in the field, and should not be regarded as the invention point of the present patent, and the present patent is not further specifically described in detail.
Having described preferred embodiments of the present invention in detail, it is to be understood that modifications and variations may be resorted to without departing from the spirit and scope of the invention as defined by the appended claims.
Claims (7)
1. The continuous production system of the methyl tetrahydrophthalic anhydride is characterized by comprising a tower reactor, a carbon five storage tank, a maleic anhydride storage tank, a film evaporator, a carbon five receiving tank, an insulating evaporator and a finished product tank, wherein the carbon five storage tank is connected with the tower reactor through a first magnetic pump, the maleic anhydride storage tank is connected with the tower reactor through a second magnetic pump, the tower reactor is connected with the film evaporator, the film evaporator comprises a steam outlet and a liquid outlet, the steam outlet is connected with the carbon five receiving tank through a first condenser, the liquid outlet is connected with the insulating evaporator, a catalyst fixer is arranged between the liquid outlet and the insulating evaporator, and the insulating evaporator is connected with a second condenser through a third magnetic pump and then connected with the finished product tank.
2. The continuous production system of methyl tetrahydrophthalic anhydride as claimed in claim 1, wherein a first flow meter is disposed between the first magnetic pump and the tower reactor, and a second flow meter is disposed between the second magnetic pump and the tower reactor.
3. The continuous methyltetrahydrophthalic anhydride production system according to claim 2, wherein the production system further comprises a monitoring and controlling system, the monitoring and controlling system comprises a DCS, the DCS is connected to the first flow meter and the second flow meter, and the first magnetic pump, the second magnetic pump and the third magnetic pump are respectively connected to the DCS.
4. The continuous production system of methyl tetrahydrophthalic anhydride as claimed in claim 3, wherein the tower reactor is divided into several sections from top to bottom, each section is provided with a heating device and a temperature monitoring device, and the heating device and the temperature monitoring device are respectively connected to DCS.
5. The continuous production system of methyl tetrahydrophthalic anhydride according to claim 4, wherein the liquid outlet is connected to the adiabatic evaporator through a heat-conducting oil heating jacket tube, the catalyst holder is mounted on the heat-conducting oil heating jacket tube, and the temperature of the heat-conducting oil heating jacket tube is controlled by DCS.
6. Continuous production method of methyl tetrahydrophthalic anhydride, characterized in that the continuous production system according to any of claims 1 to 5 is used, comprising the following steps: storing carbon five in a carbon five storage tank, storing maleic anhydride in a maleic anhydride storage tank, and conveying specified amounts of the carbon five and the maleic anhydride to a tower reactor by using a first metering pump and a second metering pump respectively, wherein the molar ratio of the maleic anhydride to the carbon five is 1: 1.03 to 1.10, controlling the synthesis temperature in the tower reactor to be 70 to 80 ℃, ensuring that the carbon five which is not reacted enters a thin film evaporator with the temperature controlled at 120 ℃ after the residence time in the tower reactor is 30 to 40 seconds, pumping and recovering the carbon five which is not reacted into a carbon five receiving tank after being condensed by a first condenser under the high vacuum state, introducing the liquid at the bottom of the thin film evaporator into a catalyst fixer with a catalyst for isomerization reaction at the temperature of 160 ℃ and 200 ℃, then entering a heat insulation evaporator with the temperature controlled at 140 ℃ and 130 ℃ and collecting the gasified product in a finished product tank after being condensed by a second condenser.
7. The continuous process according to claim 6, wherein the temperature in each stage of the column reactor is equal.
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN115572274A (en) * | 2022-11-11 | 2023-01-06 | 淄博鲁华泓锦新材料集团股份有限公司 | Method for continuously co-producing nadic anhydride and methyl tetrahydrophthalic anhydride by using cracking carbon five as raw material |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN115572274A (en) * | 2022-11-11 | 2023-01-06 | 淄博鲁华泓锦新材料集团股份有限公司 | Method for continuously co-producing nadic anhydride and methyl tetrahydrophthalic anhydride by using cracking carbon five as raw material |
| CN115572274B (en) * | 2022-11-11 | 2023-03-17 | 淄博鲁华泓锦新材料集团股份有限公司 | Method for continuously co-producing nadic anhydride and methyl tetrahydrophthalic anhydride by using cracking carbon five as raw material |
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| CN112661735B (en) | 2023-12-22 |
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